Technical Data BookPetroleum Refining
Refining Department
SIXTH EDITION, APRIL1997
American
Petroleum
Institute
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SPECIAL NOTES
All rights reserved.No part of this workmay be reproduced stored in a retrieval system,or
transmitted by any means, electronic, mechanical, photocopying, recording,
or otherwise,
without prior written permissionfrom the publisher. Contactthe Publishel;
API Publishing Services, 1220 L Street, N. W , Washington,D. C. 20005.
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API publications necessarily address problems
of a general nature.With respect to particular circumstances, local,state, and federal lawsand regulations shouldbe reviewed.
API is not undertaking to meet the duties of employers, manufacturers, or suppliers to
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and safetyrisks and precautions, nor undertaking their obligations under
local, state, or federal laws.
Information concerning safety and health
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implication or otherwise, for the manufacture,sale, or use of any method, apparatus,
or product covered by letters patent. Neither should,anything contained in the publication be construed as insuring anyone against liability
for infringement ofletters patent.
Generally, API standards
are reviewed and revised, reaffirmed,
or withdrawn at least ëvery
five years. Sometimes a one-time extension ofup to two years willbe added to this review
cycle. This publication will nolonger be in effect five yearsafter its publication date as an
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This document was produced under API standardization procedures ensure
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API standards are published
to facilitate the broad availability
of proven, sound engineering and operating practices.These standards are not intended to obviate the needfor applyingsoundengineering judgment regarding whenandwherethesestandardsshouldbe
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STD.API/PETRO SRCH TECHNICAL-ENGL
FOREWORD
The project that resulted
in the publicationof the TechnicalDaruBook was initiated as a result ofageneral
recognition by the petroleum refining industry of the desirability of an authoritative publication setting forth a
collection of correlations and methods for estimating physical properties thatare used in process design.
The Subcommittee on Technical Data was originally appointed inJanuary I959 to coordinate the project
and was later upgraded to the TechnicalData Committee. The membership has been as follows:
Affiliation
Member
Shell OilCo.
AS. Lehmann, Chairman (1959-1965)
C.C. Williams III. Chairman ( 1965- )
Allied Chunical
David Zudkevitch (1975-1985)
Amoc0 o i l Co.
J.E. Wolf (1959-1981)
S.J. Kramer (1981-1994)
J o ~G
l h t n (1994- )
American Petroleum Institute
R.R. Wright, Secretary (1959-1970)
C.T. Sawyer, Secretary (1 970- 1972)
R.J. Young, S t c ~ t a r y(1972-1982)
W.C. R e h , Secretary (1982-1985)
M.H. Matheson, Secretary (1986-1988)
G.C. Hurky. S ~ ~ t a (1989-1990)
r y
D.L. Miller, Secretary (1990-1993)
G. Carroll. Sccntary (1993-1995)
Rtntiss Scarles(1995- )
Ashland Petroleum Co./Marathon Ashland
J.F. Hoffman (1989)
W.M. Rice (1998- )
Atlantic Richfield Co./ARCO Products Co.
O.H. ha ri^ (1959-1961)
A.E. Andersen ( I96 1 - 1976)
J.B. fumer (1976-1980)
G.E. Merritt (1980-1986)
V.J. Sampath (1993-1998)
Walt Dardenne-Ankringa (1998- )
Beche1 Corp.
LS.Galstaun (1966-1978)
B.P. (North America) UdJBP America, Inc.
R.M. Blunden (1970-1971)
S.Godpole (1993)
Abhash Nigan (1994- )
C.F. Braun and Co.
H.G. Hipkin* (1965-1974)
Chevron Research Co.
A.E. Ravicz (1968-1973)
C. James (1973-1977)
R.H. Kilgren (1977-1984)
J.K. Baker (1985-1987)
A.E. Ravicz (1988-1995)
YenChen (1995- )
Exxon Research and Engineering Co.
A.K. Scott ( 1959- 1969)
David Zudkevitch (1969-1975)
R.H. Johnston (1975-1977)
C. Tsonopoulos(1977- )
Foster Wheeler Corp.
J.F. Middleton. ( 1963- 1966)
S.A. Newman (1978-1993)
Gulf Canada Ud.
J.G. Spiro (1979-1986)
Gulf Research and Development Co.
J.H. Hirsch ( I 959-1 965)
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H.G. Hipkin (1978-1981)
J0eF0~(1981-!991)
S.J. Kramer(1966- )
M.C. Fogle (1966-1967)
R.F. Mansfield ( 1967-1969)
G.E. Jones, Jr. (1969-1973)
R.H. Jacoby (1973-1975)
E.O. Eisen ( 1975-1 979)
J.S. Lasher (1979-1986)
The M.W. Kellogg Co.
h F r i c n d * (1962-1973)
S.B. Adler (1973-1981)
C.F. Spencer(1982- )
iii
lgg9
*Representing the Contractors’ Advisory Subcommittee on Technical Data
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
API TECHNICAL DATA BOOK
Arthur G. McKee andCo.
O.H. Hariu* (1962-1965)
O.H. ha ri^ (1979-1985)
Mobil Oil Corp.
E.R.J. Serf ( 1 959- 1962)
H.G. Grayson( 1 962-1 965)
R.C. Shen (1965-1972)
M.G. Kesler(1972-1979)
B.1. Lee (1 979- )
Monsanto Co.
S.T. Hadden (1967-1970)
Natural Gas Processors Association
Carl Sutton( 1 970- 1987)
R.E. Cannon (1987-1989)
J. Herben (1990-1993)
M.F. Sutton (1 993- )
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Pennzoil Co.
Keith E. Thomas (1990-
Phillips Petroleum Co.
R.A. Rndlay (1965-1975)
M.A. Albright (1975-1984)
Dale L. Embry( 1985- 1992)
ROYC. Lee (1996- )
The Standard Oil Co. (Ohio)
J.W. Thomas (1961-1966)
)
Sun Oil Co.
D. Camin (1974-1976)
Texaco, Inc.
Leon Gaucher (1 960-1 962)
J.H. Greene (1962-1966)
J.R. Zoller (1966-1969)
W.R. Coons, Ir. (1969-1974)
E.H. Holst ( 1974-1977)
W.R. Hollowell ( 1 977-1979)
C.L. WU ( 1980- 1986)
Union Oil Co. of California
Bernard Kouzel( 1964- 1989)
David H. Chittenden (1990-1992)
Unocal CIS
Peter A. Nick (1992- 1997)
The Contractors’ Advisory Subcommitteeon Technical Data has advised and assisted the Subcommittee
on Technical Data. Advisory Subcommittee membership has been as follows:
Affiliation
Member
Aspen Tech
S. Watanasiri
The Badger Co., Inc.
M.L. Buckler
P.F. Way
H.E. Ramirez
D.H. Jones
F.C. Heron
R.F. Guarino
Bechtel National Inc.
L.S. Galstaun
H.G. Hipkin
J.S.M. Fox III
Roben Chu
S.J. Kramer
C.F. Braun and Co.
M.S. Nehls
Brown & Root-Braun
R.F. Detman
H.G. Hipkin
C.R. Koppany
F.C. Clark
C. Shen-Tu
Catalytic Construction Co.
D.J. Oriol0
J.J. Cicalese
The Fluor Daniel Engineering &
Constructors, Inc.
C.F. Hancock
W.M. Hathaway
R.A. Chong
Foster Wheeler Corp.
J.F. Middleton
C.W. Zimmerlein
Stephen Newman
1999
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Houdry Procc.ss and Chemical Co.
E.A. White
The M.W.Kellogg Co.
LC0 Friend
S.B. Adler
C.F.Spencer
Lewis Yen
The Lummus Co.
ABB L u m m u " t
L.M.Shipman
O.H.Hariu
E.G.Graeber
I~c.
Arthur G. McKee and Co.
J.H. Geiger
The Ralph M. Parsons Co.
andStone
A.E. Chute
O.H. Hariu
Wtbster EngineeringCorp.
C.N. Collard
E.J. Grccn
M.L.Buckler
A.S. Bnrnjcs
David Bluck
John Coon
Simulation Sciences
:t
The technical work, evaluation of correlations, and preparation book
of the
were carried out by the projec
staff at the Department
of Chemical Engineering of the Pennsy1;aniaState University.
The compilationhas revealed the true state of the
art of this information as applied to petroleum refining.
The compilation not only shows how much we know but also reveals the degree and extent of our
ignorance.
Thus.
in addition to being
an explicit tool for practicing engineers, it is an implicit guide for research to perfect and extend
methods for correlating and estimating physical properties.
There is no guarantee, express or implied, that the data or methods herein are
the best The
in existence.
only claim made for the compilation is that the data herein have been judged the best available
to the project staff
at the Pennsylvania State University at the time the various reviews were completed.
Many articles publishedin the
technical journals during the course
of the project may have provideda basis for improving the precision
or range
of the data in this book. This is inherent
in the nature of developing technology.
The information and procedures given
are based on experimental data and are believed to be correct within
the limitations designated. Although extraordinary effort has been expended in eliminating errors, no warranty,
express or implied, is given by the investigators, the Pennsylvania State University,or the American Petroleum
Institute in the useof this information.
API publications in print or electronic form
mayby anyone desiring to so.
be used
do Every effort has been
made by the Institute to assure the accuracy and reliability of the data contained in them; however, the Institute makes
no representation, warranty,or guarantee in connection with this publication and hereby expressly disclaims any
liability or responsibility for loss or damage resulting from its use or for the violation of any federal, state, or
municipal regulation with whichthis publication may conflict.
Suggested revisions are invited and should be submitted to the Downstream Department, American
Petroleum Institute,1220 L Street, N.W., Washington,D.C.20005.
Downstream Depanment
American Petroleum Institute
December 1998
1999
Copyright American Petroleum Institute
Provided by IHS under license with API
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Not for Resale
V
PREFACE
CONTENTS
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This book isa critically reviewed compilation of the physical and thermodynamic
data and correlations that are of most interest to petroleumrefiners for process evaluation
and equipment design. The book includes chapters on the following topics: general data,
characterization of hydrocarbons, petroleum fractiondistillation interrelations, critical
properties, vapor pressure, density, thermal properties, vapor-liquid equilibrium, waterhydrocarbon equilibria, surface and interfacial tension, viscosity, thermal conductivity,
diffusivity, combustion, and adsorption equilibria, in that order. The book concentrates on
hydrocarbons and their mixtures. Nonhydrocarbongases and some oxygenated compounds
important in petroleum processing are included where appropriate. Hydrocarbon systems
are divided into three groups: those in the pure state, petroleum mixtures for which the
compositions of all the species are known (defined mixtures), and mixtures whose
composition is unknown (undefined mixtures). The undefined mixtures must usually be
characterized by one or more measured physical properties, such as density, molecular
weight, viscosity, and ASTM distillation, which reflect their constitution. Obviously the
treatments for thesethree classificationsdiffer; thus, separatemethods are given for each.
Predictions for defined mixtures can often be made using correlations for undefined
mixtures, but this procedure is rarelyrecommended.
Althoughmethodsaregiven
primarily for desk calculations, alternative (and
generally more complex) methods suitablefor use on computers have also been
recommended inrecent revisions whenever feasible. Most procedures are equation based,
but many are alsopresented as figures. Computer methods are included for essentially all
critical, volumetric, and thermodynamic
properties discussed.
Most procedures for transport
properties could also be readily programmed. It has been the policy of the API Technical
Data Committee that computer methods include the requisite equations and calculation
procedures butnot a specific program. The procedures weremadeavailable as selfsupporting FORTRAN subroutines. Programming of therecommendedmethodswere
addressed separately in Chapter 16, which was available as a separate publication. This
material is now incorporated in the electronicversion discussed later.
Each chapter is devotedto a single
property or group of related properties. Within
the chapters, further
divisions in sectionsand subsectionsare madeaccording to theproperty
(when more than one is given in a chapter), the phase, and the state of the hydrocarbon
(pure, defined mixture, or undefined mixture). Generally,nonhydrocarbons are covered in
a section differentfrom the one in which the corresponding treatment for hydrocarbons is
given. Titles forthe subdivisions are given in the table of contents for each chapter. The
system used lends itself well tofuture revisions andexpansions, with minimal renumbering
of the unchanged material.
Chapter 1, "General Data," contains information on selected properties of pure
compounds, conversion factors, and other general information. Chapter 1 is also available
in the electronic versionof the bookand previously was sold in a personal-computer-based
format, the API Access Program, or APIAP,. an interactive, menu-driven program that
provides easy access toselected property values of the compounds contained in Chapter 1.
The databank accompanying this program is updated with the
latest property values.
In Chapters 2-15, for numbering purposes, the figures, tables,and procedures that
are to be used to calculate values are not treated separately according to kind but are
numbered serially in order of presentation, whether figure, table, or procedure. In the
designation "Figure 12B1.3," for example, "12" is the chapter number, "B" is the section
designation, "1" is the subsection number, and "3" indicates the third exhibit from the
subsection.
Comments are given for each figure or procedure and are normally located on the
back of the exhibit. For groups of related figures, comments are given following the last
1999
Copyright American Petroleum Institute
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API TECHNICAL DATA BOOK
figure only. Where tables and figures are used as part of a procedure (for example Table
7A1.2, which is part of Procedure 7A1.1, or Figures 7B3.4-7B3.6, which are part of
Procedure 7B3. l), the procedure and comments for theentire unit are given first, followed
by the supporting exhibits(which have no individualcomments). Included in the comments
are all or some of the following sections: purpose (particularly as distinguished from other
related exhibits), limitations,reliability, notation, specialcomments, literature sources, and
examples. It is anticipated that most erroneous applications and difficulties in using the
correlations will result from failure toconsult these comments.
In preparing the text for the procedures and comments, an effort was made to
minimize cross-referencing, althoughcorrelationstypically
require input from other
chapters. In some cases (notably Chapter 7), extensive cross-referencing could notbe
avoided without prohibitive repetition. References to other chapters are usually no more
specific than thechapter number, to permit future revisions without repercussions
throughout the book.
Neither the availability of many correlations nor theendorsement of one or more
of them in this book implies that any of them is totally satisfactory for all
conditions of
temperature, pressure,
phase, composition,and hydrocarbon type.The selections were based
on theavailable data,tempered by scientificjudgment. There is noguarantee that any of the
methods will be reliable for unusual compounds or conditions, and the user is cautioned
against blind faith and particularly against beingdeceived by the rigorous appearance of a
complicated correlation. The user iscautioned against usingany of the methods
outside the
conditions stated inthe limitations section. Many moreexperimentaldata are needed before
our correlativeknowledge can be described as satisfactory. In spite of these shortcomings,
the selected correlations
are believed to be the best compromise
among accuracy, generality,
internal consistency, and ease of use that can be
obtained from the readily available methods
and data.
PREPARATION OFTHE FIRST EDITION
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The preparation of the first editionof the TechnicalDatu Book covered a period of
more than four years from 1959to 1964. During that time, the work
of the Penn State staff,
led by the late Dr. M. R. Fenske, Dr. W. G. Braun, and Mr. W. H. Thompson, was guided
and coordinated by the API Subcommittee on Technical Data with assistance from the
Contractors' Advisory Subcommittee, underthe
sponsorship of theAPI
Refining
Department. [For more details, see A. S. Lehmann, "API Technical Data Book Project,"
Proc. APl44(III) 278 (1 964). The general patternfollowed by Penn State in preparing each
phase of each section of the book is outlined below:
1.
2.
The literature was searchedforpertinentdataand
correlations.
When there were many applicable correlations,some were eliminated from further
consideration on the basis of such factors as complexity, lack of generality, failure to be
internally consistent, and availableof improved forms.
3.
A set of data was assembledfor comparison with thepredictions of the correlations.
4.
Thecorrelations were evaluated for accuracy, generality, ease ofuse and other
characteristics.
5.
Theevaluation results, conclusions andrecommendationswere
reported to the
subcommittees for review.
6.
Occasionally,reevaluations or further checking was performed,based on comments
from the reviewers.
7.
The recommended data and correlations, along with descriptive comments, were
prepared in final form forsubcommittee review.
8.
The draft chapterswere modified to satisfy reviewers'criticisms and were submitted
for publication.
1999
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As implied, no attempt was made to develop new correlations for the first edition of the
Technical Data Book.
During the literature searches, approximately 10,000 articles were reviewed. Of
these, 3000 were useful enough to
include in reports, andapproximately750 are cited in the
book. Four bibliographies of data were prepared and published as incidental by-products
of this effort:
Fenske, M.R., Braun, W. G., Holmes, A. S., Bibliography of Vapor-Liquid Equilibrium
Data for Hydrocarbon Systems BibliographyNo. 1, Am. Petrol. Inst., New York
( 1963).
Holmes, A. S., Braun, W. G., Fenske, M.R., Bibliography of Vapor Pressure Data for
Hydrocarbons, Bibliography No. 2, Am. Petrol. Inst., New York(1964).
Jeter, L.T.,Thompson, W. H., Braun, W. G., Fenske, M.R.,Bibliography of Volumetric
and ThermodynamicData for PureHydrocarbons
ana’ TheirMixtures,
Bibliography No. 3, Am. Petrol. Inst., New York (1964).
Wilson, R. F., Thompson, W. H., Braun, W.G., Fenske, M.R.,Bibliography of VaporLiquidEquilibriumData
for Hydrocarbon-Nonhydrocarbon Gas Systems,
Bibliography No. 4, Am. Petrol. Inst., New York (1964).
These bibliographies, documentation reports(see below), and the tables of data issued by
API Research Project 44 extended the usefulness of this bookto unusual hydrocarbons and
systems.
One of the most difficulttasks was narrowing theevaluations to reasonable sizes,
consistent with the importance of the property under consideration and the available time
and funds. It was neitherpossible nor justifiable, for example, to examine in detail all of the
more than80 correlations thatare available for the vapor
pressure or the heatof vaporization
of pure hydrocarbons. For many properties,extensive data bases have been assembled and
stored on computer tapes.
Selecting a single method for use with all hydrocarbons at all temperatures and
pressures was often difficult because different correlations normally excelled in different
areas. Furthermore, theresults of error analyses were occasionally complicated, for
example, when different correlations were
applicable to different groups of data points and
the difficultyof the noncommon points varied.
(If only commondata points werecompared,
the set was usually so small and restricted that the
effects of temperature, pressure, system,
and /or hydrocarbon type could not be
studied. Theintangible criteria of generality andease
of use were always considered, along with the moreconcrete error analysis results.
Although there were usually too manyapplicable correlations, occasionally none
were available for technicallyimportant circumstances. Notable examples of thisare
correlations for mixtures containing hydrogen or high concentrations of unsaturated or
aromatic hydrocarbons. Methods are given for
these mixtures, but data were rarely available
to confirmthe methods’ validity.
After the evaluations were completed, the results and recommendations were
reported to the subcommittee members in 85 different documents, including 29 formal
reports. Fourteen more formal reports weredraft chapters,which contained draft copiesof
the figures in the Technical Data Book. Most figures had previously been redrawn from
their original sources tounifystyle,tomakethem
more convenient and useful for a
quantitativeapplication, andin somecases, to correct errors. Comments from the
subcommitteemembers resultedin the elimination of
many troublesomeerrors and obstacles
for the inexperienced user.
After the publication of the
Technical Data Book,
the AmericanPetroleumInstitute
made Documentation Report Nos. 2-66 through 14-66 to holders of the book. These reports
are an organization of theevaluation reports anddocument the selectionof the correlations
1999
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Copyright American Petroleum Institute
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Not for Resale
S T D * A P I / P E T R OS R C HT E C H N I C A L - E N G L
L777
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inthisbookon
a chapter-by-chapter basis. In addition to providing answers to many
questions about the selection of the contents of the book, the information was useful in
estimating the reliabilities of the various correlations in specific situations. These reports
are now unavailable.
The extensive literature surveys, correlation evaluations and thereview procedure
outlined above make this
book the mostcompleteand reliable work yetcompiled specifically
for general use in the evaluation of petroleum refining processing and related equipment.
The direct product of the work
described above is, of course, the book. The project
also resulted in partial or total support for a number ofundergraduate and graduate students
and fora professional staff. Many of thestudents have completed their academic work and
have since entered industry, and anunusually large proportion have entered thepetroleum
industry. A11 have an increased understanding of and sympathy for the problems of the
petroleum industry.
PREPARATION OF THE SECOND THROUGHFIFTH EDITIONS
1999
X
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Since the literature search for the first edition was completed, a large number of
new correlations and an even larger amount of experimental data of potential use in the
Technicul Datu Book have appeared in the open literature. This information prompted
further studies, also supported by the American Petroleum Institute as a vital part of its
continuing program to provide the best current data and correlations for the practicing
engineer, which ultimately resulted inpublication of the second and third editions.
Revisions for the second edition, published in 1970, were made in Chapters 1, 7,
8.9, and 1 1. In Chapter 1, the physical property tables of the C & ,hydrocarbons were
extensively revised based on the changes in, or additions to, the tables of API Research
Project 44. Also included were tables for the physical properties of biphenyls, diphenyls,
tetrahydronaphthalenes,and decahydronaphthalenes. In Chapter 7, the tablesof coefficients
for the calculations of ideal gas enthalpies, the enthalpy-temperature diagrams, and the
enthalpy-entropy diagrams for methane, ethane, propane, and ethene were revised. In
Chapter 8, material was added on the solubility of gases in water and the water content of
natural gases. Chapters 9 and 1 1 concerning water-hydrocarbon phaseequilibria and
viscosity, respectively, were completely revised. The numerical solutions of all of the
example problems in the book were changed to reflect the revisions of the properties that
were made inChapter 1. Inadvertent errors in chapters, which were listedin Revision Sheet
1 (July 1, 1967) and Revision Sheet 2 (December 1 , 1969), were corrected.
For the third edition, published in 1976, Chapters 4, 6, and 7 were completely
revised, and necessary changes were madein Chapters 1 and 2. Chapter 4 was expanded in
1974 to include procedures to calculate critical properties for all types of hydrocarbon
densities
systems. Chapter 6,as revised in 1972. included newmethods for saturated liquid
for pure hydrocarbons, defined hydrocarbon mixtures, and nonhydrocarbons. In the 1976
publication,the vapordensity section of Chapter 6 and all of Chapter 7 were revised. Vapor
densities and thermodynamic properties for pure hydrocarbons and defined hydrocarbon
mixtures were all predicted by the modified Pitzer
corresponding-states method of Lee and
Kesler. Desk and computer methods were made consistent. New methods for predicting
thermodynamic properties of petroleum fractions were presented that use the methods of
Chapter 4to predict criticalproperties. The acentric factors of Chapter 2 were revised for
consistency with Chapters 6 and 7. Certain properties in Chapter 1 , as revised by API
Research Project 44, were updated.
For the fourth edition, Chapter 5 on vapor pressure, Chapter 8 on vapor-liquid
equilibria,Chapter 12 on thermal conductivity, and Chapter 13 on diffusivity were
completely revised, with a largeamount
ofnewmaterial
added.Chapter
2 on
characterization andChapter 3 on distillation relationships were partiallyrevised with new
procedures for estimatingproperties. Chapter 4 on critical properties wasupdated. Chapter
Not for Resale
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L777 W 0732270 Ob17522 7111 W
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API TECHNICAL DATA BOOK
9 on water-hydrocarbon equilibria and hydrates
gas
was completely revised and substantially
expanded. Data and correlations for water-hydrocarbon systems previously in Chapter 8
were updated and included in Chapter 9. Chapter 10 on surface tension was revised, and
methods for prediction of interfacial tension were included for the first time.
For the fifth edition, a revision package was issued in 1985 that completelyrevises
Chapter 14 on combustion, Chapter 1 1 on viscosity, andthe liquid portion of Chapter 6 on
density. A new Chapter 15 on gas-solid and liquid-solid adsorption equilibriawas added.
In addition, theprocedure for computer calculation of vapor-liquid equilibria in Chapter 8
was revised. "he ninth revision package,released in 1988, included complete revisions of
Chapters 1-4 coveringgeneral data,characterization,distillation, and critical properties. The
tenth revision package contains a complete update of Chapter 7 on thermal properties.
Numerous other changes to the entire book make is consistent with changes previously
published (primarily in Chapter 1).
PREPARATION OF SIXTH EDITION
The eleventh revision package(1994) included complete revisions of Chapter 3 on
petroleum fraction distillation interconversions,Chapter 5 on vapor pressure, and Chapter
8 on vapor-liquid equilibriumK-values. Substantiveadditions and improvements were made
in Chapters 3.5. and 8.
The twelfth revision package(1996) included complete revisions of Chapter 9 on
water-hydrocarbon equilibria, Chapter 11 onviscosity, and Chapter 12 onthermal
conductivity as well as an update of all property values and addition of some important
compounds in Chapter 1. Ideal gas tables of Chapter 7 and revised procedures to predict
Reid vapor pressure in Chapter 5 were also included.
The thirteenth revision package
(1998) contains (1) a revised Chapter 2 containing
routines for additional inspection properties as well as updates of previous routines, (2) an
updated Chapter 4 procedure for calculation of
critical properties froman equation of state,
(3) a revised Reid vaporpressure prediction method inChapter 5, (4) changes in Chapter 7
procedures for heat capacity of petroleumfractions, ( 5 ) new heat offormationand
combustion tables in Chapters 7 and 14, (6) totally revised and updatedvalues and
correlations forinteraction coefficients forhydrocarbon-non-hydrocarbonsystems for the
Soave equation of state, and (7) additional revisions and additions tothe hydrocarbon-water
portion of Chapter 9.
COMPUTERIZATION
Concurrent with the publication of the ninth revision package, the first portion of
an effort begun in 1975 to provide standard FORTRAN subprograms for each procedure in
the Technical Data Book was released. The programming standards, standard variable
names, user documentation for each completed procedure, and a description ofthe
computerized version of the pure-component data base of Chapter 1 are included in a
separate binder. This first release included subprograms for almost all procedures in
Chapters 2-9 as well as certain defining equations. Subprogramsand the pure-component
data base are supplied on disk or tape as desired by the purchaser. Use of the subprograms
requires availability of the
entire book for reference as the subprograms are used. A second
release containing material on equilibrium flash vaporization relationships forChapter 3,
procedures for reacting systems for Chapter 7, and all procedures in Chapters 10-15 was
published in 1988.
A third release completely revising Chapter 7 routines, correcting a few errors,
updating test routines tomatch thefifth edition, and reorganizing and renumbering the pages
was published in Spring 1993. A fourth release includes complete revisions of the code for
xi
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API TECHNICAL DATA BOOK
Chapters, 3,5,and 8 to match the changes made for the eleventh revisionpackage. A fifth
release included all changes made in revised package 12 and was published in early 1997.
Beginning with the thirteenth revision package the computerized material is only
published in the electronic version. This version replaces the printed version witha modem
Windows interface. This single-screen approachaccesses the latestprediction methods. All
properties are predicted by the recommended methodspresented in the Technical Data Book
with comments and limitations available on-line. Temperature-dependentproperties can be
tabulated and graphed over the entire applicable range. Distillation interconversions can be
displayed graphically. Results can be exported to in-house and simulation software.
EPCON International has developed this software. The first version is available (Dec.
1998). Updates and additions will be available in early 1999 with a complete product by late
1999. EPCON International is at 281-398-9400 or at www.epcon.com.
DOCUMENTATION
--`,,-`-`,,`,,`,`,,`---
Documentation reports on most chapters are available from Global Engineering
Documents, 15 Inverness Way East, Englewood, CO 80150. A complete list of the
documentation reports still current and how to order them is given in the
A P I Publications
Catalog.
They include the following reports in the format: Chapter@)- year of service.
2-8 1
6-72
10-82
2,346
6-84
11-84
2-98
716-76
1 1-96
3-98
7-9 1
12-80
4-73
8-70
12-96
4-85
8-78
13-80
14-83
48-98
8-93
5-78
9-82
71 14-98
5-93
9-96
15-83
5-98
9-98
ACKNOWLEDGEMENTS
The responsibility for the details in evaluating, selecting, and presenting the
correlations in the various chapters, as constituted in December 1996, was placed with the
following people, who are credited with the contentsof the chapters:
Chapter 1 , "General Data": R. E. Pulley and T. E.Daubert
Chapter 2, "Characterization": P.M. Hinderliter, M. R.Riazi, and T.E. Daubert.
Chapter 3, "Petroleum Fraction Distillation Interconversions":T. E. Dauben
Chapter 4, "Critical Properties": C. Chrostowski, J. R. Elliott, Jr., and T. E. Daubert.
Chapter 5. "Vapor Pressure," M.J. Thorwart, R.E. Pulley, P.M. Hinderliter and
T.E. Daubert
Chapter 6, "Density": J. E.Lobo, R. P. Danner, andT. E. Dauben
Chapter 7, "Thermal Properties": K.R. Hanawalt, G. Singh, and T.E. Daubert
Chapter 8, "Vapor-Liquid Equilibrium": M. J. Thorwart and T. E.Daubert
Chapter 9, "Water-Hydrocarbon Equilibria": R. E. Pulley, J. Guo, P.M. Hinderliter, M. K.
Maslanick, and T. E. Daubert
Chapter 10, "Surface and Interfacial Tension": M. J. Engel, T. E. Dauben, and R.P.Danner
Chapter 1 1, "Viscosity": D. J. Fitzgerald and T.E. Dauben
Chapter 12, "Thermal Conductivity": R.R. Wu and T. E. Daubert
1999
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Chapter 13. "Diffusivity": N. O. Umesi, R.P. Danner, and T. E. Daubert
Chapter 14, "Combustion":M. K. Maslanick, J. E. Lobo, C. Chrostowski, P.M. Hinderliter,
T. E. Dauben, and R.P.Danner
Chapter 15, "Adsorption Equilibria": S. D. Mehta, R.P.Danner, and T. E. Dauben
Chapter 16. "Computerization": K. R. Hanawalt, J. R. Elliott, Jr., M. J. Thorwart, N. C.
Daubert, and T.E. Dauben
Individuals, members, or representatives were authorized to act for the entire
Technical Data Committeeas chapter coordinators in resolvingreviewers'criticisms of each
of the draft chaptersand in expediting the preparation of the finalcopy.
Many other staff members and students of the ChemicalEngineering Department
of the Pennsylvania StateUniversity assisted in the literature work,
data handling, evaluation
details, resultscompilation, figure preparation, andrepon preparation.
Members of the Technical Data Committee and their
associates who reviewed the
reports have contributed admirably to correlative knowledge in the areas covered in this
book. Several of the developed correlationswerenotselectedforuse
in this book.
Nevertheless, thecomments and criticisms from
these authors were typically objective and
impartial, despitetheir personal interest.
The companies with which the committee membersare affiliated are thanked for
their support, formaking their own technicaldata book available for project use, and for
evaluations of certain of the calculations methods.
The Contractors'Advisory Subcommittee on Technical Data also assisted in the
preparation of the book. The members of this subcommittee are thanked for their helpful
comments on theevaluation reports.
Most of the exhibits in this book were taken directlyfrom the literature. Credit is
due to theauthors of the correlationsfor developingmethods thatare useful to the petroleum
industry, and the copyright holders are againthanked for their releases. The experimenters
who have measured the experimental data, without which this project would have been
futile, are alsothanked, and they are urged
to continue because our experimental knowledge
is far from satisfactory.
We thank the AmericanPetroleum Institute for providing the funds and the original
initiative to prepare this book. It is earnestly hoped that this book will reward
confidence
the
of the sponsors over the past almost 40 years by leading to savings in new designs and to
more energyefficient operation of existing units.
Thomas E. Daubert
Chemical Engineering Department
The Pennsylvania State University
University Park, Pennsylvania I6802
December 1998
1999
xiii
--`,,-`-`,,`,,`,`,,`---
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CONTENTS
(For complete listings and pagination, see individual chapters.)
CHAPTER 1-GENERAL
DATA
1-0 Introduction
1A Fundamental Constants and Conversion Factors
1Al Fundamental Constants
1 A2 Conversion Factors
1B
Letter Symbols Used in Chemical Engineering
1B1 Letter Symbols for the Principal Concepts Used in Chemical Engineering
1C
Property Definitions
1C1 Hydrocarbons-Primary Properties
IC2 Hydrocarbons-Secondary Properties
1C3 Nonhydrocarbons-Primary Properties
1C4 Nonhydrocarbons-Secondary Properties
1C5 Key to References
Bibliography
CHAPTER 2-CHARACTERIZATION OF HYDROCARBONS
2A
Characterization of Pure Hydrocarbons
2A1 Characterization Factors of Pure Hydrocarbons
2B
Characterization of Petroleum Fractions
2B 1 Characterizing Boiling Points of Petroleum Fractions
2B2 Molecular Weight of Petroleum Fractions
2B3 Acentric Factor of Petroleum Fractions
2B4 Molecular Type Composition of Petroleum Fractions
2B5 Refractive Index of Petroleum Fractions
2B6 Watson Characterization Factor of Petroleum Fractions
2B7 Flash Point of Petroleum Fractions
2B8 Pour Point of Petroleum Fractions
Bibliography
CHAPTER 3"PETROLEUM FRACTION DISTILLATION INTERCONVERSIONS
3-0 Introduction
3A
ASTM, True Boiling Point and Simulated Distillation Relationships
3A1 ASTM and True Boiling Point Distillation Relationships at Atmospheric
Pressure
3A2 ASTM and True Boiling Point Distillation Relationships at Subatmospheric
Pressures
3A3 AS",
TBP, and Simulated Distillation Relationships at Atmospheric
Pressure
3A4 Distillation Interconversions
Bibliography
1999
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--`,,-`-`,,`,,`,`,,`---
2-0 Introduction
API TECHNICAL DATA BOOK
CHAPTER 4-CRITICAL PROPERTIES
4-0 Introduction
4A
Critical Properties of Pure Hydrocarbons
4B
Critical Properties of Defined Mixtures
4C
Critical Properties of Natural Gases
4D Critical Properties of Petroleum Fractions
Bibliography
CHAPTER 5-VAPOR
PRESSURE
5-0 Introduction
5A
Vapor Pressures
5A1 Vapor Pressures of Pure Hydrocarbons and Narrow-Boiling Petroleum
Fractions
5B Reid Vapor Pressure and True Vapor Pressure
Bibliography
CHAPER 6-DENSITY
6-0 Introduction
6A Density of Liquid Systems
6A1DensityConversionTables
6A2 Density of Pure Liquid Hydrocarbons
6A3 Density of Liquid Mixtures
6BDensity of Gas Systems
6B 1 Density of Pure Hydrocarbon and Nonpolar Gases
6B2 Density of Gaseous Hydrocarbon and Nonpolar Mixtures
Bibliography
CHAPTER 7 T H E R M A L PROPERTIES
7-0 Introduction
7A Thermal Properties of Ideal Gases
7A1 Thermal Properties of Pure Ideal Gases
7B
Enthalpy of Liquids and Real Gases
7B 1 Enthalpy-Temperature Diagrams
7B2 Enthalpy-Entropy Diagrams
7B3 Enthalpy of Pure Hydrocarbon Liquids and Real Gases
7B4 Enthalpy of Mixed Hydrocarbon Liquids and Real Gases
7CHeat of Vaporization
7C1 Heat of Vaporization of Pure Hydrocarbons
7C2 Heat of Vaporization of Mixed Hydrocarbons
7D Heat
7D1
7D2
7D3
7D4
Capacity of Liquids and Real Gases
Heat Capacity of Pure Liquid Hydrocarbons
Heat Capacity of Mixed Liquid Hydrocarbons
Isobaric Heat Capacity of Pure Hydrocarbon Real Gases
Isobaric Heat Capacity of Mixed Hydrocarbon Gases
xvi
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7E
Heat Capacity of Liquids and Real Gases
7E1 Heat Capacity Ratio of Pure Hydrocarbon Real Gases and Liquids
7E2 Heat Capacity Ratio of Mixed Hydrocarbon Gases
7F
Entropy of Liquids and Real Gases
.7F1 Entropy of Pure Hydrocarbon Real Gases
7F2 Entropy of Mixed Hydrocarbon Gases
7G
Fugacity Coefficient
7G1 Fugacity Coefficient of Pure Hydrocarbons
7H Thermodynamic Effects in Reacting Systems
7H 1 Heat Effects in Reacting Systems
Bibliography
CHAPTER 8-VAPOR-LIQUID
EQUILIBRIUM K-VALUES
8-0 Introduction
8A
Graphical Procedures for Vapor-Liquid Equilibrium K-Values for Hydrocarbon
Systems
8A1 Vapor-Liquid Equilibrium K-Values for Hydrocarbon Systems
8B
Graphical Procedure for Vapor-Liquid Equilibrium K-Values for Systems
Containing Hydrocarbons and Hydrogen
8B 1 Vapor-Liquid Equilibrium K-Values for Systems Containing Hydrocarbons
and Hydrogen
8C
Graphical Procedure for Vapor-Liquid Equilibrium K-Values for Systems
Containing Hydrocarbons and Nonhydrocarbon Gases
8C1 Vapor-Liquid Equilibrium K-Values for Systems Containing Hydrocarbons
and Nonhydrocarbon Gases
8D Alternate (Computer) Procedure for Hydrocarbon, Nonhydrocarbon, and Petroleum
Fraction Vapor-Liquid Equilibrium K-Values
Bibliography
CHAPTER 9-PHASE
EQUILIBRIA IN SYSTEMS CONTAINING WATER
9-0 Introduction
9A Vapor-Liquid Equilibria in Systems Containing Water
9A1 Solubility of Water in Hydrocarbons
9A2 Solubility of Hydrocarbons in Water
9A3 Water Content of Hydrocarbon Gases
9A4 Equilibrium Constants in Water-Hydrocarbon Systems
9A5 Salt Effects of Solubility of Hydrocarbons in Water
9A6 Computer Method for Phase Equilibrium Calculations for WaterHydrocarbon Systems
9A7 Solubility of Nonhydrocarbon Gases in Water
9A8 pH of Nonhydrocarbon Gases in Water
9B
Gas Hydrates
9B1 Graphic Procedures for Prediction of Gas Hydrate Equilibria
9B2 Alternative (Computer) Procedure for Prediction of Gas Hydrate Equilibria
Bibliography
1999
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API TECHNICAL DATA BOOK
API TECHNICAL DATA BOOK
CHAPTER 10"SURFACE AND INTERFACIAL, TENSION
10-0 Introduction
1OA
Surface Tension
lOAl Surface Tension of Pure Hydrocarbons
10A2 Surface Tension of Defined Hydrocarbon Mixtures
10A3 Surface Tension of Crude Oils and Petroleum Fractions
10A4 Surface Tension of Nonhydrocarbons
10B Interfacial Tension
1OB1 Interfacial Tension of Hydrocarbon-Water Systems
Bibliography
CHAPTER 11-VISCOSITY
11-0 Introduction
11A Viscosity of Liquid Systems
1 1Al Viscosity Scales and Conversion Tables
11A2 Liquid Viscosity of Pure Hydrocarbons
11A3 Liquid Viscosity of Defined Hydrocarbon Mixtures
1 1A4 Liquid Viscosity of Hydrocarbon Mixtures of Undefined Composition
11A5 Effect of Pressure on the Viscosity of Liquid Hydrocarbons
11A6Viscosity Index
11A7 Liquid Viscosity of Hydrocarbons Containing Dissolved Gases
11B
Viscosity of Gaseous Hydrocarbons
11B1 Viscosity of Pure Hydrocarbon and Nonhydrocarbon Gases
11B2 Viscosity of Defined Gaseous Hydrocarbon Mixtures
11B3 Viscosities of Undefined Hydrocarbon Gas Mixtures
11B4 Effect of Pressure on the Viscosity of Gaseous Hydrocarbons
11c
Viscosity of Nonhydrocarbons
11C1 Viscosity of Gaseous Nonhydrocarbons
Bibliography
CHAPTER 12-THJ2RMAL
CONDUCTIVITY
12-0 Introduction
12A Thermal Conductivity of Liquid Hydrocarbon Systems
12A1 Thermal Conductivity of Pure Liquid Hydrocarbons
12A2 Thermal Conductivity of Defined Liquid Hydrocarbon Mixtures
12A3 Thermal Conductivity of Undefined Liquid Hydrocarbon Mixtures
12A4 Effect of Pressure on Liquid Hydrocarbon Thermal Conductivities
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12B Thermal Conductivity of Gaseous Hydrocarbon Systems
12B1 Thermal Conductivity of Pure Hydrocarbon Gases
12B2 Thermal Conductivities of Defined Mixtures of Hydrocarbon Gases
12B3 Thermal Conductivity of Undefined Mixtures of Hydrocarbon Gases
12B4 Effect of Pressure on Gaseous Hydrocarbon Thermal Conductivities
12C Thermal Conductivity of Nonhydrocarbons
12C1 Thermal Conductivity of Nonhydrocarbons
Bibliography
1999
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1797
m
0732290 ObL75Z7 O b b
m
API TECHNICAL DATA BOOK
CHAPTER 13"DIFFUSIVITY
13-0 Introduction
13A Diffusivity in Liquid Systems
13A1BinaryLiquid
Systems
13A2 Multicomponent Liquid Systems
13B
Diffusivity in Gas Systems
13B1 Binary Gas Systems
13B2 Multicomponent Gas Systems
13C
Diffusivity inGas-Liquid Systems
13C1 Gas-Liquid Systems
Bibliography
CHAPTER 14"COMBUSTION
14-0 Introduction
14A Heats of Combustion
14B Heat Available from Combustion of Refinery Gases and Liquid Fuels
14C Enthalpy of Flue Gas Components
14D Grossmet Calorific Value of Solid Fuels
Bibliography
CHAPTER 15"ADSORPTION EQUILIBRIA
15-0 Introduction
15A Pure GasAdsorption
15A1 Isothermal Adsorption Data
15A2 Correlation of Adsorption Capacities
15B
Gas-Mixture Adsorption
15B1 Isothermal Isobaric Adsorption Data
15C Liquid-Mixture Adsorption
15C1 BinaryIsothermal Adsorption Data
Bibliography
xix
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STD.API/PETRO TDB CHAPTER L-ENGL
1797 111 0 7 3 2 2 9 0 0 5 b b 5 B b 7Tl BI
CHAPTER 1
GENERAL DATA
Revised Chapter 1to First Edition (1966), Second Edition
(1970), Third Edition (1977), Fourth Edition (1982), and
Fifth Edition (1992)
--`,,-`-`,,`,,`,`,,`---
Copyright American Petroleum Institute
Provided by IHS under license with API
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Not for Resale
Copyright Q 1997 American Petroleum Institute
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Copyright American Petroleum Institute
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~~
~~
S T D . A P I / P E T R O T D B C H A P T E R 1-ENGL 1777
m
0732270 05bb588 574
~
m
PREFACE
The revision of Chapter 1incorporates new data from the DIPPR Compilation and
the TRC tables for hydrocarbons. A new computer method, to copy the data directly from
other fies and to generaie the tables for the chapter, was used to minimizeerrors.
Compounds that have been used in recent editions of other chapters have been added to
Chapter 1. The computerized versionof the chapter has alsobeen modified to include these
compounds.
Major work on this chapter was carried out and directed by Richard E Pulley, Jr.,
ResearchAssistant in ChemicalEngineering,under
the supervision of Dr. Thomas E.
Daubert, Principal Investigator.
Thomas E Daubert
Department of Chemical Engineering
The Pennsylvania State University
University Park, PA 16802
June 1995
--`,,-`-`,,`,,`,`,,`---
1997
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iii
Not for Resale
~
~
~~
~
STD.API/PETRO T D B CHAPTER L-ENGL L777 m 0 7 3 2 2 9 0 0 5 b b 5 B S 400 W
CHAPTER 1
GENERAL DATA
1-0 Introduction..
................................................
1A Fundamental Constants and Conversion Factors..
1Al Fundamental Constants
Table lAl.1
.................
.....:...............................
Fundamental Constants. ..................
.......................................
1A2 Conversion Factors..
Table 1A2.1 Lcngtb Conversions ......................
Table 1A2.2 Area Conversions.. ......................
Table lA2.3 VolumeConversions .....................
Table 1A2.4 LiquidVolumeConversions ...............
Table 1A2.5- Mass Conversions........................
Table lA2.6 DensityConversions. .....................
Table 1A2.7 Pressure Conversions.. ...................
Table lA2.8 Flow Conversions ........................
Table 1A2.9 KinematicViscosity Conversions.. .........
Table 1A2.10 Absolute Viscosity Conversions,...........
Table 1A2.11 Energy Convenions ......................
Table 1A2.12 Power Conversions.. .....................
Table 1A2.13 Specific Energy Conversions.. .............
Table 1A2.14 Specific Energy per Degree Convenions. ...
Table 1A2.15 Heat Flux Conversions ...................
Table 1A2.16 Heat Transfer Coefficient Conversions. .....
Table 1A2.17 Thermal Conductivity Conversions .........
1B Letter Symbols Used in Chemical Engineering. ...................
1B1 Letter Symbols for the Frincipal Concepts Used in
Chemical Engineering. ......................................
Table lB1.l Letter Symbolsfor the Principal Concepts
Used in Chemical Engineering.. ...........
Table 1B1.2 Alphabetical Index of SymbolsUsed in
Chemical Engineering ....................
1C Property Definitions.. .........................................
Table 1cD.1 Index of Compounds .....................
1C1 Hydrocarbons-Primary Properties
Table lC1.l Paraffins..
Table 1C1.2 Cycloparaffins
Table 1C1.3 Monoolefins and Diolefins
Table 1C1.4 Cycloolefins and Acetylenes.
...........................
..............................
...........................
................
..............
1997
V
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....................
Table lCl.5 BenzeneDerivatives..
Table1C1.6Condensed
Ring Aromatics and Derivatives.
.......................
................................
1C2Hydrocarbon-ndaq
Properties..
Table 1C2.1 ParafEh
Table1C2.2
Cycloparaffins
Table 1C2.3 Monoolefins and Diolefins
Table1C2.4
c y d o o l c m and Acetylenes..
TablelQ.SBenzeneDerivatives..
Table1C2.6
Condensed Ring Aromatics and Derivatives.
...........................
................
.............
....................
1C3 Nonhydrombons-Rimary
Table 1U.1 Acids.
Properties. .......................
..................................
....................
..............................
................................
TablelC3.2Alcoholsand
Phenols
Table lC3.3
Aldehydes
Table l U . 4 Amines..
TablelC3.5
Other Nitrogen-Containing Compounds
Table1C3.6
Esters
Table1Q.7
Ethers..
.i..
Table
lC3.8
Gases
Table 1Q.9
Halogenated Compounds
Table 1C3.10 Ketones..
Table 1C3.11 Sulfur-Containing Compounds.............
Table 1C3.12 Miscellaneous ...........................
....
..................... :. ...........
................ ............
..................................
.................
...............................
.....................
..................................
....................
..............................
...............................
1C4 Nonhydrocarbo-ecndary
Properties.
Table1C4.1 . Acids.
Table1C4.2AlcoholsandPhenols
Table 1C4.3 Aldehydes
Table1C4.4
Amines..
Table1C4.5’
Other Nitrogen-ContainingCompounds
Table
1C4.6
Esters
Table1C4.7
Ethers
Table
1C4.8
Gases
Table1C4.9
HalogenatedCompounds
Table1C4.10 Ketones..
Table1C4.11 Sulfur-Containing Compounds.
Table1C4.12Miscellaneous
..................................
..................................
....
..................................
.................
...............................
............
...........................
................
.........
....
Bibliography ......................................................
.....................
1CS Key to References..
i..
Table 1c5.1 Key toReferenceoHydrocarbons
Table1C5.2Key
to References-Nonhydrocarbons..
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STD.API/PETRO
T D B C H A P T E R L-ENGL 1777 m 0 7 3 2 2 7 0 05bb57L Ob7
CHAPTER 1
GENERAL DATA
1-0 INTRODUCTION
--`,,-`-`,,`,,`,`,,`---
Almost all the procedures in the API Technical Data Book
require pure component physical properties.
'Ilus chapter provides a collection of properties for many hydrocarbons and selected nonhydrocarbons. The compounds and the properties
that were selected for inclusion in this chapter are those
judged most useful for petroleum refining and associatedindustries. Further information on physical properties may be
found in the Design Institutefor Physical Properties Research
(DIPPR) Data Compilation: Tables of Properties of Pure
Compounds (8). The majority of data for the compounds in
this chapter were takenfrom the following sources (in order
of
priority):
l. DIPPR Compilation (8)
2. GPA 2145-94 (13)
3. M I Monograph Series (1-3)
4.TRC Tables (32-34,39-47)
5. Previous API Technical DateBook - Petroleum Refining(9).
Unless otherwise indicated, predictions of hydrocarbon data
were made using the current Data Book procedures. Predictions of nonhydrocarbon datawere made using DIPPRCompilation (8) procedures.
In addition to the pure component data tables (Sections IC1
through 1C4), other general information is presented in this
chapter. Section IA contains a list of constants and lists of
conversion factors. Section 1B is a list of letter symbols with
their definitions. Section 1C enumerates the property definitions with other pertinent information on the propertiesin the
data tables. Note that the footnote codes in thedata tables indicate whether data are predicted(P), extrapolated (T), experimental (no code), or if it is unknown whether the source is
predicted or experimental ( S ) . Codes such as C, G,K, and N
provide further information for experimental data points. The
key for these codes follows Table 1C4. Section IC5 is the reference key for the properties in the data tables.
For the 1994edition, 14 hydrocarbons and five nonhydrocarbons have been added to this chapter. The A P I identification
numbers for the compounds that were in the previous edition
have not been changed. However, the added compounds were
placed in the appropriate order on the physical property
tables,
causing a departure from numeric order in the tables.This departure is considered necessary for maintaining consistency
with the numbering used in other chapters.
The data contained in Tables IC l . 1 through 1C4.12 are also
available in computer readable format on tape or disk.The
data are identical except that the number of significant digits
may be different.
1997
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1-1
Not for Resale
~
~~
~~
1-ENGL 1997
S T D - A P I / P E T R OT D BC H A P T E R
m
~.
~~
0 7 3 2 2 9 0 05bb572 T T 5 D
lAl.l
TABLE l A l . l
FUNDAMENTAL CONSTANTS’
Basic Constants
Name
Velocity of light (vacuum)
Avogadro constant
Planck constant
Faraday constant
Absolute temperature of the “ice” point:
2.997925 x lo*
6.02214x lp
6.6261x lo-*’
96,485.3
C
NA
h
F
oc
273.15
491.67
To c
Tu F
32 F
Pressure-volume product for 1 mole of
a gas at O C (32F) and zero pressure
(ideal gas)
2,271.11
22.4141
2.27111 x lo6
359.039
5,276.42
units
m per sec
molecules per g-mole
(ergs) (sec) per molecule
coulombs per mole
K
deg R
joules per g-mole
(liters) (atm) per g-mole
(CUm) (Pa) per kg-mole
(CUft) (atm) per lb-mol
(CUft) (psia) per lb-moi
Derived constants
Symbol
e =-F
Electronic charge
units
1.60218 x 10”’
N*
R =-(PWGOC
Gas wnstant
To c
Boltzmann wnstant
k =-R
Sewnd radiation constant
hc
c2 = k
8.3145
1.9872
l.9859
82.058
1,545.4
10.732
62.364
0.084786
0.73024
554.99
8,314.5
coulombs
joules per (g-mole) (K)
g d per (g-mole) (K)
Btu per (lb-mole) (deg R)
(CUcm)(atm) per (g-mole) (K)
ft-lb [force] per (lb-mole) (deg R)
(psia) (CUfi)per (lb-mole)-(degR)
(mm Hg) (liter) per (g-mole) (K)
(kg per sq cm) (liter) per (g-mole) (K)
(atm) (CU ft) per (lb-mole) (deg R)
(mm Hg) (CU ft) per (lb-mole) (deg R)
(Pa) (CU m) per (kg-mol) (K)
1.38066 X
ergs
per
(molecule)
1.43877
cm-deg C
N A
--`,,-`-`,,`,,`,`,,`---
ValueName
(K)
Defined Constants
Name
Value
Symbol
Standard gravity
cal
4.1840
I.T. cal
4.1840 X 10’
4.1868
atm
Standard atmosphere
Standardmillimeter of mercury pressure
Calorie (thermochemical)
Calorie (International Steam
Tables)
Liter
mmHg
980.665
32.174
1,013,250
14.696
101,325
1
760
gQ
cal,;
1,m
atm
joules
ergs
joules
CUcm
1987
1-2
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Units
cm per sec per sec
ft per sec per sec
dynes per sq cm
psia
pascals
Not for Resale
S T D * A P I / P E T R O T D B C H A P T E R 1 - E N G L 2977
m
0 7 3 2 2 9 00 5 b b 5 9 3
931 W
1A l .1
TABLE 1Al .1 (Continued)
Conversion Factors--Engheering Units Vs. Metric Units
Value
Units
= 2.54 cm
Definition:
in.
= U.S. inch
Definiton: U.S. foot (1 ft = 12 in.)
Definition:
lb
= avoirdupois
pound
Definition:
gal
gallon
= U.S.
= 30.48 cm
= 453.59237 g
= 231 c11 in.
= 0.133680555 CU ft
= 3,785.43449 CU cm
= 3.785412 liters
=
1 I.T. cal
1 watt-hr
.
Int
Definition: I.T. = Intemationai Steam
Tables
= 4.18674 joules
= 4.18605 int joules
= 1.000654 cal
Definition: cal = thermochemical calorie
I.T.cal per g
1 Btu per lb
-
1 Btu
= 251.996 I.T. cal
Definition: Btu = I.T. British thermal
unit
”
1.8
= 1,055.040
joules
= 1,054.866int joules
= 0.293018
int watt-hr
=252.161 cal
= 0.293067 abs watt-hr
1 hP
sec
Definition: cal = thermochemical calorie
per [force]ft-lb = 550
= 745.701 watts (abs)
= 745.578 int watts
1 erg
= 1 dyne-cm
Mathematical Constants
= 3.14159
(base of natural logarithms) = 2.71828
natural logarithm (base e), log, 10 = In 10 = 2.30258509
-T
I
e
Temperature Conversions
C = (F - 32)/1.8
F = 1.8 C + 32
K = C + 273.15
R = F + 459.67
R = 1.8 K
Where:
C = degrees centigrade
F = degrees Fahrenheit
K = kelvins
R = degrees Rankine
*Values taken from,or derived from,those given in Natl. Bur.
Std.
(U.S.), CODATA Bull. N o . 63 (1986).
1-3
1987
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
--`,,-`-`,,`,,`,`,,`---
Name
1A2.1-1A2.2
TABLE lA2.1
LENGTH CONVERSIONS
To convert the numerical valueof a property expressedin one of the units in the left-hand
column ofthe table to the numerical value expressedin one of the unitsin the top row of the
table, multiply the foxmer value by the factor in the block common to both units.
Units-*
J.
Feet
Yards
0.083333
0.027778
Inches
Inches
1
Miles
Microns
Millimeters
Centimeters
Meters
,&-5
5783
25,400
25.400
2.54
0.0254
1-8939
x 10-4
3-0480
x
304.80
30.480
0.30480
10s
914.40
1.6093
X 109
1.6093
1.03
X 106
X
I
Feet
Yards
1
12
0.33333
1
3
36
Miles
I
X
10-~
X
1
1,760
63,360
5,280
I
0.91440
IV
1.6093
x l@
Kilometers
2.5400
X 10-5
3.0480
X 10-~
9.1440
91.440
X
10-~
1.6093
~
MhOIlS
Millimeters
3.2808
x 10-6
3.2808
x 10-3
1.0936
x
6.2137
1.O936
6.2137
0.032808
0.010936
0.39370
39.370
3.2808
1 .O936
3 9370
3.2808
3.9370
x
10-5
3 9370
10-2
X
x
10-~
X
10-~
10-3
10-4
1
o.1
0.001
10
1
0.01
106
1,Ooo
loo
1
0.001
lo9
106
10s
1,o00
1
1O"O
10- ~
~~
Centimeters
Meters
Kilometers
x
lv
6.2137
x 10-6
6.2137
X 10-~
0.62137
x Id
TABLE 1A2.2
AREA CONVERSIONS
To convert the numerical valueof a property expressedin one of the units in the left-hand
in one of the units in the top row of the
column of the table to the numerical value expressed
table, multiply the former value by the factor in the block common to both units.
Units4
Square
Inches
Square Feet
Square Yards
1
6.9444 x lo-'
7.7160x IO-'
Square Feet
144
1
0.11111
Square Yards
1,2%
9
1
J.
Square Inches
Acres
Square Meters
6.2726 x 106
1,550
4,840
10.764
1.1960
Square
Square
Centimeters AcresMeters
6.4516
x
929.03
2.0661 x loe4
8,361.3
0.83613
4.0469 X 10'
4.0469 X
lo'
1
43,560 1
2.4711 X lo"
1-4
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
6.4516x lo-*
1.5942 x loq7
--`,,-`-`,,`,,`,`,,`---
Not for Resale
2.2957 9.2903 x lo-'
IV
1987
~
S T D - A P I / P E T R O T D B C H A P T E R L - E N G L L997 m 0 7 3 2 2 7 0 0 5 b b 5 7 5 704 m
lA2.31A2.4
TABLE 1A2.3
VOLUME CONVERSIONS
To convert the numerical value
of a property expressed in
one of the units in the left-hand
in one of the units in the top row of the
column of the table to the numerical value expressed
table, multiply the former value by the factor in the block common to both units.
Units-*
1
5.7870
X 10-~
Cubic Feet
1,728
1
Cubic Yards
46,656
27
6.1023
3.5315
X 10-5
Cubic Inches
Cubic Centimeters
Cubic
Centimeters
2.1433
X 10-5
3.7037
2.8317
x
X
i
1
61,023
l . 6387
x lo+
2.8317
104
1.3080
x
1
x lo-*
j
7.6455
1
35.315
Cubic
Meters
16.387
1.3080
1
0.76455
x l@
I
I
1
I
lo6
1
"
x
I
Meters
Cubic
Cubic Yards
Cubic Feet
Cubic Inches
1
1
TABLE 1A2.4
LIQUID VOLUME CONVERSIONS
To convert the numerical value
of a property expressedin one of the units in the left-hand
column of the table to thenumerical value expressed
in one of the unitsin the top row of the
table, multiply the former value by the factor in the block common to both units.
Units-*
-1
Fluid
(U.S.)
7.8125
x 10-3
6.5053
x 10-3
1.8601
x 10-4
32
1
0.25
0.20817
i 9524
10-3
128
4
1
(US.)
(US.)
Gallons
(U.S.)
Imperial
Gallons
--`,,-`-`,,`,,`,`,,`---
Barrels (Oil)
1.0567
Liters
33.814
Cubic
0.033814 10567
i 10-3
Cubic
2.6417
x 10-4
~
?::x'
4.5461
0.16054 277.42
4,546.1
158.99 5.6146
9,702
1.0307
1
x
5.7870
x 10"
16.387
0.016387
3.7854
x
10-3
4.5461
x lo-3
,
0.15899
1i 6387
0.1781129.922
6.2289 7.4805
1,728957.51
28.317 1 28,317
0.028317
0.21997 0.26417
6'2898
x
61.024
0.035315
1
1,000
IX
2.1997
x 10-4
o.o61o24
x 5315
0.001
1
l x lo+
6.2898 219.97
35.315
61,024.264.17
1,OOO
l x lo6
1
1,056.7
33,814.
946.35 0.94635
0.028594
3.6047
,
0.033420
3,785.4
4 3290
0.017316 0.55411
10-3
29.574 0.029574
2i 9574
3.7854
34.973 421
x
57.75
Cubic
Meters
x lo-3
0.13368
168
5,376
Inches
0.83267
0.023809 231
1
Cubic Feet
Meters
I
1.20095
4.8038 153.72
Cubic Inches
Centimeters
(Oil)
Cubic
Centimeters
Cubic Cubic
Feet
Barrels
Gallons Imperial
(U.S.) Gallons
0.03125
Fluid Ounces
Quarts
Quarts
(U.S.)
6.2898
x 10-6
~
10-~
~~
Note: According to ASME Guides SI-1 (22) and S I 4 (23),
lml=lcucm.
1-5
1907
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
~~~
L-ENGL
S T D . A P I / P E T R OT D BC H A P T E R
~~~
~
m
L777
I1732270 0 5 b b 5 7 b bllO
1A2.5-1 A2.6
TABLE 1A2.5
MASS CONVERSIONS
--`,,-`-`,,`,,`,`,,`---
TOconvert the numerical value ofa property expressed inone of the units in the left-hand
column ofthe table to the numerical value expressed one
in of the units in the top row of the
table, multiply the former value by the factor in the block common to both units.
units-,
3.
Grains
Ounces
(Avoir)*
‘Ounds
(Avoir)
Ounces
(TroyM
’Ounds
(Troy)t
Tons
(Short)$
Tons
(Long)§
1
(Troy)t
1.7361
X 10-~
437.5
1
0.91146
0.075955
7,000
16
480
1.0971
0.068571
1
0.083333
5,760
13.166
0.82286
12
1
x lo7
32,000
2,000
29,167
2,430.6
1
0.89286
1.5680
35,840
X 10’ I
2,240
32,667
2,722.2
1.1200
1
Grams
15.432
Kilograms
x lo‘
Metric
Tons
Tons
Tons Pounds
Grams
(Short)$ (Long)§
6.376
7-1428
0.064799
X IO-^
X io-*
Ounces
Pounds
Ounces
(Avoir)* (Avoir)* (Troy)t
2.0833
1.4286
2.2857
X 10-~ X
X 10-3
1 15432
107
0.0625
14.583 1 1.2153
0.035274
2046
i 10-3
0.032151
2.2046 35.274
3.5274
2.2046
3.2151
x
x
X
lP
12’
i 10-5
4285
i lo-s
4.1143
X
10-4
2.6792
x
1.1023
lP
2.8350
0.028350 28.350
x
x lo-s
3*0612
x
10-5
453.59
31.103
o.98421
.
0.45359
4.5359
x
0.031103
3 1103
i
3.7324
0.37324 373.24
x
3.6735
X 10-4
2 6792 9.8421 1.1023
i 10-3 x 10-6 x 1 ~ - 7
1.1023 9 8421
2.6792 32.151
x 10-3
10-4
104
6 4799
2.7902
5 X i r 4 4*4643
x 10-4
Metric
Tons
6.4799
x
9.0718
x
le
x 106
9.0718
o.w718
x lo2
1.0160 1.0160
x 103
10-~
i,ooo
10-~
1
106
1
$Common in the United States and Canada.
England.
Used for ordinary commodities.
§ Common in
t Used for drugs, jewels, precious metals.
TABLE 1A2.6
DENSITY CONVERSIONS
To convertthe numerical value ofa property expressed in oneof the units in the left-hand
column of the table to the numerical value expressedin one of the units in the toprow of the
table, multiply the former value by the factor in the block common to both units.
Units-,
.1
g
cum
lb
Cu
in.
lb
Cuft
lb
gal (U.S.)
kg
cum
g
lb
CU
CU
cm
1
27.680
lb
aft
in.
62.428
0.036127
I
1
1,728
lb
gal (U.S.)
kg
8.3454
loo0
231
27,680
CU
m
0.016018
5.7870 x lo-.
1
O. 13368
16.018
0.11983
4.3290
7.4805
1
119.83
0.001
X
10-3
X
lo-’
1
0.0083454 0.062428 3.6127
1987
1-6
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
1A2.7-1A2.8
TABLE 1A2.7
PRESSURE CONVERSIONS
I
Bars
Atmospheres
'
106
1
wcm
1
1,333.2
1.01972
750.06
~
1
I
1 29.530
1.3595
1.31579
x 10-3
&-3
1
1.0332
14.696
!
735.56
¡
x 10-3
0.033421 0.033864
0.03453
33,864
lb [force]
sq in.
1
14504
1
!
I
I
I 1 3332
II
29.921
760
0.96784
'
1
1
1
I
mm Hg* at O C
in. Hg at 32 F
1
1.01325
980,670
28.959 0.98067
~
0.986923
1
, x 106
kg
j
1
0.03937
25.400
j
0.49116
1
jI
1x 16
33.900
1I
1.01325
x lfy
32.809
~
0.019337
I
1
14.223
33.457
98,066.5
0.044605
133.32
1.1330
3,386.4
1
0.43352 0.88265
1
I
1.4504
x 10-4
1
2.0360 51.715
1
0.070307
2.3066
0.068046 0.068948 68.948
1
I
--`,,-`-`,,`,,`,`,,`---
To convert the numerical valueof a property expressedin one of the units in the left-hand
column of the table to the numerical value expressed in oneof the units inthe top row of the
table, multiply the former value by the factor in the block common to both units.
6,894.7
~
ft H20at 39.2F
29,889
il
Pascals
1o.OOo
,
I
0.029889
0.029499
l x 10-5
9.86923
x 10-6
0.030479
x 10-5
I
1 22.419 7.5006
1.01972
2.9530
I
x 10-3
x 10-4
3.3456
X
2,988.98
*lTorr=lmmHg.
TABLE 1A2.8
FLOW CONVERSIONS
To convert the numerical valueof a property expressedin one of the units inthe left-hand
column of the table to thenumerical value expressed in oneof the units in the toprow of the
table, multiply the former value by the factor in the block common to both units.
Un?+
min
(u.s.)
gal (U.S.)
hr
CU
ft
sec
CU ft
-
min
hr
bbl (42)
day
liters
sec
CU m
hr
i
i
1
!
I
'
gal2S.)
cu ft
sec
2.2280
X 10-~
gal (U.S.)
hr
60
1
448.83
2.6930
7.4805
448.83
1
0.016667
0.70000
42
'
1.7500
'
X
0.029167
15.850
min
bbl (42)
hr
0.13368
1.4286
3.7133 2.2280
x 10"
X 10-~
0.016667
X
Cu ft
641.20
60
lo4
1
1
0.093576
6.4984
3.8990
x
X
CU m
-
hr sec
0.22712 0.063090 34
1.0515
0.57143
X 10'
1'5388
x
1
28.317
3.7854
X 10-3
101.94
256.47 10.686
1.6990 0.47195
1
24
0.044163
0.15899
0.041667
1
1.8401
X 10-3
6.6245
X 10-~
2.1189 0.035315 951.02
4.4029
543.44 22.643
1
3.6
6.2898 0.58858 0.0098096O. 27778
264.17 150.96
1
1987
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
0.023810
liters
-
bbl (42)
day
1-7
Not for Resale
1A2.9-1A2.10
TABLE 1A2.9
KINEMATIC VISCOSITY CONVERSIONS
To convert the numerical valueof a property expressed in one of the units in the left-hand
column of the table to the numerical value expressedin one of the units in the top row of the
table, multiply the former value by the factor in the block common to both units.
sqft
hr
Units-,
-1
sqcm
sqm
sqft
sec
sec
(Stokes)
hr
sqft
1
sqfi
3,600
1
3.345 x loz
10.76
2.990 X 10-3
1
3.875
l.076 x lo-’
0.3600
hr
WC
sq m
hr
sqcm
WC
X
(Stokes)
Id
-x
1.076X 10-~
x
Sec
(Centistokes)
9.290 x lo-’
10-~
I
Sqmx102
Sec
(Centistokes)
2.778
25.81
9.29 x 10‘
929
277.8
2.778
100
1
3.600 X 10”
0.2581
3.875 0.0100
1
TABLE 1A2.1 O
ABSOLUTE VISCOSITY CONVERSIONS
To convert the numerical value of a property expressedin one of the units in the left-hand
column of the table to the numerical value expressed inone of the unitsin the top row of the
table, multiply the former value by the factor in the block common to both units.
~~
lb
lb
hr-ft
lb [forcel-sec
sqft
hr-m
sq ft
x102
sec-cm
(Centipoises)’
kg
hr-m
1
3,600
0.03108
5,357
1,488
2.778 x
1
8.634 x 10“
1.488
0.4134
32.17
1.158X lo5
1
1.867 x
47,880
2.089 x lo-’
x
xld
SeC-Cm
(Centipoises)’
kg
lb [forcel-sec
hr-ft
Sec-ft
.1
SC-ft
lb
-
lb
Units-,
0.6720
5.801 x
2.4191 6.720
0.2778
(ak)
1.724X l@
3.600
1
* 1 poise = 100 centipoises = 1 L.
Kinematic viscosity, in centistokes, times density - at same temperature equals
centipoises.
SeC-Cm
--`,,-`-`,,`,,`,`,,`---
1-8
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
1A2.11
TABLE 1A2.11
ENERGY CONVERSIONS
To convert the numerical valueof a property expressed in one of the units in the left-hand
in one of the units in the top row of the
column of the table to the numerical value expressed
table, multiply the former value by the factor in the block common to both units.
International Calories
Joules
Units-*
1
Absolute
1
Joules
International l.m
Joules
4.1840
Calories
&:ies
9 4783
i 10-4
9 4799
0.23905 0.23889 i 10-4
2.7778
x 10-7
2.7782
0.99984 0.23901 0.23885
1
4.1833 1
0.99935
British
Thermal
Units
3 6OOO
x 106
Hours
Horsepower~ o u n X lo6
Foot-pounds
[Force]
CU ft-lb [force]
195.24
sq in.
Liter
Atmospheres
Ea$$:
I1,899.1
3.5994
x 106
x 105
2.6841 2.6845
X 106
X 105
1.3556
195.21 46.663
i 10-3
3*7257
'
1.8
453.59 453.89
10-~
10-3
X
5 1228
98706 5.2666
X 10-~
4.1292 2.2032
2.1430
x 10-2 X 1 0 - ~
4.1319 2.2046
x lo-2 X 10-~
x 10-2
2.1444
x 10-2
3'9301
X 10"
I
1.3410
2h552
x 106
18,439
35,528 1,895.7
1
1.9800
x lo6
13,750
26,494 1,413.6
6.9444
X 10-3
1.3381 7.1394
X 10-4
X 10-2
1
l.9268
5.1900
1
5.4233
x
2.8147
0.096042 x24.202
24.218 101.31 101.33
1,898.8
i
X
6.4120 6.4162 o.7457o
2,544.5
X IV
1 2851
0.32384 i0.32405
10-3
x 10-7
0.18505
5 1220
2.9307
X 10-~
8.5986 8.6042
x lcf 3,412.2
! 46.633
0.73756
0.73768
10"
1.1622 3 96571.5586
3.0860
x 10-6
x 10-6
1.5596 1.1630
3.0880
x 10-6
X 10-6
1,054.9 252.16
1,055.0 252.00 1
&lowatt-
3.7251
X 10-7
x
3.9683
1
1.0007 4.1861
4.1867
X 10-3
I.T. Calories
Centigrade
Heat
units
98690 5.2657
Absolute British
FootLiter
n e m a l Kilowatt- Horsepower- Pounds CU fi-lb[force] AtmosHours Units
pheres
[Force]
5.2752
x
10.412 0.55556
5.4039 778.16
5.0505 3.7662
X
10"
7.2727
X
3.7745
10-5
7'0741
x lo-"
X
74.735
1,400.7
o. 10281
5.3356
x lo-*
18.742 19.7269
--`,,-`-`,,`,,`,`,,`---
1987
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
~~
1-9
Not for Resale
1A2.12-1A2.13
TABLE 1A212
POWER CONVERSIONS
To convert the numerical value ofa property expressed in oneof the units in the left-hand
column of the table to the numerical value expressedin one of the units inthe toprow of the
table, multiply the former value by the factor in the block common to both units.
Btu
-
Btu
-
uni-
sec
hr
min
1
ft-lb
-
ft-lb
min
power
Horse-
1
Metric
Btu
1
60.00
Btu
0.016667
1
0.21615
12.969
i 9301
10-4
3'9846
x 10-4
7.7105
x lo-*
1.2851
X 10-3
4.6263
1
60.00
x 10-3
x 10-3
1
0.016667 0.77105
3*0303
X 10-5
3*0723
550.00
1
min
hr
ft-lb
sec
ft-lb
min
Horsepower 42.408
,
2,544.5
2,509.7
542.48
32,549
0.98632
735.50
Horsepower 41.828
Watts
0.056869 3.4117
(Absolute)
cal
0.23794
sec
sec
joules (abs)
sec
14.277
0.023580 0.023908
778.16 12.969
33,000
X
sec
I
17.584
'
I
I.T.cal
1 joules(abs)
I
nm7cL
3.0860
1.3410
AA
185.16
0.29307 0.069999 0.070
1.3558 1.3558
0.022597
10-5
i
4008
745.70 1.0139
178.23
0.32384 0.32405
i
3973
0.022597
10-3
178.11
I 0.056869 I 3.4122 I 0.73756 I 44.254
I 0.23901 1 0.23885
I 1.:
5 6108
i 10-3
745.70
x
735.50
I
5.6886
x 10-3
i 10-3
I 1i 3410
10-3 I
sec
17.584 4,1999
4.2027
! 175.79 1 175.67 I
185.28
3.0880 14.286
0.23810
cal
-
Watts
Horsepower (Absolute)
10-3
1.3596
x 10-3
4.1840
0.99935
4.1867 4.1867
1.0007
1
I1
~
1
4.1840
1
I 0.23901
0.23885I
Notes:
One boiler horsepower= 33,471.9 Btu per hr.
One standard commercial ton of refrigeration = 288,000 Btu per day.
TABLE 1A2.13
SPECIFIC ENERGY CONVERSIONS
To convert the numerical value ofa property expressed in oneof the units in the left-hand
column of the table to the numerical value expressedin one of the units in the toprow of the
table, multiply the former value by the factor in the block common to both units.
I
units+
joules (abs)
l
I
joules (int)
cal
Btu
I.T. cal
I
v
joules (ab)
g
joules (int)
g
Cal
-
0.99984
1.o002
1
4.1840 4.1833
g
I.T. cal
g
Btu
lb
1-10
1
O. 42993 0.23885 0.23901
0.23905
0.23889
O. 43000
1
0.99935
l.7988
4.1867
4.1861
1.0007
1
1.8
2.3260
2.3256
0.55592
0.55556
1
1987
--`,,-`-`,,`,,`,`,,`---
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
m
S T D * A P I / P E T R O T D B C H A P T E R 1 - E N G L 1777
0732270 O5bbbO1 838
m
--`,,-`-`,,`,,`,`,,`---
1A2.14-1A2.15
TABLE 1A2.14
SPECIFIC ENERGY PER DEGREE CONVERSIONS
To convert the numerical valueof a property expressed inone of the units in the left-hand
of the units inthe toprow of the
column of the tableto the numerical value expressed in one
table, multiply the former value by the factor in the block common to both units.
g-K
1
joules (abs)
g-K
Units-,
5joules (abs)
g-K
jouies (int)
g-K
cal
g-K
I.T. cal
cal
g-K
I.T. cal
g-K
0.23901
0.23885
joules
(int)
0.99984
1
I'
Btu
Ib-degF
0.23885
~
1
1
1.0002
n
4.1840
1
4.1833
4.1867
I
4.1861
B
Btu
lb-deg F
I
0.23905
4.1867
I
1
1
0.23889
0.99935
I
0.99935
1
1
1
1
i
1
i
I
1
1
1
1.0007
iI
4.1861
0.23889
1.0007
TABLE 1A2.15
HEAT FLUX CONVERSIONS
To convert the numerical valueof a property expressedin one of the units in the left-hand
column of the tableto the numerical value expressed in oneof the units inthe top row of the
table, multiply the former value by the factor in the block common to both units.
~
Units-,
-1
Btu
hr-sq ft
cal
sec-sq cm
kgsal
hr-sq m
watts (abs)
sq cm
joules (abs)
sec-sq m
I
Btu
,
!
1
I
I
3,170.0
2.7778 x 10"
0.31700
i
0.23901
2.3901 x
3.1546 x 10'
1
1
4.1840
36,000
1
8,604.2
O. 86042
m
sec-sq
1.1622 X 10"
~
3.1546
41,840
~
1.1622
1
10,Ooo
1 x 10"
1
1-1 1
1987
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
~
I
2.714
10-5
1
0.3684
kg-cal(abs)joules
' (abs)watts
m hr-sq
i
sq cm
1
X
13,263.
I
i
1
cm
sec-sq
7.5397
1
I
cal
Not for Resale
TABLE 1A2.16
HEAT TRANSFER COEFFICIENT CONVERSIONS
To convert the numerical valueof a property expressed in one
of the units in the left-hand
column ofthe table to the numerical value expressedin one of the units in the toprow of the
table, multiply the former value by the factor in the block common to both units.
Units-,
L
Cal
sec-sq cm-K
Btu
hr-sq ft-deg F
Btu
hr-sq ft-deg F
x 10‘
1
cal
sec-sq cm-K
kgcal
hr-sq m-K
watts (abs)
sq cm-K
joules (abs)
sec-sq m-K
watts (abs)
sq cm-K
kg-cal
hr-sq m-K
joules (abs)
sec-sq m-K
1.3571 5.6783 x lo4
4.8857
5.6783
I
7,368.4
1
36,000
4.1840
0.20468
2.7778 X 10”
1
1.1622 X lo4
l. 1622
1,761.1
0.23901
8,604.2
1
10,Ooo
0.17611
2.3901X
0.86042
1x
lo4
41.840
1
TABLE 1 A2.17
THERMAL CONDUCTIVITY CONVERSIONS
To convert the numerical valueof a property expressedin one of the units in the left-hand
one of the units in the toprow of the
column of the table to the numerical value expressed in
table, multiply the former value by the factor in the block common to both units.
1
Btu
hr-sqh-ckgFperin.
Btu
hr-sqfr-degfperft
col
sec-sqcm-Kpcran
I
r
g
d
hr-sqm-Kperm
watts (ab)
sqcm-Kpcrcm
BtU
hr-sqh-degFperin.
Btu
hr-sqft-degfperh
cal
watts (ab)
@-cal
scc-sqan-Kpcrcm
hr-sqm-Kperm
sqcm-Kpercm
joules (ab)
xc-sqm-Kperm
1
0.08333
3.4471X lo-“
12.000
1
4.1366X
1.a92
0.017307
1.7307
2,901.0
241.75
1
360
4.1840
418.40
8.0582
0.67152
2.7778 x
1
0.011622
1.1622
1
100
693.35
joules(abs)
scc-sqm-kpcrm
0.23901
57.779 86.042
2.3901 X 10-3
1-12
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
1.4423 x 10
0.5778
0.86042 6.9335
0.01
0.12410
O.14423
1
1987
Not for Resale
--`,,-`-`,,`,,`,`,,`---
Ullitgt
STD.API/PETRO
T D B C H A P T E R 1-ENGL 1997 m 0 7 3 2 2 9 0 0 5 b b b 0 3
bOO
m
161.1
TABLE 161.1
LETTER SYMBOLS FOR THE PRINCIPAL CONCEPTSUSED IN CHEMICAL ENGINEERING
--`,,-`-`,,`,,`,`,,`---
The letter symbols for the concepts most widely used in chemical engineering
are listed on
the following pages.
A letter symbol is asingle letter used to representaprimaryconcept for aphysical
quantity, and itmay be used with a subscript
or superscript. A subscript
may designate a place
in space or time, a system of units, or a constant or reference value. A superscript may
or
designate a dimensionless form, a reference or equilibrium value, a sequence in time
space, or a mathematical identification (average value, derivative, tensor index). The symbols are listed under categories whichare basic to all operations and processes. An alphabetical listing of the symbols is given in Table 1B1.2.
The list has been adapted from the official tables of the American Institute of Chemical
Engineers and of the American National Standards Institute. Suitable modifications have
been made in the units to conform with the editorial policies of the American Petroleum
Institute. Several additions have been made for symbols used frequently
in this book. Listing
is alphabetical by concept within each category. Illustrative units
or definitions are supplied
where appropraite.
General Concepts
Symbol
Unit or Definition
Acceleration . . . . . . . . a
ft per sec per sec
Of gravity.. ....... ¿?
ft per sec per sec
Acentricfactor ...... W
Base of natural
logarithms . . . . . . . . e
Coefficient.. . . . . . . . . C
Difference,finite . . . . A
Differentialoperator . d
Partial.. .......... d
Efficiency. . . . . . . . . . . tl
[force]
ft-lb
Btu;
Energy,dimension. .. E
Enthalpy.. . . . . . .index
. . . .Refractive
H
Btu
Entropy ............ S
Btu
Resistance
per
R deg
Force.. . . . . . . . . . . .stress
. . Shear
F [force] lb
FugacityCoefficient. . 4
Function.. . . . . . . . . . . C$, \Ir, x
Gas constant,
To distinguish,
use
R.
universal.. . . . . . . . . R
Gibbsfree energy. . . . G, F
G = H - TS,Temperature
Btu
Heat . . . . . . . . . . . . . . . P
Btu
A = U - TS,Btu
Helmholtz free energy A
Internal energy.. . . . . U
Btu
Mass,dimension of . . m
lb
Mechanical equivalent
of heat.
J
[force]
ft-lb
per
Watson
Btu
characteriMoment of inertia
i
factor. . . zation
Ib-ft2
Symbol
Newton lawof motion,
conversionfactorin g,
Unit or Definition
g, = malF, (lb) (ft per sec
per sec) per lb [force]
Number
Ingeneral. ........ N
Ofmoles ......... n
Pressure ............ P
Quantity,ingeneral. . Q
Radius of gyration . . . a
Ratio,
general.
in
.... R
.....
R
.........
T
lb [force] per sq ft; atm; :j
[force] per sq in. (abs)
.......... R
Temperature
Absolute. . . . . . . . . . T
Dimension of. ..... e
In general.. ....... T,t
-
logarithmicmean . . 8
lime
Dimension of. ..... T
In general.. ....... r, 7
...... K
Work.. ............. W
lb [force] per sq ft
K; deg R
deg C; deg F
difference,
deg F
sec
sec; hr
Btu
Geometrical Concepts
Symbol
Angle .............. a, 0, cb
In *,y plane. ...... a
In y , z plane. ......
In z,x plane.. ..... e
Solid angle.. ...... W
Area
Cross-section. ..... S
Fraction free crosssection ......... (T
+
Symbol
Unit or Definition
Unit or Definition
Ingeneral. ........
Projected .........
Surface
Per unit mass. ...
Per unit volume..
Linear dimension
Breadth ..........
Diameter .........
Distance along
path. ...........
1987
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
A
A,
A,, S
A,, u
sq ft per lb
sq ft per CU ft
b
D
ft
ft
S, x
ft
1-13
Not for Resale
lB1.l
TABLE 161.1 (Continued)
General Concepts-(continued)
--`,,-`-`,,`,,`,`,,`---
Height above
datum plane.. ... 2
Height equivalent.. .. H
Hydraulic radius. .. rH
Lateral distance
from datum
plane.. ......... Y
Length, distance or
dimension of.. .. L
Longitudinal distance from datum
plane.. ......... X
Symbol
Mean free path. ... A
Radius ........... r
Thickness
In general.. ..... R
Of film ......... Bf
Wavelength ....... h
Other
Particle-shape
factor .......... 4*
Volume
Fraction voids ..... E
Humidvolume .... VH
In general.. ....... V
Unit or Definition
Symbol
ft
ft (Use subscript p for
equilibrium stage and
r for transfer unit.)
ft;sqftperft
ft
ft
Unit or Definition
c m ; ft
ft
ft
ft
c m ; ft
cuftperlbdryair
cuft
ft
Intensive Roperties
Symbol
Absorptivity for
radiation. .........
Activity.. ...........
Activity coefficient,
molal basis.. ......
Coefficient of
expansion
Linear.. ........
Volumetric. .....
Compressibility
factor ............
Density.. ...........
Diffusivity
Molecular,
volumetric ........
Thermal ..........
Emissivity ratio for
radiation.. ........
Enthalpy.. ..........
Entropy ............
Fugacity ............
Gibbs free energy. ...
Heat capacity .......
At constant
pressure ........
Unit or Definition
Symbol
Unit or Definition
a
a
Y
a
ß
ftperftperdegF
CuftpercuftperdegF
z
z = pVfRT
lbpercuft
p
D,, 6
a
for
cu ft per (hr) (fi)sq
; fi
per hr
a = Wcp, sq ft per hr
c
c
BtuVapor
per lb
Btu per (lb) (deg R)
[force]
lb
per sq ft; atm
Viscosity
Btu per lb
Btu per (lb) (deg
F)
CP
Btu per (lb)
(deg
H
S
f
G, F
F)
At constant
volume .........
Heat capacities, ratio
of. ...............
Helmholtz free
energy.. ..........
Humid heat., .......
Internal energy ......
Latent heat, phase
change ...........
Molecular
weight
....
Reflectivity
radiation.. ........
Surface tension. .....
Thermal
conductivity.. .....
c.
Btu per (lb) (deg F)
Y
U
Btu per lb
Btu per (lb dry air) (deg F)
Btu per lb
A
Btu per lb
A
c,
MW
p
u
lb [force] per ft
k
Btu per (hr) (sq fi)(deg F
per ft)
Transmissivity of
radiation.. ........ T
pressure ...... P*
Absolute or coefficieat of.. ....... CL
Kinematic.. ....... v
Volume, per mole ... V
lb [force] per sq fi; atm; lb
[force] per sq in. ( a h )
lb per (sec) (ft)
sq ft per sec
CU ft per lb-mole
Symbols for Concentrations
Symbol
Absorption factor. ... A
Concentration, mass
or moles per unit
volume ........... c
Unit or Definition
A = L/KV
saturation..
At
....
At wet-bulb
temperature. ....
lb per cu ft; lb-molesperMassconcentration
of
cuft
particles ..........
Moisture content
Fraction
Equilibrium water
By volumes ....... x,
to bone dry
By weight.. ....... x ,
stock.. .........
Cumulative beyond
Free water to bonea given size ..... 4
drylb
air
dry stock .......
Humidity ........... H,YH lb per
Total water to boneAt adiabatic saturadry Stock .......
tion temperature. H,,Y, lb per lb dry air
Hw, Y, lb per lb dry air
CP
Ibpercuft
X
lb per lb dry stock
X
lb per dry stock
Xr
lb per lb dry stock
1987
1-14
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Unit or Definition
H,,Y' lb per lb dry air
Symbol
Not for Resale
181.1
TABLE 181.1 (Continued)
Symbols for Concentrations-(continued)
Unit Symbol
Definition or
Unit Symbol
Mole or mass fraction
In heavy or extract
phase.. ......... x
In light or raffinate
phase.. ......... y
Mole or mass ratio
In heavy or extract
phase.. ......... X
In light or raffinate
phase. .......... Y
Number concentration
of particles.. ...... n,
Phase equilibrium
ratio ............. K
or Definition
number per
K
CU
Relative distribution
of two components
Between two
phases in
equilibrium ...
Between
successive
stages ........
Relative humidity.. ..
Slope of equilibrium
curve.. ...........
Stripping factor. .....
ft
a
a = KJK,
P
ßn=-
HR,RH
m
S
cV4,)n
(xjxi)m+l
m = dy'ldr
S = KVIL
= y'lx
Symbols for Rate Concepts
Symbol
Unit
Definition
or
Mass transfer
coefficient
Individual.. ..... k
'
Gas film.. ...... kc
Liquidfilm. ..... kL +
Overall.. ......... K
Gas film basis ... KG
Liquid film basis . KL ,
Quantity per unit
time, in general.. .. q
Angularvelocity. W
Feed rate . . . . . . . F
Frequency ...... f, N,
Fribdon velocity. . u'
Heat transfer
rate .......... 4
Heavy or extract
phase rate . . . . L
Heavy or extract
product rate. . . B
Light or rafinate
phase rate .... V
Light or raffinate
product rate. .. D
Mass rate offlow . . W
Molal rate of
transfer. ........ N
Power ............ P
Revolutions per unit
time.. .......... n
Velocity
In general.. ..... u
Instantaneous,
local
Longitudinal
( x ) component of. u
Lateral (y)
component
of.. ...... v
Normal ( 2 )
component
of.. ...... W
Volumetric rate
of flow ..... 4
1987
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
'lb-moles per (hr) (sq ft)
(driving force)
To define driving force,
use subscript:
c for lb-moles perCU ft
p for atm
x for mole fraction
lb per hr; lb-moles per hr
u* = ( g c ~ y p ) * R ft
, per sec
Btu per hr
lb per hr; lb-moles per hr
lb per hr; lb-moles per hr
lb per hr; lb-moles per hr
lb per hr; lb-moles per hr
lb per sec; lb per hr
lb-moles per hr
ft-lb [force] per sec
ft per sec
ft per sec
ft per sec
ft per sec
CU
Symbol
Unit
Quantity per unittime,
unit area
Emissive power,
total.. ........ W
Mass velocity,
average.. ...... G
Vapor or
light
phase.. ... G, E
Liquid or
heavy
phase.. ... L,2;
Radiation, intensity of ..... I
Velocity
Nominal, basis
total CTOSSsection of
packed
vessel ...... v,
Volumetric
average. . . . . . . V , T
Quantity per unit
time, unit volume
Quantity reacted
per unit time,
reactor
volume .......
Space velocity,
volumetric . . . .
Quantity per unit
time, unit area, unit
driving force, in
general ...........
Eddy diffusivity..
Eddy viscosity.. .
Eddy thermal
diffisivity .....
Heat transfer
coefficient
Individual. ..
Overall .....
Stefan-Boltzmann
constant ..........
ft per sec; CU ft per hr
or Definition
Btu per (hr) (sq h)
G = W / & lb per (sec) (sq ft)
lb per (hr) (sq ft)
lb per (hr) (sq ft)
Btu per (hr) (sq ft)
ft per sec
CU
ft per (sec) (sq ft); ft
per sec
NR
mole per (sec)
(CU
fi)
A
CU
ft per (sec)
(CU
ft)
k
uE
sq ft per hr
sq ft per hr
aE
sq ft per hr
h
U
Btu per (hr) (sq ft) (deg F)
Btu per (hr) (sq ft)(deg F)
D
0.173 X lo-' Btu per (hr)
tiE
(SS ft)(deg R)4
--`,,-`-`,,`,,`,`,,`---
1-15
Not for Resale
1B1.l
TABLE 181.1 (Continued)
Modifying S i for Phcipal Symbols
Superscript
Remarks
Subscript
Superscript
Concept
Remarks
Subscript
Concept
-
Written over
symbol
Follows symbol
Average value
Dimensionless
form
Equilibrium
value
Fluctuating
component
+
-
Written over
small
capitals
Partial molal
quantity
(Bar)
(Plus)
Sequence in time
Followssymbol
or space
Follows symbol * (Asterisk)
(Bar)
' (Prime)
(Double
prime)
(Degree)
"
Usually applied
' (Prime)
to local
velocity
Initial or reference value
Modified form
o
(Zero)
-
Molal quantity
Follows symbol
Standard state
First derivative
. (Dot)
with respect to Written over
symbol
time
Written
over
(Double
Second derivasymbol
dot)
tive with respect to time
O
Follows symbol
Follows symbol ' (Prime)
" (Double
prime)
(Tilde)
Written over
symbol
,.2. 3. etc.
Dimensionless Numbers Used in Chemical Enginering
Condensation
number.. ......... Nc0
Unit or Definition
h v'
h v'
3;
( y ) ' (P)
In
Euler number ......
friction
Fanning
factor ............
Fourier
number.
.....
Definition
Symbol
or
Peclet number.. ..... Npr
&PD ( h p f )
f
k
Prandtl number. ..... NP,
3 or v
handtl velocity ratio . u *
-
Reynolds number..
L=
e
Lv
or k
cpD,
....
D,
F
F
PD"
Stanton number
a
or -
ru* p
Sherwood number ...
V2
Lewis number.. ..... N k
9
Schmidt number. .... N s ~ L
L3p2$gAt or L '$g At
Heat transfer factor. . jH
a
N R ~ . -.
LUP DG
Reynolds number,
local ............. Y +
U
Grashof number.. ... Nc,
a
U
-
F
aL ' gL
Graetz number ...... N G ~
..
Crl
L.
a
U*
2G2(AL)
NFo
Froude number.. .... NF,
Nusselt number..
LLlcp or-,Lu.DF
k
cpL2 Or
Mass transfer factor..
Unit
--`,,-`-`,,`,,`,`,,`---
Symbol
.....
Ns,
Vapor condensation
number. .......... Nc,,
_h. _
h
cpu ' CG
L 'p'g X
kpAt
23
jM
NNu
.
k'k
Note: Pounds mass is abbreviated as lb and pounds force as Ib[force]
1-16
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Not for Resale
181.1
TABLE 1 61.2
ustic
U
A
b
Primary
Concept
Subscript
Concept
Acceleration
Activity
Area, alternate for
Surface per unit volume
Absorption factor
Area
Helmholtz free energy
Breadth
Primary Concept
Adiabatic
Arithmetic
Absolute
Area basis
Component A
Z
j
J
k
K
L
m
Subscript Concept
Generalized
component
Interface
Internal or inner
1
Base
Normalboilingpoint
B
Black body
Heavy product rate
Thickness
Boiling point
Component B
C
Concentration, mass or moles Concentration basis
Contraction
volume
unit per
Specific heat, heat capacity
Conversion factor
Critical
Cutoff size
C
Coefficient
Component C
d
Differential operation
Discharge
Disperse
Drop
Dry
D
Component
Diameter
D
Diffusivity
Distillate
Light or raffinate product rate
e
Base of natural
logarithms
Effective
Exit
E
Component E
Energy
Dimension of
Eddy
Entrainment
In general
Frequency
f
Friction factor, Fanning
Fluid
Fugacity
Friction
F
Feed rate
Feed
Force
Gibbs free energy
Acceleration of gravity
Gage
g
Gravity
Vapor
G Gibbs freeVapor
energy
basisfilm
Vapor
velocity
Mass
In general
Of vapor
h
Individualcoefficient of heat Heat
transfer
H
Enthalpy
Heat basis
Humidity
equivalent
Height
Humidity
Intensity of radiation
Moment of inertia
Transfer
factor
Generalized
component
Mechanical
equivalent of heat
Masstransfercoefficient,individual
Quantityperunittime,unit
area, unitdrivingforce, in
general
Thermal conductivity
Watson
characterization
factor
Mass transfer coefficient,
overall
Phase concentration ratio
Heavy or extractphaserate
Liquid
Length
Liquid film basis
Mass velocityof liquid or heavy
phase
Mass
Mass
Dimension of
Mean
In general
Slope of equilibrium curve
M
Mass basis
Molecular
MW Molecularweight
n
N
Number
concentration
Number of moles
Refractive index
Revolutions per unit time
Molal rate
Number, in general
O
O
p
Pressure
P
Power
PC
q
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IN CHEMICAL ENGINEERING
--`,,-`-`,,`,,`,`,,`---
ALPHABETICAL INDEX OF SYMBOLS USED
Quantityperunittime,ingeneral
Rate of heat flow
Rate of volumetric flow
Generalized stage
number
Initial
Outer
Overall
Constant pressure
Particle
Plate or stages
Pressure basis
Projected
Pseudocritical
Rate basis
1-17
Not for Resale
1B1.2
TABLE 1B1.2 (Continued)
Primary Concept
Q
r
Heat
Quantity, in general
Radius
R
Gas constant
K
Ratio, in general
Reflux ratio
Resistance
Radius of gyration
Distance along path
Specific surface
S
S
T
U
U
V
V
W
W
X
X
Y
Y
--`,,-`-`,,`,,`,`,,`---
f
Cross-section
Entropy
Stripping factor
Temperature
lime
Absolute temperature
Temperature, in general
Longitudinal component of
local velocity
Velocity, in general
Subscript Concept
Radius or radial
Reduced
Radiation
Reactor volume basis
Relative value
Saturation
Shape
Stress
Surface basis
Cross-section basis
Solid
Solvent
Tangential
Terminal
Transfer unit or units
Constant temperature
Total
Upper
Heat transfer coefficient,
overall
Internal energy
Constant volume
Lateral component of local
Velocity basis
velocity
Volumetric
Nominal velocity
Specific volume
Vapor
Light or raffinate phase rate
Volume, in general
Volumetric average velocity
Mass basis
Mass flow rate
Wet bulb
Normal component of local
velocity
Work
Total emissive power
basis
Density
Mole fraction basis
Distance along path
Fraction
Mole or mass fraction in heavy
or extract phase
Mole ratio basis
Longitudinal distance from
datum plane
Mole or mass ratio in heavy or
extract phase
Mole or mass fraction in light
or raffinate phase
Humidity
Lateral distancefromdatum
plane
Primary
Concept
Subscript
Concept
Mass or mole ratio in light or
raffïnate phase
Compressibility factor
Height above datum plane
Absorptivity for radiation
Angle
Angle in x,y, plane
Coefficient of linear expansion
Relative distribution of two
components
between
two
phases at equilibrium
Thermal diffusivity
Coefficientof volumetric
expansion
Relative distribution of two
components between successive stages
Activity coefficient, molal
basis
Ratio of heat capacities
Differential operator, partial
Diffusivity,
volumetric
basis
Film
Difference, finite
Emissivity ratio for radiation
Fraction voids
Efficiency
Angle
Angle in z,x plane
Temperature, dimension of
Log mean temperature difference
Latent heat of phase change
Mean free path
Wavelength
Volumetric space velocity
At constant viscosity
Viscosity, absolute
Viscosity, kinematic
Density
Reflectivity for radiation
Fraction free cross-section
Stefan-Boltzmann constant
Surface tension
Shear stress
Tune, alternate for
Transmissivity for radiation
Angle
Angle in y , z plane
Fraction cumulative, larger
than a given size
Function
Fugacity coefficient
Particle factor
1987
1-18
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1c
TABLE 1Bi .2 (Continued)
Subscript Concept
Primary Concept
x
Primary
Concept
Subscript
Concept
Function
Function
JI
W
Acentric
factor
Angular frequency
Angular velocity
Solid angle
Greek Alphabet
A
a
B
ß
r
A
Y
6, d
E
E
z
5
H ‘ 1
8
0
1
K
A
M
N
Alpha
Beta
Gamma
Delta
Epsilon
Zeta
Eta
Theta
L
K
A
Y
=
5
II
ST
I
O
o
Iota
Kappa
Lambda
MU
Nu
xi
Omicron
Pi
P
p
Z
u
T
Y
u
@
9
X
P
‘
Q
T
x
d~
W
Rho
Sigma
Tau
Upsilon
Phi
Chi
Psi
Omega
SECTION 1C. PROPERTY DEFINITIONS
The data in Chapter 1 are divided into four main tables, as listed below:
IC1 Hydrocarbons-Primary Properties
1C2 Hydrocarbons-Secondary Properties
1C3 Nonhydrocarbons-Primary Properties
1C4 Nonhydrocarbons-Secondary Properties
A list of properties included in the data tables as well as a definition of the property and
any other pertinent information follows.
1. Compoundname.
2. Chemicalformula
PRIMARY TABLE PROPERTIES
3.
4.
5.
6.
Molecular weight (MW) based on IUPAC “Atomic Weights
of the Elements,” 1986 (102)
Boiling point at one atmosphere in degrees Fahrenheit.
Freezing point in air at one atmosphere in degrees Fahrenheit.
Critical properties.
--`,,-`-`,,`,,`,`,,`---
The conditions of equilibrium for coexisting vapor and liquid phases of a pure substance
are defined on a pressure-temperature diagramby the vapor pressure curve. This curve
starts
at the triple point, where vapor, liquid, and solid phasesare in equilibrium, and ends at the
critical point. As the critical point is approached by the coexisting phases, their properties
approach each other until they become identical at the critical temperature and pressure,
where a single homogeneous phase is present.
Values of critical temperature in degrees Fahrenheit, pressure in pounds per square inch
absolute, volume in cubic feet per pound, and compressibility factor are given.
Further information on critical properties is given in Chapter 4.
7 . Acentric Factor
The acentric factor is calculated from the definition:
W
=
-log pro., -1.000
Where:
W
= acentric
factor.
= the reduced vapor pressure at a reduced temperature, T,, of 0.7, P*IP,
P* = vapor pressure, in pounds per square inch absolute.
P, = critical pressure, in pounds per square inch absolute.
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--`,,-`-`,,`,,`,`,,`---
1c
-
I
T, reduced temperature, m..
T = temperature, in degree Rankine.
'T = critical temperature, in degrees Rankine.
When vapor pressure data were not available at T,= 0.7, Procedure 2Al.l
was u d .
Further information on the accnrric factor is given in Chapter 2.
8. Density of Liquids
gr
p(60 F, IWgal)
8.33718
w
h
e
r
e
:
p = liquid density.
Liquid densities at 60 F are giwn in pounds per gallon at one atmosphere when 60 F is
below the normal boiling pointor atsaturation pressure when 60 F is at or above the normal
W i g point. For compounds that are solid at 60 F, the liquid density is the liquid value
extrapolated back to 60 F.
Densities at othntemperatures can be calculated from the density at 60 F by
Where:
T = temperature, in degrees Fahrenheit.
$ (S),=coeffiaent of expansion, in degrees Fahrenheit".
API gravity is defined as:
&g API=--
U1.5
spgr
Further information on liquid density is given in Chapter 6.
9. Refractive Index of Liquids
Values of the refractive index,no, of the air saturated hydrocarbon relative to air at the
sodium D-line (S892.6A) are reponed at 77 F.
10. Vapor Pressure
Vapor pressure is the pressure at which the vapor phase of a substance is in equilibrium
with the liquid phase of that substance at a specified temperature. Values of vapor pressure
at 100 degrees F are reported in units of pounds per square inch absolute.
Further information on vapor pressure is given h.Chapter S.
11. Heat Capacity of the Liquid and Gas
Heat capacities at constant pressure are reported for the liquid and ideal gas at 60 F and
1 atm pressure. Tbesc are related to the enthalpy by:
The observed heat capacityfor a saturated liquid or vapor is C,.This may be convened to
the heat capacity at constant pressure by:
Where:
dP'ldT = the temperature derivative of the vapor pressure, in pounds per square inch
absolute per degree Rankine.
When values of the ideal gas heat capacity calculated from spectroscopic data were not
available, they were predictedby the second order method of Bcnson using the CHETAH
program (31). Heat capacities are reported in units of British thermal units per pounddegree F. For compounds wherethe normal boiling point is below 60 F, liquid heat capacity
is reported at the saturation pressure.
Further information on heat capaaty is given in Chapter 7.
1-20
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S T D . A P I / P E T R O T D B C H A P T E R 1 - E N G L 1797
0 7 3 2 2 9 0 OSbbbLL 7 8 7
--`,,-`-`,,`,,`,`,,`---
1c
u C 0 2 (gas.77F.lam)+-H
b O(gas.77F.lam)
2 2
Net hear ofcombustion is related 10 gross heat of combustion by the relacionship:
1-21
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~~~~
STD*API/PETRO TDB CHAPTER
1-ENGL
0732270 05bbbL2 b13
L777
m
1c
B r com$unds where the heat of formation was not available, the net heat of formation
was predicted by the Kcond order method of Benson using the CHETAH program (31)
&er which the heat of combustion as calculated from the definition.
Net heat of combustion at 77 F is reporredin units of British thermal units per pound. The
heat of combustion is defined as the heat c v o h d ; literefore, the values for heat of combustion in this chapter are posirivc.
Funher infomation on heat of combastion is given in chapter 14.
15. Surface Tension of the Liquid
Surface tension is the tension ahibited by the fice surfacc of a liquid.
The liquid surface tcnsion at 77 F is w e d m units of dynes per centimeter.
Fanher information on surface lcadon is giren in Chapter 10.
SECONDARY TABLE PROP16. search Number
This number is for compoundidentificationand is used only with the computerized version
of the data tables.
Parameta
17. Solubility
The solubility parameter is defined by:
AUwp
&=(F)
Where:
AU- = internal energ change on vaporiza?ion to the ideal =gis,in &mol.
-V& = liquid molar voiume at 25 C, in cm”/mol.
h approximation of the internal energy cbange yields:
6=
(T?=
-
mue:
X = heat of vaporization at 25 c, in d-rnol.
VA = liquid molar volume at 25 c, in m’/mol.
R = gas constant = 1.9872 caVmol -K.
--`,,-`-`,,`,,`,`,,`---
T = absolute temperature, 298.15 in kelvins.
The above equation was used to calculate solubility parameters in units of (Cavem')".
18. Flash Point Temperature
The flash point of a Liquid or solid is the lowest temperature at which sufficient vapor is
given off through evaporation or sublimation to fonn an ignitable mixture with the air near
the surface of the liquid or in the vessel used. Rash point temperatures are given in degces
Fahrenheit.
19. Heat of Formation
CJL.
Heat of formaion of a hydrocarbon,
in the ideal gas state is reportcd at 77 F in units
of British themal mritr per pound. Heats of formation of h e hydrocarbon in the liquid state
are related to those in tbt ideal gas State by the following equation:
AH;q
(Bnrllb) =
(BWlb)
- X (Btdb)
Where:
A = the heat of vaporization at 17 F.
To derive a liquid heat of formation of a hydrocarbon.
from a heat of combustion,
the following qnations, which neglect prcss~rcco~eCEions,can be used
A?ì?(Btdb) = AH, (net, Btullb)
1-22
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1c
22FlammabiryLimitr
Lower and upper limits of fianrmabiliry are rrponcd as volume percent in a mixrurc with airWhen e x p c x i m a ~data
~ wem not available. lower Aammabiliry limits were predicted by the
method of Shebeko et aL (361, and upper 5ammabiliry limits were pru&cudby the DPPR Compllation method ( 8 ) .
SECONDARY TABLES-HYDROCARBONS ONLY
23. Coefficient of Expansion
The coefficient of cxpansi~nis C
a
t
-
by the definition:
ß=
i(
--`,,-`-`,,`,,`,`,,`---
K=
(MeABP)
V%
Where:
MeABP = m m average
pior
nomtal boiling point for a pure component. in degrees
Ran3rinc
Funhtr infoxmadon on the Warron charautrization factor is given in Chapter2
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TABLE lCO.l
INDEX OF COMPOUNDS
CmPaJND
SEQUENCE
TABLE
NLMBER
NAME
ENTRY
TABLE
ACENAPHTHALENE
ACENAPHTHENE
ACENAPHTHYLENE
ACETALDEHYDE
ACETENE
ACENAPHTHALENE
ACENAPHTHENE
ACENAPHTHALENE
ACETALDEHYDE
ETHYLENE
471
ACETIC ACID
ACETIC ALDEHYDE
ACETIC ETHER
ACETIDIY
ACETOUE
ACETIC ACID
ACETALDEHYDE
ETHYL ACETATE
ETHYLACETATE
ACETONE
701
ACETOIIITRILE
ETHYLACETATE
VINYL ACETATE
n-PRCPYLACETATE
ACETYLENE
744
755
757
ACROLE1N
ACRIDINE
ACROLEIN
ACROLEIN
n-DODECANE
732
751
1r32
732
74
ACETCU I TRI LE
ACETOXYETHANE
1-ACETOXYETHYLENE
1-ACETOXTPROPANE
ACETYLENE
ACRALDEHYDE
ACRIDINE
ACROLE1N
ACRYLICALDEHYDE
ADAKANE 12
MTHYLIS CHLORIDW
A IR
MWFRENE TYPE 2
MLENE
ALLYLENE
ALLYL ALDEHYDE
ALLYLIC ALCOHOL
M I N I C ACID
AMINOBENZENE
1-MINOBUTANE
2-AMIYOBLlTANE
AMINOETHANE
1-MINOETHANE
2-MINOETHANOL
bete-MINOETHYL ALCOHOL
2-AMlNOlSOBUTANE
AMINOIIETHANE
l-AMINO-2-HETHYLPROPANE
2-AMlNO-2-HETHYLPROPANE
MINOPHEN
1-AMINOPRWANE
2-AMINWRWANE
AmOYlA
AMYLACETATE
n - M Y L ACfTATE
AMYL ACETICESTER
AMYL ACETIC ETHER
AMYLALCOHOL
n-AMYLALCOHOL
SeC-MYL ALCOHOL
471
729
192
729
755
T55
821
759
322
ETHYLCHLORIDE
AIR
DICHLORODfFLWRtXlETHANE
PRWADI EWE
METHYLACETYLENE
ACROLEl N
ACETONE
FORMIC ACID
ANILINE
n-BUTYLMINE
sec-BUTYLAMINE
ETHYLMINE
ETHYLNINE
WOETHANOLAHINE
WOETHANOLMINE
tert-BUTYLAMINE
IETHYLMINE
1-TYLAMINE
tert-BUTYLAMINE
ANILINE
732
821
700
747
TJ9
741
736
736
a53
853
742
735
740
742
747
1,2-PROPYLENEGLYCOL
ISWROPYLMINE
M I A
n-PENTYLACETATE
n-PENTYLACETATE
738
771
762
762
n-PENTYLACETATE
n-PENTYLACETATE
1-PENTANOL
1-PENTANOL
í!-PENTANOL
762
762
717
717
718
1-24
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472
--`,,-`-`,,`,,`,`,,`---
1CO.1
850
1997
Not for Resale
STD.API/PETRO
TDB
C H A P T E R L-ENGL L777
0 7 3 2 2 7 0 OSbbbL5 3 2 2 D
TAB= lCO.l (Continued)
1co.1
fOnpaJN0
tcrt-AMYL ALCOHOL
tert-n-AMYL ALCOHOL
AMYLENE
aLpha,bets-UYLENE
cis,bets"YLENE
ENTRY
TABLENUMBER N U ESEWENCE
2-METHYL-2-BUTANOL
2-METHYL-2-WANOL
2-WTHYL-2-BUTENE
2-WTHYL-2-WENE
cis-2-PENTENE
TABLE
R D
R D
203
203
199
~~
trans,beta"YLENE
AMYLENE
HYDRATE
AMYL
HYDROSULFIDE
n-AMYLMERCAPTAN
AMYLSULFHYDRATE
AMYLTHXMLCOHOL
ANILINE
ANHYDROL
ANHYDROUS
HYDROBROMIC ACID
ANHYDROUS
HYDROFLUORIC ACID
MO
trens-2-PENTENE
2-WTHYL-2-BUTANOL
I-PENTANETHIOL
1-PENTANETHIOL
1-PENTANETHIOL
720
841
841
841
841
767
71O
1-PENTANETHIOL
ANILINE
ETHANOL
HYDROCEN
BROMIDE
HYDRffiEN
FLUORIDE
782
785
--`,,-`-`,,`,,`,`,,`---
ANTHRACENE
TRICHLOR0FLUOK"HANE
ETHYL FORMTE
ARGON
METHYLCHLORIDE
c74
801
AUBENZENE
9-AUFLWRENE
1-AZAINDENE
1-AUNAPHTHALENE
2-AUNAPHTHALENE
PYRIDINE
DIBENZOPYRROLE
INDOLE
OUINOLINE
ISOQUINOLINE
746
750
748
AZINE
BEN2 (a) ANTHRACENE
2-BENZANINE
BENZANTHRACENE
PYRIDINE
BENZANTHRACENE
lSWUlNOLINE
BENZANTHRACENE
INDOLE
746
ANTHRACENE
ARCTON 9
ARECIUAL
ARGON
ARTIC
1-BENZAZOLE
BENZENE
BENZENE,HYDROXYBENZENOFORH
BENZENOL
BENZSNOFORM
754
m
800
749
881
480
881
480
748
335
BENZENE
PHENOL
TETRACHLORIDECARBON
PHENOL
TETRACHLORIDECARBON
724
802
R4
802
~~
BENZO (JK) FLUORENE, IDRYL
BENZOL
BENZOLENE
CHRYSENE BENZO ( a ) PHENATHRENE
BENZO ( c ) PYRIDINE
1 ,Z-BENZOPHENAWTHRENE
BENZOPHEYOL
BEYZOPYRROLE
B I BENZEME
FLUORAUTHENE
BENZENE
BENZENE
478
ISWUXNOLINE
881
CHRYSENE
PHENOL
I UDOLE
INDOLE
478
BENZENE BICARRBURET O f HYDROGEN
CiS-BICYCLOt4,4,0]DEUNE
trans-BICYCLOI4,6,OIDECANE
B 1CY
CLOHEXYL
1,1 -B I CY CLOHEXY L
BICICLOPENTADIENE
cis-OECAHYDRONAPHTHAENE
trans-DECAHYDRONAPHTHALENE
BICYCLOHEXYL
BICYCLOHEXYL
DICYCLOPENTADIENE
1997
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4T7
335
335
724
748
74a
335
184
185
183
183
319
1-25
Not for Resale
TAB= lCO.l (Continued)
1co.1
COIpQAtl)
BIETHILENE
BIHEXYL
BIISOPROPYL
BIMETHYL
BIPHENYL
1,l"BIPHENYL
BISCYCLOPENTADIENE
BIStETHOXT(l-ETHAWOL)IETHER
BIS(2-HYDROXYLETHYL) AMINE
BJSCISOPRWYLI ETHER
TABLE ENTRY W
TABLE SEQUENCE M E R
292
1,3-BUTADIENE
n-DODECANE
2,3-DIKETHYLBUTANE
ETHANE
BIPHENYL
74
13
2
3%
3%
319
852
854
BIPHENYL
DlCYCLOPENTADfENE
TETRAETHYLENE GLYCOL
DlETHANOLAHINE
DllSOPROPYL ETHER
865
292
BIVINYL
BROMINE
BUTADIENE
BUTA-1,3-DIENE
1,2-BLITADIENE
1.3-BUILSIENE
alpha,gamna-BUTADIENE
BUTAL
BUTALDEHYDE
n-BUTANAL
m
292
292
291
1,s-BUTADIENE
1,3-BUTADIENE
n-BUTYRALDEHYDE
n-BUTYRALDEHYDE
n-BUTYRALDEHYDE
292
292
731
731
731
~~
BUTANALDEHYDE
s~-BUTANAMlNE
i-BUTANE
n-BUTANE
BUTANECARBOXYLIC ACID
n-BUTYRALDEHYDE
se-BUTYLAMINE
I SOBUTANE
n-BUTANE
n-PENTANOIC ACID
731
741
5
4
t05
BUTANE, 2-HYDROXY
n-BUTANETHIOL
tert-BUTANETHIOL
2-BUTANETHIOL
n-BUIAWOIC ACID
se-BUTANOL
n-BUTANETHIOL
tcrt-BUTANETHIOL
2-BUTANETHIOL
n-BUTYRIC ACID
715
n-BUTANOL
sec-BUTANOL
t
-BUTANOL
tert-BUTANOL
n-BUTAN-1-OL
n-BUTANOL
sec-BUTANOL
tert-BUTANOL
tert-BUTANOL
n-BUTANOL
713
715
716
716
713
BUTAN-2-OL
BUfANOL - 2
2-BUTANONE
trans-2-EUTENAL
cis-2-BUTENE
tranS-2-BUTENE
1 -BUTEUE
ripha-BUTENE
BUTENYNE
BUTEN-3-YHE
n-BUTYL
1-BUTYL
n-BUTYL
í!-BUTYL
BUTYL
ACETATE
ACETATE
ALCOHOL
ALeMlOL
ALDEHYDE
1-26
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stc-BUTANOL
SM-BUTANOL
METHYL ETHYL KETONE
trans-CROTONALDEHYDE
cis-2-BUTENE
834
835
036
703
71
5
715
822
733
1%
trans-2-BUTENE
1-BIITENE
1-BUTENE
VINYLACETYLENE
VINYLACETYLENE
1%
194
194
326
326
n-BUTYL ACETATE
W B U T Y L ACETATE
n-BUTANOL
SM-BUTANOL
n-BUTYRALDEHYDE
761
761
713
71 5
731
--`,,-`-`,,`,,`,`,,`---
1997
Not for Resale
-
S T D . A P I / P E T R O T D B C H A P T E R L-ENGL L 7 7 7 M 0 7 3 2 2 7 0 0 5 b b b L 7 L T 5 m
TABLE lCO.l (Continned)
1co.1
#IwxIwD
W W Y L ALDEHYDE
n-BUTYWINE
S~-EUTYLMINE
tert-BUTYLAMINE
1-BUTYWINE
1-MYLBENZENE
n-BUTYLBENZENE
S--BUTYLEENZENE
tert-BUTYLBENZENE
n-BUTYLWEINOL
ENTRY
YAME
TABLE
n-BUTYRALDEHYDE
..
~ -- ~
I .
T
V
A YI I Y C
I
"
.
"
L
c ~ - R-..-..na.
! l l Y IA Y I Y C
BUTY
LAUIYF
tert---.
.__._.__
n-BUTY'UnINE
TABLE
SEPUENCE
731
739
741
742
739
~-MYLBEW'=Y=
n-BUTYLEEh,..,I7FYF
s"pl"wl
aru.)e.,c
W I IL m c m u x c
349
349
35 1
tert-L.,.mVLBENZENE
,,
352
0""-
1-PENT-,, auru
W E R
-.
vr -I,I
71O
n- BU
".
--`,,-`-`,,`,,`,`,,`---
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
1-27
Not for Resale
STD-API/PETRO TDB CHAPTER 1-ENGL 1 9 9 7 W 0 7 3 2 2 9 0 0 5 b b b L B O 3 1
TABLE lCO.l (Continued)
1co.1
URBON TETRACHLORIDE
CARBON TETRAFLWRIDE
URBON TRIFLORIDE
CARBONIC ANHYDRIDE
U R B O W I C OXIDE
CARBOWYL D I N I D E
URBOWYL SULFIDE
CARBOXYETHANE
CAUSTIC SDDA
CETANE
URBON TETRACHLORIDE
802
TETRAFLUORIDE
TRIFLUORWETHANE
CARBON DIOXIDE
CARBOW KYIOXXIDE
803
807
CARBON
UREA
CARBONYL SULFIDE
PROPIOIIIC ACID
SODIull HYDROXIDE
n-HEXADECANE
CHI NOL I NE
CHLOR I NE
CHLOROOIFLWROCIETHANE
CHLOROETHANE
CHLOROETHENE
WINOLINE
CHLORINE
QiLORODIFLWROnETHANE
ETHYL CHLORIDE
VINYL CHLORIDE
CHLOROETHYLENE
CHLOROFORM
CHLORWETHANE
CHLOROTRIFLLlORWETHANE
CHRYSENE
VINYL CHLORIDE
CHLOROFORM
METHYL CHLORIDE
CHLOROTRIFLLQRaf(ETHANE
CHRYSENE
C I NNAWENE
CINNAMINOL
CINNIUWIL
COAL NAPHTHA
m-CRESOL
TABLE
SEWENCE
NUWER
775
774
743
776
702
847
78
749
m
804
818
811
81 1
806
809
799
478
STYRENE
STYRENE
STYRENE
BENZENE
arCRESOL
384
384
384
335
726
o-CRESOL
o-CRESOL
P' CRESQL
pCRESOL
725
727
2-CRESOL
3-CRESOL
L-CRESOL
O-CRESOL
*CRESOL
D-CRESOL
727
m-CRESYLIC ACID
O-CRESYLIC ACID
P-CRESYLIC ACID
CROTONAL
trans-CROTONALDEHIDE
CROTONIC ALDEHYDE
CROTONY LENE
CROTYLALDEHYDE
CUMENE
psi -CIMENE
m-CRESOL
O-CRESOL
p-CRESOL
trans-CROTONALDEHYDE
trans-CROTONALDEHIDE
m
726
726
725
727
f33
733
733
trans-CROTONALDEHIDE
DIMETHYLACETYLENE
trans-CROTONALDEHYDE
ISOPROPYLBENZENE
1,2,4-TRIUETHYLBENZENE
324
733
342
CYCLmTANE
CYCLOHEPTANE
CYCLOHEXANE
CYCLOHEMTRIENE
CYCLOHEXENE
CICLMANE
CYCLOHEPTANE
CYCLOHEXANE
BENZENE
CYCLOHEXENE
179
146
335
315
CYCLOHEXYLBENZENE
CYCLOHEXYLMETHANE
CYCLON
CYCLONONANE
181
CYCLOOCTANE
CYCLOHEXYLBENZENE
HETHYLCYCLOHEXANE
HYDROCEN CYANIDE
CYCLOWONANE
CYCLOOCTANE
347
911
383
147
784
180
1997
1-28
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
--`,,-`-`,,`,,`,`,,`---
TABLE ENTRY W E
Not for Resale
S T D - A P I / P E T R O T D B C H A P T E R L-ENGL
T78 M
--`,,-`-`,,`,,`,`,,`---
TABLE lCO.l (Continued)
1co.1
ENTRY
TABLE
CDnPOUND
~
N W
SEWENCE
TABLE
NWBER
318
319
319
101
310
CYCLOPENTADIENE
DICYCLOPENTADIENE
DICYCLOPENTADIENE
CYCLOPENTANE
CYCLOPENTENE
CYCLOPENTADIENE
CYCLOPENTADIENEDIMER
l83-CYCLOPENTAD1ENE,DINER
CYCLOPENTANE
CYCLOPENTENE
~~~
n-DECANE
1-DECENE
n-DECYLBENZENE
n-DECYLCYCLOHEXANE
n-DECYLCYCLOPENTANE
~
~
~~~
~
~~~~~
357
356
358
358
184
185
184
185
62
n-DECANE
1-DECENE
n-DECYLBENZENE
n-DECYLCYCLOHEXANE
n-DECYLCYCLOPENTANE
1-n-DECYLNAPHTHALENE
1-n-DECYL-1,2,3,4-TETRAHYDRONAPHTHALENE
1-DECYNE
DELPHINIC ACID
DEVOTON
ACETATE
DIBENZYLIDNE, (E form)
DICHLORWIFLLOROMETHAWE
DICHLOROFLUOROHETHANE
1.1-DICHLOROETHANE
1,2-DICHLOROETHANE
768
pCrWENE
cis-DECAHYDROWAPHTHALENE
trens-DECAHYDRONAPHTHALENE
cis-DECAHYDRONAPHTHALENE
trans-DECAHYDRONAPHTHALENE
CWL
cis-DECAWDROI(AP;PIHALENE
trans-DECAHYDRWHTHALENE
cis-DECALIN
trans-DECALIN
OIBENUL (cis)
OIBENZM, (E fom)
DIBENZOFURAN
DIBENZOPYRROLE
DIBENZO
(B,D)
PYRROLE
93
CYCLOPRDPWE
TETRAHYDROFURAN
*CYMENE
O-CYMENE
pCYMENE
CYCLOPROPANE
CYCLOTETRAMETHYLENE OXIDE
m-CYMENE
O-CYMENE
p-CYNENE
279
376
168
135
1-n-DECYLNAPHTHALENE
l-n-DECYL-l,2,3,4-TETRAHYDRONAPHTHALENE
1-DECYNE
3-METHYLBUTYRIC ACID
METHYL
445
c62
334
707
753
cis-1,2-DIPHENYLETHENE
420
trens-182-DIPHENYLETHENE
421
DIBENZOFURAN
DIBENZOPYRROLE
DIBENZOPYRROLE
769
750
750
~~~~~
~~~
~
420
800
cis-1,2-DIPHENYLETHENE
DICHLORWIFLUOROMETHANE
DlCHLOROFLUOROHETHANE
1,I-DICHLOROETHANE
1,2-DICHLORMTHANE
805
815
816
-~
~~
DICHLORWETHANE
DICHLORa40WOFLUOROHETHANE
1,2-DICHLOROPROPANE
PANE
alpha,beta-DICHLOROPROPANE
DICHLORWETHANE
808
METHYL
1,2-DICHLOROPROPANE
BICYCLOHEXYL
DIETHANOLAMINE 854
856
a-DIETHYLBENZEWE360
o-DIETHYLBENZENE 359
p-DIETHYLBENZENE
O-DIETHYLBENZENE
B-DIETHYLBENZENE
p-DIETHYLBENZENE
1,l-DIETHYLCYCLOPENTANE
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
820
820
183
319
DICYCLOPENTADIENE
DIETHANOLAMINE
N,N-DIETHAWOLMETHYLMINE
m-DIETHYLBENZENE
o-DIETHYLBENZENE
p-DIETHYLBENZENE
1,2-DIETHYLBENZENE
1,3-DIETHYLBENZENE
1.4-DIETHYLBENZENE
~,~-DIETHYLCYCLOPENTANE
805
DICHLOROFLLtOROMETHANE
DICYCLOHEXANE
ADIENE
NE
05bbbL9
361
359
360
M1
127
1-29
Not for Resale
TABLE lCO.1 (Continued)
1co.1
--`,,-`-`,,`,,`,`,,`---
TABLE ENTRY N M E
CmPaJND
TABLE S E W E N C E "BER
128
19
851
cis-l82-DIETHYLCYCLWENTANE
cis-l82-DIETHYLCYCLOENTANE
DIETHYLDIMETHYLMETHE
DIETHYLENE cLYrnL
DIETHYLENE OXIDE
DIETHYL ETHER
2,3-DIMTHYLPENTANE
DIETHYLENE GLYCOL
TETRAHYDROFW
DIETHYL ETHER
768
765
DIETHYL KETONE
DIETHYL OXIDE
3,3-DIETHYLPEYTANE
DlETHYLSULFlDE
DIETHYLTHIOETHER
DIETHYL KETONE
DIETHYL ETHER
3.3-DIETHYLPENTANE
3-THIAPENTANE
3-THIAPEWTANE
a23
765
DICHLORODIFLWROWETHANE
1,l-DIFLWROETHANE
DIGLYCOLAMINE
DI HEXYL
D1CHLORQ)IFLUOROnl ' H E
I81-D1FLWROETHANE
DIGLYCOLAnINE
n-DODECANE
MEWUTHENE
800
817
SULFOLANE
YATER
2,3-DIHYDROINDENE
3-THIAPENTANE
DIETHYLENE GLYCOL
862
815
1,t-DIHYDDROACEWHTHALENE
DIHYDROBUTADIENE SULFONE
DIHYDROGEN OXIDE
2,3-DIH'IDROINDENE
2,2"D1HYDROXYDIETHYLAnINE
beta,betal-DIHYDROXYDIETHYL ETHER
DI(í!-HYDROXETHYL) AMINE
1,2-DIHYDROXYPROPANE
DIISOBUTYL
D I I S O P R O P A N O M I NE
1,3-DIISOPROPYLBENZENE
55
838
838
855
74
472
c66
838
851
854
DIETHANOLAHINE
1,2-PROPYLENE GLYCOL
~,2,3,3-TETRAMETHYLBANE
DIISOPROPYLAHINE
1,3-DI ISOPROPYLBENZENE
850
40
858
541
~~~~
1.4-DIISOPROPYLBEWZENE
m-DIISWROPYLBENZENE
p-DIISOPROPYLBENZENE
ETHER
DI ISOeROPYL
DI ISOPIIWYL OXIDE
1,4-DIISOPROPYLBENZENE
1,3-DIISOPROPYLBENZENE
1,4-DIISOPROPYLBENZENE
DIISOPROPYL ETHER
DIISOPROPYL ETHER
D I METHY L
DIMETKYLACETIC ACID
DIMETHYLACETONE
DIMETHYLACETYLENE
t?rDIHETHYLBENZENE
O-DIMETHYLBENZENE
p-DIHETHYLBENZENE
1,2-DIHETHYLBENZENE
1.3-DIMETHYLBENZENE
184-DIMETHYLBENZENE
2,3-DIWETHYL-l83-BUT~1ENE
2,2-DItETHYLBUTANE
2,3-DIKETHYLBANE
1,3-DIHETHIl BUTANOL
2,3-DIHETHYL-l-BUfENE
2,3-DIMETHYL-2-BUTENE
3.3-DIMETHYL-1-BUTENE
DIMETHYLCARBINOL
1,l-DIHETHYLCYCLOHEXAWE
cis-1,2-DIMETHYLCYCLOHEXANE
71
542
541
542
M5
865
ETHANE
2"ETHYLPROPIONIC ACID
DIETHYL KETONE
DIMETHYLACETYLENE
mXYLENE
2
704
a23
324
339
O-XYLENE
p-XYLENE
o-XYLENE
m-XYLENE
D-XYLENE
338
U0
338
339
u0
2,3-D1CIETHYL-l83-BUTAOIENE
300
í!,2-DIMETHYLBUTANE
2,3-DIHETHYLBANE
4-MTHYL-2-PENTANOL
2,3-DIMETHYL-l-BUTENE
12
13
723
218
Z83-DIUETHYL-2-BUTENE
3,3-DIMETHYL-l-BUTENE
ISOPROPANOL
1,l-DIMETHYLCYCLOHEXANE
CiS-1,2-DIHETHYLCYCLOHExANE
1-30
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
~
220
219
2
149
150
1997
Not for Resale
S T D * A P I / P E T R O TDB C H A P T E R L-ENGL L777
TABLE lCO.l (Continued)
1c0.1
TABLE ENTRY
NAHE
TABLE
SEWENCE
NLUBER
151
152
153
151
155
104
105
106
107
108
1,l-DIMTHYLCYCLWENTANE
cis-1,2-DIMTHYLCTCLOPEWTAIlE
trerrs-l,2-DIIIETHYLCYCLWENTANE
cis-1,3-DI)(ETHYLCYCLOPENTANE
trans-l,3-DlMETHYLCYCLOPENTANE
c~s-~,~-DICQTHYLCYCLWROPANE
trans-l,2-DlNEl~LCYCL~AE
96
cis-l,2-DIHETHYLCYCLOPRWANE
trarrs-1,2-D1HETHYLCCLœRWANE
97
829
290
DlWETHILDlSULFlDE
DIWTHYLENEllETHANE
1,l-DIMETHYLEIHANETHIOL
2,3-DITHIABOTANE
PROPADIEYE
tcrt-BUTMETHIOL
1,1-DIMETHYLETHANOL
DIMETHYL ETHER
DICIETHYL ETHER of POLYETHYLENE GLYCOL
1,1-DIMETHYLETHYLAMINE
DI(1-ME1HYLETHYL)MlNE
ttrt-BUTANOL
DIMETHYL ETHER
SELEXOL
tert-BUTYLAMINE
DIISOPROPANOLMINE
716
763
tert-BUTYLBENZENE
1,2-DIM€THYL-3-ETHYLBENZENE
1,2-DlMETHYL-4-ETHYLBENZENE
1,3-DIMETHYL-2-ETHYLBENZENE
1,3-DlU€THYL-4-ETHYLBENZENE
352
362
363
364
(1,l-DIMETHYLETHYL) BENZENE
1,2-DlMETHYL-3-ETHYLBENZENE
1,2-DIHETHYL-4-ETHYLBENZENE
1.3-DIMETHYL-2-ETHYLBEWZENE
1,3-DIHETHYL-4-ETHYLBENZENE
~~
1,3-DI~THYL-5-EflnLBENZENE
1,4-DlMETHYL-2-ETHYLBENZENE
DIMETHYL ETHYL CARBINOL
1,1-DIMETHYLETHYLCYCLOHEXANE
1,1-DIMETHYL-2-ETHYLCYCLOPEYTAWE
cis-1,2-DIMETHYLETHYLENE
tram-1,2-DIHETHYLETHYLENE
1,l-DIMETHYL ETHYL ETHYL ETHER
2,2-DIMETHYL-3-ETHYLPENTANE
2,~-DIMETHYL-3-ETHYLPENTANE
~~
~
835
863
742
858
~~
M5
-
1.3-DIMETHYL-5-ETHYLBENZENE
1,4-DIMETHYL-2-ETHYLBENZENE
2-METHYL-2-BUTANOL
tert-BUTYLCYCLOHEXANE
1,1-DIMETHYL-2-ETHYLCYCLOPENTANE
cis-2-BUTENE
trans-2-BUTENE
ETHER ETHYL
tert-BUTYL
2,2-DIMETHYL-3-ETHYLPENTANE
2,4-DIMETHYL-3-ETHYLPENTANE
DIMETHYLETHYNE
DIMETHYLFWLDEHYDE
DIMETHYL F O R W I D E
N,N-DIWETHYLFORKAMIDE
2,6-DIMETHYL-1,5-HEPTADIENE
N,N-DIMETHYLFORMAHIDE
Y,W-DSMETHYLFORWlDE
2,6-DIMETHYL-l ,S-HEPTADIENE
2,2-DIMETHYLHEPTANE
2,6-DIMETHYLHEPTANE
2,Z-DIMETHYLHEXANE
2,3-DIMTHYLWE
2,4-DlMETHYLHEXANE
2.2-DIMETHYLHEPTANE
2,6-DIHETHYLHEPTANE
2,2-DlMETHYLHEXANE
2,3-DIMETHYLHEXANE
2,4-DlMETHYLHEXANE
DIMETHYLACETYLENE
ACETOIlE
~~
~
~
366
367
R0
161
129
195
893
56
57
324
821
859
859
308
46
47
28
29
30
31
32
33
276
272
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
--`,,-`-`,,`,,`,`,,`---
Not for Resale
1-31
~~
STD.API/PETRO
TDB
CHAPTER L-ENGL L977 m 0 7 3 2 2 9 0 0 5 b b b 2 2 S b 2 m
TABU3 lCO.1 (Continued)
1co.1
TABLE ENTRY N M
twwuwD
TABLE
SEWENCE
2,3-DIMETHYL-2-HEXENE
2,4-DIIQTHYL-3-ISOPROPYL PENTANE
ACETONE
ACETaE
N,N-DXUETHYLFORIUntDE
2,3-DIMETHYL-2-HEXENE
2,4-DIHETHYL-3-ISOPROPYL PENTANE
DIMETHYLKETAL
D I E T H Y L KETONE
N.N-DI(QTHYUIETIMLIAXDE
DIETWLHETHANE
6,6-DIHETHYL-2-IQTHYLENEBICYCLOC3,1 ,l )HEPTANE
2,4-DIMETWL-3-(1-CnTHYLETHYL~PENT~E
D I E T H Y L -FIDE
l82-DIMETHYLI(APIIT€"€
PROPANE
beta-PINENE
2,4-DIMETHYL-3-ISOPRaPYLPENTANE
D I E T H Y L SULFIDE
1,Z-DIIIETHYLNAPIITWLElE
M E R
2A
R
821
821
859
3
321
72
a29
632
433
553
554
309
501
67
18
19
20
21
244
2,3-DIETHYL-l-PENTENE
2,3-DIMETHYL-2-PENTENE
2.4-DIETHYL-1-PENTENE
2,4-DI~THYL-2-PENTENE
3,3-DIMElHYL-l-PENTENE
249
245
250
246
247
25 1
252
240
253
trans-4.4-DlMETHYL-2-PENTENE
2,2-DlMETHYLPROPANE
2,2-DlMETHYL-l-PROPANOL
DIMETHYL SULFIDE
DIHETHYLSLILFOXIDE
~
~~~~
2,2-DlMETHYL-1,2,3,4-TETRAH~RONAPHT~LEYE
2,6-01METHYL-1,2,3,4-TETRAHYDRONAPHTHALENE
6,7-DIMETHYL-1,2,3,4-TETRAHYDRONAPHTHALENE
D I E T H Y L THIOETHER
D I PHENY
L
DIPHENYLACETYLENE
1,2-DIPHENYLBENZENE
1.3-DIPHENYLBENZENE
1.4-DIPHENYLBENZENE
DIMETHYL SULFOXIDE
2,2-DIMETHYL-l,2,3,4-TETRAHYDRONAPHTHALENE
2,6-DIHETHYL-1,2,3,4-TETRAHYDRONAPHTHALENE
6,7-DSnETHYL-1,2,3,4-TETRAHYDRONAPHTHALENE
DIMETHYL SULFIDE
NITROUS OXIDE
NITROUS OXIDE
NITROGEN TETRAOXIDE
SULFOLANE
SULFOLANE
BIPHENYL
DIPHENYLACETYLENE
1.2-DIPHENYLBENZENE
1.3-DIPHENYLBENZENE
1.4-DIPHENYLBENZENE
1-32
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
a
722
829
861
~
DIMETHYLSULPMOXIDE
DIWITROGEN HONOXIDE
DIWITROGEN OXiDE
DINITROCEN TETRAOXIDE
1.1-DIOXIDE TETRAHYDROTHIOFURAN
DIOXDTHfOUN
254
861
449
450
451
829
791
791
793
862
1162
396
c23
424
425
426
--`,,-`-`,,`,,`,`,,`---
~
trans-4,4-DIMETHYL-2-PENTENE
NEOPENTANE
2,2-DlHETHYL-l-PROPANOL
SULFIDE
DIWETHYL
DIMETHYL SULFOXIDE
1997
Not for Resale
~
S T D - A P I I P E T R O TDB CHAPTER L - E N G L L777 W 0 7 3 2 2 7 0 0 5 b b b 2 3 4T7 W
TBLE lCO.l (Continued)
1co.1
TABLE ENTRY WAnE
--`,,-`-`,,`,,`,`,,`---
p-DIPHENYLBENZENE
1,l-DIPHENILBUTANE
1,1-DIPHENYLDEUNE
1,l-DIPHENYLDODECANE
DIPHENYLENEIHINE
DIPHENYLENIWIDE
1,1-DIPHENYLETHANE
1,2-DIPHEYYLETHANE
1,2-DIPHEMYLETHEYE (2 FORM)
cis-f,2-DIPHENYLETHENE
trsns-1.2-DIPHEWTLETHEWE
DIPHENYLETHYNE
1,l-DIPHENYLHEPTANE
1.1-DIPHEYYLHEXADECANE
1,1-DIPHENYLHEXANE
DIPHENYLUETHANE
1.1-DIPHENYLNOWAYE
1,l-DIPHENYLOCTANE
1,l-DIPHENYLPENTADECANE
1,1-DIPHENYLPENTANE
TABLE SEWENCE W E R
426
407
413
415
1,4-DIPHENYLBENZENE
1,l-DIPHENYLBUTANE
1.1-DIPHENYLDECANE
1.1-DIPHENYLDODECAWE
DIBENZOPYRROLE
750
750
DIBENZOPYRROLE
1,l-DIPHENYLETHANE
1,2-DIPHENYLETHANE
cis-1,2-DIPHENYLETHENE
ci$-1,2-DIPHENYLETHENE
403
406
420
420
trans-1,2-DIPHENYLETHENE
DIPHENYLACETYLENE
1,l-DIPHENYLHEPTANE
1,1 -DIPHENYLHEXADECANE
1,1-DIPHEYYLHEXANE
421
423
DIPHENYLHETHANE
1.1-DIPHENILNOWANE
1,l-DIPHENYLOCTANE
1,1-DIPHENYLPENTADECANE
1,1-DIPHENYLPENTANE
402
410
419
m
412
41 1
418
408
1.1-DIPHENYLPROPANE
1,2-DIPHENYLPROPANE
1,1 -DIPHENYLTETRADECANE
1,1-DIPHENYLTR1DECAWE
1,1-DIPHENYLUNDECANE
DIPROPYLMETHANE
2,3-DITHIAWANE
DITHIOCARBONIC ANHYDRIDE
DIVlNYL
DIVlNYL SULFIDE
n-DOCOSANE
n-DOOECANE
DOOECANE
1-DQ)ECENE
n-DOOECYLBENZENE
405
406
417
416
414
n-HEPTANE
2,3-DITHIABUTANE
CARBOW DSSULFIDE
1,3-BUTADIENE
THIOPHENE
n-DKOSANE
n-DODECANE
n-DOOECANE
1-DODECENE
n-DOOECYLCYCLOHEXANE
n-DODECYLCYCLOPENTANE
DRY ICE
n- 1COSANE
E
1-EICOSENE
n-DODECYLCYCLOPENTANE
CARBON DIOXIDE
n-E I COSANE
1 -E I CUSENE
n-EIWSYLCYCLOHEXANE
n-EICOSYLCYCLOPENTANE
1 ,4-€POXYEUTANE
ERYTHRENE
ETHANAL
n-EICOSYLCYCLOHEXANE
n-EICUSYLCYCLOPENTANE
TETRAHYDROFURAN
1,3-BUfADIENE
ACETALDEHYDE
ETHANE
ETHANECARBOXYLIC ACID
ETHANENITRILE
ETHANETHIOL
ETHANOIC ACID
ETHANE
PRWlONIC ACID
ACETONITRILE
ETHYL MERCAPTAN
ACETIC ACID
831
292
891
84
74
74
281
n-DODECYLBENZENE
378
n-DODECYCLCYCLOHEXANE
170
137
m
82
289
178
145
768
292
729
2
702
744
831
701
1-33
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
14
828
Not for Resale
STD.API/PETRO
T D BC H A P T E R
L-ENGL L997
TABLE 1CO.1 (Continued)
1co.1
CmPaJNO
ETHANOL
ETWOLAMINE
kta-ETHAISOUnINE
ETHENE
ETHEWYL ACETATE
ETHENYL BENZENE
1-ETHENYL ETHANMTE
ETHER
ETHER HYORotHLORIC
ETHER CURIATIC
TABLE ENTRY NANE
TABLE S
E
P
u
E
C
lE W E R
ETHANOL
)KIWOETHAIIOLWINE
MONOETHANOLMIWE
ETHYLENE
VINYL ACETATE
71O
853
853
STYRENE
VINYL AEETATE
DIETHYL ETHER
ETHYL EWLORlDE
ETHYL CHLORIDE
384
757
765
818
818
ACETYLENE
DIETHYL ETHER
ETHYL ACETATE
n-BUTYRlC ACID
ETHYL ACETATE
ETHI NE
ETHOXYETHANE
ETHYL ACETATE
ETHYL ACETICACID
ETHYL ACETIC ESTER
322
765
755
703
755
METHYL-n-PROPYL KETONE
ETHYUCETYLENE
ETHANOL
ACETALDEHYDE
ETHYLAUINE
ETHYUtETOWE
ETHYLACETYLENE
ETHYL ALCOHOL
ETHYL ALDEHYDE
ETHYLAHINE
ETHYLBENZENE
ETHYLBENZOL
1-ETHYL- kis-BICYCLOC4,4,01DECANEl
1-ETHYL- [trsns-BICYCLO[4,4,0lDEUNE
~-~~L-~~~s-BICYCLOC~,~,O~DECAWEI
ETHYLCYCLOBUTANE
ETHYLCYCLOHEPTANE
ETHYLCYCLOHEXANE
1-ETHYLCYCLOHEXENE
ETHYLCYCLOPENTANE
825
325
710
729
736
337
337
ETHYLBENZENE
ETHYLBENZENE
9-ETHYL- tcis-DEUHrDROIIAPHTHALENEl
9-ETHYL- ttran5-DEWHIDR~APHTHALENEl
1-ETHYL- tcis-DECAHYDROWAPHTHENEI
~
2-ETHYL- Ctrens-BICYCLO[4,4,0IDECAWEl
2-ETHYL-1-BUTENE
ETHYL-tert-BUTYL ETHER
ETHYL
ETHYL
ARBINOL
CHLORIDE
192
757
~~~~
190
191
188
~~
~~~~
1-ETHYL- Ctrans-DECAHYDRO)(APHTHALEWEl
189
2-ETHYL-1-BUTENE
217
ETHER
tert-BUTYL ETHYL
893
n-PROPANOL
711
CHLORIDE
818
ETHYLCYCLOBUIANE
ETHYLCYCLOHEPTANE
ETHYLCYCLOHEXANE
1-ETHYLCYCLOHEXENE
ETHYLCYCLOPENTANE
1O0
182
148
317
1-ETHYLCYCLOPENTENE
3-ETHYLCYCLWENTENE
ETHYLCYCLOPROPANE
1-ETHYL-cis-DECAHYDRONAPHTHALENE
~-ETHYL-~~~M-DECAHYDRONAPHTHALENE
1-ETHYLCYCLOPENTENE
3-ETHYLCYCLOPENTENE
ETHYLCYCLOPROPANE
312
9-ETHYL-cis-DEUHTDROWMHrHALEWE
9-ETHYL-tr~-DEUHIDROWAPnTHALEM
1-ETHYL-2.3-DIWETIIILBEWZEYE
9-ETHYL-cis-DECAHYDROIIAPHTHALENE
9-ETHYL-trwrs-DEUH~R~~HT~LENE
1 03
~~
313
1-ETHYL-trens-DECAHYDROWAPHTHALENE
~
ETHYLDIMETHYLMTHANE
ETHYLENE
1,2-DlMETHYL-3-ETHYLBENZENE
ISWENTANE
ETHYLENE
ETHYLENE CHLORIDE
ETHYLENE DICHLORIDE
ETHYLENE DIGLYWL
ETHYLENE FLUORIDE
ETHYL ETHANOATE
1,2-DICHLOROETHANE
1,2-DICHLOROETHANE
DIETHYLENE GLYCOL
1,l-DIFLUOROETHANE
ETHYL ACETATE
~-
190
191
362
7
192
816
816
85 1
817
755
1997
1-34
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
95
188
189
--`,,-`-`,,`,,`,`,,`---
1-ETHYL-cis-DECAH~RONAPHTHALENE
Not for Resale
TABLE lCO.l (Continued)
1co.1
TABLE ENTRY W
_ _ _ _ ~
~
l-ETHYL-2-ElMENYL BENZENE
1-ETHYL-3-ETHENYL BENZENE
1-ETHYL-6-ETHENYL BENZENE
ETHYL ETHER
ETHYLETHYLENE
~~
~~~~
~
~
--`,,-`-`,,`,,`,`,,`--~~~
NTENE
TENE
ETHYL KETONE
ETHYL MERCAPTAN
ETHYL
o-ETHYLMETHYLBENZENE
p-ETHYLMETHYLBENZENE
MERCAPTAN
7%
45
27
269
270
271
2
830
71 O
m1
1.1-DIPHENYLETHANE
1,l-DICHLOROETHANE
1,1-DICHLORMTHANE
1,1-DIFLWROETHANE
1,l-DIFLLUROETHANE
403
815
815
817
817
DIETHYL K E T W E
ETHYL
823
830
754
343
344
WETHYLTOLUENE
345
715
sec- BUTANOL
764
HETHYL ETHYL ETHER
~
~
~
~
~
~~~
KETONEETHYLMETHYL
853
ETHYLPROPYL
alpha-ETHYLSTYRENE
ETHYL
ETHYL
l-ETHYL-1,2,3,4-TETRAHYDRONAPHTHALENE
~~~~
822
430
431
HONOETHANOLAHINE
3-ETHYLPENTANE
241
242
243
KETUNE
1-ETHYL-4-PHENYLBENZENE
DIETHYL
~~~
~
~
400
823
~~
840
2-PHENYL-1-BUTENE
IIERCAPTAN
3%
a30
838
l-ETHYL-1,2,3,4-TETRAHYDROUAPHTHALENE
448
1-35
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
71O
O-ETHYLTOLUENE
u3
p-ETHYLTOLUENE
345
2-ETHYL-1-PENTENE 2-ETHYL-1-PEKIEYE
3-ETHYL-I-PEYTENE
3-nHYL-2-PEWTENE
1-ETHYL-C-PHENYLBENZENE
ETHYL PROPIONYL
SULFHYDRATE
m2
~
ETHYL METHYL KETONE
1-ETHYLNAPHTHALENE
2-ETHYLNAPHTHALENE
ETHYLOLAMINE
3-ETHYLPENTANE
17
SULFIDE
325
819
754
ETHANOL
ETWE
ETHYL MERCAPTAN
ETHANOL
ACETIC ACID
~
HTHALENE
HTHALENE
~~
~
~~
1-ETHYL-2-METHYLBENZENE
1-ETHYL-3-METHYLBENZENE
1-ETHYL-4-METHYLBENZENE
ETHYL METHYL CARBINOL
ETHYL METHYL ETHER
HYLTOLUENE
394
765
194
3-ETHYLHEPTANE
3-ETHYLHEMNE
2-ETHYL-1-HEXENE
3-ETHYL-1-HEXENE
4-ETHYL-1-HEXENE
l,ll-ETHYLIDENEBISBENZENE
ETHYLIDEWE CHLORIDE
ETHYLIDENE DICHLORIDE
ETHYLIDENE DlFLUDRIDE
ETHYLIDENE FLUORIDE
HYLTOLUENE
W E R
392
393
ETHYLACETYLENE
ETHYL FLUDRIDE
ETHYL F W T E
PRo91ONIC ACID
ETHYL F O R W T E
ETHYL HYDRATE
ETHYL HYDRIDE
ETHYL HYDROSULFIDE
ETHYL HYDROXIDE
ETHYLIC ACID
METHANOATE
TABLE
SEQUENCE
~
~~
ETHYLETHYNE
ETHYL FLUORIDE
ETHYL FORMATE
ETHYLFORMIC ACID
ETHYLFORMIC ESTER
-
~~
1-ETHYL-2-ETHENYL BENZENE
1-ETHYL-3-ETHENYL BENZENE
1-ETHYL-C-ETHEUYL BENZENE
DIETHYL ETHER
1 -BUTENE
3-ETHYLHEPTAUE
3-ETHYLHEXME
2-ETHYL-1-HEXENE
3-ETHYL-1-HEXENE
4-ETHYL-1-HEXENE
THYL
NE
~
Not for Resale
TABLE lCO.l (Continued)
1co.1
ENTRY
TABLE
COrPQtlSO
N M
TABLE SEQUENCE W E R
ETHYLTHIOALCOHOL
ETHYLTHIOETHANE
2-ETHYLTOLUENE
&ETHYLTOLUENE
*ETHTLTOLUENE
ETHYLMERCAPTAN
3-THIAPENTANE
o-ETHYLTOLUENE
p-ETHYLTOLUENE
6-ETHYLTOLUENE
8 0
o-ElHYLfOLUENE
pETHYLTOLLlENE
~-ETHYL-wXYLENE
Z-ETHYL-p-XYI.€NE
3-ETHYL-o-XYLEHE
o-ETHYLTOLENE
pETHYLTOLUENE
343
345
4-ETHYL-&XYLENE
4-ETHYL-O-XYLENE
5-ETHYL-&XYLENE
ETHYYE
ETHYNLBENZENE
838
343
345
344
1,3-DIETHYL-2-ETHYLBENZENE
344
1,4-DI~THTL-2-ETHYLBEIlZENE
1,2-DIWETHYL-3-ETHYLBENtENE
367
1,3-DIefnUYL-4-ETH'fLBENZENE
365
1,2-DIHETRIL-4-€lHYLBENZENE
363
366
1,3-DlltETHYL-5-ETHYLBEN~NE
362
ACETYLENE
PHEYYUCETYLENE
322
422
ETHYUYLETHEME
FLUOrUIlTHEIE
FLWRENE
FLWRHYDRfCACID
FLUORINE
VINYLACETYLENE
FLWNTHENE
FLUORENE
HYDROGEN
FLUORIDE
FLUORINE
326
FLWROURBW 11
FLUOROCARBON 12
FLUORQ)ICHLORWETHANE
FLWROETHANE
FLmORn
TRfCHLOROFLWROllETHANE
DICHLORWIFLUORWETHANE
DICHLOROFLUORWETHANE
ETHYL FLWRIDE
TRIFLWROHETHANE
FLWROnETHANE
FLWROTRICHLORWETHANE
FORM4LDEHYDE
FoRnlC ACID
FORMIC ALDEHYDE
METHYL
FLUORIDE
TRICHLOROFLWROCIE'I'HANE
FORMALDEHYDE
FORMIC ACID
FORMALDEHYDE
FORMICANAUHONIDE
FORMOL
FORCIONITRILE
FORMYLDIMETHYLAMINE
FORMYLIC ACID
FORMYL TRICHLORIDE
FREOU 10
FREON 11
FREON 12
FREOU 14
477
473
785
778
810
801
?28
700
728
HYDROGEN CYANIDE
FORMALDEHYDE
HYDROGEN CYANIDE
N,N-DIMETHYLFORMAHIDE
FORMIC ACID
CHLOROFDRM
URBON TETRACHLORIDE
TRICHLOROFLWRGUETHANE
DICHLOROOIFLUOROWETHANE
URm TETRAFLUORSDE
806
802
801
800
803
~~
FREON 2U
FREON 21
MLOROFORH
DICHLOROFLWMTHANE
TRI FLWRWETHANE
DICHLORDNETHANE
1,1,1-TRIFLWROETHANE
F E W 23
FEW 30
mow
x3
FREON 1 5 U
2-FURALDEHYDE
1,1 -DI FLWROETHANE
2-FURANALDEHYDE
2- FURANURBOWAL
FURANIDINE
1-36
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
FURFURAL
FURFURAL
FURFURAL
TETRAHYDROFURAN
806
805
807
808
814
817
849
849
849
768
1997
--`,,-`-`,,`,,`,`,,`---
Not for Resale
S T D . A P I / P E T R O T D B C H A P T E R L - E N G L L997
TABLE lCO.l (Continued)
1CO.1
SEWENCE
co(IwuwDTABLE
NAHE
ENTRY
TABLE
FURFURAL
FURFURALDEHYDE
FUROL
2-FURYLHETHANAL
GEYETRW 12
W E R
FURFURAL
FURFURAL
FURFURAL
W9
W9
FURFURAL
DICHLORQIIFLUOROHETHANE
849
800
1,l-DIFLUORETHANE
ACETICACID
DICHLORODIFLWROCIETHANE
CARBOW TETRAFLUORIDE
HELIW
HELIW-3
HELIW-4
O-HELIW
p-HELIW
D
l?
800
803
m
HELILM-4
HELIUM-3
HELIUM-4
779
780
m
m
HELIW-4
HELIUM-4
HENDECANE
n-WENEICOSANE
n-HEPTAMSANE
n-UNDECANE
n-HENEICOSANE
n- HEPTACOSANE
n-HEPTADEUNE
1-HEPTADECENE
DECYLCYCLOHEXANE
817
817
1,1 -D IFLUaROETHANE
GENETRW 100
GENETROW 1 5 U
GLACIALACETICACID
HALON
HALW 14
n-HEPTADECANE
1-HEPTADECENE
n-HEPTADECYLCYCLOHEXANE
n-HEPTADECYLCYCLOPEWTANE
n-HEPTANE
1-HEPTANETHIOL
1-HEPTENE
W9
73
83
89
79
286
142
17S
n-HEPTADECYCLCYCLOPENTANE
n-HEPTANE
1-HEPTANETHIOL
1-HEPTENE
8cc
14
221
I-n-HEPTENE
n-HEPT-1-EWE
cis-2-HEPTENE
trans-2-HEPTENE
cis-3-HEPTENE
1-HEPTENE
1-HEPTENE
221
cis-2-HEPTENE
trans-2-HEPTENE
cis-3-HEPTENE
222
221
trans-3-HEPTENE
n-HEPTYLBENZENE
n-HEPTYLCYCLOHEXANE
n-HEPTYLCYCLOPENTANE
HEPTYLHYDRIDE
trens-3-HEPTENE
n-HEPTYLBENZENE
n-HEPTYLCYCLOHEXANE
n-HEPTYLCYCLOPENTANE
n- HEPTANE
225
223
224
373
165
132
14
I-n-HEPTYLNAPHTHALENE
~-~-HEPTYL-~,~,~,~-TETRAH~ORDIIAPHTHALENE
1-HEPTYNE
alpha-HEPTYLENE
n-HEUCOSANE
n-HEXACOSANE
n-HEXADECANE
1-HEXADECENE
n-HEXYLDECYLBENZENE
n-HEXADECYLCYCLOHEXANE
n-HEXADECYLCYCLOPENTANE
1,Z-HEXADIENE
1,5-HEXADIENE
2,3-HEXADIENE
HEXAHYDROBENZENE
HEXAHYDROTOLUENE
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
331
I-HEPTYNE
1-HEPTENE
n-HEXADECANE
1-HEXADECENE
n-HEXAOECY
n-HEXADECYLCYCLOHEXANE
n-HfXADECYLCYCLOPENTANE
1997
1-n-HEPTYLNAPHTHALENE
441
459
1-n-HEPTYL-1,2,3,4-TETRAHYDRONAPHTHALENE
1,2-HEXADIENE
1,s-HEXADIENE
2,3-HEXADIENE
CYCLOHEXANE
HETHYLCYCLOHEXANE
221
88
78
382
285
174
141
301
302
146
303
147
1-37
--`,,-`-`,,`,,`,`,,`---
Not for Resale
TABU lCO.l (Continued)
1 co.1
TABLE
ENTRY
NAME
TABLE
COllPOUWO
HEXAMETHYLENE
HEXAWHTHENE
n-HEXANE
1-HEXANETHIOL
n-mxAwOIC ACID
S E W E N C E “BER
146
146
CYCLOHEXANE
CYCLOHEXANE
n-HEXANE
1-HEXANETHIOL
n - H W O I C ACID
9
843
708
~~
2-HEXANOWE
HEXENE
1-HEXENE
n-HWENE
cis-2-HExEwE
trans-2-flMENE
cis-3-HEXENE
trans-3-HEXENE
n-HEXILBENZENE
n-HEXYLCYCLOHEXANE
METHYL-N-BUTYL E O N E
1 HEXENE
1 HEXENE
1 -HEXEN€
cis-2-HEXENE
--
825
204
204
204
205
206
207
208
372
164
trans-2-HEXENE
cis-3-HEXENE
trans-3-HEXENE
n-HEXYLEENZENE
n-HEXYLCYCLOHEXANE
~-
APHTHALENE
n-HEXYLCYCLOPENTANE
131
1-n-HEXYLWHTHALENE
2-n-HEXYLNAPHTHALENE
1-n-HEXYL-1,2,3,4-fEfRAHYDRONAPHTHALENE
1 -HEXYNE
n-HEXYLCYCLOPENTANE
1-n-HEXYLNAPHTHALENE
l-n-HU(YL-l,2,3,6-fETRAHYDROWAPHTHALENE
HYDROCHLORIC ACID, ANHYDROUS
HYDROCHLORIC ETHER
HYDROFURAN
HYDROCEN
HYDROGEN BROMIDE
HYDROGEN CHLORIDE
ETHYL CHLORIDE
TETRAHYDROFURAN
HYDROGEN
HYDROGEN BROMIDE
IWDROGENURBOXYLIC ACID
HYDROGEN CHLORIDE
HYDROGEN CYANIDE
HYDROGEN FLWRIDE
HYDROGEN SULFIDE
FORHIC ACID
HYDROGEN CHLORIDE
HYDROGEN CYANIDE
HYDROGEN FLUORIDE
HYDROGEN SULFIDE
HYDROXYBENZENE
1 -HYDROXYBUTANE
2-HYDROXYBUTANE
beta-HYDROXYETHYLMWINE
bis(2-HYDR0XYETHYL)ETHER
HYDROXYMETHANE
l-HYDRDXY-2-HETHYLBENZENE
1-HYDROXYPRWANE
2-HYDROXYPROPANE
3-HYDROXYPROPENE
2-HYDROXYTOLUENE
4-HYDROXYTOLUENE
n-PROPANOL
ISOPROPANOL
ACETONE
o-CRESOL
p-CRESOL
700
783
75
785
786
Not for Resale
713
715
853
851
727
714
*CRESOL
O-CRESOL
p-CRESOL
NITROUS OXIDE
n-E I COSANE
--`,,-`-`,,`,,`,`,,`---
724
726
~
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
782
709
725
l-HYDROXY-6-UETHYLBENZENE
1-HYDROXYMETHYLPROPANE
wHYDROXYTOLUENE
O-HYDROXYTOLUENE
p-HYDROXYTOLUENE
HYPONlTRWS ACID ANHYDRIDE
ItOSANE
783
81a
768
781
PHENOL
n-BUTANOL
Sec-BUTANOL
WOETHAWOLAUINE
DIETHYLENE GLYCOL
UETHANOL
O-CRESOL
m-CRESOL
p- CRESOL
I SOBUTANOL
1-HIDROXY-3-HETHYLBEWZEWE
439
440
458
330
71 1
712
821
725
R7
~
~~
R6
725
R7
791
82
TABLE lCO.l (Continued)
1co.1
DIETHANOLAHINE
2,3-DIHYDROINDENE
INDENE
INDOLE
INDENE
2,2'-IWINODIETHANOL
I NDANE
INDENE
INDOLE
INDONAPHTHENE
1-IMLENE
8Lphs-ISWMYLENE
kt8-IMLENE
201
gmIm-IsOmYLENE
2-UETHYL-1-BUTENE
3-METHYL-1-BUTENE
2-HETHYL-2-BUTENE
2-ETHYL-I-BUTENE
ISDQENTANE
201
IMLHYDRIDE
LIWBER
854
446
c63
748
463
202
203
7
I SOBUTANE
ISOBUTANOL
IWENAL
ISOBUTEWE
1-YL
ALCOHOL
ISOBIITME
I #]BUTANOL
HETHACROLEIN
ISOBUTENE
ISOBUTANOL
ISOBUfYUnIWE
I SOBUTY LBENZENE
ISOBUTYLCYCLOHEXANE
1SOBUTYLCYCLWENTANE
IM
Y LENE
lSOBUfYUnINE
ISOBUTYLBENZENE
ISOBIITYLCYCLOHEXAIIE
lSOBUfYLCYCLOPENTANE
I SOBUTENE
740
350
159
125
197
L-ETHYL-2-PENTANOL
4-WETHYL-2-PENTANOL
2,2,4-TRIHETHYLPENTANE
2-WETHYLPROPIONIC ACID
n-PROPYLBENZENE
723
R3
37
ISODIPHENYLBENZENE
ISOHEPTANE
ISOHEXANE
I SOOCTANE
ISOPENTADIENE
1,3-DIPHENYLBENZENE
2-HETHYLHEXANE
2-HETHYLPENTANE
2-HETHYLHEPTANE
2-HETHYL-1,3-BUTADIENE
425
15
IWPENTANE
ISOPENTAWOIC ACID
ISOPRENE
I SOPROPANOL
ISOPROPENYLBENZENE
ISOPENTANE
3-HETHYLBUTYRIC ACID
2-HETHYL-l,3-BUTADIENE
ISOPROPANOL
2-PROPENYLBENZENE
7
m7
299
712
387
DIISOPROPYL
ISOPROPYL
2-PROPENYL BENZENE
ISOPROPANOL
ISOPRDPYLMINE
865
ISOBUTYL !ETHYL CARBINOL
ISOBUTYLETHYLMETHANOL
ISOBUfYLTRlHETHYLETHANE
ISOBUTYRIC ACID
1 SO(UIENE
2-ISOPROWXYPROPANE
ISOPROPYL ACETATE
ACID ACETIC
ISOPROPYL
ISOPROPYL ALCOHOL
ISOPROPYLAHINE
ISOPROPYLCYCLOPENTANE
TABLE
SEWENCE
ETHER
ACETATE
ISOPROPYLBEUENE
ISOPROPYLBENZOL
ISOPROPYL CAR8lUiX
ISOPROPYLCYCLOHEXANE
ISOPRCPYLCYCLOPENTANE
ISOPROPYL ETHER
lSOPROPYLETHYLENE
ACID IWPROPYLFDRMIC
O-CYHENE1-IMPRWYL-2-METHYL BENZENE
l-ISOPROPYL-3-METHYL BENZENE
ISOPROPYLBENZENE
ISOPROPYLBENZENE
1-UTANOL
ISOPROPYLCYCLOHEXANE
ETHER
734
197
714
704
341
10
24
299
Ibo
387
712
m
342
342
714
157
110
DIISOPROPYL
3-METHYL-1-BUTENE
2-UETHYLBLITYRIC ACID
865
202
m-CYMENE
357
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
5
714
--`,,-`-`,,`,,`,`,,`---
T U L E ENTRY NAWE
706
356
1-39
Not for Resale
TABLE lCO.l (Continued)
1co.1
TABLE
ENTRY
ColpQlwD
~
N M
TABLE S E W E N C E NUIBER
~~
1-ISOPRWYL-4-HETHYL BENZENE
4-ISOPROPYL-1-METHYL BENZENE
ISOPROPYLTOLUENE
aISOPROPYLTOLUENE
O-ISdPRWYLTOLUENE
p-CYMENE
pCYMENE
pcr)lEnE
m- CYMENE
O-CYMENE
pISOPROPYLTOLUENE
IEOOUINOLINE
ISOVALERIC ACID
WRUN
KEENE
pCYMENE
IWWINOLINE
ISOPRWYLBENZENE
FORMLDEHYDE
ETHYL CHLORIDE
ACETONE
ACETONE
KRYPTON
n-DODECYLBENZENE
BIPHENYL
KETOUE PROPANE
brta-KETOPROPNE
KRYPTON
WR Y L B E N Z E N E
LEHWENE
L W L I NE
LUPROSI L
MRCAPTOETHANE
MERCAPTOHETHANE
MESITYLENE
ISOOUINOLINE
PROPIONIC ACID
ETHYL MERCAPTAN
METHYL MERCAPTAN
1,3,5-TRIMETHYLBENZENE
358
358
358
357
356
821
821
787
378
3%
881
702
830
827
368
METACETONE
METHACROLEIN
METHACRYLALDEHYDE
IIETHACKYLIC ALDEHYDE
)IETHALDEHYDE
DIETHYL KETONE
METHACROLEIN
nETHACROLE1N
METHACROLEIN
FORMALDEHYDE
a23
734
734
734
728
METHANAL
METHANE
METHANE CARBOXYLIC ACID
METHANE DICHLORIDE
METHANE TETRACHLORIDE
FORMALDEHYDE
METHANE
ACETIC ACID
DICHLOROC\ETHAWE
CARBON TETRACHLORIDE
728
1
701
METHANETHIOL
METHANE TRICHLORIDE
RETHANOIC ACID
METHANOL
METHENYL TRICHLORIDE
METHYL MERCAPTAN
CHLOROFORM
FORMIC ACID
METHANOL
CHLOROFORM
METHYLACETALDEHYDE
METHYL ACETATE
METHYLACETIC ACID
METHYLACETYLENE
METHYLACROLEIN
n-PROPIONALDEHYDE
METHYL ACETATE
PROPIONIC ACID
METHYLACETYLENE
WETHACROLEIN
2-METHYLACROLEIN
alpha-METHYLACROLEIN
M€THYL ACRILALDEHYDE
m M Y L ALCOHOL
METHYL ALDEHYDE
WETHACROLEIN
METHACROLEIN
METHACROLEIN
METHANOL
FORMLDEHYDE
METHYLALLENE
1"ETHYLALLENE
METHYLAMINE
~-METHYL-~-AMINOPROPANE
~-METHYL-2-AMINOPROPAWE
1,2-BUTADIENE
1,2-BUTADIENE
METHYLAMINE
ISOBUTYLAHINE
tert-BUTYLAMINE
--`,,-`-`,,`,,`,`,,`---
1-40
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
808
ao2
730
753
702
323
734
Tu
734
734
m
728
291
291
735
740
742
S T D . A P I / P E T R O T D B C H A P T E R L-ENGL L777
575
m
TABLE lCO.l (Continued)
1co.1
SEPUENCE
TABLE
NAHE
ENTRY
TABLE
QlnPOUND
NWBER
~~~~
4-METHYL-2-PENTANOL
E T H Y L - t e r t - N Y L ETHER
N-UETHYL-2-PYRROLIDONE
TOLUENE
TOLUENE
UETHYLAMYLALCOHOL
METHYL-tcrt-AMYL ETHER
l-C(ETHYLAUCYCLOPENlANE-2-~E
MTHYLBENZENE
METHYLBENZOL
~"ETHYL-~C~S-DEUHYDROI~APHTHALENE~
l-ETHYL-ttrarrr-DEUHYDROI1APHTHALENEl
2-UETHYL-1,3-BUTADIENE
cis- 183-PENTADIENE
2-METHYL-183-BUTADlENE
2-ETHYL- [cis-BICYCL0~4,4,OlDECANEl
2-UETHYL- [trans-BICTCLO~4,4,OlDEUWE1
ktu-METHYL BIVIWYL
cis-1-METHYL BUTADIENE
2-ETHYL BUTADIENE
2-14ETHYL-I,3-BUTADSENE
3-METHYL-1 ,í?-BUTADIENE
3"ETWYL-1,2-BUTADIENE
ISOPENTANE
METHYL n-BUTYlUTE
2-METUYL-183-BvrADIENE
3-METHYLBUTADIENE
3-IIETHYL-l,2-BUTADIENE
2-METHYLBUTANE
METHYLEUTANOATE
~
~~
767
860
336
336
186
187
299
294
299
299
298
298
7
758
~~
2-METHYLBUTANOIC ACID
3-METHYLBUTANOIC ACID
2"ETHYL-1-BUTANOL
2-METHYLBUTANOL-2
2-METHYL-2-BUTANOL
2-HETHYLBUTYRlCACID
3-UETHYLBUTYRIC ACID
2-METHYL-I-BUTANOL
2-METHYL-2-BUTANOL
2-WETHYL-2-BUTANOL
706
707
3-HETHYLBUfAN-2-OL
3-METHYL-2-BUTANOL
2-UETHYL-1-BUTENE
3-METHYL-1-BUTENE
2-UETHYL-2-BUTENE
3-METHYL-2-BUTAWOL
3-METHYL-2-BUTANOL
2-METHYL-1-BUTENE
3-ETHYL-I-BUTENE
2-METHYL-2-BUTENE
R1
R1
2-METHYL-3-BUTENE
METHYL-t-BUTYL ETHER
METHYL-tert-BUTYL ETHER
METHYL-n-BUTYL KETONE
WETHYLBUTYLSULFIDE
3-METHYL-1-BUTINE
ETHYL BUTYRATE
METHYLn-BUTYRATE
2-METHYLBUTYRIC ACID
3-METHYLBUTYRIC ACID
3-METHYL-1-BUTENE
METHYL-tert-BUTYL ETHER
METHYL-tert-BUTYL ETHER
KETONE
METHYL-n-BUTYL
2"THIAHEXANE
n-BUTYRATE
n-BUTYRATE
N-METHYL-gamna-BUTYROLACTAC(
ETHYL CARBINOL
METHYL
CHLORIDE
METHYLCYCLOBUTANE
RETHYLCYCLOHEWE
1-UETHYLCYCLOHEXENE
WTHYLCYCLWEWTAUE
1-METHYLCYCLOPEHTENE
METHYLCYCLOPROPANE
1-MTHYL-cis-DEUHRONAPHTHALENE
1-METHYL-trans-DECAHYDRONAPHTHALENE
METHYLDIETHANOLAHIWE
N-UETHYLDIETHANOLAMINE
~-~~HYL-2,3-DIHIDROINDENE
2-METHYL-2,3-01HYDROINDENE
CHLORIDE
720
720
20 1
202
203
202
766
766
826
839
3-METHYL-I-BUTYNE
METHYL
METHYL
2-METHYLBUTYRIC ACID
3-METHYLBUTYRIC ACID
329
N-METHYL-2-PYRROLIDONE
ETHANOL
UETHYL
RETHYLCYCLOBUTANE
HETHYLCYCLOHEXANE
860
1"ETHYLCYCLOHEXENE
METHYLCYCLOPENTANE
1-METHYLCYCLOPENTENE
METHYLCYCLDPROPANE
316
1-METHYL-cis-DECAHYDRONAFHTHALENE
1-METHYL-trans-DECAHYDRONAPHTHALENE
DIETHANOLAMINE
HETHYL
DIETHANOLAJ4INE
METHYL
1-METHYL-2,3-DIHYDROIWDENE
2-METHYL-2,3-DIHYDROINDENE
758
758
706
707
71O
809
W
147
102
311
94
186
187
856
856
467
468
1-41
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
719
--`,,-`-`,,`,,`,`,,`---
~~
723
Not for Resale
TAB=
lCO.l (Continued)
1co.1
#)(pq(lsp
4-ETHYL-2,3-DIHYDROINDENE
5-ETHYL-2,3-DIHYDROINDENE
l-WETHYL-1,l-DlMETHYLETHYLETHER
UETHYLENE BICHLORIDE
ETHYLENE CHLORIDE
ETHYLENE DICHLORIDE
METHYLENE GLYCOL
METHYLENE OXIDE
2-UETHYLENEPROPANAL
4,7-~THYLEUE-4,?,8,9-TET~H~ROI~ENE
TABLE ENTRY NAME
TABLE
4-METHYL-2,3-DIHYDROlNDENE
5-METHYL-2.3-DIHYDROIYDENE
METHYL-tcrt-BUTYL ETHER
DICHLORWTHANE
DICHLORWTHANE
DICHLORWTHANE
1,2-PROPYLENE GLYCOL
F-LDEHYDE
METHACROLE I N
DICYCLOPENTADIENE
S E W E N CE NUMBER
u9
470
766
808
808
808
850
na
734
319
~
1-ETHYL ETHANOL
METHYL ETUENE
l-IIETHYL-2-ETHENYL BENZENE
1-METHYL-3-ETHENYL BENZENE
HETHYL ACETATE
ISOPROPANOL
PROPYLENE
1-METHYL-2-ETHENYL BENZENE
1-UETHYL-3-ETHENYL BENZENE
I-METHYL-4-ETHENYL BENZENE
METHYL ETHER
1-METHYLETHYL ALCOHOL
1-METHYLETHYLBENZENE
4-METHYLETHYLBENZENE
l-METHYL-4-ETHENYL BENZENE
DIMETHYL ETHER
I 50PROPANOL
ISOPROPYLBENZENE
p-ETHYLTOLUENE
390
763
712
342
m-METHYLETHYLBENZENE
O-METHYLETHYLBENZENE
p-METHYLETHYLBENZENE
l-METHYL-2-ETHYLBENZENE
I-METHYL-3-ETHYLBENZENE
PETHYLTOLOENE
O-ETHYLTOLUENE
p-ETHYLTOLUENE
O-ETHYLTOLUENE
m-ETHYLTOLUENE
314
343
1-IIETHYL-4-ETHYLBENZENE
3-METHYL-2-ETHYL-l-BUTENE
1 -METHYLETHYLCYCLOHEXANE
1-METHYLETHYLCYCLOPENTAME
p-ETHYLTOLUENE
3-METHYL-2-ETHYL-l-BENE
ISOPROPYLCYCLOHEXANE
ISOPROPYLCYCLOPENTANE
345
1-METHYL-1-ETHYLCYCLOPENTANE
I-METHYL-1-ETHYLCYCLOPENTANE
111
cis-1-METHYL-2-ETHYLCYCLOPENTANE
112
113
HElIfYl E l W T E
cis-1"ETHYL-2-ETHYLCYCLOPENTANE
trans-1-METHYL-2-ETHYLCYCLOPENTANE
tram-1-METHYL-2-ETHYLCYCLOPENTANE
cis-1-METHYL-3-ETHYLCYCLOPENTANE
trans-1-METHYL-3-ETHYLCYCLOPENTANE
UETHYLETHYLENE
trans-1-UETHYL-3-ETHYLCYCLWENTANE
cis-1-METHYL-3-ETHYLCYCLOPENTANE
PROPYLENE
753
712
193
388
389
345
345
343
314
255
157
110
114
115
193
METHYLETHYLENE GLYCOL
1-METHYLETHYL ETHAWOATE
METHYL ETHYL ETHER
METHYL ETHYL KETONE
2-METHYL-3-ETHYLPENTANE
1,2-PROPYLENE GLYCOL
ISOPROPYL ACETATE
HfTHYL ETHYL ETHER
METHYL ETHYL KETONE
3-METHYL-3-ETHYLPEWT~E
METHYLETHYL SULFIDE
METHYLETHYNE
METHYL FLUORIDE
METHYL FLUOROFORM
3-ETHYL-3-ETHYLPENTANE
2-THIABUTANE
ETHYLACETYLENE
METHYL FLUORIDE
1,1,1-TRIFLUORMTHANE
35
832
323
METHYL FORMATE
2-METHYLHEPTANE
3-METHYLHEPTANE
4-METHYLHEPTANE
2-HETHYL-1-HEPTENE
752
24
25
26
760
764
822
34
810
812
264
--`,,-`-`,,`,,`,`,,`---
METHYL FORMATE
2-METHYLHEPTANE
3-METHYLHEPTANE
4-METHYLHEPTANE
2-UETHYL-1-HEPTENE
t-)(ETHIL-3-ETHYLPENTANE
850
1997
1-42
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
TABLE lCO.l (Continued)
1co.1
TABLE ENTRY NAHE
3-METHYL-1-HEPTENE
trans-3-METHYL-3-HEPTENE
4-RTHYL-1-HEPTENE
trans-6-HETHYL-2-HEPTENE
2-CIETHYL-1,S-HEXADIEYE
~~
~~~
NLMEER
265
268
266
267
305
3-ETHYL-I-HEPTENE
trens-3-METHYL-3-HEPTENE
4-CIETHYL-1-HEPTENE
trarrs-6-HETHYL-2-HEPTENE
2-HETHYL-1,5-HEXADIENE
~
Z-METHYL-2.4-HEXADXENE
2-CIEfHYLHEXAWE
3-METHYLHEXAWE
(3rs)-HETHYLHEMUE
2-METHYL-1-HEXENE
2-METHYL-2,4-HEXADIENE
2-HETHYLHEWNE
3-METHYLHEXAWE
3"ETHYLHEXANE
2"ETHYL-1-HEXENE
2-CIETHY1-2-HWENE
cis-2-HElHYL-3-HEXENE
trans-2-METHYL-3-HEXENE
3-METHYL-1-HEXENE
cis-3-HETHYL-2-HEXENE
Z-METHYL-2-HEXENE
C~S-~-METHYL-~-HEXENE
trans-2-HETHYL-3-HEXENE
3-HETHYL-1-HEXENE
cis-3-HETHYL-2-HEXENE
230
237
238
227
231
trans-3-WETHYL-2-HEXENE
cis-3-METHYL-3-HEXENE
trans-3-MElHYC-3-HEXEYE
4-METHYL-1-HEXENE
cis-4-METHYL-2-HEXENE
trans-3-HETHYL-2-HEXENE
cis-3-METHYL-3-HEXENE
trans-3-METHYL-3-HEXENE
4-METHYL-1-HEXENE
cis-4-METHYL-2-HEXENE
232
trans-4-METHYL-2-HEXENE
5-HETHYL-1-HEXENE
cis-5-METHYL-2-HEXENE
trans-5-METHYL-2-HEXENE
METHYL HrORIDE
trans-4-METHYL-2-HEXENE
5-UETHYL-1-HEXENE
cis-5-METHYL-2-HEXENE
trans-5-METHYL-2-HEXENE
METHANE
234
229
235
236
1
-
~~
METHYL HYDROXIDE
1-METHYL-4-HYDROXYEENZENE
n-CIETHYLIMIUDOIETHAWOL
n-METHYL-2,2-lMINDOIETHANOL
2,2-(UETHYLIMINO) DIETHANOL
1-HETHYLINDENE
2-METHYLINDENE
METHYL ISOBUTYL CARBINOL
PIETHYL ISOBUTYL KETONE
P-METHYLISOPROPYLBENZENE
239
240
228
233
HETHANOL
p-CRESOL
HETHYL DIETHANOLAHINE
METHYL OIETHANOLAHINE
METHYL DIETHANOLAHINE
709
727
856
856
856
I-METHYLINDENE
2-METHYLINDENE
4-WETHYL-2-PENTANOL
METHYL ISOBUTYL KETONE
P- CYMENE
464
~~
465
?23
a24
358
~~~
1-METHYL-4-ISOPROPYLCYCLOHEXANE
METHYL KETONE
METHYL MERCAPTAN
METHYL METHANE
METHYL METHANOATE
1-METHYL-4-ISOPROPYLCYCLOHEXANE
ACETONE
METHYL UERCAPTAN
ETHANE
METHYL FORMTE
162
821
1-METHYL-2-(1-METHYLETHYL)EENENE
1-METHYL-3-(l-nETHYLETHYL)BENZEWE
1-METHYL-4-(1-METHYLETHYL)BENZENE
~-~THYL-4-(1-)fETHYLETHYL)CYCLOHEXAIIE
356
357
358
1"ETHYL-4(4-WTHYLPHENYL)-BENZENE
O-CYMENE
m-CYMENE
p-CYMENE
1-METHYL-4-ISOPROPYLCYCLOHEXANE
l-WETHYL-4(4-METHYLPHENYL)-BENZENE
METHYL C(013aSULflDE
1"ETHYLNAPHlHALENE
2"ETHYLWAPHTHALENE
2-)IIETHYLNONANE
3-HETHYLNCMANE
DIMETHYL SULFIDE
1-METHYLNAPHTHALENE
2-METHYLNAPHTHALENE
2-METHYLNOWANE
3-METHYLNOWANE
162
401
1-43
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
827
2
752
--`,,-`-`,,`,,`,`,,`---
~~
TAELE
SEOUENCE
Not for Resale
TABLE 1CO.1 (Continued)
1co.1
TABLE
ENTRY
NAHE
4-METHYLNOWAIIE
S-METHYLWWAWE
2-METHYLOCTANE
3-METHYLOCTANE
4-METHYLOCTANE
4-METHYLNOWANE
S-H€THYLNONANE
2-METHYLOCTANE
3-METHYLOCTANE
4-METHYLOCTANE
NETHYLOLPROPANE
3-METHYL-l,2-PENTADIENE
HETHYLPENTANE
2-METHILWITAWE
3-METHYLPENTAYE
tt-BUTAWOL
~~~
3-IIETHYL-l,2-PENTADIENE
2-METHYLPENTANE
2-METHYLPENTANE
3"ETHYLPEYTANE
2-METHYL-4-PENlANOL
4-METHYL-2-PENTANOL
4-METHYL-2-PENTANONE
2-METHYL-1-PENTENE
2-METHYL-2-PENTENE
4-METHYL-2-PENTANOL
KETONE
ISOBUTYL
UETHYL
2-METHYL-1-PENTENE
2-METHYL-2-PENTENE
3-METHYL-1-PENTENE
cis-3-METHYL-2-PENTENE
trans-3-METHYL-2-PENTENE
4-METHYL-1-PENTENE
cis-4-METHYL-2-PENTENE
3-METHYL-1-PENTENE
cis-3-METHYL-2-PENTENE
trans-3-METHYL-2-PENTENE
214-METHYL-1-PENTENE
cis-4-METHYL-2-PENTENE
trans-4-METHYL-2-PENTENE
METHYL-tert-PENTYL ETHER
METHYLPENTYL SULFIDE
2"ETHYLPHENOL
3"ETHYLPHEWOL
trans-4-METHIL-2-PENTENE
METHYL-tert-AMYL ETHER
2-THIAHEPTANE
O-CRESOL
la-CRESOL
~~
4"ETHYLPHENOL
m-METHYLPHENOL
O-METHYLPHENOL
p-HETHYLPHENOL
1-HETHYL-2-PHENYLBENZENE
~~
cis-METHYLPHENYL-ETHYLENE
O-METHYLPHENYLOL
2-METHYL-I-PHENYLPROANE
2-METHYL-2-PHENYLPROANE
2-METHYL-1-PROPANAnlNE
2-METHYL-2-PROPANAMINE
N
N
46
209
212
210
213
214
1
215
216
767
842
725
726
~
727
pCRESOL
la-CRESOL
O-CRESOL
p-CRESOL
1-METHYL-2-PHENYLBENZENE
l-METHYL-3-PHENYLBENENE
1-METHYL-4-PHENYLBENZENE
2-PROPENYLBENZENE
2-PROPENYLBENZENE
2-PROPENYLBENZENE
O-CRESOL
1SOsUTYLBENZENE
tert-BUTYLBENZENE
ISOBUTYLBENZENE
tert-BUTYLMINE
~
2"ETHYL P R W A W E
2-METHYL-1-PROPANETHIOL
2-METHYL PROPANOIC AClD
METHYL PROPUOL
1-CIETHYLPROPANOL
726
725
727
397
~
ISOBUTANOL
I SOBUTANOL
tert-BUTANOL
I SOBUTANOL
tert-BUTANOL
398
399
387
387
u17
725
350
352
74o
742
~~~~
I SOBUIANE
2-METHYL-1-PRWANETHIOL
2-CIETHYLPROPIONIC ACID
I SDBUTANOL
SC!C-BUTANOL
1-44
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
713
304
10
10
11
~~
1-METHYL-3-PHENYLBENZENE
1-METHYL-4-PHENYLBENZENE
1-METHYL-1-PHENYL-ElHYLENE
as-METHYLPHENYLETHYLENE
2-METHYLPRWAWOL
2-METHYL PROPAN-1-OL
2-HETHYL PROPAN-2-OL
2-METHYL PROPANOL-1
2-METHYL PROPANOL-2
NlMBER
65
66
42
43
46
~
-2-PENTANOL
TABLE
SEWENCE
--`,,-`-`,,`,,`,`,,`---
ccwcuND
5
837
704
714
715
714
714
716
714
716
1997
Not for Resale
TABLJ3 lCO.l (Continued)
1co.1
SEQUENCE
TABLE
NLMBER
NAHE
ENTRY
TABLE
716
tert-BUTANOL
UfTMCROLE I N
2-METHYL-2-PROPANOL
ï?-METHYLPROPENAL
734
1-MElHYL-4-<trens-l-n-PROPENYL)BENZENE
1-M€THYL-4-(trans-l-n-PROPENYL)BENZENE
2-IIETHYLPROPENE
2"EfHYLPRWIONIC ACID
ISOBUTENE
2-HETHYLPROPIOWIC ACID
alpha-METHYLPROPIONICACID
2-HETHYLPROPYLALCOHOL
1-IIETHYLF'RWYL BENZENE
2-ETHYLPROPYL BEYZEWE
t-U€lHYLPROPIDIIC
ACID
1W A N O L
BK- BUTYLBENZENE
ISOBUTYLBENZENE
704
714
1-METHYL-2-n-PROPYLBENZENE
l-lIETHYL-2-n-PROPYLBEWENf
391
197
704
35 1
350
353
~~
I-MTHYL-3-n-PROPYLBENZENE
l-~THIL-4-n-PROPYLBENZEYE
1"ETHYL-3-n-PROPYLBENZENE
1-METHYL-4-n-PROPYLBENZENE
IS080TYLBENZENE
2-PENTAm
K~-BUTYLCYCLDHEXANE
2-WETHYLPROPYLBENZENE
METHYLPROPYLCARBINOL
1"ETHYLPROPYLCYCLOHEXANE
ISOBUTYLCYCLOHEUNE
2"ETHYLPROPYLCTCLOHEXANE
1-METHYL-1-n-PROPYLCYCLOPENTANE
1-METHYL-1-n-PROPYLCYCLOPENTANE
ISOBUTYLCYCLOPENTANE
KETONE
METHYL-n-PROPYL
N-METHYL-2-PYRROLIDONE
2"ETHYLPROPYLCYCLOPENTANE
METHYL-n-PROPYLKETONE
1-METHYLPYRROLIDINONE
trans,beta-HETHYLSTYRENE
THIMLCOHOL
DE
860
860
860
N-METHYL-2-PYRROLIDONE
2-PROPENYLBENZENE
cis-1-PROPENYLBENZENE
trens-1-PROPENYLBENZENE
860
387
860
860
860
385
386
m-METHYLSTYRENE
1-METHYL-3-ETHENYLBENZENE
389
O-METHYLSTYRENE
p-METHYLSTYRENE
METHYLSULFHYDRATE
MERCAPTAN
METHYLSULFOXIDE
SULFOXIDE
l-METHYL-l,2,3,4-TET~H~RON~~TMLENE
1-METHYL-2-ETHEWYLBENZENE
1-METHYL-4-ETHENYLBENZENE
388
METHYL
m-METHYLTOLUENE
o-METHYLTOLUENE
p-METHYLTOLUENE
METHYL
NE
mOCHLa(ETHANE
WOCHLOROETHANE
WO)(OCHLOROETHYLENE
WOCHLORWETHANE
ETHYL
159
126
125
825
N-METHYL-2-PYRROLIDONE
N-METHYL-2-PYRROLIDONE
N-METHYL-2-PYRROLIDDE
N-METHYL-2-PYRROLIDDNE
N-METHYL-2-PYRROLIDONE
N-METHYLPYRROLIDINONE
N-METHYL-alpha-PYRROLIDINONE
1-ETHYLPYRROLIDONE
N-METHYLPIRRULID0E
N-METHYL-2-PYRROLIDONE
W-IIETHYL-alpha-PYRROLlDOWE
alpha-METHYLSTYRENE
cis,beta"ETHYLSTYRENE
354
355
350
718
160
WOCHLOROTRIFLUOROnETHANE
WOWOETHANOLWINE
WOETHYLAHIWE
W))(OFLUOROOICHLOROnETHANE
WONOFLUOROTRICHLORWETHANE
METHYL
DIMETHYL
l-HETHYL-1,2,3,4-TETRAHYDRONAPHTHALENE
m-XYLENE
o-XYLENE
p-XYLENE
CHLORIDE
n-BLITYLAMINE
ETHYL
827
339
338
u0
806
739
818
VINYL CHLORIDE
ETHYL CHLORIDE
8'18
811
809
CHLOROTRIFLWRWETHANE
)IOWOETHANOLAHINE
ETHYLMINE
DICHLOROFLWRWETHANE
TRICHLOROFLLtORWETHANE
853
736
805
801
fpp
1-45
1997
--`,,-`-`,,`,,`,`,,`---
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
390
827
861
447
Not for Resale
STD.API/PETRO TDB CHAPTER
L-ENGL
L777
0 7 3 2 2 7005 b b b I b
057
m
TAB= lCO.l (Continued)
1co.1
CCwaJm
TABLE
ENTRY
NAME
--`,,-`-`,,`,,`,`,,`---
PHENOL
METHANOL
WETHYLNINE
n-PROPYLNINE
1,2-PROPYLENE GLYCOL
WOWOHYDROXIBENZENE
WQWOHYDROXIWETHANE
WUOnTHYWINE
WONOPROPYLAIIINE
W O P R O P Y L E N E GLYCOL
~WINYUCETYLENE
IIORPHOLINE
NAPHTHACENE
VINYLACETYLENE
llORPHOL1 NE
NAPHTHACENE
NAPHTHALENE
ANTHRACENE
WHTHMENE
pNAPHTHALENE
N~HTHALUIE-'1,2,3,4-7~RAH~RIDE
NAPHTHALINE
1,2-(1,8-NAPHTHYLENE)BENZENE
W E W L ALCOHOL
NEOHUUWE
TABLE SEPUENCE W 6 E R
1,2,3,4-TETRAHIDROWAPHT~LENE
NAPHTHALENE
FLUORANTHENE
2,Z-DIMTHYL-1-PROPANOL
2,2-DIHETHYL-l-PROPMOL
NEW
NEOPENTANE
NEOPENTMOL
NITRIC W I D E
NITRILO-2,2',2"TRIETHANOL
NEON
NEOPENTANE
2,2-DIMETHYL-1-PRWANOL
NITRIC OXIDE
TRIETHANOLAMINE
2,2,2-NITRILOTRIETHAWOL
2,2',2'-NITRILOTRIETHANOL
NITROGEN
YlTROGEN DIOXIDE
NITROGEN PEROXIDE
R4
m
735
737
850
326
745
482
427
474
416
427
477
722
722
788
8
722
790
a57
TRIETHANOLAHINE
TRIETHANOLNlNE
NITROGEN
NITROGEN DIOXIDE
NITROGEN TETROXIDE
857
857
NITROGEN TETROXIDE
N I T R W S OXIDE
n-NONACOSANE
n-NONADECANE
1 -NONADECENE
NITROGEN TETROXIDE
NITRaJS OXIDE
n-NONAMISANE
n-NONADECANE
1-NONADECENE
793
n-NUNADECYLCYCLOHEXANE
n-NONADECYLCYCLOPENTANE
n-NONANE
1-NCUENE
n-NONYLBENZEYE
n-NONADECYLCYCLOHEXNE
n-NONADECYLCYCLOPENTANE
n-NONANE
1 -NONENE
n-NDNYLBENZENE
177
1 U
~
n-NONYLCYCLOHEXANE
n-NONYLCYCLOPENTANE
134
1-n-NONYLNAPHTWALENE
2-n-NONYLNAPHTHALENE
1-n-NONYL-l,2,3,4-TETRAHYDONAPHTHALENE
1-NONYNE
N W I NENE
n-OCTACOSANE
n-OCTADECANE
1-OCTADECENE
n-OCTADECYLCYCLOHEXANE
n-OCTADECYLCYCLOPENTANE
2,6-OCTMIENE
n-OCTANE
1 -OCTENE
~
792
793
791
91
81
288
41
278
375
~_______
n-NWYLCYCLOHEXANE
n-NONYLCYCLOPENTANE
1-n-NONYLNAPHTHALENE
2-n-NONYLNAPHTHALENE
l-n-NONYL-1,2,3,4-TETRAHYDRONAPHTHALENE
1 -NONINE
kts-PINENE
n-OCTACOSANE
n-OCTADECANE
1-OCTADECENE
n-OCTADECYLCYCLOHEXANE
n-OCTADECYLCYCLOPENTANE
2,6-OCTADIENE
n-OCTANE
1-OCTENE
167
443
U6
461
333
321
90
80
207
1 76
143
307
23
257
1997
1-46
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
789
Not for Resale
S T D - A P I I P E T R O T D B CHAPTER
L-ENGL
TABLE lCO.l (Continued)
SEQUENCE
TABLE
NUCIBER
NAHE
ENTRY
TABLE
COnPWND
cis-2-DCTENE
trarrs-2-OCTENE
cis-3-DCTENE
trans-3-OCTENE
cis-l-OCTENE
cis-2-OCTENE
trens-2-OCTENE
cis-3-OCTENE
trsns-3-OCTENE
cis-L-OCTENE
258
259
trans-4-OCTENE
alpha-OCTENE
n-OCTYLBENZENE
n-OCTYLCYCLOHEXANE
n-OCTYLCYCLOPENTANE
trans-4-OCTENE
1-OCTENE
n-OCTYLBENZENE
n-OCTYLCYCLOWEXANE
n-OCTYLCYCLWENTANE
263
260
261
262
257
374
166
133
~
1-n-CCTYLNAPHTHALENE
l-n-OCTYL-1,2,3,4-lE~R~~HT~LENE
1-0CTYNE
ORTHOCRESOL
OXACYCLOPENTANE
~
8 51
DIETHYLENEGLYCOL
FORMALDEHYDE
DIETHYL ETHER
DIETHYLENEGLYCOL
DIETHYLENE
GLYCOL
3-OXAPENTANE-1 ,5-DIOL
OXOCIETHANE
1,l"OXYBISETHANE
2,2'-OXYBIS(ETHANOL)
2,2'-OXYDIETHANOL
720
765
as 1
85 1
OXYGEN
O-OXYTOLUENE
p-OXYTOLUENE
OZONE
PARANAPHTHALENE
OXYGEN
O-CRESOL
p'CRESOL
OZONE
ANTHRACENE
n-PENTACOSANE
n-PENTADECANE
1-PENTADECENE
n-PENTADECYLBENZENE
n-PENTADECYLCYCLOHEXANE
n-PENTACOSANE
n-PENTMECANE
1-PENTADECENE
n-PENTADECYLBENZENE
n-PENTADECYLCYCLOHEXANE
~~
n-PENTADECYLCYCLOPENTANE
1,2-PENTADIENE
cis-1,3-PENTADIENE
trans-1.3-PENTADIENE
l,CiS-3-PENTADIENE
~~~
1-n-OCTYLIUPHTHALENE
c42
1-n-OCTYL-l,2,3,4-TETRAHrDRW~HTHALENE
W
1-OCTYNE
332
o-CRESOL
R5
TETRAHYDROFURAN
768
a7
77
284
381
173
~~~~
~_____
n-PENTADECYLCYCLOPENTANE
1,2-PENTADIENE
cis-1,3-PENTMIENE
trans-l,3-PENTADIENE
cis-1.3-PENTADIENE
140
293
2%
294
--`,,-`-`,,`,,`,`,,`---
1,trans-3-PENTADIENE
1,4-PENTADIENE
2,3-PENTADIENE
PENTAHETHYLENE
n-PENTANE
trans-1,3-PENTADIENE
1,4-PENTADIENE
2,3-PENTADIENE
CYCLOPENTANE
tert-PENTANE
1-PENTANETHIOL
n-PENTANOIC ACID
PENTANOL-1
PENTANOL-2
NEOPENTANE
1-PENTANETHIOL
n-PENTANOICACID
1-PENTANOL
2-PENTANOL
8
841
I-PENTANOL
1-PENTANOL
1-PENTANOL
í!-PENTANOL
n-PENTYL
717
717
717
718
762
n-PENTANE
PENTAN-I-M
n-PENTAUOt
PENTANOL
2-PENTANOL
1-PENTANOLACETATE
ACETATE
296
297
101
6
705
717
718
1-47
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
295
Not for Resale
TAB= 1CO.l (Continued)
1co.1
TABLE ENTRY
NAHE
2-PENTANONE
3-PENTANONE
-
ETHYL-n-PROPYL KETOWE
DIETHYL KETONE
PEMTASOL
1-PEWTANOL
1- W T E N E
1 PEUTEME
cis-2-PENTENE
cis-2-mME
trm-2-PENTENE
R-PENTINE
PENTOLE
1-PENTYL ACETATE
n-PENTYL ACETATE
PENTYL ALCOHOL
n-PENTYL ALCOHOL
ce-PENTYL ALCOHOL
n-PENTYLBENZENE
n-PENTYLCYCLOHEXANE
tr6svs-2-PEYTENE
CYCLOPENTADIENE
CYCLOPENTADIENE
n-PENTYL ACETATE
n-PENTYL ACETATE
-PENTANOL
n-PENTYLCYCLOPENTANE
PENTYL ETHANOATE
ACETATE
1-n-PENTYLNAPHTHALENE
l-n-PENTYL-1,2,3,4-TETRAHYORONAPHTHALENE
6-n-PENTYL-1,2,3,4-TETRAHrDROWAPHTHALENE
1-PENTYNE
í!-PENTYE
PERWLORMETHAWE
PHENANTHRENE
PHENOL
TABLE SEQUENCE W E E R
1 -PENTANOL
1
2-PENTANOL
fr-PENTYLBENZENE
n-PENTYLCYCLOHEXANE
n-PENTYLCYCLOPENTANE
n-PENTYL
1 -n-PENTYLNAPHTHALENE
l-n-PENTYL-1,2,3,4-TETRAHYOROWAPHTHALENE
6-n-PENTYL-1,2,3,6-TETRAHYDROWAPHTHALENE
1-PENTYNE
2-PENTYNE
CARBON TETRACHLORIDE
PHENANTHRENE
PHENOL
824
823
717
198
199
200
318
318
762
762
.
"
717
717
718
371
163
130
762
438
456
657
327
328
802
475
R4
PHENYLACETYLENE
PHENYL ALCOHOL
PHENYLBENZENE
í!-PHENYL BIPHENYL
3-PHENYL BIPHENYL
PHENYLACETYLENE
PHENOL
BIPHENYL
1,2-DIPHENYLBENZENE
1,3-DIPHENYLBENZENE
1,4-DIPHENYLBENZENE
4-PHENYL BIPHENYL
2-PHENYL-1-BUTENE
4-PHENYL DIPHENYL
PHENYLETHYLENE
PHENYLETHYNE
2-PHENYL-1-WTENE
1,4-DIPHENYLBENZENE
STYRENE
PHENYLACETYLENE
3%
426
384
422
BENZENE
ISOBUTYLBENZENE
TOLUENE
tert-BUTYLBENZENE
n-PROPYLBENZENE
335
350
336
352
341
cis-1-PROPENYLBENZENE
trans-l-PRWENYLBENZENE
2-PROPENYLBENZENE
2-PROPENYLBENZENE
2-PROPENYLBENZENE
385
386
387
387
387
2-PROPENYLBENZENE
2-PRCPENYLBENZENE
alpha-PINENE
alpha-PINENE
heta-PINENE
387
387
320
320
321
PHENYLHYDRIDE
I-PHENYLIS08UTANE
PHENYWTHANE
2-PHENYL-2-HETHYLPROANE
1-PHENYLPROPANE
Cis-l-PHENYL-l-PROPENE
trans-1-PHENYL-1-PROPENE
2-PRENYLPRCPENE
Z-PHENYL-~-PROPEKE
beta-PHENYLPROPENE
2-PHENYLPROPYLENE
beta-PHENYLPROPYLENE
PINENE
2-PINENE
2(10)-PIYENE
1-48
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
--`,,-`-`,,`,,`,`,,`---
COlPOUWD
422
R4
3%
424
425
426
1997
Not for Resale
L777
0 7 3 2 2 7 0 0 5 b b b 3 7 Bbb
(Continued)
--`,,-`-`,,`,,`,`,,`---
1co.1
1-49
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
TABLE lCO.l (Continued)
1co.1
KwaJND
TABLE ENTRY W E
TABLE SEWENCE W E R
n-PROPYLCYCLOPENTANE
1-n-PROPYLCYCLOPENTENE
PROPYLENE
PROPYLENE CARBONATE
1,2-DICHLORWROPANE
109
314
193
868
820
1.2-DICHLOROPROPANE
1.2-DICHLOROPROPANE
1.2-PROPYLENE GLYCOL
1,Z-PROPYLENE GLYCOL
1,2-PROPYLENE GLYCOL
820
820
n-PROPYL ACETATE
1 -PENTENE
n-PROPYL F O R M T E
WBUTYRIC ACID
PROPANE
E9
198
~~
n-PROPYLCYCLOPENTANE
1-n-PROPYLCYCLOPENTENE
PROPYLENE
PROPYLENE CARBONATE
PRWYLENE CHLORIDE
~
~~
~~
~~
PROPYLENE
aLpha,kta-PRWYLEXE
PROPYLENE
1,2-PROPYLENE
alpha-PROPYLENE
DICHLORIDE
DICHLORIDE
BLYEOC
GLYCOL
GLYWL
PROPYL ETHAWOATE
PRWYLETHYLENE
n-PROPYL FORMTE
PROPYL FORMIC ACID
PROPYL HYDRIDE
~~~
ALDEHYDE
PROPYLIC
RMATE
n-PROPYL P R W Y L HETHANOATE
PYLNAPHTHALENE
1-n-PRWYLNAPHTHALENE
OPYLNAPHTHALEWE
2-n-PROPYLNAPHTHALENE
l-n-PROPYL-l.2,3,6-TETRAHYDROWAPHTHALENE
~~
850
850
850
756
703
3
~~~~~
~~
130
756
434
l-n-PROPYL-1,2,3,4-TETRAHYDRONAPHTHALENE
452
6-n-PROPYL-1,2,3,4-TETRAHYDROWAPHTHALENE
6-n-PROPYL-l,~,3,6-TETRAH~R~APHTHALENE
1-PROPINE
ltETHYLACETYLENE
PRUSSIC ACID
CYANIDE
HYDROGEN
PYRENE
PYRENE
PYRIDINE
PYRIDINE
453
PYROACETIC ACID
PYROPENTYLENE
PYRROLYLENE
PUIYOLINE
sEma
--`,,-`-`,,`,,`,`,,`---
SKELLYSOLVE A
S O D I l M HYDRATE
S O D I U M HYDROXIDE
cis-STILBENE
trans-STILBENE
ACETONE
CYCLOPENTADIENE
1,3-BUTADIENE
QUINOLINE
SELEXOL
n-PENTANE
S O D I U I HYDORXIDE
SOoIlM HYDROXIDE
cis-1,2-DIPHENYLETHENE
trens-1,2-DIPHENYLETHENE
323
m
476
746
821
318
W2
769
863
6
847
847
420
421
STYRENE
STYROL
STYROLENE
SULFOUNE
SULFUR DIOXIDE
STYRENE
STYRENE
STYRENE
SULFOLANE
SULFUR DIOXIDE
384
SULFUR TRIOXIDE
SULFURIC ACID
SULFURIC ANHYDRIDE
SULfURWS ACID ANHYDRID€
IDE
SULFUROUS ANMYOR
SULFUR TRIOXIDE
SULFURIC ACID
SULFUR TRIOXIDE
SULFUR DIOXIDE
SULFUR DIOXIDE
797
866
SULFURDUS OXIDE
SULPHURIC ACID
,TERPHENIL
O-TERPHENYL
p-TERPHENYL
SULFUR DIOXIDE
SULFURIC ACID
1,3-DIPHEWYLBENZENE
1.2-DIPHENYLBENZEWE
1,4-DIPHEWYLBENZENE
1-50
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
384
384
862
796
T97
796
796
796
846
c25
424
426
1997
Not for Resale
TABLE lCO.l (Continued)
I co.1
TABLE ENTRY W E
--`,,-`-`,,`,,`,`,,`---
TETRACHLORIDE
TETRACHLORIDE
n-TETRACOSANE
n-TETRADEWE
1-TETRADECENE
802
802
a6
76
n-TETRADECYLBENZENE
n-TETRADECYLCYCLOHEXANE
n-TETRADECYLCYCLOPENTANE
TETRAETHYLENE GLYCOL
3,3-DIETHYLPENTANE
380
CARBOW
CARBOW
TETRACHLOROCARBOW
TETRACHLOR04ETIUNE
n-TETRACOSANE
n-TETRADEWE
1-TETRADECEWE
n-TETRADECYLBENZENE
n-TETRADECYLCYCLOHEXE
n-TETRADECYLCYCLOPENTANE
TETRAETHYLENE GLYCOL
TETWTHYLMETHANE
TE'TIUFLWRmTHANE
TETRAHYDROFURAN
283
172
139
852
55
TETRAFLUORIDE
TETRAHYDROFURAN
803
768
1,2,3,4-TEfRAHIDROllAPHT~LENE
446
CARBOW
1,2,3,6-TETRAHYDR~HTHALM
TETRAHYDROTHIWHENE
TETAHYDDIIOTHIWHENE
TETRALIN
~~~
TABLE SEQUENCE NUMBER
892
1,2,3,6-TETRAHIDRWHTHALENE
~
1,2,3,4-TETRAMETHYl BENZENE
1,2,3,5-TETRAMETHYL BENZENE
1,2,4,5"IETRAMETHYL BENZENE
2,2,3,3-TETRAnETHYLBTANE
TETRAMETHYLENE
TETWETHYLENE OXIDE
TETRMETHYLENE SULFONE
TETRMETHYLENE SULPHIDE
2,2,3,3-TETRAMETHYLHEXANE
2,2,5,5-TETRAMETHYLHEXANE
~~
1,2,3,h-TETWTHYL BENZENE
1,2,3,5-TETRMETHYL BENZENE
1,2,6,5-TETRAMETHYL BENZENE
2,2,3,3-TETRAMETHYLBT~E
CYCLWTANE
TETRAHYDROFURAN
SULFOLANE
TETRAHYDROTHIOPHENE
2,2,3,3-TETWETHYLHEXANE
2,2,5,5-TEIRMETHYLHEXANE
~
TETRAHETHYLMETHANE
2,2,3,3-TETRMTHYLPENTANE
2,2,3,4-TETR~THYLPENTANE
2,2,4,4-TETRAMETHYLPENTANE
2,3,3,4-TETRAnETHYLPENT~E
862
892
70
71
~~
NEOPENTANE
2,2,3,3-TETRAnETHYLPENTANE
2,2,3,6-TETRAMETHYLPENTANE
2,2,4,4-TETRAnETHYLPENTANE
8
58
59
60
61
2,3,3,4-TETRAllETHYLPENTANE
2-THIAWTANE
THIOPHENE
TETRAHYDROTHIOPHENE
SULFOLANE
2-THIAHEXANE
3-THIAHEXANE
3-THIAPENTANE
THIAPHENE
2-THIAPROPANE
2-THIAHEXANE
3-THIAHEXANE
3-THIAPENTANE
THIOPHENE
DIMETHYL 'SULFIDE
T H I U
768
~~~~
2-THIABUTANE
THIACYCLOPENTADIENE
THIACYCLOPENTANE
THIACYCLOPEWTANE DIOXIDE
2-THIAHEPTANE
THILANE
THIOETHANM
THIOETHYL ALCOHOL
THIOFURAN
446
~~~
2-THIAHEPTANE
832
891
892
862
842
839
860
838
891
829
TETRAHYDROTHIOPHENE
ETHYL HERCAPTAN
ETHYL MERCAPTAN
THIOPHENE
TETRAHYDROTHIOPHENE
892
830
TETRAHYDROTHIOPHENE
THIOPHENE
METHYL MERCAPTAN
TETRAHYDROTHIOPHENE
THIOPHENE
892
891
827
892
891
830
891
892
~
TH 1OLANE
TH I OLE
THIOnETHYL ALCOHOL
THIOPHANE
THIOPHENE
1-51
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
~~~
~
~~
STD-API/PETRO TDB CHAPTER L-ENGL L797 W 0 7 3 2 2 9 0 0 5 b b b 4 2 3 5 0 W
TABLE lCO.l (Continued)
1CO.1
TABLE
ENTRY
NAHE
TABLE SEQUENCE W E R
TOLUENE
TOLUENE HEXAHIDRIDE
n-TRIACONTANE
TRIATOMIC OXYGEN
l,l,l-TRICHLOROETHANE
TOLUENE
RETHYLCYCLOHEXANE
n-TRIACONTANE
OZONE
l81,1-TRICHLOROETHANE
336
147
l81,2-TRICHLOROETHE
TRICHLORMLUOROlETHE
TRZCHLOROFORn
TRICXLORWETHANE
n-TRICOSAWE
1,1,2-TRICHLCUOETWNE
TRICHLOROFLUOROWETHE
CHLCUOFORn
CHLOROFORU
WTRIWSANE
813
801
92
795
812
806
806
85
~
~~
TRI DANE
n-TRIDECANE
1-TRIDECENE
n-TRIDECYLBENZENE
n-TRIDECYLCYCLOHEXANE
n-TRIDECTLBENZENE
n-TRIDECANE
1 -TRIDECENE
n-TRIDECYLBENZENE
n-TRIDECYLCYCLOHEXANE
379
n-TRIDECYLCYCLOPENTANE
TRIETHANOLAHINE
TRIFLWROCHLOROMETHANE
1,1,1-TRIFLWROETHANE
TRIFLUORWETHANE
n-TRIDECYLCYCLOPENTANE
TRIETHANOLAHINE
CHLOROTRIFLUOROMETHANE
1,1,1-TRIFLWROETHANE
TRIFLWROMETHANE
138
857
TRIFLUORWETHYL CHLORIDE
TRZ(HYDR0XYETHYL)AHINE
sym-TRIMETHYLBENZENE
1,2,3-TRIHETHYLBENZENE
1,2,4-TRIHETHYLBENZENE
CHLOROTRIFLUOROMETHANE
TRIETHANOLAMINE
1,3,5-TRIMETHYLBENZENE
1,2,3-TRIMETHYLBENZENE
l82,4-TR1UETHYLBEWtENE
857
348
346
347
l83,5-TR1HETHYLBENZENE
2.2,3-TRSH€THYLBUTANE
2,3,3-lRIWETHYL-l-BUTENE
TRIMETHYLCARBINOL
'I81,2-TRIMETHYLCYCLOPENTA#E
1,3,5-fRIHETHYLBENZENE
2,2,3-TRIMETHYLBUTANE
2,3,3-TRIMETHYL-1-BENE
tert-BUTANOL
1,1,2-TRIHETHYLCYCLOPENTANE
348
22
256
716
116
1,1,3-TRIHETHYLCYCLOPENTANE
118
l8c-2,~-3-TRIMETHYLCYCLOPENTANE
~,C-~,C-~-TRIMETHYLCYCLOPENTANE
~,c-Z,~-~-TRIMETHYLCYCLOPENTANE
l,c-2,t-4-TRIMETHYLCYCLOPENTANE
117
181,3-TRIUETHYLCYCLOPENTANE
1 ,C-2,c-3-TRIUETHYLCYCLOPENTANE
1 ,c-Z,~-~-TRIUETHYLCYCLOPENTANE
1 ,c-~,~-~-TRIHETHYLCYCLOPENTANE
I,c-2,t-4-TRIHETHYLCYCLOPENTANE
l,t-Z,c-3-TRIHETHYLCYCLOPENTANE
l,t-2,c-4-TRIMETHYLCYCLOPENTANE
TRIMETHYLENE
3,3,4-TRIHETHYLHEPTANE
3,3,5-TRIMETHYLHEPTANE
l8t-2,~-3-TR1METHYLCTCLOPENTANE
l,t-Z,c-4-TRIMETHYLCYCLOPENTANE
CYCLOPROPANE
3,3,4-TRIMETHYLHEPTANE
3,3,5-TRIHETHYLHEPTANE
75
282
379
171
m
814
807
799
121
119
122
120
123
93
68
69
2,2,3-TRlMETHYLHEMNf
2,2,4-TRIUETHYLHEXME
2.2,5-TRIMTHYLWEXE
2,3,3-TRlMETHYLHEXANE
2.3.5-TRIMETHYLHEXANE
2,2,3-TRIHETHYLHEXANE
2,2,4-TRIUETHYLHEXANE
2,2,5-TRIMETHYLHEXANE
2,3,3-TRIUETHYLHEXANE
2,3,5-TRIHETHYLHEWNE
48
49
2,4,4-TRIHETHYLHEXANE
3,3.4-TRIMETHYLHEXANE
TRIHETHYLUETHANOL
2,2,3-TRIMETHYLPENTANE
2,2,4-TRIM€THYLPENTANE
2,4,4-TRIUETHYLHEXANE
3,3,4-TRIHETHYLHEXANE
tert-BUTANOL
2,2,3-TRlMETHYLPENTANE
2,2,4-TRIMETHYLPENTANE
53
54
716
36
37
50
51
52
1997
1-52
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
--`,,-`-`,,`,,`,`,,`---
cowouND
Not for Resale
TABLE lCO.l (Continued)
1CO.1
TABLE ENTRY NAME
TABLE
SEWEWCE NUMBER
38
39
2,3,3-TRIHETHYLPENTANE
2,3,4-TRIMETHYLPENTANE
2.3.3-TRIMETHYL-1-PENTENE
2,4,6-TRIlETHYL-l-PENTENE
2,4,4-TRIMETHYL-2-PENTENE
TRIPHENYLENE
TR 1PTANE
n-lJNDECAWE
1 -UNDECENE
n-UUDECYLUENZEWE
275
276
277
c79
TRIPHENYLENE
2,2,3-TRlHETHYLBUlAE
n-UNDEME
1-UNDECENE
n-UWDECYLBENZENE
22
73
tso
377
~~~
n-WDECYLCYCLOHMAUE
n-UIIDECYLCYCLPENTANE
UREA
ACID
ACID
VALERIC
VINEGAR
VINYL ACETATE
VINYLACETYLENE
VINYL BENZENE
VI NY L CHLOR I DE
VINYL ETHYLENE
UATER
XENON
1.2-XYLENE
1 ,J-XYLENE
1’4-XYLENE
VINYL ACETATE
VINYLACETYLENE
STYRENE
VINYL CHLORIDE
1.3-BUTADIENE
M5
M1
757
326
384
811
292
UATER
XENON
O-XYLENE
III-XYLENE
p-XYLENE
845
B-XYLENE
O-XYLENE
339
330
340
m
338
339
340
P-XYLENE
--`,,-`-`,,`,,`,`,,`---
œ-XYLENE
O-XYLENE
p-XYLENE
n-UWDECYLCYCLOPENTAE
UREA
ACID
AClD
n-WDECYLCYCLOIIEUNE
1 69
136
743
1-53
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
1c1.1
TABLE lCl.1
PARAFFINS: PRIMARY PROPERTIES
canpand
IO.
F o n u l a N.U.
Freezing
Point in
air at
1 atm
deoF
Boiling
P o i n t at
1 atm
&g F
T
C r i t i c Ca ol n s t a n t s
kentrie
collprers- :actor
~~
Pressure
VOluœ
pia
CU
ft
per lb
ibility
Factor
-
P a r a f f i n s , C1 t o C3
1 ETHANE
CH4
2 ETHANE
3 PROPME
czH6
-258.68
ata
16-04
30.07
44.10
UH10
UH10
58.12
58.12
31.10
10.90
72.15
96.93
82.12
C5H12
49.10
43.67
0.0985
0.2860
0.0115
0.2790
0.0995
-296.42 P -116.66
119.91
-297.04
-127.46
-305.82
206.02
667.04
616.13
O.OR7
0.2760
-216.92 P
550.57
529.11
0.0703
0.0724
0.2740
0.2002
0.2820
0.1058
706.64
o. om
~
Paraffins.
4
5
0.1523
UHlO
m W E
ISOsllTWE
-255.30
P a r a f f i n s , C5H12
6 n"ENTANE
7 ISWENTANE
8 NEOPENTANE
C5H12
72.15
C5H12
R.15
C6H14
86-18
86.18
86.18
86.18
86.18
-201.51
385.79
488.79
0.0695
0.2700
0.2515
455.82
369.10
321.13
490.38
463.98
0.0679
O -0674
0
.
2
m O .u75
O 2690 0.1%
155.71
-139.58
140.47
-244.48 P
145.89
-261.22
-145.97 P
121.51
136.36 -19a.33
P
454.o1
438.75
436.57
453.11
446.87
0.0690
0.0681
0.0681
0.0667
0.2660
0.3013
0,2774
0.27'37
453.54
0.0665
0.2690
0.2461
209.17
194.09
197.33
512.69
495.00
503.78
513.48
477.23
507.56
475.95
505.85
496.44
397.41
0.0664
0.0673
0.0646
O. 0665
0.2610
0.2610
O. 3277
2.21
9 n-HMAWE
10 2+€THYLPENTANE
II ~~IETHYLPENTANE
12 2,241METHYLBUIWE
13 2,3-OIRETHYLBUTAWE
=H14
C6H14
C6H14
C6H14
435.83
448.30
420.13
440.29
O. 2670
o.Zn0
0.2720
0.2350
P a r a f f irs. C7H16
14
15
16
17
18
19
20
21
HEPTANE
2-METHYLHEXANE
WETHYLHEXANE
?4THYLPENTANE
2.2-DIMETHYLPENTANE
2,3-O1K€THYLPENTANE
Z,HIMETHYLPENTANE
3,3-D1METHYLPENTANE
22 2,2,>TRIMETHYLBUTANE
-
-131.04
-180.85 P
200.25
174.54
176.89
193-61
186.91
-210.01
177.58
I
I
-182.92
-181.48
-190.86
-..
-182.63
-12.24 P
396.54
400.14
419.28
402 .u
421.78
396.97
427.22
428.39
0.2550
0.3435
0.0665
0.2680
O. 2670
0.3216
0.3094
0.2879
0.0628
0.2560
0.2957
0.0668
0.2650
0.3014
0.0662
0.0636
0.2730
0.2672
0.2660
0.25%
0.0682 P
0.0684
0.0651
0.064
0.0638
0.0670
0.2560
0.2610
0.2520
0.2590
0.3996
0.2530
0.3628
0.3378
P a r a f f i n s , CBw18
23 nOCTANE
24
25
26
27
2"ETHYLHEPTANE
3"ETHYLHEPTANE
4"ETHYLHEPTANE
34THYLtEXAllE
i!.2-DIMETHYLHEXANE
28
29 ETHYLHEX HEX AWE
30 2,4-DIMETHYLHEXANE
-10.19
-164.18
-184.99
258.22
243.77
246.07
245.37
240.10
I
___
31 2,!%lIUETHYLHEXANE
32 3,3-OIMETHYLHEWNE
563.99
567.68
554.94
551 -46
558.05
529.97
554.45
536.63
530.33
551.93
361.15
360.28
369.27
368.69
378.55
366.95
381 A6
371.30
361 -15
384.36
0.0657
0.0662
0.0676
0.0621
0.2650
0.2630
0.2630
0.2620
0.2510
0.3772
0.3718
0.3706
0.3472
0.336
0.3576
0.3202
Notc Footnote codes follow Table 1C4.12.
1997
1-54
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
--`,,-`-`,,`,,`,`,,`---
P a r a f f i f s , C6Hll
1c1.1
TABLE 1Cl.1 (Continued)
ecific A p I
avi t y
apor
ressure
Gravity
a t 60 F
deg
/60
t
100 F
sin
tineretic Viscosity
eatCapacity
t
60 F and Cmstant of the Liquid
ïquid a t
a t 100 F
210 F
atm
I
I
I
araffins, Cl t o C3
1 . 2 9 9 9
340.38
1.3554
266.66
147.99
1.5063
4
2.500 i
2.963
4.221
...
."
...
".
l. 00040
0.5261
1.18489
1.28614
0.4068
0.9621
0.3873
0-6284
O.V?!ï
O -3939
O. 3854
0.5712
O. 5669
O. 2533
1.1686
0.2773
1.1873
O 3394
I .2643
."
".
'araf f ins, UH10
1
1.5849
110.42
4.876
1.5644
119.22
I 1
4.705
il . M 8
1.32920
1.31755
v.80
Surface
T-iM
cent istokes
t u l l b deg F
deal Gas
of Cambustion
Vaporization at
ressure
I
a t 77 F
Btu/Lb
Boiling
Poi nt
218.98
209.86
182.74
165 .R
157.89
~
*/an
I
19920
6.88
1W56
19594
1
2
3
4
1 1 -92
9.84
5
~
~~
,arsffins. C5H12
56.6614
o3862
O. 5427
0.5378
0.5553
4.9816
6.7671
6.1037
9.8490
7.4158
0.3829
O 3797
0.3747
O .3T16
0.371 1
0.5350
0.5266
0.5188
0.5136
0.5140
0.4152
1.6126
2.2657
2.1281
2.0043
3.4914
2.3467
3.2968
2.7687
3-3735
0.3816
0.3785
O .3758
O. 5269
0.5218
0.5146
0.5142
0.5167
0.5098
O. 5238
0.5013
0.4991
0.5046
o -5373
O. 3807
0.3776
o -3744
O .3768
0.3839
O. 5246
0.5173
0.5136
0.5157
0.5158
0.5139
O. 5055
0.5179
0.5113
0.5052
O .63&
O 5908
0.5757
0.5616
0.5335
0.6152
15.5838
?O.W3
0.3865
0.3811
0.3066 T
...
...
...
153.83
147.73
135.37
'&.51
14.45
1,
6
7
8
-10.89
Daraffins, U H 1 4
-
o -3862
O. 3924
0.4712
0.4841
...
...
143.61
139.40
141 .o0
131 -75
136.56
19233
19203
19214
19163
191%
17.91
16.87
17.58
15.80
16.87
19156
19134
19147
19155
19097
19139
19114
19120
19104
19.83
18.79
19.30
19.92
17.46
19.46
17.G
19.07
14
15
16
11
...
136.60
131 -95
133.14
133.04
125.55
130.82
127.17
127.59
124.33
18.99
-
0.3997
0.3635
0.3524
O 3326
0.3265
0.3616
0.3659
0.4141
0.3703
0.3649
130.48
126.55
127.31
126.82
126.80
121.15
124.88
122.23
123.19
122.84
19098
19080
15WO
19093
19097
19054
19089
1907-2
19060
19070
21.13
20.18
20.74
20.56
o8
21 .
19.15
20
-53
19.59
19.28
20.17
...
...
...
9
10
11
12
13
-
Daraffins, C7H16
LII
3.6902
73.53
D.6822
D.6922
--`,,-`-`,,`,,`,`,,`---
0.7043
5.754
75.91
R.91
69.42
0.6818
76.04
0.6994
70.82
0.6764
77.70
5.639
0.6961
71.76
5.604
0.6954
71
.98
5.688
5.771
5.872
5 . W
5.831
5.798
1.38511
1 .3822a
1.38609
1.39084
1.37955
1.38946
1.3m
1. W 2
1.38692
0.3830
0.3819
0.3679
0.3914
0.3797
0.3743
0.4730
0.4481
0.4410
0.5740
0.5183
0.4416
O. 5625
O. 6994
0.3515
...
.-.
...
...
...
...
...
II
15
2c
21
2:
Paraffins, C8H18
0.7073
O. 7029
0.7092
O .7W6
0.7173
O -7002
0.7162
0.7017
0.6983
0.7141
68.56
69 82
68.03
67.92
65
-
T
.7
m.60
66.07
70.16
71.12
66.65
5.897
5.860
5.912
5.916
5.980
5.837
5.971
5.850
5.822
5.954
1.39505
1.39257
1.39610
1.39553
1.39919
1.39104
1 -39880
1.39291
1.39004
1.39782
i
0.7664
0.7302
0.7641
0.7457
1 .x01
0.8610
1 .O969
1 .O974
1 O306
.
0.3793
O -3694
0.3878
0.3727
0.3838
0.5630
O. 7057
0.5827
0.5856
r
24
21
24
2;
21
r
31
3
3;
-
1-55
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
-
Not for Resale
STD.API/PETRO TDB CHAPTER L-ENGL
L997
0 7 3 2 2 9 0 OSbbb4b
TTb m
1c1.1
TABLE lC1.l (Continued)
1
~
Critical
o.
CaIwJnd
Forrnulr
M.Y.
Boi 1n
ig
Point at
1 atm
deoF
Freezing
Point i n
air at
1 atm
Constants
Acmtril
:onpress- Factor
lbility
:actor
VolUr
CU f t
per lb
deoF
Paraffins, OH18
a
3,COIMETHYLHDUNE
C8H18
34 2-KElHYL-3-ETHYLPENTAN€
a18
35 3-METHYL-3-ETHYLPENfAWE
36 2,2,3-TRIMETHYLPENlANE
37 2,2,&TRlRETWLPENTANE
38 2,3,3-TRIETHYLPENTANE
39 2.3,C-TRIIIETHYLPEWTANE
40 2.2.3,flETRAnETHYLBUTANE
a 1 8
CSH18
WH18
C8H18
W18
CBH18
114.23
114.a
114.23
116.23
114.23
114.23
114.23
114.23
243.91
240.17
128.26
128.26
128.26
128.26
128.26
128.26
128.26
128.26
128.26
128.26
128.26
128.26
128.26
128.26
128.26
128.26
128.26
128.26
128.26
128.26
128.26
303.48
289.90
291.61
288.39
289.76
270.84
2?s .38
272.44
259.77
255 .M
279.82
268.45
267.19
301.O1
142.29
142.29
142.29
142.29
142.29
142.29
142.29
142.28
142.28
142.28
u 5 .a
332.60
334.04
330.26
329.27
314.42
319.77
323.42
312.22
320.56
244.89
229.72
210.63
238.59
236.25
223.32
-174:;i
-131.57
-170.07
-161.27
-149.67
-164.56
213.46
564.17
560.93
578.03
554.63
519.46
572.63
559.67
562.13 P
390.16
o "54
391.61
407.56
3% .W
0.0621
0.2450
0.2540
0.2670
0.3361
0.3294
0.3050
0.2971 0.2540
0.2660
0.3022
0.2690
0.0646 P
0.2670
0.2800
0.2903
0.3161
0.2650
332.14
332.14
339.39 P
339.39 P
346.65 P
0.0679
0.0676
0.6661
0.0653
0.0659
P
0.2520
0.2540
0.2520
0.2500
0.2570
0.4212
0.4123
0.6129
0.4080
310.84
0 . w P
0.2540
0.3899
333.59 P
362.60
353.90
337.94P
0.0649 P
0.2480
0.3927
0.3181 0.2610
0.3457
O3 %
0.3124
0.8268
0.3522 0.2600
372.46
609.01
3% .96
416.27 P
0.0638
0.0611
0.0656
0.0638
0"
Peraff ins, C9HZO
41 W O N A N E
42 24ETHYLOCTANE
43 HETHYLOCTANE
44 CWETHYLOCTANE
45 34THYLHEPTANE
46 2,241METHYLHEPTANE
47 Z,&DIMETHYLHEPTANE
48 2,2,3-TRlMETHYLHEXANE
49 2.2.4-TRIMETHYLHEXNE
50 2.2.5-TRIMETHYLHEWE
51 2.3.3-TRIMETHYLHEXAWE
52 2,3,5-TRIHElHYLHEXE
53 2,4,CTRIHETHYLHEXANE
54 3,3,C-TRIHETHYLHEXANE
55 3,MIETHYLPENTANE
56 2,2-OIMETHYL-~THYLPENTANE
57 2,4-01METHYL-3-ETHYLPENTANE
58 2,2,3,3-lElRAnETHYLPENTANE
59 2,2,3,&TETRAnETHYLPENTANE
60 2,2,4,CTETRAnETHYLPENTANE
61 2,3,3,&-lETRAnETHYLPENTANE
C9H2O
C9H2O
C9H20
C9HZO
C9HZO
C9H20
C9H20
C9H20
@H20
C9H20
C9HZO
C9H2O
C9H2O
ISH20
C9HZO
C9H2O
C9H2O
C9H20
C9HZO
C9H2O
C9HZO
295.14
272.91
278.10
28L.52
271 -45
252.12
286.79
4-28
-112.67
-161.68
-1 71-76
-174.82
-171.40
-153.22
...
-18L.00
-158.37
-178.22
-198.22
-172.07
-150.12
-27.45 P
-147.05
-188.25
14.20
-185.96
-87.16
-151.82
610.61
596.48
602.60
598.10
602.33
578.57
582.53
596.93
574.79
562.82
611.33
586.13
622.67
638.42
602.33
604.13
639.86
606.20
568.76
P
P
P
P
P
P
P
P
P
0.0636
0.0642
0.0648 P
0.0629
349.55 583.25
0.0638
356;80 P
0.0638 P
382.91
0.0625
0.0591 P
387.98 P
372.75 P 0.0638 P
366.95 P 0.0639P
0.0597
396.80
0.0612
371 -81
342.42
O
393.93 634.19
0.0616
372.75
P
P
P
P
.o629
0.2620
O .2560
0.2620
0.2560
0.2640
0.2490
0.2b80
0.2640
0.2570
0.2500
0.2650
0.4435
0.3236
0.3381
0.3353
0.3530
0.2800
0.3106 0.2550
0.3159
0.3127
Paraffins, C10H22
62 H E U N E
63 24ETHYLIIOWANE
64
65
66
501
67
~"ETHYLNONANE
U~ETHYLNONAYE
~~ETHYLNONANE
2.2-DIIIETHYLOtTANE
2.74IWTHYLOtTANE
68 3,3,LTRIMETHYLHEPlANE
69 3,3,5-TRIMElHYLHEPTAUE
2,2,3,3-TET~ETHYLHEXANE
m
ClOHU
c1on22
ClOW
ClOHU
ClOH22
C10H22
C10H22
Clon22
ClOHU
ClOHZ
- 2 1 -35
-102.37
-120.64
-145.66
-125.86
45-20
652.19
638.33
643.73
638.33
638.33
623.93
627.53
-65 -20
661.73
...
...
...
P
P
P
P
306.03
0.0675
307.49 P
0.0656
313.29P
0.0656
313.29 P 0.0656
313.29 P 0.0656
313.29 P 0.0646
3c8.94 P 0.0647
0.0624
349.55 658.13
o .o635
336.49 637.61
0.0620
364.05
P
P
P
P
P
P
P
O -2470
0.2440
0.2470
0.2L80
0.2480
0.2480
0.2440
0.2590
0.2580
0.2670
O. 4923
0.4723
0.4669
0.4651
0.4562
0.4288
0.4420
O.Sc31
0.3853
0.3666
1997
--`,,-`-`,,`,,`,`,,`---
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
P
P
Not for Resale
~
S T D . A P I / P E T R O TDB C H A P T E R L - E N G L L997
m
0732270 O S b b b 4 7 7 3 2
1c1.l
TABLE lC1.l (Continued)
--`,,-`-`,,`,,`,`,,`---
r
~
ecific
wi t y
1/60
191
Gravity
a t 60 F
dts MI
Liquid
Dmsity
a t 60 F
Lb/gal
Refractive
Index of
the Liqvid
77 F
at
k a t capeci ty
s t 60 F and Constant
pressure
l t u / l b deg F
:imamtic Viscosity
,f the L i w i d
Ideal tas Liquid at
1 atm
t t 100 F
:entistokes
It 210 F
k a t of
raporizItion at
lorn1
loi t ing
loi nt
Ituf Lb
Net Heat
iwid
of canbust ion
ofLiquid
a t 77 F
'urfac
ensic
It 77
BtWLb
" W C
IO.
-
'araffirs, a n 1 8
. .I
1.7243
1.?240
3.7317
3.7200
0.6988
0.7301
0.7240
63.87
63.94
61.89
65.02
70.98
62.30
63.94
1.40522
1.40198
1.46%0
0.9466
O . 9769
O -8265
0.3848
0.3771
1.40311
1.40080
1.40400
1.40390
1.40700
1.39930
1.39830
1.CD820
1.40100
1.39728
1.41 190
l.40370
1A0515
1.41540
1. 4 1 m
1.40104
1.41 146
1.lb2140
1.41246
1.40459
1.42003
0.1809
0.2561
0.2520
0.2732
O. 2698
0.4191
0.3652
O -3797
0.5213
o.mm
0.3774
0.3748
0.3760
0.3817
0.3794
0.3750
0.5146
0.7382
0.6516
0.6521
0.6461
0.8424
0.8436
6.121
1.40967
6.092
1.c0750
6.144 60.51
1.41030
6.137
1.40950
6.139 60.67
1.41000
6.0?3
1.&o600
6.W
1.40620
6.342
1A2130
6.227
1.41470
6.406
1A2600
0.0610
0.0841
6.036
...
...
6.020
5.982
6.042
6.039
6.089
5.958
5.950
6.116
6.000
5 -935
6.185
6.054
6.070
6.251
6.315
6.161
6.188
6.342
6.1%
6.033
6.326
64.47
65.70
63.74
63.86
62.26
66.50
66.75
61 -39
65.12
67.26
59.21
63.36
62.84
57.22
55.30
59.97
59.14
54 -52
58.94
0.7236
64.06
0.7588
54.98
0 . 5 ~ ~O -3639
0.3720
O -3788
0.3750
Paraffins, C9H20
0.7220
0.7176
0.7247
O. 7243
O. 7303
0.7146
O. 7137
0.7336
0.7197
0.7119
0.7419
0.7261
0.7281
O. 7498
0.7575
0.7390
O . 7423
0.7607
O. 7430
I
.m82
0.4997
0.5072
0.5087
0.5027
0.4892
0.5046
0.5095
O.UM P
6.038
6.036
6.100
6.003
5.826
6.087
1.40180
1.40167
1. m 9
1.40066
1.38898
O
o.am
0.8336
1.1421
1.7124
O
.u82
0.5854
0.6282
0.3864
O A694
0.5050
O. 2492
0.2825
O. 4294
O -3845
0.3613
O A754
O -7293
0.3415
0.3652
O .3897
O .3780
...
...
0.3701
...
...
O .3799
...
0.5080
0.5166
o. 5078
0.51%
0.5034
...
...
0.5173
...
...
...
0.6912
0.5286
0.6315
O. 6797
0.60T7
0.7021
0.6823
...
...
...
0.4359
...
...
0.8279
...
0.3221
0.3768
0.3983
0.3738
O -3623
0.4053
...
1. C694
1.4329
1.3818
1.3817
1.3779
3.4716
3.4716
...
..3.2795
.....
0.4121
...
125.37
lzS.19
lf5.48
120.40
115.86
121 .94
122.78
117.89
125.11
122.36
122.02
121.30
121.O3
117.47
118.61
111.97
112.63
112.69
115:ii
113.61
...
19092
19094
19088
19073
19064
190n
19080
19059
19055
19037
19064
19040
19053
19013
19019
19030
19029
18994
19035
19025
19038
19047
19055
19064
19073
19045
19053
19039
19047
0.3861
0.3648
0.3719
O -3784
O. 3703
0 . m
0.3902
0.5090
0.6732
0.4813
0.4954
0.4731
O -4858
0.4902
0.5058
0.8137
0.8105
0.8145
0.8393
0.8119
0.8429
O -3064
O. 4535
0.4518
0.3601
0.4131
0.3579
0.6139
118.27
115.21
116.43
115.57
114.67
109.06
116.33
0.3793
0.3769
0.3745
0.3758
O -3748
0.3786
0.3749
O. 5220
0.5164
1.O154
O .96M
O. 9256
0.8820
O. 8986
0.5537
0.5401
0.5158
0.4946
O. 5036
0.5337
O. 4922
119.68
117.28
117.57
118.73
115.89
112.26
114.07
111.50
19019
19003
19009
19009
1W09
18979
109.39
1901 1
Y.21
!1 .o5
!1 .53
33.23
18.u
21.11
33
u
35
34
37
3e
20.68
39
20 -96
40
-
!2.40
41
?1.44
42
El .92
3-92
Z2.37
e0.28
20.49
21.41
43
W
45
5(
5'
5;
20.
19.59
21 -95
20.82
20.75
44
45
cd
47
kt
5:
21.92
22.34
22 -94
21.57
19.91
22.85
54
55
56
57
28
59
60
61
23.3
62
22.79
232
.9
- -
Paraffins, ClOH22
o. 7342
0.7307
O. m 9
0.7361
O. 7363
0.7285
0.7279
O 7607
0.7469
0.7&
-
61.22
62.14
60.73
62.75
62-90
54.52
57.95
52.66
0.0864
0.0986
O -0964
0.1500
0.1288
0.1401
0.1742
0.1584
...
...
...
0.5068
0.5187
0.5153
0.5132
o .so29
...
...
...
...
...
...
...
...
...
...
18986
19010
19008
63
23.11
64
65
66
23.z
23.11
21.3'
21 .&
26.2'
21.3;
27.3:
501
67
68
69
TO
1-57
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
0.9964
0.9177
22 -4'
Not for Resale
1c1.1
TABLE lC1.l (Continued)
Critical
canpwnd
0-
FOM L I
KY.
Boi 1 ins
Point at
1 atm
a S F
Freezing
Point i n
air at
1 atm
Constants
~~~
Teraturt
Pressure
psis
deoF
VOlUnc
-
T
- entric
C:œpress-- Fa1ctor
AC1
CU f t
1b i l i t y
per Lb
F:actor
dcoF
-
"
"
Paraffins, ClOH22
71 2 , 2 , 5 , 5 - T E T ~ T H Y L ~
72 2,MIIIETHYL-3-ISOPROYLPENTANE
~~
ClOH22
142.28
C l OH22
279.43
9.32
314.67 162.28
-115.06
586.85
317.64
0.0642
640.67P
m.59 P
0.0625 P
0.2580
0.2510
"
~~
0 .3780
0-3707
"
Paraffins, C11 t o C30
73 WNDECANE
rr-DODEUNE
74
75 n-TRIDECANE
76 rtTETRADECANE
77 n-PENTUtDECANE
78 WEXADECAYE
79 n-HEPTADECANE
80 M T b D E U N E
81 H D W C S E U N E
82 n-EltOYUIE
83 n-HENEIMSANE
84 nDOCDSANE
85 PTRI COSANE
86 n-TETRACOSANE
87 rr-PENTACOSANE
88 ri-HEWCDSANE
89 ri-HEPTACOSANE
90 n-OCTACOSANE
91 AONACOSANE
92 n-TRIACONTANE
C l ln24
C12H26
C13H28
c14n30
C15H32
C16H34
C17HM
C l 8H38
Cl9H40
C2OH42
C21H 4 4
c22H46
C23H68
C24HSO
U5HS2
C26H54
C27H56
C28H58
156.31
170.34
1N.37
198.39
212.42
226.45
240.47
2s4.50
268.53
282.55
296.58
310.61
324.63
338.66
346.72
352.69
380.74
394.77
CZPH~O
408.80
C30H62
422.82
384.67
421.38
455.84
488.46
519.23
568.36
575.87
602.08
625.82
650.80
673.70
695.48
716.36
736.30
f55.42
m.96
791.78
808.88
825.44
861.46
-14.04
14.75
42.55
49.86
64.68
71.57
82.69
104.36
111.20
117.50
123.08
128.30
132.98
138.20
142.16
146.66
149.90
690.5 3
282.83
724.7 3
263 -97
755.3 322.30 243.67
P
787.7 3
227.71
814.7 3
214.66
861.7 3
203.06
865.1 3
194.35
184.20
884.9 '3
175.50
P
904.7 3 89.60
P
168.25
922.7 3 97.57
160.99
940.7 3 P
'3P
153.74
956.9
147.94
9T3.1 3 P
142.14
987.5 3 P
137.79
1001.9 ' 3 P
131.99
1014.5 3 P
128.07
1027.1 3 P
1037.9 ' 3 P
123.28
119.80
1048.7 3 P
116.03
1059.5 3 P
P
P
P
P
P
P
P
P
P
P
P
P
P
0.0675 P
O. 2420
0.06?3 P
0.2380
o 2320
0.0673 P
O. 0670
0.0610 P
0.0668 P
0 . w P
0.0667 P
0 . w P
0.0663 P
0.0664 P
0.0665 P
0.0666 P
0.0667 P
0.0663 P
0.0664 P
0.0663 P
0.0661 P
0.0662 P
0.0663 P
0.2260
o. 2240
0.2200
0.2190
0.2170
0.2150
0.2130
0.2110
0.2090
0.2080
o. 2070
o. 2050
O. 2030
O. 2030
0.2000
0.2000
o. 2000
1
0 -5303
0-5764
0 -6174
O..UM
0 .W
0,
,1174
.769?
0,
0 -81
, 14
0 ,.a522
0. W 9
0 .%20
0. 9 m
1.0262
1.0710
1.1053
1.(544
1-2136
1.un
1-2545
1 .3072
-
Note: Footnote codes follow Table 1C4.12.
1-58
1997
--`,,-`-`,,`,,`,`,,`---
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
1c1.1
TABLE 1C1.1 (Continued)
T
Heat Capacity
It
Gravity
60 F and
CWlStMt
Pressure
Btu/Lb dcg F
Kinanatic Viscositl
of t h e L i w i d
catistokes
Liquid at
1 ata
Heat of
Vaporiretion at
Norma 1
Boi 1i n g
Point
Yet Heat
Df
Liquid
Surface
Can-
bustion
T e n s i o r1
Liquid
n t ?7 F
a t TT F
Df
Btuf Lb
iNo.
1
Btuflb
--
Paraffins, Clon22
."
...
0.3400
0.1747
, Cl1
0.7439
0.7524
0.7611
O. 7665
0.7717
0.77fX
0.7752
0.7841
o -7880
0.7890
0.7954
0.7981
0.8123
0.8027
0.8048
0.8067
0.8085
0.8077
0.8120
0.8123
...
I
...
...
...
108.48
18939
21.26 13
71
19071
26.44 I
R
-
"
t o c30
56.57
6.273
54.42
58.71
6.390
53.11
51.85
".
1 I
6.345
6.202
6.434
51.09
6.461
6.452
51.03
48.W 6.537
48.07
6.569
6.586
47.62
46.41
6.631
6.654
45.79
6.m
42.70
44.79
6.692
6.710
44.31
6.725
43.91
43.51
6.741
43.69
6.734
42.76
6.m
42.70
6.734
R
R
R
R
R
R
R
R
R
R
R
R
R
R
1.41507
1.41507
1.42346
1.42685
1.42979
1.43250
1.43480
1.43690
1.43880
1.64050
1.44200
1.44340
1.cU70
1.44590
1.44700
1.44810
1.44906
1.64990
1.45086
1.45150
0.0205
O .O071
o -3832
0.0025
0.3792
0.3789
0.0003
0.0001
<.o001
0.3786
0.3783
0.oow
<.o001
~.WOl
<:.o001
...
...
...
...
...
...
...
...
...
...
0.3829
0.3781
0.3785
0.3787
0.3788
...
O -3889
0.3816
0.3974
o -3821
0.3813
0.3005
0.3815
0.3813
...
0.5219
0.5210
0.5227
0.5217
O. 5229
0.5258
0.5247
0.5223
0.5167
0.5051
...
0.5166
0.5167
0.5166
0.5164
0.5160
0.5156
0.5150
0.5144
...
1.2588
1. S 5 2
1.8634
2.2294
1.1328
2.6415
1
3.1229
1
3.6045
1
4,1620
1
4.6090
F
5.3165
\
\
\
\
\
\
\
\
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
...
...
...
...
...
...
...
...
...
...
0.6397
0.7469
0.8624
0.9885
100.84
1.2859
1.6413
1.5815
1.7940
1.9889
2.1703
2.4099
2.m4
2.8982
3.1566
3.4612
3.8167
3.9400
4.2260
4.6401
--`,,-`-`,,`,,`,`,,`---
Not for Resale
116.11
112.16
108.35
104.01
97.57
96.24
92.05
90.24
87.31
&.?v
8
24
.6
81.26
79.81
78.05
76.85
76.13
74.11
72 .O5
70.89
lam
24.22
24.93
18964
18942
18925
1 W
18894
18683
18863
18854
18707 P
P
18766 P
18?76 P
18761
n
25.55
26.14
188R
1am
73
74
26.71
27.15
27.52
28.01
28.27
28.54
27.75
27.91
29.18
28.14
28.29
76
77
M
1
r
79
80
81
82
1
a3
1r
v
v
1
W
W
~
~
V
10758 P 22.96
10745 P 28.49 V
18754 P 27.01 V
18741 P 20.63 V
18740 P 24.40
04
85
ab
87
88
89
90
91
92
1-59
~~
~
~~
~~~
~
~~
S T D - A P I / P E T R O T D B C H A P T E R L-ENGL L777 W 0 7 3 2 2 9 0 O5bbb5O 4 2 7 W
TABLE 1C1.2
CYCLOPARAFFINS: PRIMARY PROPERTIES
T
C r i t i cC
a la r s t a n t s
Fomulr
"U.
Boiling
Point at
1 atm
dcoF
Freezing
Point in
air at
1 atm
\cent r i,
:actor
Pressure
pia
dcoF
Alkylcyclopmpanes,
C3 t o C5
93 CYCLOPWANE
94 HETHYLCYCLOPROPM
95 ETWYLCYCLOPROPAWE
96 citil,2-DlUETHYLCYCLOPROPPAYE
97 trms-l,2-DIWETHYLCYCLOPROPANE
I-
42.08
56.11
70.13
70.13
m.13
-27.00
33.31
96-67
98.65
54.52
97.34
159.08
-131.21
C6H12
56.11
70.13
84.16
C5H10
C6Hl2
cm14
CM14
CM14
C7H14
CM14
c7H14
70.13
84.16
98.19
98.19
98.19
98.19
98.19
98.19
120.65
161.26
218.25
1ÇQ. 13
211. 15
197.37
195.39
197.11
-136.91
-220.36 P
-217.19 P
-93.62 P
-65.00
-179.63
-208.66
-209.15
461 .50
499.35
565.47
524.93
557.60
536.00
532.13
535.73
C8H16
cBH16
C8H16
112.22
112.22
112.22
267.73
259.57
250.74
-179.21
-168.45
326.84
613.13 P
607.73 P
587.93 P
C8H16
112.22
262.49
-158.71
C8H16
112.22
250.16
-158.67
cBH16
112.22
250.00
...
C8H16
C8H16
CEM6
112.22
112.22
112.22
250.00
236.71
220.81
-6.95
C8H16
112.22
cBH16
c3H6
c4H8
C5HlO
CS1110
Sn10
82.78
-
-197.61
-287.14
-236.59
-221.57
-237.23
256.57
674.87P
407.82 P
410.92 P
."
797.00
659.29 P
0.1269
0.1570
0.2170
0.2410
569.04 P
569.04 P
...
...
Alkylcyclobutants, C4 t o C6
98 CYCLOBUTANE
UM8
99 l4ETHYLCYCLOWfANE
6HlO
100 ETHYLCYCLOBUTANE
Alkylcyclopentanes,
1o1
102
103
104
1o5
106
107
108
-
P
368.20 P
417.45 P
488.55 P
722.30 P
0.0600 P
529.03 P
0.0624 P
0.0625 P
0.2730
0.2828
0.2733
O. 0589
0.0607
0.0612
0.0587
0.0604
0.0587
0.0587
0.0587
P
0.2730
0.2730
0.2690
0.2730
0.2710
0.2700
0.2710
0.2700
438.02 P
440.92 P
438.02 P
0.0611 P
D.0600 P
D.0611 P
0.2610
0.2590
0.2670
0.3266
0.3030
0.3298
605.43 P
b38.29 P
D.0611 P
0.2628
0.3278
587.26 P
438.29 P
0.0611 P
0.2673
O J293
586.98 P
438.29 P
0.0611 P
0.2674
0.3280
-224.39
586.98 P
567.37 P
543.92 P
438.29 P
438.29 P
438.29 P
0.0611 P
0.0611 P
0.0611 P
0.2674
0.2725
0.2789
0.3291
0.3324
0.3318
253.40
-177.57
592.00 P
438.29 P
0.0611 P
0.2661
0.3307
112.22
243.50
-169.60
577.38 P
438.29 P
0.0611 P
0.2699
0.3325
-H16
112.22
230.36
-170.87
558.57 P
438.29 P
0.0611
P
0.2749
0.3315
W16
112.22
242.60
-206.19
575.42 P
438.29
0.0611 P
0.2704
0.3281
...
-224 -95
608.44 P
0.1647
0.1830
0.2250
CS t o C7
CYCLOPENTANE
UETHYLCYCLOPENTANE
ETHYLCYCLWENTANE
1,l-DIUETHYLCYCL~ENTANE
cis-l,24lCtETHYLCYCLOPENTANE
trans-l,2-DIUETHYLCYCLWENTANE
cis-l,3dlUETHYLCYCLOPENTANE
trans-l,3-DIUETHYLCYCLOPENTAWE
652.97
568.98
P
P
P
P
P
492.85
499.66
499.67
499.67
499.66
499.66
P
P
P
P
P
P
P
P
P
0.1959
o. 2302
0.2716
o. 2724
0.2662
O. 2698
O. 2743
O. 26W
Alkylcyclopentanes, c8H16
109
110
111
112
HRWYLCYCLWENTANE
1MPROPYLCYCLOPEWTANE
1-HETHYL-1fTHYLCYCLOPENTANE
CiS-l-UETHYL-2-ETHYLCICLOPENTANE
113 trans-14ETHYL-2-ETHYLCYCLOPENTANE
114 cis-l-HETHYL-3-ETHYLCYCLOPENTANE
115 trsns-l-UETHYL-3-€THYLCICLOPENTANE
116 1,1,2-TRIUETHYLCYCLWENTANE
117 1,1,3-TRIUETHYLCYCLOPEUlANE
118 l,c-Z,c-~lRlMTWYLCYCLOPENTANE
119 I,C-2,t-3-TRIRETHYLCYCLOPENTANE
120 I,t-2,C-3-TRlUETHYLCYCLOPEWTANE
121 I,C-2,C-4-TRlHETHYL-
-
CYCLOPENTANE
...
P
N o k Footnote c
o
d
a follow Table 1C4.12.
1-60
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
1997
Not for Resale
--`,,-`-`,,`,,`,`,,`---
1c1.2
S T D . A P I / P E T R O TDB C H A P T E R L - E N G L L997 m 0 7 3 2 2 9 0 OSbbb5L 3 b 3 m
1c1.2
TABLE lCl.2 (Continued)
~
1/60
AP I
Gravity
a t M) F
deg API
L i q iR
de f r a c t i v e
Density I*X
of
a t M ) F the Liquid
lb/galat
77 F
:inmatic Viscosity
I f theLiquid
I
:entistokes
~
0-l
~
: 210 F
:deal Gas
Liquid a t
I atm
0.3041
0.33% I
O. 4970
0.3160 P
03357 P
0.3355 P
eat of
'aporizItion at
ailing
'oint
nu/lb
let Heat
Liquid
Jf callSurf ace
ustion
T u t s i cm
I f Liquid at 77 F
It
77
--`,,-`-`,,`,,`,`,,`---
ccific
avity
F
ItWlb
rlkylcyclopropew, C3 t o CS
45 .m
...
...
...
...
0.UG I
0.3699 I
O. 2487
...
...
...
...
...
...
...
...
...
...
M3 .34
...
220.14
221.o6
...
19286
&lkylcyclokrtams, C4 to C6
D.6991
D.7327
0.6977
1 I 1
70.90
71.30
61.61
5.829
1.36200
6.109
5.817
1.39940
1.38100
i
I
1
o. 7502
3.7540
1.7712
1.7593
3.7771
3.7561
3.7496
3.7534
57.12
56.17
51.98
54 85
50.59
55.63
57.28
56.31
-
6.254
6.286
6.430
6.331
6.479
6.304
6.249
6.281
I1Ilkylcyclopentanes,
0.2891
0.3254 I
0.0339 I
0.4562
0.3356 P
0.3427 P
0.3528
9.9185
0.2721
0.2992
0.3125
0.3148
0.3167
0.3177
0.3177
0.3177
0.4227
0.4404
0.4433
O -4493
0.4502
0.4453
0.4529
0.4481
0.4973
4.5044
1 .&o66
0.3249
0.3157
0.2705
0.4514
0.3616 i
0.3620 F
O. 7257
34.1629
...
...
1.40363
1.40700
1.41730
1.41091
1 A1963
1.40941
1 .bo633
1.40813
2.5730
1.6484
2.1929
2.2497
2.2066
...
,..
0.5646
0.6199
0.5845
0.56%
O. 5870
0.5928
0.5886
...
...
...
...
...
0.3901
...
183.76
222.37
207.28
l .
...
."
...
166.55
149.04
140.41
134.17
138.85
136.60
134.66
135.80
18825
18769
18758
18720
18749
18723
18728
1 8736
0.4613
0.4370
0.4354
133.70
129.46
127.30
18749
24.42
18752 P 23.84
18732
24.18
0.3655
'
!1.78
5-33
Y.20
5-62
101
102
103
104
105
z1.20
106
20.93
21.38
107
108
!1.65
C8H16
3.7811
D. 7806
o. 7853
49.66
49.78
48.70
6.512
6.508
6.547
1.42389
1.42350
1.42476
0.4714
0.5964
0.78%
47.71
6.583
1 .C2695
0.5500
O .m
51 -46
6.448
1.41950
0.7200
0.7712
51.97
6.430
1 -41
0.7712
51.97
50.58
56.47
6.430
6.479
1.41700
0.7400
0.7771
0.7528
1A2051
0 . m
6.276
1.40870
1.3930
O. 7837
49.05
6.534
1 .c2380
0.7750
51.09
6.461
0.7581
55.16
0.7760
50.84
0.7236
700 0.7100
...
...
...
...
..-
0.3760 I
...
...
0.3761 I
...
...
...
0.3755 f
0.3604
0.3604
0.3761 I
0.3767 I
0.377!i I
O -6900
...
0.3759 I
1.41960
0.8500
...
0.3764
I
6.320
1 .c1140
l. 1400
0.3770
6.C70
1.42000
o. 8400
0.3764
...
...
0.7335
0.7249
...
...
...
...
...
I
...
...
...
...
...
I
...
...
18873 P 24.83 P 112
18873
P
22.81 P 113
...
18873
P
22.51 P 114
....
..
...
18873 P 22.51 P 115
18829 P 23.24 P llt
18829 P 20.42 P 117
...
...
133.37
...
18873
P
24.05 P l i e
18840 P
22.99
P
115
18840 F
21.02
P
12[
P
12' 23.06
188.40 F
1-61
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
...
...
...
...
109
110
111
Not for Resale
1c1.2
TABU lCl.2 (Continued)
Foraulc w.u.
Boiling
Freezing
Point a t
Point in
1 atm
air at
-T-
1 am
degF
dcoF
Critical
Constants
Pressure
p i e
v0 L u l l e
CU
ft
per lb
T.centric
actor
O .3306
~lkylcyclopmtames, W 1 6
I 2 2 l,c-2,t4TRIIIEIHYLCYCLOPENTAUE
1 2 3 l,t-2,c"TRIUETHYLCYCLOPEUTME
f
:ampress
bility
:actor
C8H16
112.22
242.12
-206.59
sT1.38
P
438.29 P
0.0611 P
0.2699
W16
112.22
228.72
403.40
555.60 P
436.29 P
0.0611 P
0.2757
C9H18
C9H18
126.24
126.24
313.88
298.31
-162.35
-175.41
658.13 P
664.12 P
394.51 P
422.40 P
0.0613 P
0.0579 P
0.2540
0.2561
03719
0.2670
C9H18
C9H18
294.80
302.90
308.41
...
-180.40
631.02 P
6C2.72 P
650.m P
395.00 P
395.00 P
395.00 P
0.0613 P
0.0613 P
0.0613 P
0.2610
0.2583
0.2564
0.3760
C9H18
126.24
126.24
126.24
O .3?30
C9H18
126.24
280.40
...
610.20 P
395.00 P
0.0613 P
0.2661
0.5m
355.35
321.99
291.53
265.42
242.22
221.91
203.06
185.65
171.15
158.09
145.04
133.44
172.68
165.52
158.92
152.83
0.0613
0.0615
0.0616
0.0617
0.0618
0.0618
0.0619
0.0619
0.0620
0.0620
0.0621
0.0621
0.0622
0.0623
0.0623
0.0623
0.2460
0.2380
0.2290
0.2210
0.2130
0.2050
0.1960
o. 1890
0.1810
O. 1740
O. 1670
0.1600
0.2117
0.2098
0.2081
O . 2067
0.4184
0.46A6
0.5100
0.5525
0,5956
0.6314
0.6741
0.7163
o.aro
nlkytcyctcpmtam, m18
124
MYLCYCLOPEUTANE
ISOBUTYLCYCLOPENTANE
125
126
l-HETHYL-1"PROPYLCYCLOPENTAUE
127 1,l-OlETHYLCYCLOPENlANE
128 ciS-l,2-DIETHYLCYCLOPENTAE
129 1,l-OI~ETHYL-2-€lHYLCYCLOPENTANE
P
.I.
~
0.3730
~~~
hlkylcyclopentanes, C10 t o C25
130
131
132
133
134
135
136
137
138
139
140
141
142
143
1U
145
n-PENTYLCYCLOPEUTAUE
n-tiEXYLCYCLOPENTANE
MEPTYLCYCLOPENTANE
I"OCTYLCYCL0PENTANE
n-WONYLCYCLOPENTAUE
MECYLCYCLOPENTANE
n-UNDECYLCYCLOPENTANE
MCOECYLCYCLOPENTANE
n-TRIDECYLCYCLOPENTANE
n-TETRADECYLCYCLOPENTANE
r+PENTADECYLCYCLOPEUTANE
n-HEXADECYLCYCLWENTANE
MEPTADECYLCYCLOPENTANE
nOtTADECYLCYCLOPENTANE
n"DNADECYLCYCLOPEN1ANE
--`,,-`-`,,`,,`,`,,`---
-M1M)SYLCYCLOPPENTANE
ClOH2O
C l 1 H22
Cl2H24
C13H26
C14H28
C l 5 H30
C16H32
C l7
H
u
Cl8HM
C19H38
c20H40
C2ln42
u 2 w
140.27
154.30
196.38
210.40
224 -43
238.46
252.48
2M.51
280.54
308.59
C23H46
322.62
C24H48
336.65
350.67
C25H50
356.90
397.22
503.60
534.88
564.44
592.16
618.62
644.00
M7.40
690.80
710.60
732.20
752.00
770.00
-117.40
-99.40
-63.40
-47.20
-20.20
-7.83
14.00
23.00
41 .o0
48.20
62.60
294.5669.80
80.60
86-00
95-00
100.40
699.17
735.71
769.01
799.43
827.15
852.71
876.29
898.25
918.41
937.13
954.59
970.79
1000.42
1017.61
1032.87
1046.21
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
0.7582
0.7949
0.83%
0.8755
0.9060
1.o010
0.9660
1.on0
kltylcyclohexans, C6 and C7
146 CYCLOHEXAWE
147 l4ETHYLCYCLOHEXANE
C6H12
C7H14
43.77
-195.83
P
536.77
570.27
590.75
503.C3
636.80 P
440.92
426.19
426.19
426.19
0.0586
0.0600
0.2730
0.2690
0.2096
O. 2350
0.2580
0.2690
o. 2680
0.2730
0.2455
0.2326
O. 2324
0.2379
Llkylcyclohexanes, C8H16
148
149
150
151
ETHYLCYCLOHEXANE
an16
C8H16
C8H16
,~-OIMETHYLCYCLOHEXANE =H16
~,I-OIIIETHYLCYCLOHEXAWE
cis-l,2-DIMETHYLCYCLOHEXAUE
trans-1
-168.36
-28.28
-S?. 98
-126.69
604.40 P
631.40 P
613.40 P
P
P
P
P
0.0614
0.0642
0.0657
0.0657
P
P
P
P
Notr Footnote codes follow Table lC4.12.
1997
1-62
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
~
STD.API/PETRO TDB CHAPTER
L-ENGL
0732270 05bbb53 L3b
L977
--`,,-`-`,,`,,`,`,,`---
1c1.2
TABLE 1C1.2 (Continued)
ressure
tu/lb ckg F
centistokes
. i q ~ i dat
I lm
1 I 1
1
at 100 F
,
210 F
klkylcyclopentanes, -H16
0.7680
52.74
6.403
1.41612
...
0.3719
...
."
1.lm
1.40812
6.268
0.7518
56.71
~~
0.8810
____
Alkylcyclopcntanes, C9H18
0.1567
...
...
".
...
...
0.3246
...
...
...
...
...
...
...
...
1.5148
...
...
...
...
...
...
...
1.1280
1.4150
1.7480
2.1300
2.5700
3.0500
3.6300
4.2500
4.9500
5.7100
6.5600
7.4900
0.6200
o. 7300
0.8500
0.9118
0.4546
0.3867 P
0.3868 P
0.3865 P
0.3863 P
0.3874 P
-
I i .:
kat of
Wet Heat
h p o r i 2-
of
rtim at
lornL
loi 1 n
ig
boi nt
ltu/lb
bustion
of Liquid
a t 77 F
Btu/lb
40.
com-
...
...
!2.18 P
122
10.33 P
123
-
123.18
170.32
18743 , 25.36
18831 P 24.29
171.18
lm P
173.30
18860 P
174.72
18869 P
26.56 P 124
20.76 P 127
26.20 P 128
167.42
18831 P
25.16 P
116:ii
114.07
111.66
109.27
18738
18733
18730
18726
18723
18721
18719
18717
18716
18714
18713
18712
18863 V
18862 v
18861 \
18860
26 30
26.90
27.40
28.00
28.60
28.89
28.47
28.70
28.86
29.01
29.13
29.23
29.42
29.52
29.59
29.66
124
125
129
-
Alkylcyclopentanes, C10 t o C25
6.631
6.675
6.712
6.743
6.771
6.794
6.816
6.834
6.851
6 . a
6.880
6.892
6.903
6.914
6.922
6.932
...
...
...
...
...
...
...
...
...
1.43360
1.43700
1.44000
1.44250
1.Cc460
1.4U59
1.44820
1.44970
1.45100
1.45220
1.45330
1.45430
1.45520 I;
1.45600 fi
1.45600 I
1.45750 1
R
R
R
R
R
R
...
...
...
...
...
.....
0.3495
0.3568
O. 3629
O"80
O .3R5
0.3763
0.3796
O -3826
0.3852
O. 3876
O -3897
0.3916
...
...
".
...
0.3962
0.4058
0.4150
0.4239
0.4326
0.410
0.4493
0.4574
0.4654
0.4732
...
...
...
...
...
P
P
P
P
P
P
P
P
P
P
...
...
...
...
...
a.mo
1.1200
l . 2700
1 .u00
1.6100
1.7800
1 .9800
2.1900
2 .coo0
...
...
...
...
...
...
...
...
".
103.61
97.46
94.82
...
...
...
-
130
131
132
133
f
f
F
I
I
I
\
\
1
134
135
136
137
138
139
1CO
141
142
143
1U
145
-
Alkylcyclohexanes, C6 and C7
0.7823
0.7748
I
49 38
51113
I
6 522
61460
1
1.42354
1.42058
3.2977
1. a 7
~~
...
O. 2926
0.3100
0.4757
153.09
136.95
18676
1WO
24.64
23 -30
0.3277
0.3185
0.3230
0.3279
0.5122
0.5043
0.6717
0.5043
130.66
124.30
128.51
125.92
186M)
25.05
23.65
25.19
23.57
~~
14t
Ilì
-
Alkylcyclohexanes, a l i 1 6
0.7926
0.7854
0.8006
0.7803
48.67
45.23
49.05
47.02
j
6.608
6.548
6.675
6.505
1
1.42642
1.43358
1.42470
1.43073
0.4834
0.8193
0.5398
O .?o60
18662
18637
141
145
150
151
1-63
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
18635
Not for Resale
~
~
~
~
S T D - A P I / P E T R O T D B C H A P T E R L - E N G L L997 m 0 7 3 2 2 7 0 0 5 b b b 5 q O72 m
10.2
TABLE lCl.2 (Continued)
No.
Conpovld
F o WL a
n.Y.
Boi ling
Point at
1am
dtoF
T
Freezing
Point in
air at
1 atm
Critical
Constants
Pressure
psis
Volune
-
l
-
Lcentric
Tcap
traturc
CU
ft
per Lb
Coaprcssibility
Factor
:actor
0.2690
0.2720
0.2720
0.2690
0.066
dcsF
AlkylcycloheaaneS, a 1 6
152
153
154
155
-104.03
-130.14
-125.37
-34.49
112.22
112.22
248.16
256.03
t12.22
112.22
255.78
246.85
C9H18
C9H18
ClOH20
ClOH2O
C10H20
C10H20
126.24
-138.82
314.15
-128.90
310.57 126.24
357.77
-102.51
ClOH2O
140.27
339.30
C l 1H22
398.66
436.46
472.82
PZW
151.30
168.32
182.35
196.38
210.40
224.43
238.46
252.48
266.51
280.54
294.56
308.59
c23n46
322.62
cz4m
U5H50
UbH52
336.65
350.67
a 1 6
W16
an16
cis-l,CDIHETHYLCTCU)IIUUWE
t ~ ~ l , 4 - D I H E l H Y L C Y C L O ~c8n16
cis-l,MIHETHYLClCLOHDUWE
tranr-l,3-DIlETWLCYCLOHEXE
604.40
616.73
617.00
602.60
P
P
P
P
426.19
426.19
426.19
426.19
P
P
P
P
0.0642
0.0657
0.0657
0.0642
P
P
P
0.0605
0.0589
0.0610
0.0476
0.0593
0.0583
P
P
0.2335
0.231 1
0.2370
-
Alkylcyclohexaries, C9 and Cl0
156
157
158
159
160
161
162
n-PROPYLCYCLOHEXANE
ISOPROPYLCYCLOHEXANE
n-BtJlYLCYCLOHEXANE
ISOBUTYLCYCLOHEXANE
sec-BUTYLCYCLMIEXANE
tert-BIITYLCYCLOHEXANE
l"ETHYL4-ISWROPYLCYCLOHEXANE
140.27
140.27
140.27
140.27
340.32
354.70
340.83
690.80 P
668.93 P
407.13 P
413.36 P
P
0.3006
P
P
0.2486
0.2510
375.05 P
0.0593 P
0.2534
0.3530
320.54
291.53
265.42
242.22
221.91
239.32
187.10
171.15
158.09
145.04
134.89
124.73
168.29
161.47
155.18
149.36
0.0604
0.0606
0.0608
0.06Op
0.0611
0.0612
0.0613
0.0614
0.0614
0.0615
0.0616
0.0616
0.0618
0.0618
0.0618
0.0619
0,2320
o. 2240
0.2160
o. 2080
0.2010
0.2270
0.1860
0,1780
0.1710
0.1640
0.2140
0.1510
0.2104
0.2087
0.2072
0.2058
O. 4498
0.4931
0.5280
0.5793
O. 6205
0.6627
0.6988
O. 7402
O. 7?49
0.81 15
0.8506
O. 8897
0.9168
0.9510
0.9887
1.O217
O. 2700
0.2430
0.2904
0.2680
0.3520
0.4276
...
740.93
729.05
710.17
702.39
P
573.77 P
375.05 P
382.92 P
."
688.03 P
-71 -50
45.40
744.53 P
778.19 P
I..
42.09
P
P
P
0.2520
0.2540
0.2470
0.25%
0.3295
O .2?&3
0.4084
0.3520
0.3380
372.75 P
P
P
163 n-PENTYLCYCLOHEW3(€
164 MEXYLCYCLOHEXANE
165 MEPTYLCYCLOHEXANE
166 n-OCTYLCYCLOHEXAUE
167 n-NONYLCYCLOWUUWE
168 rrQECYLCYCLOHEXANE
169 ~PUNDECYLCYCLOHEXANE
170 n-000ECYLCY'CLOHEWNE
171 rt-TRIDECYLCYCLOHEMNE
172 rt-TETRADECYLCYCLOHEXNE
173 n-PENTADECYLCYCLOHEXE
174 ri-HEXMECYLCYCLOHEXANE
175 f+HEPTADECYLCYCLOHEXANE
176 rMCTADECYLCYCLOHEXANE
177 n-WONADECYLCYCLOHEXANE
178 n-€ICOSYLCYCLOHEXANE
C12H24
C13H26
C14H28
C15H30
C16H32
c1m34
C18H36
C19H38
C2OH40
c21H42
364.70
5w.w
538.70
567.68
5% .58
621 -86
646.70
669.20
692.60
714.20
735.80
755.60
m.60
791.60
32.90
-4.72
13.64
28.89
42.44
54.50
65.30
76.28
85.M
92.66
100.04
104.90
113.36
119.30
808.79
P
1136.87
862.61
892.58
900.15
928.31
947.03
964.49
980.69
P
P
P
P
P
P
P
P
995.63 P
1025.40 P
1040.47 P
1053.63 P
1067.09 P
~
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
~~
Cycloparaffins, C7 t o C12
179 CYCLOHEPTAHE
180 CYCL00tTANE
181 CYCLOUWANE
182 ETHYLCYCLOHEPTANE
183 BICYCLOHEXYL
cm14
CBH16
WH18
CPHl8
ClZn22
17.60
58.69
51-80
I
.
.
38.53
628.07
692.33 P
768.00
691.77 P
848.93 P
-
Note: Footnote codes follow Table lC4.12.
1997
1-64
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
--`,,-`-`,,`,,`,`,,`---
Alkylcyclohexanes, C11 t o C26
1c1.2
TABLE lCl.2 (Continued)
c
7
1
Specific API
Gravity
Gravity
160160
at 60 F
Liquid Refractive
Density Indcx of
a t 60 F the Liquid
'rasure
i t d l b de0
F
8t
lb/gsl
F
centistokes
leat of
Nlet Heat
I
f q r iz-
aIf
htim at
lorma 1
tustion
5
1
CIfLiquic
I l
loi 1 n
ig
boi nt
itu/Lb
F
aI t
EI t W l b
I
copr
n
I
I
Ideal G a
Ligrid a t
a t 100 F
t 210 F
1 atm
1.42063
1.42843
1 .S2731
1.41853
6.423
6.580
6.5G
6.395
41.75
6.654
6.723
6.698
6.
801
0.8161
6.813
6.809
0.8167
33.30
7.158
0.7981
0 . U
0.8033
43.98
U.64
41.88
0.81R
0.8586
1.43470
45.79
1.43861
1.43855
...
0.7819
0.6509
0.6606
0.8201
0.4360
0.8900
D.5134
0.3250
0.3250
0.3254
0.4435
0.6645
0.8797
0.7491
D.44W
O
m
l.
0
0.?390
O. 1925
0.0575
O .O907
0.3750
0.3428
...
."
...
1.44450
41.65
1.44470
...
P
O. 3268
...
...
...
...
0.4422
0.4382
1.0010
0.4485
1.0491
0.4510
1.2539
0.4514
0.3685 P
0.5143 P
0.3684 P
...
...
...
...
0.3686 P
D.5040
D.4724
0.5759
0.5569
0.6881
...
..-
...
...
125.37
127.38
126.97
124.43
-
124.14
124.87
118.75
"
18619
18647
18647
18621
...
...
AlkylcyclohexMes,
o -8077
0.8115
0.8140
0.8177
0.8202
0.8223
o. 8244
--`,,-`-`,,`,,`,`,,`---
0.8261
0.8277
0.8291
0.8303
0.8316
0.8327
O 8337
-
0.8346
0.8355
0.0190
43.69 6 . 7 3
1.44160
1.44410
o .O062
42.86 6.766
42.17 6.793
1.44630
o .o020
1.44840
0.0006
41.55 6.817
o. 0002
1.44WO
41.02 6.838
0.0001
1 .C5141
40.59 6.855
<.o001
40.14
1.45270
6.873
39.80 6.887
1.45390
< O001
<.o001
R 1.45500 6.901
39.45
<.o001
R 1.45590 6.912
39.18
<.o001
38.93 6.922 R 1.45680 E
38-66 6.933 R 1.45760 I <.o001
38-44 6.942 R 1.45830 I:
38.22
6.951 R 1.45900 I:
38.05
6.958 R 1.45960 E
6.964 R 1.46420 I;
37.85
.
...
...
...
...
:
0.8545
0.8900
I z:::1 1
42.24
6.790
1.44240
34-10 7.124
1.46440
27.49
1%
157
138
159
160
161
162
"
C11 t o C26
0.3643
...
....
..
...
1.5560
1.9400
2.3800
2.9000
3.4800
4.1675
4.8700
5.6700
6.5800
7.5800
8.6700
9.8700
0.7700
0.8900
l. 0300
l. 1700
1.3200
1.3916
1 .MD0
1 .a300
2.0300
2.2300
2.4500
2.6700
...
...
."
...
...
...
...
...
0.3496
0.3520
0.3540
0.3559
0.3574
0.3568
0.3600
0.3610
0.3620
o. 3628
O. 36%
."
...
."
0.3726 P
0.3782 P
0.3836 P
0.3889 P
0.3942 P
0.4740
0.4049 P
0.4102 P
...
...
...
...
...
113.78
18666
18670
18671
...
...
102.50
18672
...
106.26
99.71
...
...
...
.....
...
...
I . .
...
"
0.8145
26.07
25 .m
26.51
;25.34
;26.W
:26.18
18754 IP :3
3.88 F
163.42
152
153
154
155
"
"
I
22.59
24.15
23.94
22.52
18662
18656
18667
18781 IP
18781 IP
18746 IP
167.02
Ho.
7.420
1.47768
1.45,
0.7926
0.2233
...
...
O. 0054
0.307%
0.2988
0.3795
...
0.3040
0.4308
0.4498
1.4796
2.1251
.I.
0.3603 P
2.9174
0.4212
...
...
...
...
146.89
139.54
129.95
180.58
115.08
18826 V
18826
18827
V
V
1 63
164
165
166
167
168
169
29.29
171
172
173
1 74
175
1 76
177
178
29.51
29.53
29.61
29.76
29.83
29.89
29.95
"
18783
18824
18856
18901 P
18233
26.W
29 -32
34.95
26.43
32.17
-
1M
175
180
181
182
182
1-65
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
...
0.8080
0.8820
18675
18676
18677
18670
18676
18678
18678 R
18677 R
18825 V
27.00
27.50
27.90
28.40
28.90
29.34
28.98
29.16
Not for Resale
~~
STD.API/PETRO TDB CHAPTER
L-ENGL
L997
m
0732240 05bbb5b 9Y5
m
--`,,-`-`,,`,,`,`,,`---
1c1.2
TABLE 1C1.2 (Continued)
Freezing
Fowls
i
t o n s t a n tCsr i t i c a l
Pressure
air a t
7
i
Acntric
Factor
per l b
erature
1 atm
Factor
Decahydromphthalenes, C10 t o Cl2
Cif+DEUHYDROlAPHTMLENE
tr8ns-OEUHYDRONAPHTHMENE
14ElHYL-Icif+DECAHYDRO-
Clon18
ClOH18
NAPHTHALENE1
138.25
138.25
384.47
152.28
469.40
369.16
14ETHYL-ttrans4ECAHYDRO-
152.28
NAPHTWENEI
455.00
l-€fHYL-[ci+-OEUHTDRO-
166.31
500.00
ClZHZZ
166.31
491 .OO-
c12H22
166.31
451 .O0
Cl2H22
166.31
437.00
NAPHTHALENE]
l-ETHYL-[trans-DEUHYDRO-
NAPHTHALENE1
~THYL-Ccis4EUHYDR&
NAPHTHALENE1
%ETHYL-Ctrans-OECAHYDR&
NAPHTHALENE3
45.31 P
-22.65 P
...
...
...
.I.
...
...
Note: Footnote eodes follow Table lC4.12.
1-66
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
W .38
469.93
777.02
430.77 P
0.0556
0.0556
0.2660
0.2500
899.53 P
388.28 P
0.0568 P
0.2303
0.2939
0.2?24
0.3ocO
~
178.45 P
388.28 P
0.0568 P
0.2339
0.3oCO
1
853.03 P
353.82 P
0.0573 P
0.23%
0.3960
824.95 P
353.82 P
0.0573 P
0.247
0 -3960
837.77 P
353.82 P
0.0573 P
0.2425
0.3960
817.27 P
353.82 P
0.0573 P
0.242
O. 3960
1c1.2
TABLE 1C1.2 (Continaed)
Spcific
Gravity
60/60
API
Liqid
Gravity D e w i t y
a t 60 F a t 60 F
deg API Lb/gal
Heat Capacity
Kinematic
Viscosity
a t 60 F erd Constant oftheLiquid
Pressure
at
Btu/lb dcg F
catistakes
Refractive
l r d u of
Liquid
77 F
the
at
n
I
Detahydronephthalm, C10 to C12
25.41
0.9018
0.8755
U).13
1.0146
7.97
...
...
.”
...
.-.
..--`,,-`-`,,`,,`,`,,`---
0.8900
27.49
0.8668
32.12
8.459
...
P
.”
---
7.210
1 .M980
I
1
0.0354
0.0533
...
II.
of
ation
N o m1
Boi 1 ing
bustion
c m
ofLiquid
a t T7 F
BtWLb
0.2773
0.2782
...
...
”.
...
...
...
...
...
...
...
...
0.3924
2.6334
1.0925
0.3861
1 A198
0.8535
0.3690
...
...
0.3b94
...
...
...
0.3732
...
...
...
0.3739
...
0.3731
0.3736
Liquid No.
Surface
Tension
a t 77 F
dYne/m
...
...
...
123.77
118.70
18323
38288
177.77
...
174.57
159.11
...
...
159.89
...
...
156.99
...
158.07
31.71
29.44
52.5 P
18c
185
186
49.28 P 187
c3.75 P 100
39.74 P 189
31.74 P 190
28.21 P 191
1-67
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Net Heat
Btu/lb
...
1.46400
Heat of
Vaporiz-
Not for Resale
1Cl .3
TABLE 1C13
MONOOLEFJNS AND DIOLEFINS: PRIMARY PROPERTIES
1
Critica
Cla s t a n t s
M.Y.
A c n t r iI
Freezing
Boit i n g
point o t
1 am
Point in
a i r at
l a m
dcsF
dcpF
Tcllp
erature
:arprcss- Factor
Pressure
pria
VOlrar
731.
o
0
676.61
0.0748
0.0717
0.2810
0.2890
0.0865
0.1398
0.0683
0.0668
0.0679
0.0682
O.27m
0.2740
0.2730
0.2750
0.1905
0.2048
0.2177
0.1943
O. 0674
0.0667
0.2680
0.2690
0.2720
0.2570
0.2840
0.2540
0.2312
0.2452
0.2&
O.aO0
0.2297
0.2753
0.2650
0.2m
0.2670
0.2804
0.2722
0.2613
0.2787
0.285&
0.2406 0.2690
0.2640
dcsF
bility
:actor
ft
per Lb
CU
k n d e f i r s , C2 Md t3
28.05
192 ETHYLENE
193 PROPYLENE
48.54
-272.47
-301.47 -53.84 198.36
-154.73
42.08
n a p o l e f i r s , t4H8
194
1%
196
197
1-BUTENE
cis-2-WlENE
trars-2-EUlEWE
ISOBUTENE
56.11
56.11
M. 11
56.11
20.75
=.m
70.13
70.13
70.13
70.13
13
13
85.93
98.47
97.41
19.58
-301.63
-218.00 P
-157.95 33.58
-220.61
296.24
324.37
311.86
292.55
586.40
-265.40
376.93
395.69
393.89
509.53
527.95
530.85
493.14
510.54
493.14
615.41
594.66
580.16
Momolefirs, C5H10
198 14EWTENE
199
cis-2-PEYTENE
200 trans-Z-PEWTENE
201 2-HETHYL-)-EUTENE
202 3-nETHYL-lWEWE
203 2-MTHYL-2-BUTENE
C5H10
CSHI0
QHlO
bHl0
C5H10
C5H10
m.
m.
-240.52
-220.47
315.63
-271.28
88.08
68.10
101.40
-208.77
146.26
-219.57 P
-222.07
-207.36
-216.08
-172.16
-212.31
. -243.31
-24.55
-211.14
-210.71
-217.20
-210.73
-221 .u
-204.77
-251 .O?
-175.36
-101.61
3n.33
351.00
388.13
0.0669
0.0667
0.0690
0.0667
Monoolefirm, C6H12
204
14EXENE
205 C is-2-HEXEWE
206
tr&-HEXENE
207
cis-3-HEXENE
208 t r 8 n s ” E X E N E
209
2-CIETHYL-I-PENTEWE
210 Z-METHYL-I-PENTENE
CWETHYL-1-PEWTENE
211
212
2-UETHYL-24ENTENE
213 cis-3”ElHYL-24ENlEN€
214 trans-3”ETtlYL“PENlENE
215 cis44ETHY1-2-PEWTENE
216 t r ~ E T H Y L - 2 4 E U T E N E
217
2-ETHYL-l-BUTENE
218
Z,3-OIMETHYL-l4LtlENE
219 3,WIHETHYL-I#JTEWE
220
2,3DlHETHYL-2-BUTUIE
u n 12
C6Hl2
WH1 2
C6Hl2
C6H12
C6H12
C6H12
c6H12
W12
C6W12
C6H12
CM112
C6H12
W12
CM112
W12
m12
84.16
84-16
84.16
84.16
84.16
84.16
84.16
84.16
84.16
84.16
84.16
84.16
84.16
84.16
84.16
86.16
84.16
155.98
154.17
151.61
152.76
143.78
129.52
128.95
153.14
153.86
158.79
133.4
137.48
148.41
132.10
106.25
163.76
447.58
463.73 P
w.73 P
456.53 P
456.53 P
452.93 P
431.33 P
b33.13 P
465.53 P
467.33 P
470.93 P
438.53 P
442.13P
461.93 P
440.33 P
404.33 P
483.53 P
455 -43
458.33
458.33
459.78
459.78
458.33
477.18
O. 0674
P
0.0683 P
P
P
0.0685 P
0.0668 P
P
0.0668 P
P
0.0.0653
0.0657
0.0691
0.0653P
0.0653
0.0659
0.0659
0.0693
P
0.0664 P
0.0634 P
P
0.0708 P
0.2740
0.2690
0.2680
0.2ao
0.2550
0.2690
0.2670
0.2700
0.2700
0.2750
0.2700
O. 0674
0.0692
0.0662
0.0687
0.0662
0.2620
0.26cO
0.2560
0.2bGO
O .2580
P
467.03 P
458.33 P
477.21 P
462.68 P
467.03
467.03
458.33
467.03
477.18
458.33
P
P
0.2630
0.2630
P
P
P
P
P
P
P
P
P
P
0.2389
0.2445
0.2585
0.2627
0.2442
0.2552
0.2277
0.2269
0.2257
0.2333
-.
Wonoolefins, C7H14
221 I-HEPTEWE
222
cis-Z-HEPTEWE
223 t r d - H E P T E N E
224
cis-3-HEPTENE
225 trms-3-HEPTENE
cn14
C7H14
CM14
C7H14
CM14
98.19
98.19
98.19
98.19
98.19
200.55
209.14
208.31
204.35
204.21
-164.47
-165.06
-213.95
-213.93
507.45
528.53
517.73
521.33
512.S
-181.98
410.46
411.91P
P
413.36P
411.91 P
P
P 413.36 P
P
P
P
P
P
0.3310
0.2942
0.3372
0.2949
O 3x1
--`,,-`-`,,`,,`,`,,`---
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
1c1.3
TABLE 1C13 (Continued)
SPe c i f i c W1
lapor
'ressure
601
It
Liquid Refractive
Gravity Density Index of
60 F theLiquidst
s t 60 F
deg L 9 1 lb/gal a t T7 F
Gr avi ?y
/ 6 0
100 F
si a
H e a t Capecity
t 60 F wd tomtant
If
ressure
tu/Lb deg
:inemtic Viscosity
rf the Liquid
F
:entistokes
Liquid a t
1 atm
r t 100 F
: 210 F
k a t of
lapor izhtion a t
lorn 1
boi 1 ing
Cint
,tu/Lb
let Heat
If comustim
If L i c p ï d
iquid
Yo.
urface
msion
t T 7 F
It T7 F
ltu/lb
ivnlrn
L
I
lomotefins. C2 Md C3
1.1388
1.5192
888.00
1.157 P
4.329
141.04
1.36320
1.36250
...
28.8880
0.3579
0.3584
1.3688 P
0.6164
...
...
...
o. 2599
...
...
...
0.1801
206.96
188.63
2027s
1967s
169.56
19469
19416
19389
192
I93
-
~
hmoolefins, UH8
1.38030
1. m o o
1.35200
1.39260
52.2985
1.36835
1.37980
1.37610
1.37460
1,36110
1. m 2 0
19.1498
15.1372
15.4368
18.3571
26.3699
14.347a
k5 . W 8
69.9157
63.8138
0.3542
0.3317
0.3631
0.3652
0.5388
O. 5300
0.5373 P
O .5474
0.3582
0.3281
0.3612
0.5176
0.5081
0.5254
0.5264
0.5215
0.5119
0.2673
0.2441
179.34
12.12
I95
...
174.43
170.05
lm2
13.16
11.69
...
...
...
...
...
...
155.46
161.76
161.O1
156.69
148.45
161.73
19185
19145
19117
19101
19158
19057
16.80
16.41
15.88
13.80
16.85
145.48
147.25
148.64
147.55
148.68
144.85
139.46
140.04
147.64
147.77
150.40
140.54
142.26
144.81
140.34
132.44
150.23
19102
19045
19036
19070
19034
19014
19075
19065
18970
18993
18988
19029
138.03
136.43
138.91
138.28
137.07
Monaolefins. C58111D
5.383
0.6456 87.67
5.511
0.6610
82.57
5.u5
85.14 0.6532
5 .467
0.6558
81.28
5.275
92.12 0.6328
5 -533
0.6637
81.70
r(or0olf: f i
0.6790
O. 6920
O. 6825
0.6848
0.6823
0.6844
0.6723
0.6687
O. 6909
O. 6980
O. 7023
O. 6741
0.6736
O -6944
O. 6828
0.6580
0.7129
0.3663
0.3951
0.3493
...
...
...
...
...
0.2889 T
194
1%
I97
1.
198
199
!O0
M1
?o2
203
-
M, C6Hl2
76.W
72.97
5.661
1.38502
5.710
75.83
5.690
5.709
5.688
5.706
5.605
5.575
5.760
5.819
5.855
5.620
5.616
5.790
5.693
1.39473
1.39073
1.39189
1.39137
1.38912
1.38133
1.37974
l.
39739
1.39876
1.40166
1. N 9 8
1.S583
1.39380
1.38729
1.37313
1.Cc235
75.13
75.89
75.25
78.96
80.11
73.32
71.24
69.97
78-40
78.57
R.26
75.R
83.56
66.99
5.486
5.943
6.0089
4.9070
5 .O944
5.3748
5.2215
6.3006
8.42Tf
8.5169
5.1762
5.1371
4.6159
7.7464
7.1237
5.7045
7.9753
13.0927
4.1m
0.3415
O -3624
0.3681
0.3756
0.3946
0.3501
0.3502
0.3502
0.3502
0.3712
0.3923
0.3696
0.3977
0.3505
0.3420
0.5116
0.4978
0.51 15
O. 4922
0.51 17
0.5233
0.5396
0.4947
O. 4943
o. 4991
0.5207
0.5151
0.5368
O. 5065
0.5334
0.5243
0.4877
0.3629
0.Upo
0.3640
0.3459
0.3600
0.5107
0.4928
O .5059
0.4902
O. 5027
0.4317
0.4457
O
0.4484
0.4518
O .Mo9
0.3480
O3 7 5
0.3418
O -3673
0.3662
O -3682
0.3639
0.356
0.3585
0.3465
O .U26
0.3404
0.3556
0.3556
0.3448
0.3473
o. w o
0.3319
...
...
...
...
...
...
I . .
...
...
......
e..
a..
...
...
...
...
204
205
206
207
208
19029
18992
19029
18955
17.89
19.10
18.08
17.93
17.64
17.58
16.30
15.92
17.91
18.67
19.14
16.10
16.08
18.62
17.05
13.90
19.96
19042
19014
19003
19018
19003
19.81
20.81
20.10
19.93
19.42
22
22;
223
224
225
1W06
209
210
211
212
213
214
215
216
217
21c
215
UC
Honoolefirs, C7H14
0.7015
0.7119
0.7057
0.7073
O. 7026
70.20
67.27
69.01
5.849
5.935
5.w
5.897
5.858
i
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
i
1.39713
1.40420
1.40200
1.40330
1.40170
1.wo
1.6886
1
I .a522
1 .S11
.m
.c495
O .u143
...
...
...
...
I
_
--`,,-`-`,,`,,`,`,,`---
Not for Resale
1-69
1(21.3
--`,,-`-`,,`,,`,`,,`---
TABLE lC13 (Continued)
.
1
1
1
Forarlc
1
Freezing
Boi 1 ing
"U.
Point at
1 atm
* F
air a t
erature
Critical
Constants
Pressure
pia
volume
Cu f t
per lb
1 atm
centric
*
C
s
%
actor
,bility
:#tor
dcoF
~-
Matmlefins, C7H14
226 2-NETHYL-l-HEXEIIE
227 3+ETHYL-l-HExENE
220 UIETHYL-1-HEXENE
5"ETHYL-I-HMNE
230 2-IQTHYL-2-HEXENE
231 c i s - m H Y L 4 4 E X E N E
232 t rms-3-4ElNYL-i!4UEwE
233 cis-UaTHYL-Z-HEXENE
23.4 tr-THYL-2-HEXENE
235 cir!ì-HETHYL-2-HEXENE
us trMs"CnTtNL-2-4lEXENE
237 cis-24ETHYL-UlEXENE
238 trans4"€THYL-~EXENE
239 cis-HETHYL-UfEXENE
240 trarks"ETHYL-3-nEXENE
24 1 2-ETHYL-I-PENTENE
242 WTHYL-1-PENTENE
243 34THYL-2-PENTENE
244 2,3-OlHETHYL-l-PENTENE
245 2,M1UETHYL-l-PEITENE
246 3,3-01METHYL-1"TENE
247 3,MIHETHYL-1-PENTENE
248 4,4-D1METHYL-1-PEYTENE
249 2,3-DlUETHYL-2-PENTENE
250 2,MIWTHYL-2-PENTENE
251 cir-3,M1WETHYL-2-PENTENE
252 ~ ~ ~ M - ~ , ~ - C I W E T H Y L - ~ - P E N T E N E
253 cis4.CaIWETHYL-2-PENlENE
m
254 tr.ans-4,MIMETHYL-2-PENTENE
255 3-METHYL-2-ETHYL-l-BUTENE
256 2,3,STRIHETHYL-l-BUfENE
Uawrolcfins, CBH16
257
258
259
260
261
262
263
264
265
1"fENE
cis-2-OCTENE
tras-Z-OCTENE
cis-34UEN
trsns-3-aTEWE
cis-CoCTENE
trans44CTENE
2"ETHYL-I-HEPTENE
METHYL-1-HEPTENE
-
I
cm14
C7H14
cm14
C7H14
Cm14
C7Hl4
m14
cm14
cm14
c7H14
cm14
cn14
C7H14
cm14
cm14
C7H 14
cn14
CM14
cm14
cm14
CM14
C7H14
cm14
C7H14
C7H14
C7H14
C7H14
C7H14
CM14
C7H14
CM14
98.19
98.19
t8H16
W16
CEM16
a t 6
C8H16
t8H16
C8H16
C8H16
C8H16
112.22
112.22
112.22
712.22
112.22
112.22
112.22
246.60
112.22
112.22
98.19
98.19
98.19
98.19
98.19
98.19
98.19
98.19
98.19
98.19
98.19
98.19
98.19
98.19
98.19
98.19
98.19
98.19
98.19
98.19
98.19
98.19
98.19
197.31
183.02
188.11
185.56
203.74
207.07
2Q3.32
187.36
189.61
193.10
190.60
186.80
186.62
203.72
200.38
201-20
183.40
204.82
183.70
178.90
171.46
177.44
162.53
207.32
181.94
192.65
1W.70
176.77
170.13
187.46
172.20
1
250.32
258.15
257.00
253.22
253.94
252.57
252.07
231.80
-153.17
-198.67 P
-222.61
98.19
508.73P
490.73 P
501.53 P
490.62 P
517.41 P
525.76P
520.2s P
4p6.65 P
...
-202.63
-181.31
-200.74
...
-194.24
499.96
I
-191.81
98.19
-222.81
98.19
98.19
...
...
-157%
-197.46
98.19
98.19
P
-209:;i
-191.31
-209.88
...
-213.88
-180.89
-197.86
-172.11
-191.62
-211.83
-115.42
...
-165.73
-151.06 P
-148.36
-125.86
-194.80
-166.00
-181.66
-136.80
-125.27
...
~
,
~
P
501.75 P
498.06 P
492.46 P
492.19
520.83
515.88
517.73P
494.33
525.97
501.26
P
P
P
P
P
P
416.27 P
427.87P
440.92 P
416.10 P
416.10P
428.05P
C28.05P
428.05 P
428.05 P
416.10 P
416.10 P
416.10 P
416.10P
428.05 P
428.05 P
427.87 P
439.47 P
440.51 P
443.47 P
487.09 P
488.30 P
418.81 P
452.52P
491.90
467.83
536.54
491.59
514.62
520.68
489.06
479.16
503.28
4W.13
P
u3.47 P
427.11 P
P
P
643.47P
411.81 P
P
443.47 P
443.47 P
560.30
569.93
578.93
564.53
573.53
562.73
571.73P
560.93
541.87
P
P
P
P
427.11 P
427.11 P
P
430.88 P
P
455.43 P
P
P
P
P
P
P
P
372.46 P
315.65 P
374.20 P
375.65 P
374.20 P
375.65 P
374.20 P
377.10 P
387.28P
0.0649 P
0.0649 P
0.0649 P
0.0649 P
0.0649 P
0.0649 P
0.0649 P
0.0649 P
0.0649 P
0.0649 P
0.0649 P
0.0649 P
0.0649 P
0.0649P
0.0649 P
0.0649 P
0.0649 P
0.0649 P
0.0636 P
0.0636 P
0.0634 P
0.0636 P
0.0634 P
0.0636 P
0.0636 P
0.0636 P.
0.0636 P
0.0634 P
0.0634 P
0.0636 P
0.0622 P
0.0657 P
0.0658 P
0.0691 P
O .M58
0.w85 P
0.0658 P
0.w85 P
0.0647 P
0.-
P
0.2550
0.2670
o. 2730
0.2599
0.2528
0.2539
0.2533
0.2657
0.2646
0.2569
0.2579
0.25%
0.2595
0.2592
0.2605
0.2600
0.2740
O. 2653
0 -2685
0.2573
o. 2 m
O .2711
O .26R
0.2589
0.2561
0.2648
0.2631
0.2612
0.2640
0.2603
0.2710
0.2510
0.2510
0.2600
0.2520
o. 2600
O. 2530
o. 2600
0.2500
0.2614
0.3001
0.3057
0.3024
0.3111
0.3128
0.3096
0.3091
0.3081
0.3083
0.3120
0.3113
0.3123
0.3112
0-3067
O. 3065
0 -5085
0.3016
0.3056
0.2750
0.2871
0.2599
0.2754
o. 2747
0.2784
0.2852
0.2752
o. 2774
O. 27%
O. 2705
0.2808
0.2406
O. 3764
0.3889
0.3384
0.3800
0.3438
D.3856
0.3393
0.3551
0.3552
Note: Footnote c
o
d
a follow Table 1C4.12.
1997
1-70
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
1C1.3
TABLE 1C13 (Continued)
Liquid Refractive
Gravity Density Index Of
at 60 F at 60 F theLiquic
dto
Lb/gal a t 77 F
API
mific
ravi t y
1/60
Yapor
Pressure
a t 100 F
pia
.i*id at
I atm
I
I
I
~
Kinanatit Viscosity
of the Liquid
k a t of
l a p r iz)tion a t
centistokes
lOrmeL
a t 100 F
t
210 F
boiling
'oint
)tu/ 1b
~
~~~
Itcmolef ins, C7n
o.mn
0.6959
0.7030
O. 6965
0.7126
O.RO3
0.7188
0.7040
0.7013
68.51
71 -84
69.78
71.65
67.07
64.
PS
65.35
69.51
70.26
0.7065
68.79
0.6971
0.6981
0.6941
0.7180
0.7144
0.7122
O. 6994
0.7249
O .7097
O. 6987
0.7019
0.7022
71 .U
71.20
0.6872
O. 7323
72.36
65.S8
66.57
67.18
70.83
63.69
67.88
71.03
70.09
70.02
74.42
61.74
0.6995
70.78
0.7180
0.7212
0.7040
0.6935
0.7134
0.7096
65.58
fA-69
69.51
72.53
66.84
67.90
5.898
I
I
5 .m2
I
5.861
I
5 .m7
5.941
6.005
5 .W3
5 .a69
5 .a47
5.890
5.812
5.820
5 -787
5 -986
5.956
5.938
5.031
6.044
5.917
5 .a25
5.852
5 .a54
5.729
6.105
5 .832
5.986
6.013
5 .a69
5.782
5 -948
5.916
1.4Oog3
1.39380
1.39730
1.39400
1.40790
1 A1000
1.40910
1.39990
1.39980
1.40100
1.39790
1.39900
1.39740
1 .&o995
1.4WO
1 .&O200
1.39550
1.41220
1.40W
1.39577
1.39580
1.39650
1 .m95
1.41850
l. 40090
1.40780
2.1061
2.0162
2.5226
2.7000
1.9000
1.moo
1.9000
1 .39989
1.39525
1.40244
1.40007
2.6000
2.5000
2.3000
2.4000
2.2600
2.6000
1 .m10
1.9570
1 .m58
2.T803
1 .moo
2.moo
3.1670
3.5200
3.1300
4 A850
1 .moo
2.8690
2 -3000
2.2000
3.3510
3.7050
2.6000
3.6825
1.40620
1 .41250
1.41070
1.41110
1 .L1020
1.41240
1.40930
1.40940
1.40400
0.6572
O. 5983
0.6092
0.6614
O. 6439
0.6637
O. 6652
0.7559
1 .o000
1.41010
...
...
0.3636
."
...
...
...
...
...
...
...
...
I..
...
...
...
...
...
...
...
...
...
...
...
0.4460 P
...
0.5036
."
...
...
.
I
...
...
...
...
...
".
...
...
0.4460 I
0.4460 f
...
...
...
0.4462 I
....-
0.4464 I
...
...
...
0.4462 I
0.4463 I
0.4461 I
...
0.4022
0.4093
0.4460 I
0.4462 I
...
0.4130
0.4512
...
...
...
...
...
...
...
...
...
...
...
...
O ,4062
...
...
...
...
...
...
".
...
...
...
...
...
...
..."
...
...
...
."
...
."
...
...
."
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
."
...
136.10
134.56
131.09
".
."
."
".
...
...
...
...
I
.
.
...
...
137:ij
134.32
135.57
...
127.87
...
...
...
...
132.63
133.73
...
127.69
129.15
...
O. 4203
...
128.26
O. 5657
O. 5746
0.5570
0.5558
0.5606
0.5558
0.5612
0.4775
0.3590
O. 3492
0.3502
0.3488
0.3517
O. 3489
0.3528
O. 3076
130.98
130.81
128.99
129.76
129.01
129.05
129.17
127.25
18981
19030
19047
19017 Y
18940 Y
10947 Y
10943 Y
10989 Y
18960 Y
10980 Y
18960 Y
18985 Y
18962 Y
18x7Y
18973 Y
18990
19.63
18.33
19.14 l
18.78 P
20.24 P
21.14 P
20.97 P l
19.26 P
10.96 P
19.47 P
18.50 P l
18-40 P I
17.04 P
20.41 P
20.04 P
20.20
18.66 I
21.70 P
20.28 P
19.01 P
19.38 P
19.42 P
17.75 P
22.62 P
18.75 P
20.87 P
21.26 P
19.24 P
22
227
.
ita
!a
9C
91
.
9i
!
3
!
li
Y
95
.
54
3;
1
?3¿
91
?C(
19043
x;
19133 Y
!G!
!U
la964 Y
18954 Y
24!
19015 Y
24C
247
19002 Y
18982 Y
2c8
18930 Y
249
250
18928 Y
18946 Y
251
18946 Y
252
19007 Y
253
18934 Y 18.09 P 254
19117 Y 20.70 P 255
256
18959
17.36
Honoolefins, t8H16
0.7181
0.R89
0.7239
O. 7253
0.71%
0.7252
0.7182
0.7250
O. 7149
L
I
65.54 5.987
62 -62 6.077
63
-96
6.035
63.61
6.047
65.20 5.998
6.M
63.61
65.52
5.988
63-68 6.044
66.44 5.960
0.3662
...
0.3660
...
0.3626
...
0.3626
0.3742
...
0.5059
O 5058
0.5016
...
0.4998
0.4530
0.4991
0.4782
...
".
...
."
19005
18954
18965 P
18971 P
18965 P
18971 P
10965 P
10957 P
18978 P
21.29
22.34
21.70
21.56
20.86
21.55
20.67
21.22
20.24 P
257
258
259
260
261
262
263
264
265
--`,,-`-`,,`,,`,`,,`---
1-71
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
~~
~
STD.API/PETRO TDB CHAPTER L-ENGL
L777
0732290 0 5 b b b b 2 L Y 7 E
1C1.3
TABLE lC13 (Continued)
l-
Formla
Critical
Constants
Pressure
pia
Volme
Cu f t
centric
:aprcssibility
:actor
per l b
nona>Lcfins,
'actor
a l 6
266 C-CIETHYL-~-HEPTENE
267 trans"IETHYL-2-HEPTENE
268 trans-~HYL-3-nEPTENE
269 24THYL-1-HEXENE
270 3-EfHYL-I-HMENE
271 &ETHYL-14EXENE
272 2,3-OlHETHYL-l4EXENE
273 2,3-0111ETHYL-WEXENE
274 cis-2,2-OlUElHYL-3-HEXENE
275 2,3,3-TRIMETHYL-I-PENTENE
276 2,4,CTRIMETHYL-14ENTENE
277 2.4,CTRIMETHYLd-PENTENE
CM6
a 1 6
CDJIl6
W16
CWl6
W16
CSH16
c8H16
WH16
CSHI6
@H16
C8Hl6
235.04
242.60 112.22
249.80
248.00
112.22
112.22
112.22
230.54
235.60
230.90
112.22
112.22
112.22
112.22
112.22
...
."
...
...
...
...
.
I
-175.18
251.19
-215.23
221.77
-92.20
226.96 112.22
-136.21
214.59 112.22
-159.36
220.84 112.22
546.57
554.31
567.95P
573.53
553.27
550.35
550.13
579.69
P
P
P
P
P
P
P
m.94 P
563.38 P
535.73 P
%.T5 P
387.28 P
377.64 P
387.28 P
445.27 P
397.29 P
397.29P
400.31 P
399.65 P
386.53 P
431.55 P
381.46 P
381.46 P
0.0616
0.0646
0 . w
0.0570
0 . w
0.0646
0.0635
0.0635
0.0622P
0.2601
0.2517
0.2517
0.2570
0.2677
0.2659
0.2630
0.2553
0.2574
O. 2744
0.0664 P
0.tMO
0.0671P
0.2-
0.3555
0.359%
O .3557
O .3799
O .3%5
O .3524
0.3251
0.3272
O -3225
0.2731
O .a95
O. 2650
P
0.0670
0.0667
0.0667
0.0651
0.0664
0 . W
0.0666
0.0666
P
P
0.2490
0.2530
0.2460
0.2410
0.4171
0.4800
0.5175
0.5705
P
0.2380
P
0.2360
0.2330
0.2300
0.2290
0.2260
0.2230
0.2210
0.6063
0.6449
0.6815
o. 7242
0.7503
0.7943
0.8325
P
P
0.0666 P
0.0666 P
P
0.0661 P
0.0662 P
0.2570
0.2550
O. 2670
0.2520
o. 2490
o. 2480
0.2850
0.2710
O. 2740
o. 2640
0.1315
0.1659
0.18%
0.1542
o. 1470
0.1162
0.0837
0.2184
0.1874
0.1583
0.2540
0.2534
0.2142
0.2710
P
P
P
P
P
P
P
P
0.0634 P
~~
Monoolefins. 13t o C20
278
279
280
281
282
283
284
285
286
I-NWENE
14ECENE
l-UNDECENf
14ODECENE
C9H18
C l OH20
elln22
C12H24
C13H26
C10H28
C15H30
C16H32
C17H34
C18H36
C19H38
1-TRIDECENE
I-TETRADECENE
1-PENTADECENE
I-HUUDECEWE
1dEPTADECENE
287 14CTADECENE
288 I-UONADECENE
289 1 4 1COSENE
-
C20H40
126.24
140.27
168.32
182.35
196.38
224.43
238.46
252.48
280.54
-114.47
296.36
339.08
47.27 P
-56.49 P
378.81 154.30
416.04
-31.40 P
451 .O0
-9.53
483.98
8.87
515.23 210.4025-29
544.77
39.85P
572.59
52.25
63.70
598.68
624.24 266.5174.12
648.30
83.50
608.18
649.85
P
908.33 P
928.13 P
337.94
321.70
294.43
279.93
256.72
240.77
227.71
214.66
204.51
194.35
185.65
176.95
-30.10
51.53
24.06
112.75
111.33
107.64
-213.30
-213.16
54.09
-164.02
68.12
-215.07
68.12
-221.44 P
68.12
-125.39
78.73 -234.92
118.85
-194.17
105.53 68.12
-172.52
93.30
-230.58 P
248.00
353.93
305.64
440.33
438.53
440.33
402.53
434.93
422.33
411.53
738.25
632.37
620.34
551.15
542.45
542.45
542.45
551.15
555.50
558.41
155.77
168.80
487.10
487.01 P
688.73 P
724.01
755.33
f85.93
814.73
839.93
865.13
886.73
P
P
P
P
P
P
P
P
P
P
P
P
0.8804
Diolefins, C3 t o C5
290 PROPADIENE
291 1.2-SUTAOIENE
C3H4
292 1, m A D I E N E
293 1,&PEWTADIENE
290 cis-1 ,WENTADIENE
295 tras-1,3-PENTADIENE
296 1,wENTADIENE
297 2.3-PENTAODIENE
298 ~HYL-l,2-SUTADIENE
299 24ETHYL-l.3-BUIADIEWE
C4H6
C4H6
C5H8
C5W
4
0.6
54-09
c5nB
68.12
bH8
EH8
b
n
B
68-12
CSH8
68.12
m10
C6H10
82.15
82.15
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
0.0660
0.0652
0.0653
0.0649
0.0669
0.0649
0.0713
0.0694
0.06a4
0.0649
P
P
P
P
P
P
P
P
P
Diolefins, c6 t o C10
300 2,~IHETHYL-1,3-6lJTADIENE
301 1.2-WEXESIENE
I
-104.83
...
Note: Footnote codes follow Table 1C4.12,
--`,,-`-`,,`,,`,`,,`---
1997
1-72
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
~~
STD.API/PETRO TDB CHAPTER
L - E N G L L797 m 0 7 3 2 2 9 0 0 5 b b b b 3 08.5 M
1C1.3
TABLE 1C13 (Continued)
=ific
1/60
API
Liquid R e f r s c t i w
m s i t y Index of
Gravity D.avity
at 60 F a f 60 F the Liquid
deg A P I lb/gal a t 77 F
\Iapor
1'ressure
4It 100 F
I= i a
+rat Capacity
n t 60 F and Constant
DreOsure
Jtu/tb a0 F
Ideal Gas
li
.iquid at
est o f
: i n e m t i c Visccrsity
,f the Liquid
,
:entistokes
It
100 F
'-riz-
t 210 F
Ition a t
loma 1
loi l i n g
'oint
YetHeat
Liquid Yo.
Surface
of combustion
Tension
of Liquid at T7 F
Btu/Lb
*/m
Itu/lb
I atm
laDolefi m, Mn16
6L.79
1.7209
6.010
6.020
6.110
6.098
6.000
6.090
6.051
6.213
5.979
6.168
5.997
6.053
U.47
6'1.58
61.94
65.12
62.21
63.47
58.38
65.81
59.76
65.22
63.40
3.7221
3.7329
D.7315
0.7197
0.7305
0.7258
0.7452
0.7171
O. 7398
O. 7193
0.7260
1.40800
1A
O
I0
0
0.9400
0.8100
1At600
0.7OOO
O. 7289
1.C1320
1 .405M
1.41oM)
1.40890
1.c2440
1.M740
1 .C1510
1.10600
1.C1350
Weooclefins, C9 t o C20
O. 7330
O. 7450
0.7541
O. 7625
0.7705
0.7755
0.7804
0.7856
0.7886
0.7923
0.7954
0.7981
I
6.111
6.21 1
6.287
6.357
6.424
61 .S3
58.44
56.14
54.08
52.14
50.95
49-82
46.61
47.92
47.10
46.40
4 3 . ao
6.W
6.506
6.550
6.575
6.605 R
6.631 F
6.654 1
1.oooo
O .W
1.o134
i
0.6800
1.3090
1.1000
1 .S608
1.2880
...
."
...
...
...
0.3592
...
...
0.3691 T
...
...
...
...
0.5099
...
...
0.4772
...
...
...
...
0.5668
...
...
0.4171
...
...
0.4528 P
...
0.37S3 T
0.4935
0.3736 T
0.5009
I
.
.
0.3684
0.3648
...
...
...
...
0.3450
...
."
...
."
0.2778
0.2545
O. 2520
...
...
140.59 1
130.70
...
...
125.90
...
...
...
118.71
122.32
!O.%
P 266
! O . T O P 267
!1.58 P 268
18983 P
18932 P
18912 P
18965 P
18984 P
18991 P
18954 P
5-38
B.74
2.01
N.32
18900 P 9.55
18983 P 11.93
18949 P ' 23-22
19.25
18916
19.68
18929
1
269
270
P 271
272
P
P
273
P 274
P 275
276
277
I
1 .L1333
1 .C1913
1 .c2383
1.42782
1 A31 18
1.43412
l. 43669
1 .c3907
1.CG100
1A4280
1 .c4500
1 .c4590
o. ZMO
O. 0746
0.0245
1.41690
1.42050
1.42930
1.41773
1 .C3291
1 .C2669
1.38542
1.42509
1.41692
1.41a52
41.2690
36.6213
59.3292
11.5008
11.8213
12.7062
21 -8952
10.1483
13.2173
16.6790
0.0099
0.0031
0.Wll
0.ooo.L
0.0001
<.o001
<.o001
<.o001
<.o001
0.3654
0.W
O. 3670
O -3677
0.3682
0.3686
O. 3690
O -3693
O -3696
0.3699
0.3702
0.3703
0.5037
0.5033
0.5028
0.5043
0.5075
O. 5067
0.5064
0.5101
0.5W
0.3764 I
0.4941 I
0.4717 '
0.7004
0.8848
l . 0852
1.3359
1.6132
1 .9353
2.3160
2.7463
3.2237
3.7553
4.3732
5 .o633
0.4945 I
0.5410
0.5341
0.4931
0.5047
0.5142
0.5066
0.5270
O, 5263
0.5227
0.2149
0.2645
0.2030
O. 2667
O. 26R
0.2732
22.56
270
279
280
18865 P
18853 P
18844
18a34 P
18826 P
18818 P
18759 P
24.40
25.17
25.79
26.35
26.88
27.32
27.73
28.08
28.42
28.73 T
19920
19566
19147
19229
18BM
18825
1W33
19174
19137
18835
9.40
14.94
12.45
18.48
18.33
16.75
15.52
18.27
16.49
16.38
29t
291
292
m.4a
120.80
116.59
110.69
108.51
104.84
101-65
97.31
94.00
91 .S2
89.13
87.27
18964
18936
18914
...
214.73
189.35
178.34
169.69
168.49
167.69
154.58
175.21
168.25
161.R
...
...
151.47
214.93
0.4294
O -5027
0.5916
0.6840
0.7825
0.9062
1 .O254
1.1742
1.3127
1.4812
1.6545
1.8417
18895
18879 P
236
.0
281
202
283
284
ta5
284
287
2a
28
D i o l e f i n s , C3 to C5
0.5943
0.6576
0.6281
O.69n
O .6944
0.6811
0.O .7002
0.6916
0.6864
0.3434
0.3426
0.3404
0.3439
0.331 1
0.3378
0.3344
0.3624
0.3437
0.3497
...
0.2660
0.2w
...
...
O. 2248
0.1271
...
...
...
...
...
...
293
tpc
295
296
297
298
299
I
Diolefins, C6 t o c10
0.7323
I
61 .R
65.09
I
I
6.106
1.43620
6.001
1.42520
4.W12
...
...
...
O. ci%
0.3261
...
18777
18571 F
19.81
300
20.00 P 301
--`,,-`-`,,`,,`,`,,`---
0.7198
1-73
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
1C1.3
TABLE 1Cl3 (Continued)
Critical tonstants
F o m L a W.U.
Boiling
Point at
1 atm
degF
Freezing
Pressure
Point in
air at
lato
psia
VOLUDC
Acentric
Factor
C"$-
CU ft
ibility
Factor
per lb
deoF
Diolefins, e6 to C10
302 1,5-IIEXADlEWE
2,WEXADIENE
UlEfHYL-1,2-PENlADIENE
2~THYl.-1,5-I1EXADIENE
2-UElHYl~,~EXADlENE
2,WADlENE
303
304
305
M6
E
96.17
96.17
754.40
158.00
190.60
232.70
2,6-0IU€THYL-l,S-HEPTADlENE
256.10
289.00
3,7-01MlHYL-1 ,-AOIENE
322.00
...
...
...
."
62.93
666.11 P
a2.41 P
779.32 P
m.79
P
pt7.13 P
996.98 P
1055.55 P
485.88 P
486.64 P
506.97
437.78
437.78
392.87
370.57
339.30
P
P
P
P
P
P
0.0661 P
0.w6.5 P
0.0629 P
0.2690
0.2593
0.2321
0.2710
0.2591
0.1992
0.2280
0.0629 P
0.0629 P
0.W1 P
0.1826
0.1878
0.2870
0.3700
0.0619 P
0.1822
0.1788
0.3450
0.6450
0.0620
P
0.2880
--`,,-`-`,,`,,`,`,,`---
Note Footnote codes lollow Table 1C4.12.
1-74
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
1997
Not for Resale
--`,,-`-`,,`,,`,`,,`---
1C1.3
TABLE 1C13 (Continued)
~~
~
~
Refractive
Index of
the Liquid
at 77 F
Hent C a p c i ty
Vapr
Pressure
at 100 F
pria
at 60 F r d C m s t a n t
Pressure
Btu/lb deg F
~~
Kinematic Viscosity
of the Liquid
Liquid
Surf ace
centistokes
Tension
et 77 i
lera1 Gas LiqJid at at 100 F at 210 F
1 atQ
*/m
Btu/ Lb
Diolefins, C6 to C10
0.6975
0.6849
0.7197
0.7234
0.7480
0.7473
5.015
5.710
65.12 6 . 0 m
6.031
64.11
57.68
6.236
57.86
6.230
6.430
51.97 0.7712
6.345
54.43 0.7610
71.37
75.10
1.40100
1.39200
1.m
."
...
...
...
...
7.0291
."
...
..
...
...
...
...
f
...
...
...
."
...
...
...
...
0.4402 P
0.3262
0.4398 P
0.4398 P
0.4473 P
0.4490 P
0.4686 P
0.4718 P
0.4859 P
...
...
...
...
...
...
...
...
144.13
209 -24
210.51
252.04
279.89
257.14
241 -84
231.30
1-75
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
...
...
...
".
...
...
...
Not for Resale
1 Cl .4
TABLE lCl.4
CYCLOOLEFINS AND
.-A
PRIMARY PROPERTIES
T
C r i t i c a l Constants
IO.
Fomule
carpwld
Boiling
H.Y.
Point at
1 atm
a S F
Freezing
p o i n t in
mir a t
1 atm
deaF
T m p
erature
Pressure
p i a
a o F
VolUr
CU
eentrir
'actor
"C
ft
ibility
Factor
per Lb
-
A l L c y l ~ l o p c n t ~ Sb
, to
I
310 ClCtOPENTEllE
311 I-IIETHYL-CICLOPENTENE
bH8
68.12
C6H10
82.15
312 l-ETHYLCfUOF'ENTENE
313 WTKYLCYCLOPENTENE
314 1"PPOPYLCYCLOPENTEWE
cm12
cm12
96.17
W14
110.20
96.17
c6H1o
C7H12
C81114
82.15
181.35
96.17
110.20
230.53
278.59
C5H6
ClOH12
66-10
132.21
106.70
D7.73
I
111.61
167.88
311.04 P
-195.75
223.39
207.99
-181 .I2
268.20
452.93
522.43 P
581 -40 P
581.40 P
696.48
0.1959
0.2290
599.27 P
0.2370
620.46 P
521.15 P
780.31 P
425.56 P
1
549.05
601.61 P
648.09 P
630.92 P
550.36 P
683.59 P
0.2123
0.2s50
P
m . a p
746.96 P
643.82 P
o. 2020
0.2880
I
699.53
697.73 P
400.31 P
...
...
0.31 10
0.3270
Alkylcyclohexms, t6 t o C8
Cyclic Diolefins.
-154.26 P
-184.72
-165.93
C5 t o Cl0
318 CICLOPENTADIENE
319 DICYCLOPENTAOIENE
-121.00
452.93
89.60
Cyclic Unsaturates,tlDH16
320
alphe-PlNENE
321 betbPINENE
ClOHl6
ClOHl6
-63.20
-78.77
400.31 P
Acetylenes, C2 t o C4
322 ACETYLENE
323 HETHYLACETYLENE
324 DIMETHYLACETYLENE
ETHYLACETYLENE
325
326 VINYLACETYLENE
Acetylenes,
c!ì
C2H2
C3H4
C4H6
C4H6
332
333
334
816.29
u.09
c4114
...
I
706.35 P
338.09 P
357.53 P
717.95 P
m.89 P
I 1
o -2209
0.0581 P
0.2550
O.OS34
0.0695
0.0656
0.0654 P
0.0657 P
0.0631 P
0.2340
0.2740
0.2980
0.2640
0.0651 P
0.0649 P
0.2890
0.2580
0.2710
0.2760
0.3249
0.1873
0.2161
O. 2385
0.2469
0.1069
t o c10
327 I-PENTYNE
328 Z-PENTYNE
329
33 O
33 1
890.40
0.2690
68.12
C5H8
104.32
68.12
C5H8
133.02
~"ETRYL-I-BUTYNE
68.12
84.20
CSH8
I-HEXYNE
m10
82.15
160.39
1-HEPTYNE
C7H12
W.17
211.60
1-OCTYNE
110.20
m14
259.16
I-NWYNE
WU16
124.23
303.26
I-OECYNE
Clon18 138.25
345.20
-
406.49 P
474.53 P
604.82 P
374.09 P
609.17 P
525.05 P
455.43 P
0.0647 P
0.0628 P
0.3000
0.2720
-113.67
-111.28
469.49 P
566.53 P
593.33 P
0.0643
P
0.2610
409.01 P
0.0641 P
378.55 P
343.75 P
0.0641 P
0.0640 P
0.2560
0.2610
-47.20
616.73 P
619.80 P
-158.26
-164.78
-129.46
-205 .C2
-58.00
584.51 P
0.2540
0.2899
0.1752
0.3081
O. 3327
0.2728
O. 3 2 U
0.3480
0.4340
Note: Footnote eodes follow Table 1C4.12.
1997
1-76
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
--`,,-`-`,,`,,`,`,,`---
CYCLOHEXENE
I-WETHYLCYCLOHEXEWE
317 14THYLCYCLOHEXENE
315
316
~
S T D . A P I / P E T R O T D B C H A P T E R L-ENGL 1 9 7 7
0 7 3 2 2 7 0 0 5 b b b b 7 7217
m
1C1.4
TABLE 1C1.4 (Continued)
e c i f i c API
avity
Gravity
1 / 6 0
a t 60 F
deg API
Liquid
Refractive
D e n s i t y I n d e x of
a t 60 F the
Liquid
Lb/gal
a t 77 F
Capacity
eat
Kinematic
Viscosity
Unpor
Pressure
t 60 F a d Cutstant
et 100 F
ressure
pia
tu/Lb deg F
of theLiquid
centistokes
~
~~
t
210 F
-
i
Heat of
Vapor ization at
Noml
Boi ling
Point
EtWlb
O.
-
,lkylcyclopmtenes, C5 t a 3
L.? 1 1 !
48
6
.6
1.7854
1.8030
1.41940
1.43020
1.c3840
1.42910
6.548
6.695
6.568
6.721
6.480
44.71
48-11
44.03
50.54
11.7409
0.2736
...
~~
~
0.4197
0.43%
0.4459
0 . m
0.1531
...
...
...
...
...
...
...
...
0.3882
P
P
P
P
...
...
."
...
0.2600
...
...
...
2111.n
203.86
214.99
186.31
...
1 1 1
1.8750
6.802
1.44377
39.62
41
-78
6.894
6.808
1.45437
1.44784
32 05
30:22
26.02
25.43 P
27.03 P
i15
i16
117
18198 P
18000 P
21.66
30.69 T
118
il9
P
-
3.0120
...
...
-
0.2830
...
...
0.6645
0.4222
0.3480 P
0.3544 P
O 3962
...
...
159.22
207.60
0.3485
o -2295
0.7950
O -4449
165.78
121.91
...
...
1
...
~~
-
C5 to Cl0
43.58
6.738
9.55 1.50610
8.364
I
18486
18438
18471
22.78
I
1.44040
13.0380
o. 1134
0.2619
0.2696
0.4479
0.4275 P
Il
:yciic Unsaturates, C10H16
1.8652
25.11 P
I10
;11
;12
i13
i14
l
41.93
:yclicDiolefins,
).W2
1.0032
22.11
22.21 P
24.56 P
~
\Lkylcyclohexenes, C6 t o C8
1.8159
1.8166
1.8269
1
18551
18489
18540
18599
111558
I
1
7 1.16590
213
7:295
1.47680
I
0.1775
0.1207
I
-
~7014
1.6579
117.36
118.10
18461
18493
25.65
26.85
I20
...
...
3.m
...
275.46
238.61
210.46
1% .49
201 .o1
2055
19838
19226
19590
1.19
11.51
21 .O8
17.07
17.08
322
18.79
22.23
15.68
20.54
22.13
23.67
24.50
25.40
321
32t
325
33c
331
332
33:
334
521
-
ketylenes, C2 to CL
...
0.3960
19.3540
0.3543
21 .c953
0.2780
0.5475
0.3381
41 .S501
0.3503
45.0512
0.3288
...
...
...
0,2214
0.5951
0.2746
0.3292
0.2933
0.5620
0.4905
0.5623
0.5441
0.5000
0.4938
0.4688
0.3023
0.4769
0.6Q67
0.6573
0.8064
1.1913
19500 P
S23
J24
325
326
-
ketylenes. C5 t o c10
0.7016
0.7160
0.6719
0.7210
O. 7378
0.7511
O. 7622
0.7712
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
1. m 2 0
1.4oow
1. S 9 5 0
1.39570
1. w o
1.11380
1A1950
1.42490
13.4995
7.7659
19.m
4.41%
1A968
0.5057
0.5029
0.0695
0.3635
0.3365
0.3593
0.3655
0.3666
0.3677
0.36% I
0.4082 I
...
."
--`,,-`-`,,`,,`,`,,`---
Not for Resale
...
...
0.3407
0.2093
O. 2926
0.4171
0.4313
0.5063
...
. I .
,
'
1
172.40
178.37
164.22
159.35
143.59
136.46
174.26
164.64
I
19256
19118
19225
19161
19096
19045
18999
18968
-
1-77
1Cl .5
--`,,-`-`,,`,,`,`,,`---
TABLE 1C15
BENZENE DERIVATIVES: PRIMARY PROPERTIES
Fonda N.U.
Boiling
Point at
1 atm
degF
Freezing
T
centric
Pressure
point in
air at
1 atm
l-
Critical Constants
pria
erature
dcop
Voluac
N ft
per lb
:oprCSsbility
actor
:actor
dcoF
Llkylknzenes, C6 and C?
335BENZENE
336 TOLUENE
1
c6H6
Cm8
176.16
231.13
41 .%
-138.95
552.22
605.57
710.41
595.S3
0.0531
O. 0549
-138.91
-13.31
-54.13
651.29
674.92
651.02
649.54
523.01
541 -58
512.86
509.24
O. 0564
-147.28 P
689.41
-140.82
676.31
-113.44 P
-139.97
-80.18
-13.65
46.88
4.51
712.40 P
607.20 P
692.74
736.60
708.76
687.58
464.13
465.43
440.89 P
411.91 P
468.91
-126.13 P
-60.61
-103.78
134.22
-72.18
-76.36
-116.64
134.22
-82.48
-96.72
729.32
710.60
736.50
728.33
731.93
717.53
721.13
731.93
722.93
716.00
742.73
733.73
R4.66
764.33
740.93
748.13
737.33
719.33
733.73
787.73
762.53
755.60
0.2710
0.2640
0.2100
0.2621
ALkyLknzenes, an10
337
338
339
340
ETHYLBENZENE
+XYLENE
*XYLENE
pXYLENE
n-PROPYLBENZENE
ISOPROPYLlENZENE
o-ETHYLTOLUENE
I!+ETHYLTOLUENE
p€THYLTOLUENE
1,2,3-TRIMETHYLBENZENE
1,2.4-TRIMETtfYLBENZENE
348 1,3,5-TRINEfHYLBEWZEWE
341
342
343
344
345
346
347
C8H10
m10
CBHlO
C8H1 O
C9Hl2
C9H12
H H l2
HHl2
C9H12
HH12
HH12
C9H12
55.87
318.63
306.34
329.32
322.39
323.62
349.02
120.19
120.19
120.19
120.19
120.19
120.19
120.19
120.19
336.88
328.53
0.2630
0.2630
0.0557
O. 0567
0.0572
500.W
468.n
453.54
O .E90
0.2600
o. o586
O. 0569
0.0613
0.0653
0.0569
0.0552
0.0573
O. OSTI
P
P
P
P
0.2650
0.2610
0.2580
0.2630
O. 2590
0.2590
0.2580
0.2560
0.3026
0.3104
0.3259
0.3215
O .u47
0.3258
0.2932
O .3226
0 . M
0.3664
0 -3773
0.3990
AlkylIbenzenes, ClOH14
349
350
351
352
353
354
355
356
357
358
359
360
361
362
363
364
365
366
367
36a
369
370
C10H14
MYLBEUZENE
ISOBUTYLBENZEWE
ClOH14
sec-BUTYLEENZENE
ClOH14
tert-BUlYLBENZENE
ClOH14
I - M E T H Y L - ~ ~ R O P Y L E E N Z EClOH14
NE
I+ETHYL-WROPYLEENZENE
ClOH14
l-WETHYL-CrtPROPYLBENZENE
C10H14
M M E N E
C10H14
D"ENE
CIOH14
P-CYMENE
ClOH14
C-DIETHYLBENZENE
ClOH14
UAIETHYLBENZENE
ClOH14
pOIETHYLBENZEUE
ClOH14
1,2-OIMETHYL-~THYLBEN~NE
C10H14
1.2-0IMETHYL~THYLBEN~NE CIOH14
1,3-01METHYL-2-ETHYLE€NE~
C10H14
1,341METtIYL4-ETHYLBENZENE
c10w14
1,341I(ETHYL-5-€THYLEENZ€NE
C10H14
1,4-DII(ETHYL-2-ETHYLEEY2ENE
ClOH14
1,2,3,~lETRAIIETHYLEENZENE
ClOH14
1,2,3,5-TETRAIIETHYLBENZENE
CIOH14
1,2,4,5-TETRAMETHYLEENZENE
C10H14
134.22
134.22
361.95
343.02
343.99
336.47
134.22
134.22
134.22
364.64
359.24
361.94
352.72
347.14
350.83
362.22
358.05
134.22
134.22
134.22
134.22
134.22
134.22
134.22
362.02
134.22
134.22
lw.22
134.22
1
301.13
373.60
374.07
362.80
371.19
-82.68
-90.22
-24.20
-119.00
45-09
-57.12
4.47
2-73
-81.18
-119.79
4.53 P
20.75
-10.64
174.62
S
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
418.73
440.92
427.87
430.77
426.42
407.56
407.56
424.97
424.97
406.11
417.72
417.72
606.55
417.72
417.72
430.02
417.72
390.86
417.72
451.07
S
P
P
P
P
P
P
P
0.0575
0.0575
0.0584
0.0579
O. 0593
0.0599
0.0582
0.0593
P
P
P
P
P
P
P
430.77 P
426.42
O. 0593
0.05U P
0.0593 P
0.0587 P
0.0575 P
P
P
P
P
P
P
P
P
P
P
P
P
P
0.0605
0.0585
0.0575
0.0575
0.0575
0.0575
0.0567 P
0.0575 P
0.0575 P
0.2610
0.2560
0.2650
0.2660
0.2570
0.2490
0.240
0.2600
0.2600
0.2560
o. 2600
0.2550
0.2550
0.2580
0.2540
0.2610
0.2510
O. 2430
0.2520
0.2560
0.2540
O. 2520
0.3938
0.3797
0.2791
O. 2674
o.con
0.4128
0.4134
0.3372
0.3411
0.3666
0.33%
0.3540
O .4030
0.3621
0.4114
0.4W
0.4140
0.4169
0.4114
0.4172
0.4242
0.4341
-
Note Footnote codes follow Table 1C4.12.
1997
1-78
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
1c1.5
TABWE 1C15 (Continued)
-
"r
'ressure
I t
100 F
sia
centistokes
a t 100
210 F
'oint
Itu/lb
e t Heat
'f canustion
iquid
iurf ace
ension
If Licpid
It
StWlb
@/cm
nF
No.
77 F
~-
c7
28.72
7.363
1.49792
. M 2
F
~-
~
and
lentof
raporiztim at
lorn1
loi L
n
ig
íquid at
atm
lkylbenzenes, c6
~
~~~~
Kinmatic Viscosity
of t h e L i w i d
teat Cspaci t y
It 60 F Md Constant
'ressure
Itu/lb deg F
.E741
30.39
7.287
1.493%
3.2144
1 .OB7
0.2422
0.2621
0.4113
O .3Ç%
0.5927
0.5604
1.3306
I.3433
169.25
156.29
17260
17423
B.21
?7.92
335
336
O. 2765
O. 2891
0.2736
0.2727
0.4028
0.4133
0.4044
0.4002
O. 6540
0.7415
0.5936
0.6167
1.3970
1.4238
1.wo4
1.3704
144.42
148.78
146.59
145.46
17595
17547
17542
1'7547
28.59
29.60
337
33
335
27.93
U(
0.4190
0.4147
0.4133
O. 3985
0.4065
O. 4236
0.4203
o. 4086
0.7977
1.4534
1.4229
3.4193
3.4203
3.4173
3.3979
3.4422
O. 3872
136.12
132.99
136.1a
135.69
136.79
142.53
140.65
138.90
lm1
28.50
27.69
29 -66
28.54
28.30
30.75
29.19
27.97
1U'
1U ¿
?U?
0.4257
O. 4298
O A007
0.4179
0.3674 I
0.3676 I
O -9483
O .9895
O .S75
o. 9747
O .9664
0.9992
0.9825
0.9739
0.8066
O -7971
0.5186
0.5166
0.4997
0.5086
O .C557
0.5019
O. 5278
O. 5979
0.5128
0.4746
0.5024
0.5191
0.5208
0.4881
0.5140
0.4891
0.4994
0.4867
0.5132
0.5542
0.4810
0.4980
129.78
127.03
126.19
122.48
130.12
129.68
129.71
126.13
125.24
126.62
128.91
128.10
129.88
133.37
133.58
133.87
131 17
130.46
130.68
138.30
136.48
135.75
17824
17803
17814
17800
Inn95
17783
17787
17792
1 T m
17777
17807
17791
17795
17769
ln52
Ilkylbeozms, tSHlO
1.8737
1.8691
1.8654
1.8849
1 I I
7.205
1.49320
O .3?28
O. 2645
31.32
7.246
32.70.0215
20.41 7.3TI
1.49464
1.49325
\.Sot95
0.3285
0.3434
1 A8951
1 .m90
O.lu8
0.1875
0.1088
0.1249
0.1257
0.0713
0.0916
0.1127
0.2929
0.2883
o 2980
0.2845
0.2848
0.3072
0.0472
0.0833
O. 0748
O. W33
O .(u69
0.0507
0.2995
0.3106
0.3047
0.3051
30.45
tlkylbenzenes, tPHl2
--`,,-`-`,,`,,`,`,,`---
1.8655
1.8985
1.8805
1.8698
3.8660
1.8577
1.8657
1.8713
l. 8780
3.8659
3.8637
0.8812
5.8655
D.Bbo8
0.8839
0.8683
0.8663
0.8966
0.8788
o .E948
0.8807
O. a592
0.8816
0.9084
o a948
0.8918
-
31.99
25.99
29.21
31.19
7.239
7.238
7.379
7.246
7.216
7.491
7.341
7.251
i
-
31.90 7.220
33.47 7.151
31 -96 7.217
30.90 7.264
29.65 7.320
31 -917.219
7.201
32.33
29-09 7.246
7.216
32.00
32 .a97.176
28.59 7.369
31.45 7.240
31.83 7.223
26.33 7.475
29.52 7.327
26.63 7.460
7.343
29.16
31.29 7.247
29.01
7.350
24.28 7.573
26.G 7.460
27.17 7.435
1.50208
1.49406
1 .L9244
1 .S1150
l. 50237
1.49684
1 -48742
1.48400
1.48779
1.49024
1.49740
1.49120
1 .48980
1.49830
1.49050
1.48850
1 .S0106
1.49310
1 -49245
1.50950
1.50090
1.50850
1.50150
1 .C9580
1.50200
1 .S1810
1.51070
l. 50930
"0
0.0648
O. 0739
0.0654
O. M69
0.0530
0.0470
0.0287
0.034
O. 0338
O. 0392
0.0464
0.0416
0.0161
0.0232
...
0.2973
O .2835
...
...
.-.
0.3048
0.3019
0.3009
0.3169
0.3066
0.3055
0.3168 1
...
...
-..
...
...
0.3246
0.3126
0.3172
0.3675 I
0.4164
0.4144
0.4146
O. 4226
0.4143
0.4210
0.4335
O -3672
O .M72
O -3672
O -3665
O3 6 7
0.4238
o. 4230
...
O. 7474
0.8347
O. 7859
0.6711
0.8317
O. 8743
O .na
7 .o675
0.9751
0.9770
1 .O789
1.0665
1 .o810
O 9764
1 .O127
1 .o625
1.3635
1.1082
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
-
...
-
17710
17692
1 768L
1 7680
17649
17637
1 7631
17771
17758
17746
17755
17738
1m0
17638
541
:U!
:Ut
I
54;
u1
--
28.64
u9
26.98
350
28.02
351
27.63
352
31 .59 353
354
29.94
355
29.55
31 .O1
356
357
28.88
28.66
358
359
29.77
28.63
360
28.47
M1
33
-82362
363
31.29
364
33.43
31 .51
365
29.95
3t.t
31.62
367
35 -95 36í
33.46
365
25.23
37t
-
1-79
Not for Resale
28.26
1 Cl .5
TABLE IC15 (Continued)
T
Critical Carstants
No.
Foratlr
Carpand
1
H.W.
B
o
i1 ing
Point at
1 atm
dcoF
Freezing
Point i n
air at
1 atm
dcsF
41.63
1.27
771.53 P
780.53 P
355.35 P
355.35 P
0.0592 P
0.0590 P
0.2580
0.2560
0.3587
0 -3900
-103.00
-78.07
-54. 40
-32.80
-1 1-47
6.12
764.15 P
377.68 P
345.20 P
316.19 P
0.2530
O. 2630
0.2380
0.2340
0.2320
0 -2300
0.2280
0.2220
o. 2200
0.2170
0.2160
0.2130
0.4378
0.5272
0.5670
0.6331
O. 6797
0.7333
0.n33
0.7799
0.8130
0.8567
0.8996
Pressure
Vol-
psiß
Cu f t
kentri
:anpress- :actor
bility
:actor
per Lb
Alkylbenzem, C12H18
541
1,3-01ISlRRWYLBENZENE
542 1,4-DlISOPRCPYLBEYZENE
AlkylknzeneS, Cl1 t o
C12H18
C12H18
162.28
162.28
397. R
410.90
CllH16
ClZH18
C13H20
148.25
162.28
176.30
190.33
401.83
439.00
474.98
507.92
539.69
568.20 P
595.85 P
621.70 P
C22
wPENTYLBENZENE
n-HMLEENZENE
HEPTYLBENZENE
n-C#TYLBENZENE
~I-UONYLEENZENE
MECYLBENZENE
rtUNDECYLEENZENE
MOOECYLBENZENE
379 n-TRIDECYLBENZENE
380 n-TETWECYLBENZENE
381 n-PENTAOECYLBENZENE
382 rr-HEXAOECYLBENZENE
ClCHU
C15H24
ClW
204.36
646.30 P
37.00
50.00
669.20 P
690.80 P
712.40 P
60.80
915.53
944.33
962.33
980.33
71 -60
80.60
996.53 P
1012.73 P
192.90 P
184.20 P
0.05%
0.0585
0.0589
0.0592
0.0590
0.05%
0.0598
0.0600
0.0601
0.0601
0.0605
0.0604
44 -58
879.53 P
417.72 P
0.0529 P
0.2460
0.3783
-23.10
-79.02
-20.79
-9.76
-91.43
-123.41
-29.43
685.13
748.13
746.33
717.53
726.53
722.93
737.33
0.0541
0.0552
0.0552
0.0541
0.0552
0.0552
0.0584
0.2560
0.2450
0.2450
0.2470
0.2580
O. 2450
O. 2620
O. 2971
0.3411
O A393
P
556.95
487.33
487.33
487.33
503.29
477.18
487.33
-0.40
-103.W
-149.80
-57.46
T16.17
747.25
747.50
753.49
739.13
P
P
P
P
P
425.83
46.63
425.83
425.83
436.57
796.73 P
825.53 P
852.53 P
874.13 P
292.98 P
274.85
256.72
242.51
226.26
214.66
P
P
c22H38
218.38
232.41
246.44
260.46
274.49
288.52
302.54
C12H16
160.26
464.22
C8H8
C9HlO
C9HlO
C9H10
C9H10
C9H10
C9H10
104.15
118.18
118.18
118.18
118.18
118.18
118.18
353.98
352.87
329.90
337.66
340.88
ClOHl2
CIOH12
ClOH12
ClOH12
132.21
132.21
132.21
132.21
132.21
369.12
374.09
378.14
359.60
ClZHlO
C13H12
C13H12
C13H12
C14H14
154.21
168.24
168.24
168.24
182.26
491 O0
491.54
522.86
518.00
541.40
156.60
32.00
40.46
118.40
116.60
961.00
936.77
982.13
968.45
991.30
C14H14
182.26
559.40
249.80
968.00 P
368.34 P
t13H12
168.24
507.69
922.73 P
423.52 P
Clfn2a
C1 8H30
C19H32
QOH34
CZlHM
22-73
8p5.73 P
P
P
P
P
P
P
P
203.06 P
P
P
P
P
P
P
P
P
P
P
P
P
0.479U
Cyclohexylbenrene, ClZH16
383 CYCLOHEXYLEENZENE
ALkmylbenzm, C8 t o C10
386
387
UIB
389
390
391
STYRENE
cis-l-PRWENYL BENZENE
trans-l-PROPENYL BENZENE
2-PROPEWYL BENZENE
14ETHIL-Z+THENYL BENZENE
1-METHYL-3-ETHENYL BENZENE
l-METHYL44THENYL BENZENE
l-HETHYL44t ram1"f'ROPENYL)BENZENE
1-ETHYL-2STHENYL BENZENE
l-ETHYL-S€TRENYL BENZENE
392
393
394 1-ETHYL"ETHENYL BENZENE
3% Z-PHENYL-14TENE
-
I Phenylbenzcnes,
ClOHlZ
293.29
343.00
393.80
...
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
0.0560
0.0560
0.0560
0.0560
0.0550
P
P
P
P
P
P
P
P
P
P
P
P
0.3230
0.3412
0 -3487
0.3175
0.2423
O. 2470
0.4080
0.4230
0.4030
O. 4030
0.3536
0.2378
O. 2554
O. 2435
C12 t o C14
396 BIPHENYL
397
1-((ETHYL-Z-PHEWLBENENE
398 ~-M€THYL-~-PHENYLEENZENE
399 l~tHYL49HENYLBENZENE
400
l-ETHYL4-PHENYLBENZENE
401 l ~ T H Y L - 4 ( ~ l H Y L P H E N Y L ) BENZENE
.
P
P
P
P
558.40
510.54
510.54
510154
453.98
P
P
P
P
0.2950
0.36%
0.2940
0.2sco
0.2870
0.2770
0.4060
0.4610
0.4610
0.4910
0.0522 P
o. 2288
0.4630
0.0521 P
O. 2500
0.4615
0.0521
0.0512
0.0512
0.0512
0.0521
P
P
P
P
Diphenylalkanes, C13 t o C24
402
DIPHENYLMETHANE
n.43
Note Footnote codes follow Table 1C4.12.
1-80
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
1997
Not for Resale
--`,,-`-`,,`,,`,`,,`---
384
385
S T D B A P I I P E T R O T D B C H A P T E R 1 - E N G L L777 m 0 7 3 2 2 7 0 0 5 h b b 7 1 1 5 1
1C1.5
TABLE lCl.5 (Continued)
LiquidRefractive
Density Index of
at 60 F the Liquid
lbfgal at T7 F
lapor
'ressure
Heat
Capacity
a t 60 F and Constant
st 100 F
Pressure
=ia
Btu/lb
F
Ideal Gar
.iquid at
:inanatic Viscosity
bf the Liquid
e a t of
'aporizItim a t
:entistokes
iormal
loi 1 ing
boi nt
Itu/lb
it
100 F
210 F
I atm
No.
k
\
ly
b
le
n
z
e
n
e
s
,C12H18
1.8629
3.8606
32.48
1.48758
7.175
32.92
1.48748
7.194
0.0186
0.0121
...
...
1.m
0.7932
I .m26
b.4376
110.26
113.n
17PM
1 .I824
1 .U19
1.62%
1.E46
2.0974
2.5329
3.0119
3.5672
4.1857
4 .B66
5.7107
6.5716
7.4138
1.8546
1.9763
I . 1089
I .2491
I .3983
I .S509
I .R58
1.8853
2.0862
2.2939
123.23
117.97
111.52
108.20
106.32
101.58
100.16
96.49
95 .c8
93.87
92-06
90.41
17905
17973
18030
18078
18120
18156
18188
18217
18242
16265
18285
18304
0.3836
2.0086
O. 7936
125.15
17646
34.60
383
-
0.4113
O. 3801
0.4010
0.4013
0.4055
0.4069
0.4041
0.6637
O. 3783
0.3667
O .3659
O. 4693
0.4048
0.3964
0.4258
153.03
145.91
145.99
140.05
145.73
143.42
143.56
17416
17546 P
17532 P
17540
17535 P
17528 P
17546
30.87
32.78
32.49
31.59
33.70
33.58
34.46
384
385
3e4
192 .40
186.71
186.78
188.37
130 -64
17783 P
ln321
IT821
17821
17658
P
P
P
P
32.27
32.76
39'
39;
39:
391
16816
17156
17156
17156
17286
P 38.69
P 39.11
P 53.48
P 43.92
0.4143
0.4199
28.60
P
17936 P I 28.82
541
542
-
\lkylbenzenes, c11 t o c22
1I
32.58
32.62
35:;
I
0.0161
0.0057
0.0021
0.0007
0.0002
0.0001
<.o001
<.O001
c.0001
c.0001
<.O001
c.0001
1 :::
33.12
33.23
33.29
33.29
0.3062
0.3121
0.3171
0.3213
0.3250
0.3281
0.3309
0.3334
0.3356
0.3376
0.3391
0.3410
o A289
0.4336
0.4277 P
0.4311 F
0.43% F
0.4418 1
0.4580
0.4505
0.4571
0.3725
0.3706
0.3683
1
F
F
F
1.7334
29.09
P 29.87
P 29.m
P 30.11
P 30.35
30.52
P 31.03
P 31.25
31.84
P 32.07
P 31.97
P 30.65 P
371
372
373
n
4
375
376
377
378
379
380
381
382
Cyclohexylberuene, C12H16
1
1
1 7 . 8 ~ 7.900
0.9~s
1
1.52393
0.2681
0.0027
Alkenylbenzenes, C8 to C10
0.9097
0.9138
0.9129
0.9138
0.9165
0.9164
0.9264
24.04
23 -35
23.50
23 -35
0.9104
O .9103
O .8WO
0.8969
0.8954
23.93
0.2470
0.0684
O. OM15
0.1105
0.0802
0.0809
0.0787
22.89
22.92
21 -25
...
23.95
O. 0305
0.0330
25.90
26.26
26.53
0.0296
o. o522
0.2725
0.2652
O. 2825
0.2740
0.2860
0.2860
0.2860
...
...
...
...
-.-
O - 3667
0.3673
0.3672
O. 3671
0.4055
o. 6485
0.6484
0.8401
0.8W
0.7443
0 . m
...
...
...
...
...
...
...
...
0 -948.2
O. C924
".
O. 9879
32.73
30.87
31.54
38;
381
381
3%
39!
-
Phenylbenzenes, C12 to Cl4
.
1 O324
1.0159
1.0185
l. low
1. O m
1.1220
8.607
8.470
8.491
9.179 V
8.651 V
5.57
7.78
7.44
-2.97
4.87
I
-5.38
1
1.58728
1.58900
1.60160
9.354 V1
...
...
...
...
...
...
...
0.2461
0.2615
0.2574
0.2574
...
0.3731
...
a3747
...
...
...
...
...
...
...
...
...
...
136.03
173.37
179.09
1n.16
...
165.68
...
...
...
15573 P 60.22
39(
39
391
39
401
40
1
Oiphenylalkanes, C13 to C24
1.0101
1
8.58
I
8.422 R ( 1.57520
O -3732
O. 9834
126.31
17011
37.57
1-81
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
2.1883
Not for Resale
--`,,-`-`,,`,,`,`,,`---
0.8624
0.8622
0.8617
0.8602
0.8596
0.8590
0.8587
0.8595
33.35
0.8584
0.8587
o.as87
33.31
0.8586
1Cl .5
TABLE
JO.
tarnPud
Fornuli
M.W.
1C1.5
(Continued)
Boi 1 ing
Point at
freezing
Point in
a i r at
1 atm
1 atm
de9 F
'F
T
Critical
Constants
T
centri1
actor
:anpress.
ibility
Factor
a s f
--`,,-`-`,,`,,`,`,,`---
I
Diphmylrlkrner, C13 to C24
403 1,l-DlPHEYYLEfHANE
c04 1,2-DIPHEYYLETWE
405 1,l-DIPHENYLPROPANE
406 1,Z-DIPHEYYLPROPANE
407 1.1-OIPHEYYLWTANE
408 1,1-DIPHEWYLPEUTANE
409 1,l-DIPHEYYLHEXANE
410 1,l-DIPHEUYLHEPTANE
43 1 1,1-OIPHENYLOCTAIIE
c12 1,l-OIPHEIIYLUONAWE
413 1,l-OIPHENYLDECANE
414 1,l-DlPHENYLUNDECANE
c15 l.ld1PHENYLDOOECAYE
416 1,l-DIPHENYLTRIDECANE
417 1,ldIPHENYLfETRADECANE
418 1.1-DIPHENVLPENTADECANE
419 1,l-DIPHENYLHEXADECANE
C14H14
182.27
182.2'1
P
P
0.2510
0.2520
0.2680
0.2384
0.2640
0.2610
0.2570
P
0.2540
P
P
P
P
P
0.0531
0.0541
0.0589
0.0523
0.0592
0.0597
0.0599
0.0606
0.0610
0.0615
0.0623
0.0628
0.0633
0.0640
0.0646
0.0653
0.0658
P
P
P
P
P
0.2510
O. 2690
0.2500
o. 2480
O. 2470
O. 2470
O. 2470
O. 2470
O. 2490
O. 7600
O .9330
1 .O032
0.9210
O. 8530
P
P
0.0530 P
0.0539 P
0.2510
0.2440
0.4874
620.77 P
420.62 P
0.0521 P
0.0549 P
0.2630
O. 2560
D.2264
3.3836
565.66
509.09
0.0524
0.0534
0.0531
O .3960
0.3510
0.3290
3.4817
P
P
P
P
985.19 P
W8.33 P
1010.03 P
1019.93 P
1031.55
1039.37 P
1048.73 P
1056.29 P
1064.39 P
1070.51 P
216.11
204.51
194.35
185.65
176.95
169.70
163.90
36.50
255.56
951.53 P
1016.33 P
397.41
397.41
710.33 P
50 1037.93 P
tlSH16
C15H16
Cl6Hl8
C171120
c 181122
C19H24
C20H26
c211128
C22H30
(323832
C24H34
C25H36
C26138
C27H40
c281142
210.32
224.35
238.37
252.40
266.43
280.45
294.ca
308.50
322.53
336.56
350.59
364.62
378.64
c14n?2
C11H12
180.25
180.25
537.53
583.70
C8H6
C14H10
102.14
178.23
289.13
571.73 5
48.73
230.31
230.31
?30.31
639.50
710.33 F
708.80
133.16
188.33
413.33
f96.29
1%.29
935.33
9u.33
954.07
938.89
941.27
955.85
970.25
-0.31
124.14
56.66
32.L5
-13.36
10.36
11.23
55 .40
21.80
59.00
37.40
69.80
50.00
80.60
64.40
91 .LO
78.80
522.73
536.90
541B
.O
542.59
561 -72
586.20
609.85
633.20
654. 80
674.60
692.60
710.60
726.80
743.00
757.40
771.80
784 .40
C14H14
P
P
P
388.71
384.36
546.65
548.30
319.09
295.88
275.58
258.17
P
P
P
P
P
P
P
P
242.22 P
227.71 P
P
P
P
P
P
P
P
P
P
0.4566
0.4885
O. 5360
0.5360
0.5740
0.6240
O. 6730
O. 7286
O. 6MO
O. E80
0.7210
-..
Diphenylalkenes, ClLHt2
420 CiS-l,2-(,1PHENYLElHENE
421trans-l,24IPHENYLETHENE
f
0.4756
Phenylalkynes, C8 and C14
422 PHEWYLACETYLENE
423 DIPHENYLACETYLENE
144.
Diphcnylbenrenes, Cl8H14
4241.2-OIPHENYLBENZENE
425 I,~-OIPHENYLBEUZENE
4261,44IPHENYLBENZENE
N o t e :F o o t n o t ec o d e s
681.53
1.5585
1.5240
follow T a b l e 1C4.12.
1-82
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
1144.04
1205.06
I207.C&
1997
Not for Resale
S T D - A P I I P E T R O T D B C H A P T E R L-ENGL L777
0 7 3 2 2 7 0 115bbb73 T 2 4
m
1C1.5
TABLE 1C15 (Continued)
LipJid Refractive
Density Index of
a t 60 F the Liquid
Lb/pal a t 77 F
Pecific W1
Gravity
ravity
a t M) F
3/60
deg API
Vapor
Pressure
a t 100 F
pria
Pressure
Etu/Lb deg F
Ideal Gas
I
centistokes
100 F
Liquid a ta t
1 atm
t 210 F
Heat of
Vaporization at
Noma 1
Boi 1 ing
Point
Btu/Lb
Net Heat
of canbustion
ofLiqJid
a t 77 F
8tWLb
Liquid
Surface
Tension
a t 77 F
dYnc/m
I
I
Yo.
-
Diphenylalkanes, C13 t o C24
1 .o041
0.9914
0.w10
0.9817
O .9793
0.9700
9.43
11.22
11.29
12.63
12.98
14.38
15.82
16.79
17.94
18.82
19.61
20.29
20.92
21 .51
21.91
22.47
0.-
0.9542
0.9468
0.9413
0.9361
0.9322
0.9284
0.9248
0.9224
0.9190
0.9173
s.ni
1 .S7020
8.266
1.57040 S
8.262
8.185
8.165
8.087
1.Sm0
1..55620
1 .S5460
1 .m
1 .54280
1 .S810
1 .53360
1 -52990
1 -52660
1.52380
1.52130
1.51900 R
1.51820
1.51510 R
1.51400 R
8.008
7.952
7.894
7.848
7.807
7.m
7.740
7.710
7.690
7.W
7.648
22.75
R
R
R
R
R
-
O. W07
...
...
...
".
.....
...
...
".
...
...
...
...
...
...
...
0.2600 T
0.2602
...
...
."
...
...
...
...
...
...
...
...
...
...
...
...
2.8954
0.3729
...
0.3769
0.3769
0.3776
0.3773
0.3766
0.3755
0.3741
0.3724
0.3707
2.8099
...
...
P
P
...
...
P
P
P
...
...
."
P
P
P
."
...
...
...
...
...
...
...
P
0.3625 P
0.3607 V
0.3592 V
1.1536
1.1714
".
...
...
...
...
...
...
...
...
...
...
...
."
...
...
118.89
120.15
...
...
147.14
141 .51
136.52
...
128.04
124.20
120.57
114:ii
114.36
17101
17173
...
...
...
...
37.85 P
17423 P M.44 P
37.17 P
36.74 P
36.09 P
35.77 P
35.32 P
35.01 P
34.74 P
...
...
...
...
I . .
...
...
...
114.27
113.99
...
...
...
1.4458
...
120.75
130.89
...
36.99
x:ii
P
40.51 V
47.71 P
56.40 V
403
404
405
406
407
408
409
410
411
412
413
414
415
416
417
418
419
65.73 V
-
17039
16928
39.14
420
422
423
Diphenylsikenes, C14n12
1.0784
1.0184
8.491
8.491
I
0.2458
0.2539
0.3556
...
O. 2608
0.2451
0.8213
0.4106
...
...
0.4614
1 .S823
150.41
122.89
17488
17243 I
32.70
...
...
-..
0.2453
0.2453
0.2453
...
...
...
...
...
...
4.6828
3.5877
109.38
119.64
117.27
16900 I
16900 I
16900 I
...
...
...
7.44
1.60320
7.44
1.62640
0.0004
1.54640
0.3092
...
."
3.90;:
421
... -
Phenylatkynes, C8 and C14
I
13.45
I
7.784
8.139
1
...
...
...
--`,,-`-`,,`,,`,`,,`---
0.9336
20.06
0.9762
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
1-83
Not for Resale
~~
_
~
_
~
~
~~
S T D - A P I / P E T R O T D B C H A P T E R L-ENGL 1 7 9 7 W 0 7 3 2 2 9 0 0 5 b b b 7 4 9bCl W
1C1.6
TABLE 1C1.6
CONDENSED RING AROMATICS AND DERIVATIVES: PRIMARY PROPERTIES
No.
Canpand
Forulc
Boi 1ing
M.U.
Point at
1 am
degF
Freezing
Point i n
a i r at
1 atm
a O F
T
Tkentri
Critical
Constants
Pressure
pia
votune
tu f t
p e r Lb
587.56
530.85 P
507.66
435.12 P
459.76 P
464.13 P
449.62 P
459.78 P
459.78 P
430.77 P
412.74 P
380.71 P
374.36 P
354.60 P
326.34 P
315.56 P
301.68 P
280.43 P
243.67 P
255.27 P
229.16 P
0.0516
0.0524 P
0.0524 P
0.0533 P
0.0533 P
0.0530 P
0.0530 P
0.0533 P
0.0533 P
0.0489 P
0.0541 P
0.0549 P
0.0548 P
0.0554 P
0.0559 P
0.0559 P
0.0563 P
0.0567 P
0.0630 P
0.0570 P
0.0639 P
0.2690
0.2650
0.2570
0.2420
0.2570
0.2530
0.2450
0.2550
0.2550
0 . m
0.828
O. 2570
0.2486
0.2511
O. 2470
0.2388
0.2405
0.2375
0.2360
o. 2254
0 -2370
....
..
...
0.6168
...
0.6415
836.60
525.05 P
o. o534
O. 2670
0.3284
835.25 P
443.43 P
0.0542 P
0.2531
onPrCs*
:actor
bility
actor
ALkylMphthalenes, C10 t o C20
427
428
429
430
431
432
433
553
554
434
435
436
437
438
439
440
441
442
443
444
445
I
NAPHTHALENE
1"ETHYLNAP~T~LENE
2-#ETHILHAPIITNALENE
14THILYAPHTHALENE
2-ETHYLNAPHTHALENE
1,2-OlWETHYLNAPHTHALENE
1,MIHETHYLNAPHTHALENE
2,641HElHYLNAPHTHALENE
2.7-01UETHYLIUPHlHALENE
l+-PROPYLNAPHTHALENE
2"PROPYLNAPHTHALENE
I~TYLNAPHTHALENE
2"BUlYLNAPHTHALENE
1"PENfYLNAPHTHALENE
1"AlEXYLNAPHTHALENE
2"AlEXYLNAPHTHALENE
l+-HEPTYLNAPHTHALEYE
1"OCTYLNAPHTKkLENE
l++NOWYLNAPHTHALENE
2+-NONYLNAPHTHALENE
I-n-OECYLNAPHTHALEWE
ClOH8
424.39
472.43
176.51
-22.86
94.24
7.14
18.68
30.20
45.79
B 2 -52
206.60
16.52
26.60
-3.50
23-00
-1 1.85
C12Hl2
Cl2H12
Cl2Hl2
C12H12
Cl2Hl2
C12H12
C13H14
C13H14
C14H16
C14H16
C15H18
C16H20
Cl6H20
ClMU
C18H24
Cl9H26
C19H26
G!OH28
128.17
142.20
142.20
156.23
156.23
156.23
156.23
156.23
156.23
170.25
170.25
1a4.28
184.28
198.31
212.34
212.33
226.36
240.39
254 -42
254 .42
268.44
511.34
513.14
503.60
505.40
523.00
524.30
552.90
550.40
582.80
611.60
613.40
638.60
665 -60
690.53 I
6%. 20
713.93 I
ClOH12
132.21
405.72
CllH14
146.23
429.06
C12H16
160.26
463.23
".
860.00 P
399.20 P
0.0550 P
o. 2484
C12H16
160.26
446.00
...
835.38 P
399.20 P
0.0550 P
O. 2532
...
C12H16
160.26
460.00
68.00
850.93 P
392.66 P
0.0550 P
0.2461
...
C12H16
160.26
485 .60
50.00
888.53 P
402.53 P
0.0550 P
0.2452
C13H18
174.29
493.52
(180.36P
362.96 P
0.0556 P
O. 2447
C13H18
174.29
505.40
...
...
892.36 P
357.52 P
0.0556 P
0.2389
C14H2O
188.30
523.63
...
...
C14H20
188.30
537.80
."
ClSH22
202.
a
553.33
...
...
CllHlO
CllHlO
466.00
496.99
4w.22
-0.40
22.10
17.60
28.40
51.80
51.80
59.00
887.36
930.00
910.13
937.13 P
928.13 P
958.73 P
958.73 P
938.93 P
940.73 P
947.93 P
942.30 P
965.93 P
958.24 P
985.30 P
1003.73 P
1001.O7 P
1029.09 P
1040.20 P
1068.53 P
1070.68 P
1086.53 P
0.3022
0.3478
0.3716
0.3626
0.4213
0.4127
0.4905
0.4m
0.41%
O. 4554
0.4597
0.4951
0.5010
..c
O. 5874
T e t r e h y d r ~ t h s l e ,C10 t o C20
446 1,2,3,4-TETRAHYDRO
447
448
~
NAPHTHALENE
l~ETHYL-C1,2,3,~TETRAHYDRCNAPHTHALENEI
l-ETHYL-[1,2,3,4-TETRAHYDRONAPHTHALENEI
449 2,2-DIMETHYL-tl.2,3,4-TE~RAHYDRWAPHTHALENEI
450 2 , 6 D l ~ T H Y L - I 1 , 2 , 3 , 4 - ~ T R I c
HYDRONAPHTHALENEI
451 6,7-DIWETHYL-C1,2,3,4-TETRAHYDROWAPHTHALENEI
452 l+-PROPYL-[l,2,3,4-TETRAHYDRONAPHTHALENE]
453 6++PRWYL-Il,2,3,4-TETRAHYDRDNAPHTWENEl
454 I + I - B U ~ Y L - C ~ , ~ , ~ . ~ - ~ R A HYDROWAPHTHALENEI
455 6o-BUIYL-t1,2,3,CfETRAHYDRONAPHTHALENE]
456 l+-PENTYL-C1,2,3,4-TETRAHYDRONAPHTHALENEI
-32.35
.I.
...
...
".
...
...
...
.
.
a
...
...
...
...
...
...
...
...
...
...
...
Note Footnote codes follow Table 1C4.12.
1-a4
--`,,-`-`,,`,,`,`,,`---
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
1997
Not for Resale
~~
S T D - A P I / P E T R OT D BC H A P T E R
L997 H 0 7 3 2 2 9 0 0 5 b b b 7 5 B T 7
L-ENGL
1Cl .6
TABU 1C1.6 (Continued)
lapor
'ressure
s t 100 F
Specific API
LR
i veifdr a c t i v e
Gravity
Gravity
Dcfsity
I n k x of
60160
a t 60 F a t 60 F the
Liquid
deg 1 9 1 Lb/gat a t 77 F
=ia
leat of
bporiz'ressure
3tu/Lb deg
Idcal Gas
i
.iquidat
I atm
at 100 F
t 210 F
lorma1
boi L i n g
'oint
Itu/lb
Surface
Tmsion
a t 77 F
dm/m
Alkylnaphthalenes, Cl0 to C20
1 .O281
1 -0242
1 .O082
1 .O115
0.9961
1.0219
1 .o209
".
...
0.9943
0.9808
O. P805
o. 9698
0.9705
0.9544
0.9521
0.9537
0.9468
0.9408
O. 9339
1
centistokes
Ilo.
Liquid
6.13
6-66
8.E
8.40
10.55
6.W
7.11
...
...
10.81
12.77
12.82
14.41
14.31
16.75
17.12
16.87
17.94
18-w
20.02
19.78
8.371
a. 539
8.406
8.433
8.305
6.520
8.511
1.93200
1.61512
1.60190 P
1. m o o
1.59TIO
...
".
...
...
1.61430
1.61140
".
...
...
1 .S9300
8- 289
8.177
1 .S8500
...
8.174
a. o85
8.091
7.957
7.938
7.951
7.894
7.844
7.786
7.798
...
0.0034
o. 0038
0.0014
0.0017
0.0008
...
...
...
<.o001
...
...
...
<.o001
...
<.o001
1.57970
1.57470
1 .S7040
1.56260
1 .S6010
1.5565 O
1.55060
1.54550
l. 54420
1.54120
0.0002
...
0.2365
O -3703
0.2576
0.2w
."
0.3%
0.3714
0.3709
0.3'708
...
...
...
...
...
...
...
...
0.2799
".
...
...
...
...
...
0.3111
...
0.3145
'
'
0.3%;
0.3731
0.3839
0.3740
0.3741
0.3737
0.3736
0.3725
0.3715
0.4110
0.4162
0.4134
2. lrui
P
P
P
P
P
P
1 .m
2.6017
2.0160
."
...
...
...
...
...
... 1.1298
3.1407
1.1206
...
3.8727
P
P
P
P
P
P
P
D. 7747
0.9204
0.7750
0.9871
0.8426
...
...
5.0098
...
...
...
...
".
1.2628
...
...
...
...
1
.
.
1.G66
144.52
141 .04
140.04
132.13
131.61
.-.
...
134,16
134.34
123.95
...
...
162.57
122.63
114.50
155.94
151.27
145.43
98.63
...
16707
16917
427
40.27
428
16Bm 35.45 T 429
16982
37.95
430
17081 P 36.54
431
17854 P B.81
432
17854 P i2.47 P 433
16973
553
1697L
5%
4%
17222
16.16
1%
P 15.24
435
17x3 P 15.24
436
18032 P %.W
437
18089 P 14.70
438
439
17510 P 14 -39
18139 P I 13.54
440
18182 Pl K.la
441
18220 P ' 53.84
442
17744 P 35 56
441
1~254P 38.05 F' 4 4 4
l
m P 35.16
445
...
...
-
9.3689
2.2010
10.7887
2.4730
."
95 .59
1.M28
O. 7672
137.69
17423
...
...
183.07
17684 P 34.96
...
...
...
...
...
173.35
17785 P
169.64
17183 P 32.89 IP
lR.79
ln43
1'79.20
17733 P 35.70 iP 45
164.68
16817 P 35.15
167.11
12417 P 3.17 IP 45
...
-
Tetrahydronaphthalenes, cl0 t o U0
O .97C8
13.65
8.127
1 .S3919
O. 9623
15.56
8.023
1.53330
0.9569
16.37
7.970
1 .S2980
0.9404
18.97
7.840
1.51800
O. 9464
18-02 7 . 8 ~
1.524W
0.9584
16.15
7.990
1.53600
O. 9480
17.75
7.904
1 .S850
0.9401
19.01
7.838
1.52410
0.9382
19.32
7.822
1.51980
0.9334
20. W
7.782
1.52100
0.9310
20.49
7.762
1 .S1580
0.0177
...
i
...
...
...
...
*..
...
...
...
...
0.2647
...
...
.-.
...
...
...
...
.....
."
0.3852
0.3702 P
0.3727 P
0.3735 P
0.3728
V
0.3718 P
0.3746 P
0.3740 P
...
...
...
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
...
...
...
...
...
...
...
.-.
...
...
...
...
...
...
...
...
...
...
...
33.16
V
44(
IJ
44'
35.55 I?
u
4
4
1
33.n v 45
I
IP
..-
...
...
45
45
45
45
--`,,-`-`,,`,,`,`,,`---
I
Ition a t
F
JetHeat
>f cœMtion
,f L i v i
I t ?? F
3tWLb
1C1.6
TAB= 1C1.6 (Continued)
Fornula M.U.
Boi 1n
ig
Point a t
1 atm
a O F
Freetilsg
Point in
air a t
1 atm
deoF
r
Critical
r
Constants
centric
Pressure
pria
wes- actor
bi Li t y
VOlunc
CU f t
per l b
actor
I
Tctrahydrmaphthalefn?s,
C10 t o C20
457 &tMENT'fL-[l,2,3,4-1ElRAWlOROWAPHfiULEYn
458 l " H E X Y L - I 1 , 2 , 3 . 4 "
HYDRONAPHTHALENE1
459 l"HEPTYL-II.2.3.CTRRAHYDDROWAPHTHALENEI
460 1&TYL-[1,2,3,4-TETRAHYDRONAPHTHALENEI
461 14WYL-fl,2,3,C-TETRAHYDRONAPHTHALENE1
462 l"DECYL-Il.2.3.4-TETRAHYDRONAPHTHALENEI
I
1
ClSn22
202.33
566.60
Ct6H24
216.37
~81.00 r
Clfi26
230 -39
609.80
C18H28
244.42
635.00
...
...
...
...
Cl9H30
258.45
658.40
...
272.47
681.80
."
116.16
130.19
130.19
360.72
29.39 P
...
...
...
...
P
274.13 P
0.0571 P
o. 2250
966.40 P
266.20 P
0.0574 P
0.2304
982.08 P
249.55 P
0.0577 P
O .U76
1021.50 P
234.86
P
0.0580 P
0.2215
1014.58 P
221.81 P
0.0583 P
o .2226
776.93 P
554.05 P
501.84 P
501.84 P
0.0507 P
0.0536 P
0.0536 P
O .tu0
O 2580
942.S
...
0.5888
...
...
...
...
Indenes, c9 t o Cl0
463 INDENE
464 I-UETHYLINOENE
465
2-WETHYLINDENE
389.30
403 -34
...
175.97
805.73 P
820.13 P
~
~~
o. 2550
D.3338
0.3349
0.3508
~
Dihydroindenes, C9 t o C10
466
2,MIHYDROINDENE
WH10
468 2-)IETHYL~,MIHYDRDIWDENE
ClOHlZ
ClOHlZ
469 CWETHYL-2,MIHYDROINDENE
470 WTHYL-Z,MIH~~RO~NDENE
C10H12
ClOHl2
467 1-WETHYL-2,MIHYDROINDENE
118.18
132.21
132.21
132.21
132.21
352.35
375.08
376.52
401 .W
3%
.60
-60.54
...
...
..
....
m.15
789.71
791.87
829.85
820.49
P
P
P
P
572.91
511.99
511.99
511.99
511.99
P
P
P
P
0.0537
0.0543
0.0543
0.0543
0.0543
P
P
P
P
P
0.2750
a .2740
O. 2740
0.2660
0.2680
0.3092
o .2660
0.3987
D311
D.3493
D. 4857
D.4695
D. 5074
3.5875
3.6030
...
...
...
...
Ccmdensed Ring Aranetics,
C12 to C18
471 ACENAPHTHALENE
472 ACEIUPHTHENE
473 FLWRENE
674 ANTHRACENE
475 PHENANTHRENE
476 PYREWE
477 F L W T H E N E
478 CHRYSENE
47'9 TR!PHENYLENE
480 BEYUNTHRACENE
482 UAPHTHACENE
152.20
Cl2H8
Cl2HlO 154.21
C13H10 166.22
Cl4HlO 178.23
C14HlO 178.23
Cl6HlO 202.26
C16H10 202.26
282
.9
C18W12 2
28.29
~ 1 8 ~ 1 22
C18H12 228.29
Clan12 228.29
518.00
531.30
567.12
647.65
193.10
200.14
238.62
420.40 P
210.61 P
638.38
742.64
721 -04
825.80
839.12
829.40
829.40
303.19
230.32 P
4W.40
388.58
320.72
674.60
965.93 P
986.00 P
1106.33
llt1.73
1104.98
1225.13
1169.33
1302.53
1364.00
1302.80
1317.20
P
P
P
P
z
Z
Z
466.13
449.62
681.69
420.62
420.62
378.55
378.55
346.65
348.10
348.10
348.10
P
P
P
P
P
P
P
P
z
z
2
0.0573
0.0574
0.0385
0.0498
0.0498
0.0523
0.0519
0.0526
0.1061
0.1061
0.1061
P
P
P
P
P
P
P
P
2
2
2
0.2570
o .2600
0.2210
o. 2220
0.2210
0.2270
o. 2200
o. 2000
0.2000
o. ZOO0
0.3090
...
...
Note: Footnote codes follow Table 1C4.12.
--`,,-`-`,,`,,`,`,,`---
1997
1-86
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
1C1.6
TABU3 1C1.6 (Continued)
.
API
Specific
Gravity
60/60
Gravity
a t 60 F
deg 1 9 1
L i q u i d Refractive
Density Index O f
a t 60 F t h e L i q u i d
lb/gal a t 77 F
~
~~
Iapor
)ressure
s t 100 F
nia
~~~
I*eL
Tetrahydronaphthalmes,
-
~~
Heat C a p c i t y
6 t 60 F andConstant
Pressure
Btu/Lb &g F
Gas
.iwid a t
I atm
:iMnstic viscosity
,f t h e L i q u i d
k a t of
laporizltion a t
lormet
:ent istokes
It
100 F
t 210
F
toi Ling
'oint
Itu/ 1b
Yet neat
o f canbustion
D f Liquid
a t 77 F
.iquid
Surf ace
IO.
rcnsion
at
77 F
Btu/Lb
-
CIO t o C20
1 .S1680
...
...
...
...
...
...
...
;57
...
0.3760 P
2.9046
1.271 1
106.30
35.09
i58
...
...
...
0.3753 P
...
."
141.13
53.86 P
L59
...
0.3742 P
136.62
33.67 P
W
...
1.50450
...
1
...
0.3712 P
134.00
33.53 P
M1
...
0.3711 P
".
...
...
...
".
128.76
33-44 P
Lb2
37.79
33.95
34.52
463
34.10
466
467
1.S1270
1 .S1010
1 .so800
0.0001
1 .S0610
~
...
-
Irdenes, c9 t o c10
1
1.0036
8.367
9.49
1.57400
0.9754
13.58
0.9794
12.97
8.166
1.56270
I 1
8.132
1.55870
0.0500
0.0266
0.0173
o 2438
...
...
0.3782
0.3702
0.3500
1.3562
...
...
0.6307
O. O670
8.076
O. 2535
0.3786
l. 1652
0.6156
...
...
150.31
1~x38
142.59
17097
17436 F
143.77
189.17
189.56
197.50
17326
17560 I
17205 f
W
465
-
Dihydroindenes, C9 to C10
0.9686
14.58
0.9437
18.4~ 7.868
0.9608
15.78
17.53
0.9495
1.53580
1.52410
1.51930
1.53330
1.53110
...
7.890...
8.010...
7.916...
18.02
... 0.3672 f
...0.94640.3671 f
... 0.3666 f
...
0.3667 F
...
...
...
...
...
...
...
...
..-
17560 I
17538 I
17539 I
31.93 F
32.31 F
34.34 F
32.74 F
~
469
470
-
Condensed Ring Aranatics,
CIZ t o c18
...
...
1.1913
...
...
...
...
...
...
...
...
9.932
...
...
."
1..40170
1 .cí4200
1 .cí4700
1 -72900
1 .54aoo
1.moo
1 .73900
1 -78500
1 -75600
...
...
...
...
...
...
."
...
...
...
."
...
...
O. 2270
0.2480
0.2302
0.2387
0.2411
o. 2298
O. 2449
0.2359
..-
...
0.2409
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
."
...
...
...
0.7123
1.3826
1.0487
1 .G7
...
4.9694
...
...
".
...
--`,,-`-`,,`,,`,`,,`---
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
16599
16732
16618
16517
lb471
16221
16357
16346
16855
16619
16606
...
...
...
...
...
...
...
...
...
...
...
471
472
473
474
475
476
477
478
4m
48E
482
-
1-a7
1c2.1
TABLE 1-1
PARAFFINS:SECONDARY PROPERTIES
lo.
canpovd
Fomla
Search
N m r
;olubbi1ity
Flash.
'armeter
Point
'C?1l/cm^3)~% faap
creture
degf
Ideal Gas
Heat of
Formation
at 77 F
Btu/Lb
Btu/lb
Paraffins, C l to C3
1 METWE
1
2 ETHANE
2
3
3 PROPANE
5 .M9
6.060
6.402
...
...
-1997.06
-1198.44
-1020.60
.I.
-:;r
-456.39
40.92
j :::i
Psraffins, UH10
4 n-BUTANE
5 ISOBUTANE
an10
5
c4HlO
4
6.695 I
6.143
Paraffins, CSH12
6 n-PENTANE
7 ISWENTAIlE
8 NEOPENTANE
7
8
9
7.037
6.774
6.378
-40.00
-70.87 P
...
-874.52
-915.87
-1001.50
-52.52
-83.72
50.11
30.75
19.02
-102.13
Paraffim, =H14
9 n-HEXAHE
10 2"ETHYLPENTANE
1 1 3-METHYLPENTAWE
12 2,2-DIMETHYLBUTANE
13 2.3-DIMETHYLWANE
C6H14
C6H14
C6H14
C6H14
C6H14
11
12
13
14
15
7.282
7.047
7.169
6.730
6 989
-
-6.97
-31.27 P
-25.87 P
-20.47
-832.85
-858.09
-921.35
-882.04
-0.33
-26.63
-17.06
-43.63
-54.67
-15.59
65.32
-870.81
31.35
26.51
2.89
4.02
Paraffins, C7H16
14 n-HEPTANE
15 2"ETHYLHEUNE
16 3-METHYLHEXANE
17 3-ETHYLPENTAWE
18 2.2-DIMETHYLPENTANE
19 2,3-DlMETHYLPENTANE
20 2,4-DlHETHYLPENTANE
21 3,3-DlMETHYLPENfANE
22 2.2.3-TRICIETHYLEUlAHE
CM16
CM16
C7H16
Cm16
CM16
CM16
CM16
CM16
C7H16
17
18
19
20
21
22
23
24
25
7.428
7.194
7.306
7.350
6.940
7.243
6.984
7.101
6.964
24.53
-9.67
24.53
10.13
-9.67
4.73
10.13
-2.47
-11.47
7.526
7.355
7.424
7.399
7.428
7.125
7.340
7.160
7.204
7.2?2
55.13
39.20
42.53
42.80
42.53
24.53
41 .60
50.00
28.13
29.93
P
P
P
P
-805.12
-834.94
-820.78
-812.33
35.03
14.89
21.98
-832.80
24.53
14.62
21 .O7
-883.04
-865.28
P
P
-857.21
-877.12
60.34
39.44
40.63 P
41.05
6
.
0
4
...
29.60
30.38
9.72
~
--`,,-`-`,,`,,`,`,,`---
Paraffins, W 1 8
23 n-OCTANE
au118
24 2-METHYLHEPTANE
25 3-METHYLHEPTANE
26 4-METHYLHEPTANE
27 3-ETHYLHEXAWE
28 2,2-DlMEfHYLHEXkNE
29 2.3-DIHETHYLHEXANE
30 2,C-DIMETHYLHEXANE
312.5-DIHElHYLHEXU(E
32 3,3-OIMETHYLHEWII1E
C8H18
OH18
W18
C8H18
CBH18
CBH18
C8H18
C8H18
C8H18
27
28
29
30
31
32
33
34
35
M
-785.67
-810.51
P
P
P
P
P
78.14
41.73
43.38
40.87
-799.82
-797.7s
-793.o5
-645.33
-804.68
-825.15
-837.46
-827.97
25:!%
36.36
50.40
...
...
48.65
26.02
Note: Footnote codes follow Table 104.12.
1997
1-88
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
1c2.1
TABLE 1C2.1 (Continued)
Coefficient
of
Octane
ASTM
..rmabiLty Limits Uatson
Y Factor
,lune Percent in
r Mixture
Nurkrs
A
n
iline
Point
Hotor
Method
3rd TEL
Clear
:Lesr
.oyer
I
Icr gal
p r gal
~ d c * F
hl TEL
no.
Paraffins, Cl t o C3
...
...
..*
...
...
0.001520 E
...
...
...
+O.OS K
...
...
97.1
."
...
...
k.40
10.4 K
I .50
b1.6 K
~1.8 K
!.m
LOO
16.50
13.00
9.50
i
r
19.5
19.5
14.7
1
2
3
-
Paraffins, Un10
0.001170
0.001190
I
+0.4
89.6
181.6
225.7
I
I
97.6
.,.
K
93.8
10.1 K
...
9.O0
8.40
13.5
4
1.80
13.8
5
-
1.30
1.30
1 .40
8.00
8.00
7.50
13.0
13.0
13.4
1 .O5
1.20
1.20 P
1.20
1.20
7.68
7.00
7.70 P
7.00
7.00
12.8
12.8
12.6
12.8
12.6
1 .o0
7.00
6.00
7.00
7.00
6.00
6.80
6.50
7.00
6.10
12.7
12.7
12.6
12.4
12.6
12.4
12.7
12.4
12.4
Paraffins, C5H12
61.7
92.3
85.5
-
O 000900
86.0
bl.0
bO.1
K
K
6
7
8
-
Paraffins, C6H14
o. O00750
0.000780
o. O00750
O. 000780
o. 000750
155.5
164.8
156.7
178.2
161.4
65.2
91.1
91.3
+2.1 K
+1.a K
26.0
73.5
74.3
93.4
94.3
24.8
73.c
74.5
91.8
+0.3 Y
65.3
93.1
93.4
+0.6 K
...
9
10
11
12
13
-
Paraffins, C7H16
O. 000690
o. 000680
O. 000690
o. 000700
o. 000720
O. 000700
o. 000720
O. 000650
...
157.5
165.2
158.9
150.3
171.7
153.7
158.9
162.0
46.9
74.5
81 .o
0.0
46.4
55.8
69.3
95.6
88.5
83.8
86.6
+0.1
88.0
+2.4 K
+0-3 K
99.1
+0.6 K
+3.1 K
K
0.0
42.4
52.0
65.0
92.8
91.1
83.1
80.8
+1.8 K
43.5
73.2
74.7
85.0
+0.4 K
+0.3 I:
96.6
97.7
...
1.00 P
1.00 P
1.00 P
1.00 P
1.10
1.00 P
1.00 P
1.00 P
P
P
P
P
P
P
P
14
15
16
17
18
19
20
21
22
-
Paraffins, c8HlE
o. 000620
o. O0061o
0.000620
o. 000660
o. O00630
0.000650
0.000630
o. O O D M O
0.000650
o. 000620
159.1
165.0
162.0
160.9
155.7
172.0
159.1
164.1
172.4
162.0
...
23.0
I
28.1
60.8
...
20.6
26.8
26.7
33.5
72.5
71.3
65.2
55.2
75.5
24.8
57.8
59.6
61.1
61.1
93.3
91.7
87.3
01.6
94.6
0.80
0.90 P
0.90 P
0.90 P
0.90 P
0.90 P
0.90 P
0.90 P
0.90 P
0.90 P
6.50
5.80
5.80
5.80
5.80
5.50
5.90
5.90
5.90
5.50
P
P
P
P
P
P
P
P
P
12.7
12.7
12.6
12.5
12.4
12.6
12.4
12.6
12.6
12.4
23
24
25
26
27
28
25
3c
31
31
--`,,-`-`,,`,,`,`,,`---
1-89
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
1c2.1
TABLE 1C2.1 (Continued)
~~
~~~
FomuLa
D.
Search
YIlnbcr
bL&i lity
'aramter
CaL/cm^3)%
~~
F Lash
Point
TgPerature
a 9 F
Ideal Ces
Heat of
38.93
35.33
37.13
26.33
10.13
31.73
31.73
40.73
-800.42
-800.91
FomtiM
at 77 F
Btu/Lb
deal tas
leat of
Fra uso
i n at
:nergy of 7 - F
: o r n tion IttULb
iibbs
It 77 F
Itu/lb
~~
Paraffins, C M 8
a
an18
aHl8
34
35
36
37
38
39
W18
an18
40
37
u)
39
40
41
t8LI18
42
CSHl8
W
(%H18
u
m20
C9H20
C9H20
@H20
WH20
C9H2O
@H20
WH20
C9H20
m20
C9H2O
C9H2O
C9H2O
WH20
m20
WH20
WH20
m20
WH20
WH20
46
91
7.399
7.414
7.360
cBH18
7.179
6.881
7.292
7.2%
6.251
P
P
63.00
71.28
42:67
40.79
32.47
36.65
3.23
P
-808.63
P
-827.82
-843.10
-822.18
-817.93
-849.09
66.72
71 .51
84.27
34.95
-766.75
83.73
51.91
60.46
57.10
53
174
53.63
P
P
86-98
52.47
68-80
7.67
41
42
43
46
45
46
47
48
49
50
51
52
53
54
55
56
57
58
59
60
61
n-NONANE
2"ETHYLOCTANE
3"ETHYLOCTANE
4-UETHYLOCTANE
3-ETHYLHEPTANE
2,2-DlUETHYLHEPTANE
2,6-DIUETHYLHEPTANE
2,2,3-TRIUETHYLHEXANE
~,2,4-TRIMETHYLHEXANf
2,2,5-TRIUETHYLHEXANE
2,3,3-TRIUETHYLHEXANE
2,3,5"IRIRETHYLHEXANE
2.4,4-TRlUETHYLHEXANE
3,3,4-TRIMETHYLHEXANE
3.3-DIETHYLPENTWE
-
2,Z-DIRETHYL-3-ETHYLPENTANE
2,4-DIUETHYL-3-ETHYLPENTANE
2,2,3,3-TET~ETHYLPENTANE
2,2,3,4-TETRAHETHYLPENTANE
2,2,4,4-TETRAMETHYLPENTANE
2,3,3,4-TETRAnETHYLPENTANE
WH20
92
93
c48
W
467
432
433
47
434
435
436
437
50
430
431
51
52
53
54
7.624
7.487
7.516
7.477
7.477
7.257
7.326
7.253
7.035
7.028
7.314
7.218
7.130
7.410
7.438
7.248
7.316
7.384
7.296
6.920
7.380
87.53
73.13 P
74.93 P
71.33 P
71.33 P
74
-93
78-53
...
...
55.13
...
...
49.73 P
...
69.53
P
55.13
58.73
60.53
51.53
37.13
87.53
P
P
P
P
P
-790.75
-783.38
-788.41
-775.87
-824.95
-813.88
-809.16
-815.20
-868.41
-802.12
-812.85
-805.50
-789.05
-780.36
-775.30
-764.07
-794.78
-787.74
-812.21
-791.62
67.31
68.78
65.77
83.60
60.00
29.83
61.34
43.58
u -53
39.22
20.80
30.50
33.52
37.88
27-15
33.50
34.19
24.13
7.73
1.71
32.59
30.17
M.15
74.08
46.73
93.52
69.39
82.93
100.23
139.78
120.54
121.68
125.37
117.99
114.31
128.52
Paraffins, ClOH22
62 WDECANE
63 2-METHYLNOLIME
64 3-UETHYLNWANE
65 L-I(ETHYLNONANE
66 5"fTHYLNONANE
501 Z,2-OIWETHYLOCTANE
67 2.7-DIMETHYLDCTANE
68 3,3,4-TRIHETHYLHEPT~E
69 3,~,5-TRl~THYLHEPTANE
m 2,2,3,3-TETRMTHYLHEXNE
ClOHU
CloH22
ClOH22
ClOH22
ClOHU
ClOHU
ClOH22
ClOH22
ClOHU
4u
438
439
440
7.673
7.516
7.560
7.575
7.546
7.267
7.360
7.4M
7.255
7.387
Note Footnote codes follow Table 1C4.12.
1-90
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
114.53
105.53
100.13
100.13
100.13
87.53
91.13
...
".
".
P
P
P
P
-753.77
-77s.10
-768.70
-769.60
-769.67
-806.77
-797.71 F
-778.68
-785.33
-779.59
100.26
85.U
86.84
M.%
...
...
87.84
92.64
78.56
78.83
111.50
97.90
142.02
52.88
56.81
521%
39.28
42.30
37.47
--`,,-`-`,,`,,`,`,,`---
Paraffins, C9H2O
~
STD.API/PETRO TDB CHAPTER L-ENGL
0732270 05bbbBL
L777
m
OTO
1c2.1
TABLE 1C2.l (Continued)
L
æ
lm
u
e
b
iLty Liai t s
Ani Line
Point
of
Expansion
at 6 0 F
ltSOn
Yo.
Factor
,tunc Percent in
ir Mixture
Research Method
dcsF
œL TEL
t tear
Pr d e e F
Louer
Upper
er on1
-
-
Pa r e f f i n s , #)Hl8
154.4
In.0
150.6 H
159.4
175.0
152.6
154.9
O' . O ~ O
O .0006M
O'LOW590
Ol.oCw30
O1.oow50
OI.OM)590
C1.00o6M
-
...
...
81.7
88.1
88.7
99.9
100.0
99.4
95.9
...
97.1
M.1
*0.2
+2.0
*3.0
K
K
K
K
*LO
+O.?
...
K
K
76.3
87.3
80.8
+l-2 K
100.0
M.6
*0.2
...
94.7
0.90 P
00.0
0.90 P
95.9
P
...
.3.0
...
...
...
L:
K
33
P
12.3
12.3
12.2
12.3
12.5
12.2
12.2
12.1
12.7
12.7
12.5
12.5
12.4
12.6
12.6
12.3
12.5
12.6
12.2
12.4
12.3
12.1
12.0
12.2
12.2
11.9
12.1
12.3
12.0
41
42
43
P
5.60
5.40 P
5.40 P
5.40 P
5.60 P
5.10 P
5.40 P
5.18 P
5.18 P
5.20 P
5.18 P
5.49 P
5.20 P
5.18 P
5 .70
5.20 P
5.50 P
4.90
5.30 P
5.00 P
5.30 P
0.70 P
5-40
5.00 P
12.:
12.ï
12.;
12.t
12.!
12.t
12.1
12.'
12.:
12.1
0.w
K
5.90
5.90
5-50
5.60
6.00
5-60
6.00
5.30
1-00 P
O.%
1.00 P
1.00 P
0.90 P
P
P
P
P
P
P
u
35
36
37
38
39
40
-
FInraffins, C9H2O
164.7
I
.
.
167.0
176.0 H
c1 . ~ 0
...
cl. 000720
c1.000620
c1.000550
163.0 H
H
cl.
O00580
C1.000560
cI. 000630
C
(1.000520
c1.000550
180.9
I
...
...
...
..L
91.6
99.5
W.6
%.O
(1.000520
...
".
000560
000540
(1.000570
(l.
-
I-
...
...
...
...
14:;
(1 .O00560
(I.
...
60.5
162.0 H
Cl. 000580
172.0
C
...
...
...
...
...
...
...
50.3
."
...
...
...
...
...
...
...
...
83.5
...
...
...
...
...
.-.
...
...
+0.1 K
+0.8 K
+0.4 K
99.4
...
".
...
...
...
...
....*
...
...
...
...
...
...
...
...
...
...
77.2
...
...
...
...
...
...
...
...
...
0.70
0.85 P
0.85 P
0.85 P
0.80 P
0.80 P
0.80 P
P
P
P
P
P
P
0.80 P
0.80
0.80
0.80
0.80
0.80
0.80
...
...
...
84.0
+1.8 K
+0.5 K
+3.6 K
...
."
...
...
97.1
b6.0 K
b3.6 K
b4.0 K
...
...
...
O .70
0.80
0.80
0.80
0.85
0.85
0.80
P
P
P
P
cc
45
46
47
c8
49
50
51
52
53
54
55
56
57
58
59
60
--`,,-`-`,,`,,`,`,,`---
tI. 000630
c.l 000630
164.7
c1.000580
171.5
cl. O00590
61
-
P a r a f f ins, ClOH22
0.000550
0.000640
170.6
o .OM)640
o. 000600
o. O00600
...
O. 000590
O. 00057O
O. 000560
O . O00530
174.2 H
...
...
92.4
+0.2
w.7
...
...
...
...
...
...
...
...
86.4
+2.O
...
...
100.0
I
+2.5
k
P
P
P
P
P
P
0.72 P
0.72 P
5.00 F
5.00 F
5.00 F
4.80
5.10
4.89
4.89
4.70
F
F
F
F
F
6;
6:
&
61
&
50'
6:
61
6'
71
-
1-91
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
0.70
0.70
0.70
0.70
0.70
0.72
...
...
...
1
.
.
...
...
I:
0.70
Not for Resale
1c2.1
TAB= 1C2.1 (Continued)
~~
IO.
conpand
fomla
~~
Search Solrrbility
Y a r Parwcter
Point
<Cal/cm^3)^n f a a p
erature
&IF
I - I
Paraffins, ClOH22
71 2,2,5,5-TETRAC(ETHYLHEXANE
C l OH22
441
6.922
ClOH22
c42
7.570
73 rrWDECANE
C11 H24
74 n-DMECANE
75 n-TRIDECANE
76 n-TETRADECANE
TI n-PENTADECANE
C12H26
C13H28
C14H30
C15H32
C16134
Cl 7H36
C18H38
C19H40
C2OH42
C21H 4 4
C22H46
cm48
63
64
7.769
7.789
7.867
7.888
7.925
7.916
7.889
7.856
7.875
7.837
R 2.4-OIMETHYL-3-ISWROPYL
PENTANE
-~
~~
Flash
Ideal tas Ideal tas Heat of
Heat of
Gibbs Free F u s i o n at
a t 77 F
Energy of 77 deg F
Formation Btu/lb
Btwlb
a t 77 F
Formation
Btu/lb
....
58.32
...
-863.89
29.61
-721.88
189.16
1.81
-743.81
113.21
-727.03
-720.42
-714.69
-710.40
143.01
150.30
61.07
93-os
66:53
97.77
Paraff ins, Cl1 to C30
78 n-HEXADECANE
79 n-HEPTADECANE
80 n-OCTADECANE
81
82
83
84
85
n-NONADECANE
n-E f COSANE
n-HENEICOSANE
n-DOCOSINE
--`,,-`-`,,`,,`,`,,`---
n-TRICOSANE
86 n-TETRACOSANE
87 n-PEYTAC6SANE
88 rrHEXACOSANE
89 n-HEPTACOSANE
W n-OCTACOSANE
91 n-NONACOSANE
92 n-TRIACONTANE
C24H50
C25H52
C26H54
C27H56
C28H58
C29H60
C30862
65
66
67
68
69
70
71
73
445
75
76
77
78
79
80
81
82
446
."
".
".
...
...
...
...
...
...
...
149.00
164.93
173.93
212.00
236.93
275.00
298.40
329.00
334.13
332.33
350.33
364.n
380.93
395.33
395.33
395.33
442.13
395.33
460.13
395.33
E:E I
-733.77
P
-m.22
P
P
P
P
P
P
P
P
P
P
P
-701-27
-697.73
-694-55
-692.63 P
-690.00 P
-687.60 P
-685.53 P
167.41
171.96
-683.50 P
189.34
-681.62
-679.89
-678.27
-676.77
-675.37
70.08
155.99
101.41
71.88
104.35
162.39
73.42
106.42
...
178.19
180.91
176.05
."
I
70.45
P
P
P
193.77
P
197.62
199.50
P
I
...
70.05
1
Note: Footnote codes follow Table 1C4.12.
1997
1-92
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
STD.API/PETRO TDB CHAPTER
L-ENGL
0 7 3 2 2 9005 b b b 8 3
L977
773
m
1c2.1
TABLE 1C2.1 (Continued)
oefficimt
ASTH
Octane
Ani I ine
Y h r s
r
Research
Method
Y
I
l
e r deg
F
L Factor
IFl-bilty
Limits 'atson
YO
.
V o l m Percent in
i
r Mixture
Clear
I
o
.000630
0.000520
181.0 H
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
.
....
...
...
...
...
...
.
...
.
4.70 P
...
71
5.16 P
...
72
Paraffins. C11 t o C30
...
...
...
...
...
...
...
.
...
...
...
...
...
...
...
...
...
...
...
...
.
...
...
...
...
...
...
...
...
...
...
...
...
.
...
...
...
...
.
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
I
...
...
...
...
...
...
...
...
...
...
...
...
...
.
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
P
5.10
4-90
4.70
4.50
4.30
4.20
4.00
P
P
3.50 P
3.40 P
3.30 P
12.7
12.7
12.8
12.8
12.9
12.9
10.7
13.0
13.0
13.1
13.1
13.2
13.4
13.2
13.3
P
3.30 P
23.0
P
3.20 P
0.30 P
3.20 P
3.10 P
3.10 P
13.3
13.4
13.4
13.4
0.50
0.40
0.40
0.40
0.40
0.40
0.40
0.30
0.30
0.30
0.30
P
P
P
P
P
P
P
P
P
P
0.30 P
0.30 P
P
P
P
P
P
P
P
P
P
3.90
3.80
3.70 P
3.60 P
3.50 P
73
74
75
76
77
78
79
80
81
82
a3
84
as
a6
87
88
89
90
91
92
.
1-93
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
0.70
0.60
0.60
0.50
0.50
0.50
--`,,-`-`,,`,,`,`,,`---
Psrsffirts. ClOH22
Not for Resale
1c2.2
TABLE 1CYCLOPARAFFINS SECONDARY PROPERTIES
IO.
Formula
eonpand
r
n
Ideal cas
Search Sollbility
N k r Parameter
G i b b s Fre
Energy of
(Cal/arP3)%
Formation
at 77 F
Btu/lb
Alkylcytlopropanes, C3 to C5
uH6
96 c ~ s - ~ , ~ - D I I Q ~ H ~ C Y C L O P R O P A N6H10
E
101
350
351
352
97 trarrs-l82-DIIIETIIILnCLWROPWE C5H10
3%
93 CYCLOPROPANE
PC HETHYLCYCLOPROPANE
b ETHYLCYCLWROPANE
ctH8
ml10
7.023
...
...
...
I
.
.
."
...
...
."
..I
544.56
191.56 f
19.62 I
4.29 I
-19.62
1066.64
785 -38
...
684.77
667.99
55.64
...
...
...
...
Alkylcyzlokrtam, C4 t o C6
P8 CYCLDBLITANE
99 HETHYLCYCLOBUTANE
100 ETHYLCYCLœUlANE
102
353
354
7.829
104
105
107
108
109
110
111
112
8.088
7.868
7.942
7.556
7.898
7.m2
7.570
7.653
C8H16
C8H16
C8H16
114
115
116
7.995
7.790
7.741
W16
357
W16
358
C8H16
359
Qu116
a16
C8H16
360
118
119
QIH16
361
CBH16
362
C8H16
363
cBH16
364
...
."
-83.17 P
."
...
218.38
-41.69 F
-140.48 r
859.75
...
...
8.35
...
."
Alkylcy-clopentanes, C5 to C7
101
1O2
103
104
105
CYCLOPENTANE
METHYLCYCLOPENTANE
ETHYLCYCLOPENTANE
1,1-DIWETHYLCYCLOPENTANE
C5H10
c6Hl2
CM14
CM14
CM14
cis-1.2-DlnETHYLCYCLOPEWTAWE
106 trans-1,2-DIHETHYLCYCLOPENTANE c7H14
107 cis-l.3-DIIIETHYLCYCLOPENTAWE
CM14
108 trars-i,3-DIr(ETHYLCICLOPENTANE
cm14
-172.20
-542.51
-555.65
-605.48
-567.20
-598.52
-594.84
-586.99
238.15
185 .U
196.16
171.16
ZOO.24
168.00
171 -95
181 -81
32.45
32.46
204 .E
38.51
3.73
35 .u
30.14
4.74
7.27
31.44
~~~
Alkylcyclopentanes, C8H16
1W n-PROPYLCYCLOPENTANE
110 ISOPROPYLCYCLDPENTANE
111 I-METHYL-1-ETHYLCYCLWENTANE
112 cis-1-METHYL-?-ETHYLCYCLOPENTANE
113 trans-1-METHYL-2-ETHYLCYCLWENTANE
114 cis-l-IIETHYL-3-ETHYLCYCLOPENTANE
115 trans-l-IIETHYL-3-ETHYLCYCLOPENTANE
116 1.1,2-TRIUETHYLCYCLOENTANE
117 1,1,3-TRIWnHYLCYCLOPENlANE
118 ~,c-Z,~-~-TRIMETHYLCYCLOPENTANE
119 l8c-2,t-3-lRlMETHYLCYCLOPENTANE
120 1, ~-~,c-~-TRIHETHYLCYCLOPENTANE
121 ~,~-~,c-~-TRIHETHYLCYCLOPENTWE
1
60.53 P
49.73 P
42.53 P
... I ... I
... ...
...
...
-567.42
-577.42 P
-593.47
...
-301
...
...
...
...
...
...
...
...
...
...
...
.53
P
-301.53 P
...
-301.53 P
-383.76 P
-383.76 P
...
...
."
-301.53 P
...
...
...
...
...
...
.....
194.13
-301.53 P
".
...
...
...
...
203.25
-383.76 P
-383.76 P
-383.76 P
...
...
...
...
...
...
...
Note: Footnote codes follow Table 1C4.12.
1997
1-94
--`,,-`-`,,`,,`,`,,`---
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
STD.API/PETRO T D B C H A P T E R L-ENGL L977 0732290
05bbb85 74b
m
1c22
TABLE 1C2.2 (Continued)
-
wfficint
ASTM
- Motor Method
Aniline
Point
I
rpansim
Octane
1.86 P
i
1
1.49 P
95
io.
Yuabers
K Factor
I rtesearch Method
)
u
ln
ePercent in
ir Mixture
)908
/ _ F
:lem
h
m
l TEL
per g a l
si:;
a:;'Y
87.8
86.6
b0.2 Y
a.4 Y
+0.4 Y
+0.7 K
M.7 K
3
m
l TEL
P
' 981
Clear
.oyer
\Lkylcyclopropanes,C3 t o C5
--.
...
I . 000820
)O
. M)780
...
I
...
I si:;
...
...
..-
83.8
84.3
...
...
I
...
...
...
10.60
2.40
...
1.49 P
...
...
1.80 P
1.49 P
1.20
...
11.42 P
9.57 P
9.79 P
... 1
12.3
9.3
11.9
11.8
...
93
94
W
97
-
\lkylcyclokrtenes, C4 to CA
O. 000870
D. OOO760
o. O00730
...
loi:;
...
H
...
63.9
...
...
...
...
...
s
.
41.1
11-10 P
9.57 P
7.70
1 1 -5
11 .8
11.6
9.40
8.35
6.70
6.80
7.30
7.30
7.30
11.1
11.3
11.4
11.4
11.3
11 .S
11.6
98
W
1 O0
-
klkylcyclopentsnes, C5 to C7
o. 000700
0.000710
D - 000670
0.000660
o. 000630
0.000660
O. 000650
0.00oMo
*0.1 K
91 -3
67.2
92.3
113.0 H
103.8
116.1
...
...
73.1
121.8 H
*0.9
K
*0.5
K
79.5
+0.9
K
...
...
79.2
80.6
91.2
93.2
31.2
81.1
59.8
94.3
1.40
1.20
1.10
1.10
1.10
1.10
1.10
1.10
P
P
P
P
P
P
P
P
P
P
P
P
P
7.30 P
101
102
103
101
1 o5
106
107
1 Oe
11 .S
-
11.5
105
1 I(
0.90 P
6.40 P
6.50 P
6.10 P
0.93 P
6.52 P
11.4
Ili
0.93 P
6.52 P
11.6
113
Alkylcyclopentanes, BH16
O. 000580
O. 000540
O. 000590
112.0
ta. 1
60.5
...
76.2
89.4
...
0.000590
117.5
H
...
...
O. 000580
126.0 H
...
0.000580
o. O00580
o. 000630
0.00oMo
...
...
...
...
o.Wo590
105.8
o .O00580
105.8
o. 000660
105.8
O. O00630
1..
...
...
...
0.90 P
...
...
.-.
...
...
L..
11.5
1 1 .4
111
59.8
79.6
57.6
79.2
0.93 P
6.52
P
11.6
114
59.8
."
79.6
57.6
T9.2
83.5
95.6
87.7
...
+O.l K
0.93 P
0.93 P
0.93 P
6.52 P
6.19 P
6.19 P
11.6
11.4
11.7
115
116
117
...
0.93 P
6.61 P
11.4
118
...
0.93 P
6.61 P
11.5
119
0.93 P
6.61 P
11.7
120
0.93 P
6.61 P
11.5
121
...
...
...
...
...
...
...
...
...
...
... I ...
...
I
...
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
O .95
...
...
--`,,-`-`,,`,,`,`,,`---
Not for Resale
1-95
1c2.2
TABLE 1C2.2 (Continued)
o.
coapand
Poi nt
'araueter
erature
I d e a l Gas
Heat of
Formation
a t 7? F
EtWLb
klkyltyclopmtanes, cSnl6
122 1,PZ, t-4-TRIMETHYLCYCLBEUTAUE
123 l,t-2,c-4-TRIKElHYLcwLœ€uTANE
W16
1
...
...
...
...
365
-383.76 F
-383.76 F
...
...
Alkytcyclopentanes, C9H18
124
n-WYLCYCLOPENTANE
125 I~YLCYCLOPENTANE
126
l-IRTHYL-l-n-PFtCPYLCYCLOPENTANE
127 1.1-DIETHYLCYCLOPENTANE
128 cis-1,2-DIETHYLCYCLDPPElfAWE
129 1,1-DlMETHYL-2-ETHYLCYCLOPENTANE
Alkytcyclopentancs,
-573.16
-354.00F
... 1 ...
...
...
I
...
...
"*
-338.56 F
-338.56 F
-338.56 F
-411"
P
211.n
I
38.53
...
I ...
::: 1 :::
.'.
... 1
.
I
.
..I
C10 t o C25
n-PENTYLCYCLOPENTAUE
130
131 n-HEXYLCYCLOPENTAIiE
132 n-HEPNLCYCLOPENTANE
133 n-OCTYLCYCLWENTANE
n-UOWYLCYCLOPENTANE
1%
n-DECYLCYCLOPENTANE
135
1% n-UNDECYLCYCLOPENTAHE
137 n-DOOECYLCYCLOPENTANE
138 n-TRIDECYLCYCLWENTANE
139
n-TET~ECYLCYCLOPENTAUE
140 n-PENTADECYLCYCLOPENTANE
141 n-HEXADECYLCYCLWPENTANE
142 n-HEPTADECYLCYCLWENlANE
143
WOCTAMCYLCICLOPEUTANE
144 n-)IOIUDECYLCYtLOPENTANE
n-EICDSYLCYCLDPENTANE
145
ClOHZO
C1lH22
C12H24
C13H26
C14H28
C15H30
C16K32
C l 7H34
C18H36
C19H38
uoH40
C21 H42
t22W
C23H46
c 2 ~ a
C25H50
123
124
125
126
i27
128
129
130
131
132
133
134
373
374
37s
376
...
...
...
8.068
8.102
8.131
8,157
8.176
...
...
...
...
."
8.193
8.209
8.223
8.237
8.248
8.257
8.265
...
...
...
...
.I.
...
...
...
...
...
...
.I.
-579.29
-584.29
-588.24
-591.79
-594.61
-597.08
-599.60
-601.46
-603.31
-6w.94
-606.26
-607.62
-483.70 P
-490.27 P
-496.29 P
-501.84 P
217.00
220.40
223.50
226.11
228.34
230.29
231.79
233.30
234.65
US .69
236.77
237.76
...
...
...
...
...
...
...
...
...
67.69
...
...
...
...
...
...
...
...
...
...
Llkytcyclohexaner, C6 a d C7
146 CYClOHEXAUE
147
IETHILCYCLOHEUME
C7H14
8.191
7.849
C8H16
C8H16
C8H16
7.658
7.942
7.712
I
-4.00
21.20
-629.87
-6~7.81
163.01
119.67
13.81
29.62
151.S3
31 .W
157.90
132.09
6.31
40.01
LLkylcyctohexanes, =H16
1 1 8 ETHYLCYCLOHEXANE
149 I,I-DIIIETHYLCYCLOHEXANE
150 CiS-l,2-DIIIETHYLCYCLOHEWE
151 trans-1.2-OInETHYLCYCLOHEYAllE
7.986
142
143
--`,,-`-`,,`,,`,`,,`---
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
71-60
37.13 P
71.33 P
62.33 P
STD.API/PETRO T D B CHAPTER L-ENGL
0732290 0 5 b b b 8 7 519
L997
m
1c2.2
TABLE lC2.2 (Continued)
lmnmbilty Limits
Etson
10.
Factor
Uotor Uethod
D 357
per a0 F
Lescarch Uethod
)m
3d TEL
pcr gal
Clear
:tear
hl TEL
ollmc Percent in
i r Mixture
Louer
per gal
m r
-
Alkylcyclopcotanes, UM16
...
o.oow6o
...".
o .000600
0.000550
0.000600
o. 0006w
... 58.1 28.2
."
...
...
...
...
...
H
...
Alkylcyclopentanes, C10to
o. O00550
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
0.93 P
6.61 P
11.6
I22
0.93 P
6.61 P
11.8
123
0.80 P
0.83 P
5.90 P
5.94 P
11.6
11.6
124
125
...
...
0.83 P
0.83 P
0.83 P
5.61 P
5.61 P
5.61 P
11.3
11 -3
11.5
12t
127
12E
...
0.83 P
5.68 P
11.4
125
0.74 P
0.68 P
0.62 P
0.57 P
0.53 P
0.50 P
0.47 P
5.47
5.20
5.06
5.01
5.07
5.24
11.7
11.9
12.0
12.1
12.2
12.2
13[
13'
13;
13:
131
131
131
13;
131
13'
98.3
...
-
'
-2.0119.7
127.2
89.2
...
."
Alkylcyclopcntanes, Sn18
0.000540
0.000590
...
79.5
...
...
...
...
...
...
...
...
...
...
.....
...
...
...
...
...
...
...
-3.0
33.4
...
...
...
...
29.6
59.2
...
...
...
.f.
".
C25
...
...
...
...
...
".
...
...
...
...
...
36.7
..I
f
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
.-.
."
...
...
...
...
...
...
...
...
...
...
...
...
0.44 P
0.41 P
0.39 P
0.37 P
0.35 P
0.34 P
0.32 P
0.31 P
0.30 P
P
P
P
P
P
P
5.53 P
5.95 P
1!?J
P
12.4
12.5
12.6
12.7
12.8
12.7
12.8
12.9
12.9
7.20 P
11.c
11 -3
6.53
7.33
8.30
9.79
11.67
14.20
17.63
22.34
P
P
P
P
P
P
P
--`,,-`-`,,`,,`,`,,`---
0.000570
Vd
14
14;
14:
14,
14'
-
Alkylcyclohexanes, C6 and C7
o. 000680
87.8
77.2
O. 000630
105.8
71.1
87.3
86.2
83.0
74.8
97.4
88.2
1.30
1.15
8.00
CS .6
87.3
80.9
80.9
65.1
98.O
94.3
94.5
0.90
0.90 P
0.90 P
0.90 P
6.60
6.10 P
6.50 P
6.50 P
14.
14
-
Alkylcyclohexanes, C8H16
O. O00540
110.8
O. 000590
113.7
78.6107.1
0.000550
o. O00580
78.7118.9
40.8
85.9
65.4
95.7
90.7
90.8
11.4
14
1 1 .? 14
Il.¿
11.5
15
15
c
1-97
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
-
S T D - A P I I P E T R OT D BC H A P T E R
L-ENGL L777
m
0 7 3 2 2 9 0 0 5 b b b A A 455
m
1c2.2
TABLE 1C2.2
Yo.
Fornula
Carpod
(Continued)
Search Solubi 1 it y
Nuaber Paremctet
Ksl/cm’3)^H
ideal Cas
;it¿s
Fre
Energy o f
10-t
iM
îeat of
:usion a t
‘7 deg F
It
F
3tu/lb
Alkylcycloheuneb, C8H16
152
153
1%
155
cis-l,3-bl~THYLnCLOHR(CJIE
tras-l,C-DI~lHYLC~CLDHEXANE
114.30
139.14
145.39
121.51
7.643
7.839
7.810
7.575
144
145
146
147
trms-l,3-DIMTHYLCYCLOHEXANE
cir-1,4-D1IIETHYL~CLOHEXAYE
41.44
37.88
35.89
47.33
i
Alkylcyclohexaneo, C9 Vd C10
--`,,-`-`,,`,,`,`,,`---
156 n-PROPYLCYCLOHEXANE
157 lSOPROPYLCYCLOHEXANE
158 n-BUTYLCYCLOHEXANE
159 ISOBUTYLCYCLOHEXANE
160
$~-BUTYLCYtLOHEXANE
161 tcrt-BUTYLCYCLOHEXANE
162
l-METHYL-4-ISOPROPYLCYCLOHEXAWE
ALkylcyclohexanes,Cl1
163
ln
7.990
7.961
8.015
384
...
...
...
372
...
...
...
...
-658.30
-644.09
-653.37
-419.09 1
-350.99 I
-3e4.00 I
-..
-416.78 I
87.53 P
95.00
118.13 P
n-PENTYLCYCLOHEXANE
C l 1H22
167
168
n-HEPTYLCYCLOHEXANE
n-OCTYLCYCLOHEXANE
n-NONYLCYCLOHEXANE
n-DECYLCYCLOHEXANE
n-UNDECYLCYCLOHEXANE
n-DWECYLCYCLOHEXANE
n-TRIDECYLCYCLOHEXANE
n-TETRADECYLCYCLOHEXANE
n-PENTADECYLCYCLOHEXANE
n-HEXADECYLCYCLOHEXANE
n-HEPTADECYLCYCLOHEXNE
n-CCTADECYLCYCLOHEXANE
Cl2H24
t13H26
C14H28
C15H30
Cl6H32
C17HU
tl8H36
t19H38
C20H40
C2lH42
C22H44
C23H46
C24H48
n-YO(1ADEtYLtYtLOHEXAIlE
C2SH50
157
169
170
158
171
172
173
174
377
378
379
380
381
t26H52
382
C7Hl4
C8H16
C9H18
C9Hl8
t12H22
159
160
164
385
155
178 n-EICOSYLCYCLOHEXANE
8.067
8.100
8.126
8.151
8.170
8.137
8.200
8.216
8.228
8.241
...
.*.
...
...
-..
”.
...
...
...
...
267.53 P
.. .
...
...
...
...
...
...
...
...
. . I
Cyclopsraffins, C7 t o C12
179 CYCLOHEPTANE
180 CYCLOOCTANE
181 CYCLONONANE
182 ETHYLCYCLOHEPTANE
183 BICYCLOHEXYL
Note: Footnote codes follow T a b l e
8.411
8.489
8.589
4b.33 P
”.
165.20
8.303 -703.16
35.39
...
...
...
...
...
...
43 .C8
.”
...
178.69
184.77
190.86
194.54
198.35
201 .72
204.81
207.40
209.71
211.95
213.83
215.53
50.13
56.64
61.16
65.95
70.11
74.01
.”
i
-653.11
-651.59
-650.02
-648.90
-647.96
-650.17
-646.17
-645.54
-6cL.95
-644.27
-643.81
-643.38
-499.80
-505.43
-510.61
-515.38
F
F
F
F
-521.21
-L81.98
-452.27
-122.97 F
...
...
...
_..
277.55
%L. 70
...
...
110.13
76.91
78.08
82.34
84.64
...
...
...
...
...
8.26
9.23
6.58
...
...
1C4.12.
1-98
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
161.36
166.87
173.30
t o C26
I 6 4 n-HEXYLCYCLOHEXANE
165
166
167
168
169
170
171
172
173
174
175
176
149
150
152
386
383
1997
Not for Resale
1c2.2
TABLE 1C2.2 (Continued)
~~
Annilim
point
of
Expansion
a t 60 F
L
I
Motor Method
D 357
Research Method
OLM
D908
i r Mixture
-
~~
l d iLty L M t s
atsm
Factor
MO.
Percent i n
~
Clear
pcr deg F
1
Lwer
Alkylcyctohcxsnes, CBHl6
0.000580
125.1
0.m590
115.3
;:'I:;
0.000590
o.oDWz0
1 1
71 .O
64.2
...
83.8
85.0
83.4
71.7
66.9
67.2
68.3
."
83.5
8c.7
82.8
0.90 P
0.90 P
0.90 P
0.90 P
6.50 P
6.50 P
6.50 P
6.50 P
11.6
11.3
11.4
11.6
~
Alkylcyclohcxwr,
47.7 14.0121.6
0.000500
0.000500
0.000500
...
...
...
...
1
152
153
154
155
-
C9 wd C10
120.0 H
129.9
135.3
...
1 61...
.1
I
...
...
...
...
128.5
133.7
81.4
25.3
...
...
...
17.8
62.8
...
...
...
...
...
..-
0.95
0.80
0.85
0.74
0.74
0.74
0.74
0.68 P
42.0
79.6
22.5
...
".
...
I..
.-.
...
.-.
...
...
P
P
P
P
P
P
P
5.90 P
5.90 P
5.50 P
5.53 P
5.47 P
5.47 P
5.86 P
11.5
11.4
11.6
11.4
11.4
11.4
10.8
156
157
158
159
160
161
162
-
Alkylcyclohexanes, C11 t o C26
...
...
...
...
...
...
.....
...
."
.....
...
...
...
...
...
."
...
...
...
...
...
".
...
...
."
...
...
...
...
...
.-.
...
...
...
...
...
.-.
...
...
...
...
...
."
...
.....
."
...
...
...
...
..S
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
."
".
".
...
...
...
...
...
...
...
...
...
...
...
."
."
...
...
...
...
0.62
0.57
0.53
0.50
0.50
0.u
0.41
0.39
0.37
0.35
0.34
0.32
0.31
0.30
P
P
P
P
P
P
P
P
P
P
5.20 P
5.06 P
5.01 P
5.07 P
5.24 P
4-70 P
5.95 P
6.53
7.33
8.38
P
P
P
9.79 P
11.67 P
14.20 P
P
P
P
P
0.29 P
17.63 P
22.34 P
28.90 P
1.10 P
0.90 P
7.10 P
6.30 P
0.83 P
0.83 P
5.79 P
11 - 8
1 1 .9
12.0
12.1
12.2
12.3
12.4
12.4
12.5
12.6
12.6
12.7
12.8
12.8
12.9
12.9
~
163
164
165
166
167
168
1 bF
17C
171
172
l??
174
175
1 76
1Ti
17I
-
Cycloparaffins, C7 to Cl2
0.000520
O. 000530
."
..-
...
".
".
".
s..
40.2
58-2
...
...
...
65.3
."
...
...
...
38.8
71 .O
59.8
...
...
.I.
0.70
5.87 P
5.10
10.9
10.9
10.9
11.5
10.9
175
18[
181
18;
182
-
1-99
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
...
...
...
...
--`,,-`-`,,`,,`,`,,`---
o. O0061o
Not for Resale
1c2.2
TABLE lC22 (Continued)
IO.
Forarta
C a p M d
Search S o l u b i l i t y
NuIber P a r e t e r
(Cal/af31*%
Flash
Point
T"
erature
a S F
D e c a h y d r w t h a l e n e s , C10 t o C12
cis-DECAHYDROYAPHTWALENE
I
trans-DECAHlDROUPHTHALEllE
1 - E l H Y L - [cis-MCAHYDRONAPHTHALENE1
l-WETHYL-ttrans-MUHYDRONAPHTHALENE1
1-ETHYL-tcis-DEUHYDRONAPHTHALENE1
1-ETHYL- [trans-DECAHYDRONAPHTHALENE1
9-ETHYL- [cis-DEUHYDROWHTHALENE1
9-ETHYL-Itrws-DECAHYDRONAPHTHALENE1
l
l
Clon18
153
1%
C l1H20
176
C l ln20
177
Cl2H22
178
...
...
...
ClZH22
179
."
180
...
...
ClZH2Z
Cl2H22
181
."
8.616
8.313
...
.f.
136.04
136.04
...
I..
...
Ideal Cas
Heat of
Forumtion
a t ?? F
Btu/Lb
-526.29
-566.50
266.26
229.00
...
...
...
...
...
...
...
.-.
...
."
...
...
29.54
U.86
...
...
...
...
...
...
Note Footnote codes follow Table 1C4.12.
--`,,-`-`,,`,,`,`,,`---
1-1O0
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
1997
Not for Resale
STD.API/PETRO TDB CHAPTER L-ENGL L777 m 0 7 3 2 2 7 0
05bbbVL T 4 T
m
1c22
TABLE 1C22 (Continued)
-
oefficient
f
Research methcd
t60f
b l u e Percent i n
rir Mixture
dcsF
F
e r deg F
-
L
Decahydronsphthntc,
0.000510
0.000550
."
...
...
95.5
I
:lo t o
."
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
c12
......
...
."
".
...
...
...
...
...
...
.
...
o.m
4.90
4.90
...
0.70 P
5.72 P
...
0.70 P
5.72 P
...
0.64 P
5.52 P
...
...
0.64 P
5.52 P
...
...
...
...
0.64 P
5.28 P
10.9
190
0.64 P
5-28 P
11 .2
191
-
.*
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
i
No.
Y Fnctor
xpsrrrion
...
I I.
0.70
--`,,-`-`,,`,,`,`,,`---
Not for Resale
10.5
10.7
9.6
...
...
...
1%
1 as
1Bb
187
188
189
1C2.3
TABLE 1C23
MONOOLEFINS AND DIOLEFINS: SECONDARY PROPERTIES
~-
~
NO.
ForPula
CallpWd
deal Gas Heat of
;i&Free F u s i o n at
inergy O f 77 &g F
Search
NuPtwr
:omtion Btullb
It 77 F
ItWlb
w l e f i n s , C2 and C3
I
I
201
202
6.080
6.427
1068.86
C4H8
204
c4H8
c4118
205
6.676
7.194
6.945
6.676
538.45
500.83
483.97
445.05
29.55
56-12
74.91
45.54
480.91
451.54
427.94
408.75
4W.19
370.56
35.68
43.68
46.66
U6.42
409.90.
391 .O5
424.51
47.83
45.33
42.25
42.13
192ETHYLENE
193PROQYLENE
634.98
51.45
30.74
M m t c f i n s , C4H8
1% 1-BUTENE
1% cis-2-BLIlENE
1%
trans-2-BUTENE
197 ISOBUTENE
CbH8
206
207
-131.03
~~
Mmlefins, CSHlO
199 cis-2-PENTENE
an10
QH10
200 trans-2-PENTEWE
2012-HETHYL-I-BUTENE
M2 3-METHYL-1-BUTENE
203 2-METHYL-2-BUTENE
c5n10
CSH10
C5H10
CSHI0
1 9 8 1-PENTENE
-
215
216
217
218
219
220
1 HEXENE
cis-2-HEXENE
trans-2-HEXENE
cis-3-HEXENE
trans-3-HEXENE
2-HETHYL-1-PENTENE
3-METHYL-1-PEWTEUE
4-HETHYL-1-PENTENE
2-HETHYL-2-PENlENE
c~s-~-I(ETHYL-~-PENTENE
trans-3-~THYL-2-PENTENE
cis-4-HETHYL-2-PENTENE
tram-4-METHYL-2-PEXlENE
2-ETHYL-1-BUTENE
2,3-D1MElIfYl-l-~E~
3,3-DlMElHYL-1-BLWENE
2,3-DI(RTlln-2-WTEWE
MwDolef i n s ,
209
21o
21 1
212
213
214
216
217
218
219
U0
221
222
223
224
225
226
227
228
229
230
231
u2
7.077
7.384
7.316
7.184
6 -822
7.414
7.336
7.487
7.497
7.448
7.472
7.360
7.057
7.077
7.516
7.531
7.678
7.140
7.199
7.428
7.169
6.695
7.756
-24.07 P
-16.87 P
-16.87 P
-18.67 P
-278.05
10.40
-25.87 P
-252.61
-18.40
-38.47 P
-16.87 P
-98.67 P
16.60
-33.07 P
-29.47 P
-22.27 P
-34.87 P
-18.40
-9.67 P
7.w
7.512
7.556
7.599
7.497
32.00
17.33 P
-
-214.55
-247.09
-274.88
-243.21
51.29
48.59
32.92
-302.65
-261.55 I
-341.12
-317.59
-322.55
-283.41
-3oc.79
-285.55
-330.86
-309.06
-350.74
18.43189.15
184.230.49
41.12
349.89
351 .W
39.33
341.60
37.69
393.27
379.81
38.76
400.33
27.88
366.13
412.w
33.02
355.87
30.24
36.62
5.47
Ch14
-
C7H14
2u
235
236
249
237
29.93
15.53 P
21.20
-274.98
-303.00
-326.65 I
-300.81
-323.58 F
390.57
391.45
--`,,-`-`,,`,,`,`,,`---
221 1 HEPTENE
222 cis-2-HEPTENE
223 trans-2-HEPTENE
224 cis-S-HEPTENE
225 trans-3-HEPTENE
Note: Footnote codes Collow Table lC4.12.
1997
1-102
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
L-ENGL
S T D - A P I I P E T R OT D BC H A P T E R
L777
m
0 7 3 2 2 7 0 0 5 b b b 7 3 AL2
1C2.3
TABU lC23 (Continued)
-
FI
L d i I t y Limits
Aniline
f
Irpansion
Point
3908
cr deg F
tlear
i r Mixture
Louer
bl TEL
lpper
=r gal
-
U and C3
Wonoolefins,
5.6
Ilonoolefins, cCn8
0.001160
o. 000980
0.001070
58.8 0.001200
LO.
Factor
VIp l m e Percent i n
Research k t h o d
Motor Method
t 6 D F
BtSOn
j
...
:::
1
80.8
83.5
...
...
...
...
...
...
t0.03 K
t0.2 K
97.4
100.0
...
...
--`,,-`-`,,`,,`,`,,`---
...
...
2.30
2.00
12.30
I l .o0
48.5
14.3
I92
...
...
...
...
1-60
1.60
1.80
9.30
9
9.70
13.1
12.6
12.9
13.0
I94
1%
1%
197
12.7
12.5
12.6
12.5
12.8
12.4
198
199
200
20 1
202
203
12.5
12.3
12.5
12.4
12.4
12.3
12.5
12.5
12.3
12.2
12.1
12.5
12.5
12.2
12.3
12.6
12.0
204
205
206
207
12.4
12.3
12.4
12.3
12.4
u:
.m
a.ao
1.80
193
-
-
M m l e f i n s , C5H10
o. O00890
o. O00870
0.000900
o. 000900
o. 000950
O. 000870
66.2
64.4
64.4
...
...
55 .o
77.1
...
...
81.9
... N
84.7
82.9
...
- ..
84.2
... N
98.6
90.9
...
...
+O:;'
Y
... N
*O:;.
K
_..N
85.8
97.3
99.2
76.3
76.4
91.7
80.8
...
83.2
92.7
80.1
81 .S
81.2
80.9
...
82.3
85 -2
82.2
84.5
83.0
85.0
94.0
94.2
96.0
95.7
97.8
1.50
1.50 P
1.50 P
1.LO
1.50 S
1.CO
8.70
10.60
10.60
9.60
9.10
9.60
1.00 P
1.20 P
1.20 P
7.50
9.00
9.00
9.00
9.00
9.00
9.40
9.40
9.40
P
P
P
S
P
-
Monoolefins, W 1 2
O. 000760
o. O00730
73.0
78.8
o. O00730
80.6 H
o. ooono
o. O00770
o. 000770
0.000750
o. 000790
o. O00730
O. 000740
O. 000700
O. 000760
o. 000800
0.000740
o. 000770
O. 000900
O. 00071O
ma
80.6 H
...
...
...
...
...
...
...
...
...
...
...
...
63.4
...
...
...
...
81 .o
84.5
82.6
84.0
86.3
79.4
82.0
85 .S
82.8
...
...
93.3
60.5
84.0
50.7
68.9
.-.
...
...
97.2
99.7
98.0
98.3
+0.1 K
+1.7 K
97.4
..98.4
...
-.-
99.8
+0.05 K
+0.5
K
99.5
...
100.0
1.20 P
1.20 P
1.20 P
1.20 P
1.20 P
1.20 P
1.20 P
+O.Z
K
+O.OZ
Y
K
1.20
1.20
1.20
1.20
K
1.20 P
+0.3
+0.3
...
P
P
P
P
98.5
1.20 P
1.20 P
...
80.2
0.80 P
89.8
98.2
8.60
8.60
9.10
9.10
9.00
9.10
9.00
8.10
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
zoe
2w
21c
21 1
212
21!
214
215
2lt
217
21¿
215
22(
-
Moroolefins, CM14
0.000700
O. 000670
o. 000660
0.000710
0.000700
81
.o
...
...
94.8 H
94.8
-..
...
68.8
78.9
79.3
84.6
...
s
.
54.5
73.4
90.2
...
89.5
1.10 P
1.10 P
1.10 P
6.90 P
7.80 P
7-80 P
7.80 P
7.80 P
222
223
224
225
-
1-103
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
".
1.10 P
Not for Resale
L-ENGL 2 7 7 7 W 0 7 3 2 2 7 0 05bbb74 7 5 7 W
S T D . A P I / P E T R OT D BC H A P T E R
1C2.3
--`,,-`-`,,`,,`,`,,`---
TABLE 1C23 (Continued)
o.
compavd
Fonula
Search
Y b r
Flash
Point
:olubi 1it y
IarIIIIZter
Cal/cm^3)%
Tcap
erature
dceF
hmolcfins, CirH14
226 2-ltETHYL-1-HEXEYE
227 3-METHYL-1-HEXENE
228 4-HETHYL-1-HEXEWE
229 5-IPTHYL-l-WEXENE
230 2-IIETHYL-2-IIEKYE
231 cio-3-UETHYL-2-IEXENE
232 trars-3"ETHYL-2-HnnWE
233 cis-4-WETHYL-2-HEXENE
trens-4-tETHYL-2-HEXEWE
235 cis-5-METItYL-2-HEXENE
236 trm-5-METHYL-2-HEXEWE
237 CiS-2-METHYL-3-HEXENE
m trans-2-HETHYL-3-HEXENE
239 cit-3-METHYL-3-HEXENE
240 tras-3-UETHYL-3-HEXENE
24 1 2-ETHYL-1-PENTENE
242 3-ETHYL-1-PENTENE
243 3-ETHYL-2-PENTENE
244 2,3-DlnETHYL-l-PENTEWE
245 2,4-D1tETHYL-l-PENTENE
246 3,3-DIWETHYL-1-PENTEYE
247 3,4-DIWETHYL-l-PENTEYE
248 4,4-DIMETHYL-l-PENTENE
249 2,3-DJCIETHYL-2-PENTENE
250 2,4-DlHETHYL-2-PENTENE
25 1 cis-3,4-DtWETnYL-2-PENTENE
252 trans-3,6-DlnETHYL-2-PEWTEWE
253 cis-4,4-DIHETHYL-2-PENlENE
254 trsns-4,4-DI~ETHYL-2-PENTENE
255 3-METHYL-2-ETHYL-l-BUTEWE
256 2,3,3-TRl~ETHYL-l-BUT€NE
zu
CM14
Cm14
C7H14
CM14
cm14
C7H14
Cm14
CM14
C7H14
Cm14
Cm14
C7H 14
CirH14
CM4
C7H14
C7H14
CM14
C7H14
C7H14
C7Hl4
C M 14
Cm14
C7H 14
C7H14
C7Hl4
CM14
Cm14
CM14
C7H14
Cm14
Cm14
238
7.463
456
457
458
459
21.207.336
460
461
462
163
c66
465
466
467
239
240
468
469
24 1
470
242
471
472
243
473
244
474
475
245
266
247
476
7.527
7.568
7.561
7.386
7.372
7.396
7.349
7.314
7.285
7.653
7.564
7.551
I
I
21.20
...
".
....
..
...
."
."
...
I
.
I..
13:% P
1.13 P
7.340
...
7.593
7.368
7.177
7.230
7.280
6.880
7.632
7.314
7.460
7.526
7.136
7.112
7.387
7.155
...
...
...
...
...
...
...
...
...
...
...
...
1.40
Ideal Gas
Heat of
Formtim
a t 77 F
Btullb
-330.16
-292.01
-292.06
-305.62
-37s.68
-369.11
-369.w
-331.46
-352.47
-340.65
deal Gas
iibbs Frec
l n r g y of
:omation
It ?7 F
ItufLb
361.28
404-28
404.15
P
P
P
P
P
P
P
-360.35 P
-338.02 P
-360.79P
-356.85
-342.84
-326.82
-280.67
-385.09
-360.35
-353.79
-320.51
-327.51
-352.03
-384.00
-394.94
-374.80
-374.80
-324.45
-394.95
-364.21
-374.37
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
".
...
.....
....
...
."
56.79
...
32.98
I..
40.30
49.37
...
...
31.14
...
... 27.a
...
...
23.82
...
...
...
...
370.52
...
423.20
21.98
...... 31.14...
...
... 38.47
32.98
.I.
...
...
...
...
...
...
...
...
...
27.48
38.47
29.31
38.47
3a.47
25.65
29.31
374 -68
3.48
...
...
Itcomlefins, C8H16
257
258
259
260
261
262
263
264
265
1-OCTENE
cis-2-OCTENE
tras-2-OtTENE
CiS-3-OCTENE
trans-3-OCTENE
Cis-4-OCTENE
trarts-4-OCfCWE
2-CRfHY L- 1 HEPTEWE
3-H€THYL-l-HEPTENE
-
C8H16
C8H16
C8H16
C8H16
C8H16
C8H16
252
487
7.585
7.575
7.531
7.531
7.512
7.463
7.531
7.419
...
I
69-53
I
62.33
47.93 P
62.33
46.13 P
50.00
...
-320.30
-342.90 P
-365.12 P
-342.90
P
-362.44
-342.90
-362.44
-366.27
-345.98
P
P
P
P
P
394.63
374.89
352.86
373.05
353.25
379.57
14
356.43
MO.
.f.
59.28
...
."
...
...
...
...
...
...
Note: Footnote codes follow Table 1C4.12.
1997
1-104
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
1C2.3
TABLE 1C23 (Continued)
ASTM
Aniline
Poi nt
3a1l TEL
pcr gal
Clear
78.8
71.5
74.0
85.0
80.0
85.6
78.6
83.7
84.0
90.7
YO.
Factor
olune Percent in
ID 9 0 8
Clear
ItSOn
hl TEL
xr gal
i r Mixture
Lower
Jpper
-
Monoolefins. cm14
0.000710
O.MK)690
0.DOoMD
O. 000700
0.000670
O.MI0720
O. 000670
o. ooomo
O. 000700
O .O00530
o. 000700
0.000520
O. 000740
0.000810
0.000760
O. 000670
0.000700
o.no0680
0.000710
0.000740
o .o00660
0.00oMo
o .o00730
o. 000690
O. 000700
0.000720
o. 000720
O. 000700
O. 000740
0.000710
O. 00071O
--`,,-`-`,,`,,`,`,,`---
1
E
-
l h il t y Limits
Yutmrs
IResearch Method
Motor Method
D 357
dcsF
I
Octane
...
...
."
...
..
.
...
......
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
64.0
79.2
80.0
79.6
...
83.0
."
81.O
."
82.0
...
81.4
...
81.6
80.6
84.2
84 -6
85.8
...
...
85 .O
...
85.7
...
85.1
."
85 -8
84.2
84.1
86.4
98.6
94.8
96.8
91.8
98.4
97.4
97.4
82.2
86.4
75 .S
91.6
92.4
91.5
98.6
W.8
... K
...
94.4
tO.06
...
97.9
%.O
96.4
...
95.6
93.7
99.3
99.2
*0.3 K
".
tO.1
K
...
*O.l K
...
98.8
."
+0.05 K
97.6
*O.l K
+0.3 K
*0.6 L:
+0.1 K
+0.8 L:
94.5
+0.1 K
99.5
86.1
87.3
87.3
...
...
80.9
85.4
80.0
85.3
82.2
87.7
83.3
86.4
85.1
95.4 H
90.2
90.9
82. O
90.5
94.5
85.6
93.7
34.7
56.5
56.5
57.7
73.0
73.0
28.7
56.3
63.5
56.3
78.7
81.2
72 .S
84.2
79.6
...
89.4
73.3
70.2
...
87.9
...
...
...
...
...
...
...
...
...
98.9
+O.&
K
97.5
100.0
96.0
...
*0.5
K
+0.5
K
97.0
+0.5
1.00 P
1.00 P
K
...
...
*0.9
+Q.l
*1.2
K
K
K
1.10 P
1.06 P
1.06 P
1.06 P
1.06 P
1.06 P
1.06 P
1.06 P
1.06 P
1.06 P
1.06 P
1.06 P
1.06 P
1.00 P
1.00 P
1.06 P
1.06 P
1.06 P
1.06 P
1.06 P
1.06 P
1.06 P
1.06 P
1-06 P
1.06 P
1.06 P
1.06 P
1.06 P
1.00 P
7.80 P
8.20
8.10
8.10
7.M
7.46
7.46
7.87
7.46
7.87
7.87
7.87
7.87
7.46
7.46
7.80
8.10
7.46
7.87
7.87
7.74
8.20
7.74
7.08
8.03
7.58
7.58
7.87
7.87
7.87
7.40
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
12.3
12.4
12.3
12.4
12.2
12.1
12.1
12.3
12.3
12.3
12.4
12.4
12.5
12.1
12.2
12.2
12.3
12.0
12.2
12.3
12.2
12.3
12.4
11.9
12.3
12.1
12.0
12.2
12.4
12.0
12.1
226
227
228
229
230
231
232
233
234
235
236
237
238
239
240
24 1
242
243
211
245
246
24 7
248
249
25 O
25 1
252
253
254
255
256
-
Hmoolefins, C8H16
O. O00580
o. 000640
o. 000630
O. 000540
O. 000670
0.000450
0.000630
O. 000630
0.000670
90.5
101.3
101.3 H
...
...
...
...
...
...
...
68.1
.
s
74.3
M.3
...
...
...
...
...
...
...
91 .8
...
0.80
0.90 P
0.90
0.90
0.90
0.90
0.90
0.90
0.93
P
P
P
P
P
P
P
6.80
6.90
6.90
6.90
6.90
6.90
6.90
6.90
7.16
P
P
P
P
P
P
P
P
12.4
12.3
12.4
12.3
12.4
12.3
12.4
12.3
12.4
257
258
259
260
261
262
263
2M4
265
-
1-105
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
78.7
Not for Resale
1C2.3
--`,,-`-`,,`,,`,`,,`---
TABLE 1C23 (Continued)
o.
Formula
COClpormd
Search
U h r
iolubility
Flash
'arameter
Point
:CaL/d3)^% T"
erature
dcsF
ldeal Gas
Ideal Gas
Heat of
at T7 F
à i b b s Free : u s i o n at
lnergy of 7-F
:ormation W / l b
Btu/lb
st
Formation
lest of
77 F
Itu/lb
__.
HoMc,lef ins,
266
267
268
269
270
271
272
273
274
273
276
277
C8H16
C8H16
an16
C8H16
csH16
C8Hl6
@Hl6
t8H16
cBH16
4-METHYL-1-HEPTENE
trsns-6-nETnYL-2-HEPTENE
trans-3-CIETRYL-3-HEPTEYE
2-ETHYL-1-HEXENE
3-ETHYL-1-HEXENE
4-ETHYL-1-HEXEWE
2,3-DIHETHIL-l-HEXENE
2.3-DIl4ETHYL-2-HEXENE
cis-2,2-DlMETHYL-3-HEXENE
2,3,3-TRlMETHYL-l-PENTENE
2,4,4-TRIMETHYL-l-PENTENE
2,4,4-TRlMETHYL-2-PENTENE
W16
CBHl6
C8H 16
C8Hl6
488
489
690
...
...
258
7.E
479
...
7.394
...
...
...
680
481
fa2
253
484
256
257
...
7.096
7.321
...
...
423P
...
...
46.13
...
...
...
-340.62 I
-38.8.89 1
-403.45 I
-371-64 I
-339.47 I
-332.95 I
-374.32 I
-415.71 I
-348.66 I
-386.21 I
-422.98
-401-90
15.53
1.13
...
."
349:ii
...
35435
...
...
...
...
...
...
...
...
...
...
...
...
."
332.56
358.23
n.65
26.08
379.73
367.19
356.94
349.67
337.86
331.27
325.58
320-97
319.79
313.98
311.19
308.37
61 .S4
42.37
47
-39
50.90
53.93
55.87
60.54
57.95
56.61
55.62
54.15
53.78
~~
Hmlefins, C9 to C20
278
27'9
280
281
282
283
284
285
286
287
288
289
1-NOIJENE
1 -DECENE
1-UNDECENE
1 -OCDECENE
1-TRIOECENE
1 -1ETRADECENE
1-PENTADECENE
1-HEXADECENE
1-HEPTADECENE
1-OCTADECENE
1-NONADECENE
1-EICOSENE
~~
~~
_
_
~9~18
ClOH20
CllH22
C12H24
C13H26
C14H28
C15H30
C16H32
cm34
C18H36
cm38
C20H40
259
260
261
262
263
264
265
266
491
267
492
284
7.683
7.731
C3H4
C4H6
C4H6
c5118
C5H8
301
302
303
304
305
306
307
308
31 1
309
6.847
7.922
7.624
7.873
7.829
7.697
7.111
8.049
7.751
7.492
C6H1 O
C6HlO
312
630
7.825
~
~
7.800
7.863
7.855
7.871
7.878
7.854
7.819
7.812
7.814
...
80.33
116.60
159.53
119.93
174.20
230.00
233.33
269.60
274.73
298.40
314.33
332.33
P
P
P
P
P
-354.1s
-382.21
-404.86
-422.46
-439.95 F
-453.85 F
-465.89 F
-478.13
-485.54 I
-493.81 F
-501.22 F
-507.72 F
Diolefins, C3to C5
290 PROPAD I EN€
2 9 1 1,2-BUTAOIENE
2921,3-BUTADIENE
2931,2-PENTADIENE
294cis-1.3-PENTADIENE
295 trans-1,3-PENTADIENE
296 1,4-PENTADIENE
297 2.3-PENTADIENE
298 3-METHYL-1.2-BUTADIENE
299 2-nETHYL-1,3-BUTADIENE
C5M
c5na
C5H8
cwa
-83:ii P
...
-40.27 P
-42.07 P
-45.67 P
-67.27 P
-34.87 P
-45.67 P
-65.O0
2044
-23
1289.99
868.26
887.97
522.47
478.63
671 .42
839.87
814.69
477.97
2154.76
1578.51
1190.00
1294.49
951.91
921.62
".
55.43
63.57
...
35.65
1079.77
45.17
38.40
1257.25
1246.52
920 -82
50.30
31.08
...
Diolefins, C6 to c10
300 2,3-DIMETHYL-1,3-BUTADIENE
3011.2-HEXADIENE
...
-7.63
...
236.28 P
-344.46 F
...
754.42
...
...
Note: Footnote codes follow Table 1C4.12.
1997
1-106
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
~~
~~~~
STD.API/PETRO TDB CHAPTER L-ENGL L797 m 0 7 3 2 2 9 0 0 5 b b b 7 7 468
1C2.3
(Continued)
TABLE 1-
L a f f icient
ASTM
3f
Ani L ï n e
EXpMsim
n t 60 F
Point
Octane
F l d i L t y Limits Uatson
L Factor
Volum? Percent i n
Air Mixture
Yrnbers
Motor Method
D 357
Research Method
D908
Yo
.
dtsF
#r de9
Clear
f
3 1 1 TEL
Clear
h l TEL
P' sal
Pr
Lwcr
Uppcr
gal
Mumolefins. =H16
o.oO063o
0
.
~
--`,,-`-`,,`,,`,`,,`---
0.oow
o.ooo61o
.m m
o .o m 0 0
o.oD0680
o.oowso
o .O00630
0.000690
0.000630
o .O00630
O
0
...
...
...
...
...
...
...
...
...
...
...
90.0
...
...
...
...
...
65.5
83.6
79.3
88.0
85.7
...
...
...
80.5
71.3
...
...
88.1
...
...
86.5
07.2
88.84.6
86.2
88.0
...
...
...
...
...
...
...
...
...
...
96.3
0.93 P
0.90
0.93
0.93
0.90
0.93
0.93
...
97.1
93.1
4-7 L
+0.6 K
K
*0.3
0.93 P
0.93 P
90.2
K
...
+0.9
+l.O
*0.6
K
I:
K
P
P
P
P
P
P
0.93 P
0.90 P
0.90 P
7.16 P
6.97 P
6.64 P
6.W P
7.16 P
7.16 P
7.00 P
6.34 P
6.66 P
12.3
6.66 P
6.70 P
11.9
275
12.2
276
277
12.1
12.2
12.3
12.1
12.2
12.0
266
267
268
269
270
271
272
273
274
6.40 P
12.3
12.3
12.1
Monoolefins. C9 t o C20
.
O 000590
o.oooM1o
...
...
...
...
.
...
...
...
.
...
100.4
111.4
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
.
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
0.60 P
0.55
0.50 P
0.40 P
0.40 P
0.40 P
0.30 P
0.30 P
0.30 P
0.30 P
0.30 P
0.30 P
6.00 P
5.7U
5.30 P
12.C
12.5
12.5
5.00 P
4.70 P
4.50 P
4-30 P
4.00 P
3.80 P
12.7
12.7
12.8
12.9
3.70 P
3.60 P
13.0
4-10 P
278
279
280
281
282
283
264
285
286
287
288
289
12.5
12.6
12.6
12.9
Diolefins. C3 to C5
...
.
O OOO98D
0.001130
o .000830
o .ooogzo
0.000850
0.000830
o .O00830
0.0008M)
o 000860
.
...
....
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
42.4
81.0
...
...
...
...
...
...
...
...
49.6
79.4
...
...
...
...
...
61.0
99.1
...
71.5
98.8
2.10
2.00 P
2.00
1.50 P
1.60 P
1-60 P
1.60 P
1.40 P
1.60 P
22.60 P
12.7
12.00 P
12.2
11-50
12.5
12.30 P
11.9
13.10 P
11.9
13.10 P
12.2
13.10 P
12.2
12.10 P
11.9
15.20 P
12.0
9.00
2.0012.0
290
291
292
293
294
295
296
297
298
299
Diolefins. C6 to C10
0.000720
...
...
...
...
...
...
...
...
...
1:ii P
...
...
11.6
11.9
300
301
1-107
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
...
Not for Resale
1C2.3
--`,,-`-`,,`,,`,`,,`---
TABLE lC23 (Continued)
No.
1
F lash
Point
T a p
erature
Carpoud
Diolefins,
t6 t o CID
302
I
303
304
305
306
307
308
309
I
I
7.345
...
CM12
cm12
OU34
636
ClOH18
637
...
...
...
...
...
...
...
...
...
-50.80
...
...
...
."
I d e a l Gas
Heat o f
Formation
a t 77 F
BtWLb
UD.
16
P
65-26 P
280.38 P
180.21 P
32.72
P
-225.75 P
Heatof
Formotion Btu/lb
at 77 F
Btu/Lb
931.61
1118.99 P
358.69
I d e a l Gas
Gibt6 Free F u s i o n a t
Energy of 77 deg F
...
...
...
...
...
...
..I
...
...
...
...
...
...
...
...
Note Footnote codes follow Table 1C4.12.
1-108
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
1997
Not for Resale
1C2.3
TABLE 1C23 (Continued)
YLnkrs
Coefficient
of
Anilin
Expsnsim
Point
Research Method
D908
Motor Method
at M) F
!=r
+I
* F
F
Clear
3 6 1 TEL
per gal
71.1
0.7
per gal
Flmumbilty Limits Uatsm
K Factor
Volrar Percent i n
Air Mixture
Lover
Upper
1.30 P
1.31 P
1.31 P
1.11 P
1.11 P
10.90 P
No.
Diolefins, C6 to C10
o. 000780
0.000850
0.0010
0.000710
O.oOO580
O.OMH80
O. 000530
o. 000560
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
...
...
...
...
...
...
...
...
37.6
."
...
...
...
...
...
...
43.3
...
...
...
...
...
...
...
."
...
...
...
...
...
...
...
'
,
~
... I
...
...
...
...
...
--`,,-`-`,,`,,`,`,,`---
Not for Resale
0.97 P
0.86 P
0.77 P
...
...
9.23
9.00
7.97
7.03
12.1
12.4
11.8
P
12.0
P
P
11.8
12.0
11.8
12.1
P
6.31 P
j
M2
M3
304
305
306
307
MB
309
1-1o9
1C2.4
TABLE 1C2.4
CyCIDOLEFXNS AND ACETYLENES= SECONDARY PROPERTIES
~~
Search
NlntRr
'armeter
Point
erature
~
~
Ideal
Energy of
Formation
at ?7 F
Btu/Lb
Btu/lb
310 CYCLOPEIITDIE
311 1"ETHYL-CYMQfYTENE
3121-ETHYLCYCLOPEYTEIE
313 3-ETHYLCYCLWENTENE
3141-n-PRaPYCCYCLWENTENE
bH8
C6H10
C7H12
c7H12
C8HlC
269
620
621
622
623
8.251
CbHlO
C7HlZ
ISH14
270
271
272
8.513
...
...
...
...
...
...
...
-20.47
.I.
208.91
U9.13
-88.07
-36.21
-157.61
Gas
kat of
Gibs Free usion at
Ideal tas
Heat of
Formation
at 77 F
697. 42
".
...
...
P
P
P
...
P
7-F
itullb
21 -25
...
...
...
...
Alkylcyclohuencs, C6 to tg
315CYCLOHEXENE
316 1-HETHYLCYCLOHEXEHE
317 1-ETHYLCYCLMIEXENE
...
8.510
-22.00
...
...
563.68
-24.08
1
Cyclic Diolefins, CS to C10
--`,,-`-`,,`,,`,`,,`---
318 CYCLOPEHTADIENE
319 DICYCLOPENTADIENE
-51.67 P
90.00
C5H6
ClOHlZ
315
316
8.240
ClOHl6
ClOHl6
840
BL1
7.951
8.137
86.00
C2H2
401
402
403
404
418
9.178
8.987
8.543
8.103
8.416
-0.67
...
-56.47 P
...
3767.97
1984.14
1158.05
405
412
411
413
414
416
395
396
7.873
8.284
7.419
7.981
7.893
7.966
-29.47
-22.27
-61.87 P
-6.07
28.13
911.38
789.57
8.699
850.72
637.72
Cyclic maturates, ClDH16
320 alpha-PINENE
321 beta-PINENE
1
87.53
...
...
-162.35 P
-219.39 P
1
89.31
122.13
17.25
."
...
-~
1134.29
...
1.63
1219.50
6 8 1 .M
779.47
...
...
Acetylmæs, C2 to C4
322 ACETYLENE
323 IIETHYLACETYLEWE
DIMETHYLACETYLENE
ETHYLACETYLENE
326 VINYUCETYLENE
C3H4
CUI6 324
C4H6325
c4H4
...
3478.69
2080.07
1469.62
1607.52
2526.29
2514.73
55.33
...
...
73.52
1313.04
48.00
Acetylens, C5 to Cl0
327 1-PENTYNE
328 2-PENTYNE
329 3-METRYL-1-BUTYNE
330 1-HEXYHE
3311-HEPTYNE
332 1-OCTYYE
333 1-mrnE
3% 1-OECYNE
CSH8
c5H8
6H8
C6H10
C7H12
an14
C9H16
ClOH18
...
...
60.80
...
...
...
...
870.99
647.42
P
P
1327.31
1203.60
1307.74
1143.58
1014.78 460.45
916.83 321.09
8c3.04
213.53
783.36
127.50
...
...
...
...
...
...
Note: Footnote codes follow Table 1C4.12.
1997
1-110
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
1C2.4
TABLE 1-4
t 6 0 F
I
1
Point
(Continued)
T Research Method
Motor Method
D 357
Clear
L d i I t y Limit! datson
L factor
o l e Percent in
i r Mixture
Yo.
h l TEL
-
P-981
A i k y l c y c l o p m t m s , C5 t o CS
93.3
o. 000680
...
...
57.6
0.000550
93.6
90.3
90.8
...
91.8
97. O
95.7
%.S
...
10.7
10.9
11.0
11.1
11.2
310
31 1
312
313
314
315
316
317
318
319
-
Alkylcyclohex+nts, C6 t o C8
0.MW
83.9
89.2
85.0
O.WoM0
O. 000570
I
...
CyclicUnsaturates,
1.20
1.11 P
0.97 P
4.80
8.38 P
7.35 P
10.6
10.8
10.9
:::
I
...
...
...
...
...
1.70 P
1.00
14.60 P
8.30 P
10.2
9.2
."
...
...
...
".
0.80
0.80 P
6.60 P
10.6
10.6
...
...
...
a5 .P
...
...
2.50
1.70
2.00 P
2.00 P
2.20
39.90 P
41.80 P
32.90 P
...
-
Clon16
...
."
92.7
91.2
C5 t o C10
Cyclic Diolefins,
...
.L.
88.4
...
...
I..
6.70 P
320
321
-
Acetylenes, C2 t o t4
...
...
O. 000870
...
...
1
...I...\...
...
..... 70.2
I ::: I ::: I :::
71.5
...
...
86.4
...
e..
80.00
31.70
16.7
12.3
11.7
322
12.1
11 .5
325
11.8
11.7
12.1
l i .e
321
328
323
324
326
~
Acetylenes, C5 t o C10
0.000870
o.oOO800
O . 000760
o. 000690
O.oM)610
0.oOwM
o.oO058n
...
...
".
...
...
".
...
.
a
...
...
...
."
...
51.5
...
...
...
...
...
...
...
66.1
...
...
".
...
...
~
I
...
-".- -
...
...
...
...
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
...
75.9
1.60
1.60
1.60
1.30
1.10
1.w)
0.86
0.82
P
P
22.30 P
25.30 P
P
P
16.60 P
13.20 P
10.90 P
11-5
11 .S
33 1
9.39 P
8.35 P
12.c
12.1
33:
33
P
P
P
P
P
22.80
--`,,-`-`,,`,,`,`,,`---
Not for Resale
325
33c
332
1-111
~~
~~
STD.API/PETRO T D B CHAPTER L-ENGL L797 M 0 7 3 2 2 9 0 0 5 b b 7 0 2 b 5 5 m
1C2.5
TABLE 1C2.5
BENZENE DERIVA"nW3 SECONDARY PROPERTIES
o.
Foraula
CapoUd
Search
Y h r
olubi Iity
nrœœter
Cal/d3IA%
Ideal Gas
Heat of
Formation
at 77 F
Btu/lb
Flash
Point
Tcclp-
erature
des F
Idcal Cas Meat of
Gibbs Free Fusim s t
Energy of ?
deg
i' F
F o m t i o n Btu/lb
s t 77 F
~lkylknrtnesC6
, a d C7
9.154
8.953
335BENZENE
336TOLUENE
CBHlO
C8H1 O
C8Hl O
C8Hl O
337 ETHYLBENZENE
338 O-XYLENE
339 *XYLENE
340 p-XYLENE
504
505
506
507
8.787
8.987
8.821
8.748
1
59.00
62.33
I
77.00
77.00
529.40
37.25
55.16
77.27
121.16
70.14
494.05
73.01
491.62
69.40
33.20
27.85
m.93
--`,,-`-`,,`,,`,`,,`---
AlkylkorCfwS, C8Hio
46.93
Alkylknrms, C9Hl2
341
342
343
344
345
346
347
348
n-PROPYLBENZENE
ISOPROPYLBENZENE
o-ETHYLTOLUENE
m-ETHYLTOLUENE
p-ETHYLTOLUENE
1,2,3-TRlMElHYLBEWZENE
1,2,4-TRlHETHYLBENZENE
1,3,5-TRIMETHYLBENZENE
113.90
8.831 -49.36
WH12
516
111.92
8.777 -56.87
422.44
47.26
34.09
C10H14
ClOH14
ClOH14
C10H14
ClOH14
C10H14
C10H14
C10H14
C10H14
C10H14
ClOH14
518
8.552
8.440
8.333
8.372
8.616
8.557
8.533
8.499
8.372
8.450
8.680
8.533
8.572
8.943
8.m 2
8.865
8.626
8.587
465.74
36.00
WH12
-
Alkylbenzmcs,
515
492.19
493.26
469.30
452.24
453.56
451 .o6
418.86
512
513
8.631
8.523
8.802
8.728
8.689
8.963
-6.44
-11.45
-33.98
123.98
36.88
27.25
47.84
29.29
C10H14
349 n-BUTYLBENZENE
350 IYJBUTYLBENZENE
351 ~-BUfYLBENZENE
352 tert-BUTYLBENZENE
353 1 -METHYL-Z-n-PROPYLBENZENE
354 1-METHYL-3-n-PROPYLBENZENE
355 1-HETHYL-4-n-PROPYLBENZENE
356 o-CYMENE
357 m- CY HENE
358 p-CYMENE
359 o-DIETHYLBENZENE
360 WDIETHYLBENZENE
3 6 1 p-DIETHYLBENZENE
362 1,2-DZMETHYL-3-ElHYLBEWZENE
363 1,2-DICIETHYL-4-ET~LBENZENE
364 1.3-DICIETHYL-2-ETHYLBEWZENE
365 1,3-DIWETKIL-4-ET~LBENZENE
364 1,3-DIIQT~YL-5-ETHYLBENZENE
367 1.4-Dl~lHYL-2-ETHYLBEYZENf
368 1,2,3,4-TETRAI(ETHYlBENZENE
369 1,~,3,5-TETRAnETHYlBENZEYE
370 1,2,4,5-TETILAnET~LBENZENE
Clon14
ClOHl4
ClOH14
C10H14
ClOHl4
ClOH14
ClOH14
C10H14
ClOH14
ClOHl4
ClOHlC
519
520
521
584
585
586
522
523
S24
525
526
527
580
581
582
583
528
529
530
531
532
8.606
9.217
8.958
8.372
122.00
131.00
125.33
140.00
127.13
125.33
127.13
127.40
122.00
116.33
135.00
132.53
132.80
149.00
136.13
136.13
134.33
127.13
132.53
154.40
146.00
130.00
P
P
P
P
P
P
P
P
P
P
P
-42.09
-69.03
-54.13
-69.28
-63.36
-77.32
-74.12
-84.56
-98.98
-92.89
-50.39
-67.27
-70.47
-82.16
-102.79
-84.02
-98.66
-113.39
-103.08
-105.86
-129.86
-150.87
444.60
F
F
F
465.19
480.31
451.64
433.07
442.68
435.63
40.08
31.55
26.93
47.31
33.91
36.86
32.09
43.93
31 .O0
427.69
4 6 1 -89
53.83
440.75
35.18
33-99
u 3 -64
443
-32 63.76
416.23
I:
408.08
38.66
441.71
411.93
407.44
407.76
424.10
394.31
47.20
41.49
2a.n
4a.74
35.97
34.32
67.33
377.01
Note Footnote codes follow Table 1C4.12.
1997
1-112
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
S T D - A P I / P E T R O T D B C H A P T E R L - E N G L L997 m 0 7 3 2 2 9 0 0 5 b b 7 0 3 5 7 1
1C2.5
TABLE 1C2.5 (Continued)
I
f
Aniline
Io
r
357
cr deg F
i
luæ Percent in
r Mixture
Research Method
O908
Motor Method
t6OF
F
sansbi L t y Limits
.-r
C 1ear
k l k y l k n t m s , c6 Md c7
3.Oo0660
-22.0
D.ODo6ml
-22.0
+2.8
+0.3
K
K
... Y
+1.7
." K
+5.8
...
...
7.10
7.10
I.CO
1.20
Itson
Factor
IO.
-
9.7
a5
10.1
136
537
138
539
540
141
142
143
W
u5
-
klkylbaumes, UIHlO
0.000540
0.000550
o. O00540
0.000540
+0.8
-22.0
...
K
44.0
43.4
K
+1.5
K
42.1
K
K
K
K
O
IO
.
I .o0
6.70
6.00
Y
1-10
7-00
K
1.10
7.00
10.3
10.3
10.6
10.5
4.3 K
4.3 K
40.3 I:
3.88
6.00
10.6
3.88
6.50
5.50 P
5.50 P
5.50 P
5.20 P
10.5
10.4
10.6
10.7
10.4
10.5
10.6
+0.8
...
6.0
6.0
K
-
Alkylbenreoes, WH12
o. ooos4o
o. 000540
o. 000500
0.000540
0.000540
0.000450
0.000490
O. 000540
-22.0
5.0
...
...
...
...
...
-22.0
98.7
99.3
92.1
100.0
97.0
4.0 Y
*0.5 K
92.9
*0.06 K
40.6 K
40.6 K
40:k
94.5
98.0
95.7
40.1
...
*0.6
...
40.2
41.8
K
K
...
40.5 K
41.4
6.0
K
K
...
...
*0.5 K
*1.5 K
...
3.90
3.90
3.90
3.88
D.88
D.88
P
P
P
P
P
5.20 P
7.29
u6
u7
348
-
Alkylbenzenes, C10H14
O. 000540
O. O00530
o. 000540
O. 0005CO
0.000490
O. 000540
O. 000540
0.000550
O. 000540
o. ooos4o
O. O00500
0.000540
0.000540
O. 000560
O. (#)(J550
0.000560
O. OOOS50
0.000540
O.DO0490
0.000450
O. 000500
0.00w0
L
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
-22.0
...
...
...
...
...
...
."
."
.-.
...
...
...
..
.
."
...
...
...
...
...
...
...
40.8
40.3
40.1
...
K
92.2
+O.W K
K
95.7
40.6
...
...
...
...
I . .
K
97.7
%.O
...
97.7
...
97.0
4.2 K
99.3
93.3
95.2
91.9
...
...
95 .9
40.2
Y
K
K
%.O
+0.02 K
+0.2 K
40.4
41.6
+0.7
~43.0
40.3
*l.5
43.0
+1.5
K
0.80
K
0.80
0.80
K
K
K
40.6
K
K
*0:6' K
41.5
41.8
K
K
K
...
...
43.8
... Y
...
...
...
+1.4 K
...
w3.0 K
K
.*3.0
K
K
40.6
K
+1.6
...
...
40.4
K
*0.4
98.8
40.8 K
98.9
99.7 Y
40.6
42.7
40.6
K
41.2
K
K
-6.0
K
40.5
K
*0.9
40.5
K
K
K
...
...
...
...
...
...
...
K
...
...
".
...
0.70
0.80
0.80
0.80
0.80
5.80
6.00
6.90
P
P
P
P
0.80 P
0.70
0.80 P
0.80 P
0.80
0.80 F
0.80 F
0.80 F
0.80 F
0.80 F
0.80
0.80
0.80
0.80
F
F
F
F
5.70
5.10
5.10
5.10
5.20
5.20
5.60
5.10
5.10
P
P
P
P
P
349
10.8
10.7
10.6
10.7
10.8
10.8
10.6
10.8
350
35 1
352
353
354
10.8
P
10.6
P
10.8
10.8
6.10
4.90 P
4.90
4.90
4.90
4-90
4.90
10.8
P
P
P
P
P
P
4.60
4.60 P
4.60 P
10.5
10.7
10.5
10.7
10.8
10.7
10.5
10.6
10.6
355
356
357
3513
359
360
361
362
363
364
365
3%
367
Me
365
37c
-
1-113
--`,,-`-`,,`,,`,`,,`---
Not for Resale
STD.API/PETRO TDB CHAPTER L-ENGL L977 W 0 7 3 2 2 9 0 0 5 b b 7 0 4 428 9
--`,,-`-`,,`,,`,`,,`---
1C2.5
TABLE 1C2.5 (Continued)
D.
Forrula
carpand
search
Ideal Gas I d c a l Gas Heat of
G i b b s Free Fusion a t
Heat of
Formation Energy of 77 deg F
a t '17 F
Formatiar B t u l l b
a t 77 F
Btu/lb
Flash
Point
N-r
Tsp-
erature
deg F
I
~ t b t " ~ ~, 1 2 ~ 1 8
5411,3-DIISWROPYLBENZENE
542 1,4-DIISWROPYLBEUZENE
371
372
373
374
375
376
377
378
379
380
381
382
rrPENTYLBENZENE
n-HEXYLBENZENE
n-HEPTYLBENZENE
n-OCTYLBENZENE
n-NONYLBENZENE
n-DECYLBENZENE
n-UNDECYLBENZENE
n-DCDECYLBENZENE
n-TRIDECYLBENZENE
n-TETRAOECYLBENZENE
n-PENTADECYLBENZENE
n-HEXADECYLBENZENE
~~
Cyclohexytbenzene, C12H16
383 CYCLOHEXYLBEUZENE
C12H18
Cl2H18
543
C11N16
Cl2H18
C13H2O
ClCH22
C15H24
c16H26
ClMt8
c18H30
C19H32
C2OHS
567
UlHM
C22H38
544
568
549
569
570
554
571
574
8.103
8.274
8.538
8.518
8.489
8.489
8.499
8.445
8.411
8.323
8.245
8.132
8.059
...
1
.
149.00
176.00
203.00
-98.05 P
-144.34 P
-183.26 P
-216.45 P
-245.08 P
-33 -270.01 P
P -291.95 P
-53 -31 1.39
P
P
-328.74 P
P
-u4.32 P
P -358.36 P
P -371.12 P
8.010
224
290.93
285
328.73
344.93
100.13
379.13
557
9.154
209.93
601
646
9.295
9.251
9.237
8.958
9.271
9.149
9.246
89.33
100.13
882.96
608.45
102.00
116.60
123.80
114.53
S72
573
588
589
I
44.27
445.45
428
-94 4
8.86
415.05
53.06
56-71
402.98
392.79
60.84
64.36
66.71
70.20
357.27
352.12
347.59
-44.80
72.64
74.71
76.69
n.48
41.03
507.84
789.08
778.17
45.20
441.29
426.37
125.60
430.37 P
790.54
430.74
T78.78
420.19
761.79
765.07
417.06
."
Cl2H16
Alkenylbmzmcs,
CE t o Cl0
cana
384 STYRENE
385 cis-l-PROPENYL BENZENE
386 trans-l-PROPENYL BENZENE
387 2-PROPENYL BENZENE
388 1-WETHYL-2-ETHENYL BENZENE
389 I"ETHYL-3-ETHENYL BENZENE
390 l-CIETHYL-4-ETHEWYL BENZENE
391l-WETHYL-4-(trens1-n-PROPYL)BENZENE
392 1-ETHYL-2-ETHENYL BENZENE
393 1-ETHYL-3-ETHENYL BENZENE
3% 1-ETHYL-4-ETHENYL BENZENE
395 2-PHENYL-I-BUlENE
P h m y l b e n z m s , C12 to C14
3%
BIPHENYL
C9Hl O
C9HlO
C9Hl O
C9H10
CPHlO
C9HlO
ClOHl2
C10H12
ClMH2
ClOHl2
ClOH12
7
604
...
...
...
648
605
606
607
12!i:j;
690
558
655
656
657
659
C14H14
658
...
...
".
...
...
1 C13Hl2
563
9 .S74
398 1-METHYL-3-PHENYLBENZENE
399 l-~THrL-4-PHENYLBENZENE
400 ~-E~HYL-~-PHEYYLBENZENE
401 l-WETHYL-4(4-IIETHYLPHENYL)BENZENE
402 DIPHENYLWETHANE
613
602
603
Cl2HIO
C13H12
C13H12
C13H12
C14H14
397 1-WETHYL-2-PHENYLBENZENE
Diphenylalkmes, C13 t o C14
647
9.408
235.13
...
32.00
...
...
...
P
366.69
346.42
279.07
279.07
301.14
P
P
P
P
P
508.58
188.29 P
352.30 P
352.30 P
349.58 P
325.20 P
...
...
...
.
I
713.16
...
...
...
781.26
.I.
...
...
...
...
...
...
".
."
...
...
...
52.07
...
...
...
...
...
Note Footnote codes follow Table 1C4.12.
1997
1-114
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
~~
S T D . A P I / P E T RTODCBH A P T ELR- E N G L
0732270 05b6705 3b4
L977
m
1 C2.5
TABLE 1C25 (Continued)
efficient
m
a
m
o
n
i Motor
Point
Y h r s
Octane
ASTM
Ani line
r
I
IResearch Method
D908
method
Factor
Percent
i r Mixture
VI21-
hl TEL
x r gal
Clear
1
l d i l t y Limits
I
Lower
in
Upper
-
\lkylbmrmt, ClZHl8
...
1
...
...
I
:::
I
...
...
...
...
...
...
...
...
...
...
...
...
...
".
...
.f.
...
...
...
...
...
...
...
...
...
e
.
.
...
...
11 .o
11.1
i41
11 .o
11.2
11.3
11.5
11.6
11.7
11.9
11.9
12.0
12.1
J71
12.2
12.3
381
P
5.40 P
10.3
383
6.10
6.70 P
6.70 P
6.10
6.70 F
1 1 .o0
6.10
10.0
10.2
384
P
P
P
P
0.90 P
8.55 F
10.4
6.20
F
0.60
0.69
0.69
0.69
0.63
5.80
8.76
8.76
8.76
8.58
F
F
F
0.70 P
4.90 P
0.70 P
4.90 P
0.80 P
5.50 P
0.70 P
0.70 P
5.30 P
i42
\ l k y l b e n z m , C11 t o C22
...
...
...
...
...
...
...
...
...
...
...
".
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
."
...
...
...
...
".
...
...
0.60 P
0.60 P
0.60 P
0.60 P
0.50 P
0.50 P
0.50 P
0.50 P
...
...
0.70 P
...
...
...
...
...
...
...
...
1..
0.70 P
5.10
4.90
4.70
4.60
4.40
P
P
P
P
P
4.30 P
4.20 P
4.10 P
4.00 P
3.90
372
373
374
375
376
377
--`,,-`-`,,`,,`,`,,`---
...
...
...
...
...
378
J79
380
J82
-
Cyclohcxylkzene, ClZH16
...
."
...
,
".
tlkmylbenrenes, C8 t o C10
O .O00570
O. O00570
0.000570
D. 000570
0.000520
o 000460
0.000520
-
0.000510
0.000510
O. 000560
O. O00560
0.000560
...
...
...
."
...
...
...
...
...
...
.I.
+0.2 K
91.7
92.1
+0.1 K
...
."
...
...
...
...
...
1 ;; i
...
...
+O.l
...
91.4
100.0
...
".
...
".
.f.
".
...
m..
K
,+3.0 K
+2.5
+0.5
K
1.10
K
Y
+0.4 K
+0.4
+2.1
+1.8
K
L
1.00 P
1.00 P
+0.5
...
K
...
...
...
...
...
...
...
...
...
...
...
...
."
...
...
0.70
1.00 P
0.70
1.90
0.85
0.85
0.85
0.85
...
...
...
10.2
10.1
10.1
10.1
10.0
10.3
10.5
10.5
10.5
385
386
387
388
389
390
391
392
393
394
395
-
Phenylbenzenes, C12 to C14
:::
...
...
...
...
:::
...
...
...
...
...
...
."
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
:::
."
".
P
P
P
P
9.5
9.7
9.8
9.0
9.6
396
397
398
399
400
0.63 P
8.67 F
9.0
401
-
0.70 P
5.20 I
9.8
402
Diphenylalkanes, C13 t o C14
...
...
...
1-115
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
1C2.5
TABLE 1C2.5 (Continued)
Formla
F lash
Point
Search
Yuber
--`,,-`-`,,`,,`,`,,`---
T"
erature
* F
l d e e l Gas l d e a l tas Heat of
G i b b s Free fusion at
Heat of
Formation Energy of 77 dcg F
et 77 F
Formation Btu/Lb
at T7 F
Etu/lb
Btu/lb
Diphenyla~kMes, C13 to C14
c03
c04
405
406
407
408
409
410
411
412
413
414
415
416
417
418
419
,l-DIPN€NYLETWANE
,2-DIPHENYLETWNE
,l-DIPRENYLPROPAYE
,2-DlPHENYLPROPANE
,1-DIPHENYLBUTANE
1,,1-DIPHENYLPENTANE
1 ,l-DlPHENYLHEXANE
1 ,1-DIPHENYLHEPTANE
1 ,l-DIPHENYLOCTANE
1,1-DIPHENYLNfAANE
1 ,l-DIPHENYLD€CANE
1 ,1-OIPHENYLUNDECANE
1 ,l-DIPHENYLDOOECANE
1 ,1-DIPHENYLTRIDECANE
1 ,1-DIPHENYLTETRADEUNE
1 ,1-DIPHENYLPENTADECANE
1 ,l-DIPHENYLHEX&DECANE
Cl4Hl4
C14H14
C15H16
C15W16
Cl6ml8
c1wo
C18HU
C20H26
C2lH28
WH30
mm2
c24H34
CtsH36
mH38
C27H40
C28H42
562
564
666
467
668
669
670
671
672
673
674
680
675
676
677
678
679
9.222
8.948
...
...
...
...
264.o0
264.o0
...
...
...
...
...
...
...
...
I
.
.
.I.
...
...
...
...
.
.
I
C19H24
...
...
...
...
...
...
...
...
...
...
...
... I
273.62
337.31
254.30 P
...
...
...
...
...
...
...
...
...
...
...
...
...
Diphenylalkmes, C14H12
420 cis-1,2-DIPHENYLETHEWE
421 trans-l,2-DIPHENYLETHENE
C14H12
C14H12
735
736
9.398
9.114
249.53 P
292.73 P
563.15
603-93
~~
... I
636.88
41.51
700.57
72.05
I 1
I
."
... I
...
...
...
...
...
.I.
...
...
I
.
1
r::1
...
...
".
. I .
.f.
...
...
...
..I
...
...
...
...
...
...
...
66.38
Phmylalkynes, C8 and Cl4
422 PHENYLACETYLENE
423 DIPHEHYLACETYLEWE
C8H6
C14H10
691
424
9.193
8.899
87.80
269.33 P
...
1377.73
1037.51 P
1523.38
1229.68
51.67
516.34 P
516.34 P
516.34 P
789.64
789.64
791.50
32.09
44.97
62.96
~
Diphenylbmzems, =Hl4
424 1.2-DIPMNYLBENZENE
4251,3-DIPHENYLBENZENE
4261,4-DIPHENYLBENZENE
C18H14
ClBH14
C18H14
M1
560
559
9.017
9.359
8.421
325.13
375.53
404.33
Note: Footnote codes follow Table 1C4.12.
1997
1-116
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
L-ENGL L777 E 0 7 3 2 2 7 0 U 5 b b 7 U 7 L37
S T D - A P I / P E T R OT D BC H A P T E R
1C2.5
TABLE 1C2.5 (Continued)
ocfficient
L&ilty
t 6 0 F
Motor Method
Research Method
D908
er deg F
C L est
k
t TEL
1"
Limits Yatson
Yo.
K Factor
01Percent i n
i r Mixture
Louer
P r na1
Diphcrylslkamr, C13 t o C14
...
...
...
...
...
...
-..
".
...
."
...
...
...
...
...
...
."
...
".
...
...
...
...
...
...
...
."
...
...
...
...
...
...
...
...
...
...
...
...
...
...
I
.
...
."
...
...
...
...
...
...
Diphmylelkms,
...
...
--`,,-`-`,,`,,`,`,,`---
...
.....
".
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
0.34 P
0.34 P
...
...
".
...
0.70 P
0.70 P
...
...
...
...
1.20 P
0.70 P
11-90 P
...
...
...
...
...
0.50 P
5.30 P
5.30 P
5.30 P
...
...
...
...
...
...
...
...
L
0.60 P
0.60 P
0.58
...
...
...
...
P
P
P
P
12.41 P
14.27 P
16.77 P
0.34 P
0.34 P
0.34 P
24.69 P
24.40 P
24.13 P
23.65 P
0.58 P
0.54 P
0.50 P
0.47
0.44
0.42
0.40
0.38
...
P
"
Phertylalkynes,
o.aoacBo
...
I
CE
and
...
...
C14
I
1
...
...
5.20 P
5.20 P
8.60 P
8.60 P
8.8s P
9.31 P
10.03 P
11.03 P
P
C14H12
".
...
...
...
...
."
."
...
...
...
...
...
...
...
...
...
...
...
...
5.30 P
5.30 P
5.30 P
Diphenylbenzenes, CEH14
...
...
...
...
...
...
.-.
.-.
...
0.50 P
10.2
405
406
10.3
407
10.5
Lo8
10.6
10.8
10.9
11.1
11.3
409
410
411
412
413
414
415
416
417
418
419
1
11.4
11.5
11.6
11.7
11.7
9.8
9.8
420
421
422
423
;1
9.7
9.6
424
425
426
1-117
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
...
0.50 P
404
10.1
"r
I
"
...
...
...
403
...
...
23.88 P
9.9
10.1
Not for Resale
STD-API/PETRO TDB CHAPTER L-ENGL
L777 S 0 7 3 2 2 7 0 0 5 b b 7 0 8 O73
1C2.6
--`,,-`-`,,`,,`,`,,`---
TABLE l a 6
CONDENSEDRINGARO~TICSANDDERIvATnTEs:SECOND~YPROPERTIEs
>. coapovd
Fomla
EMrCh
Y&r
olrrbility
armeter
bl/d3)%
Flash
Point
Tap-
erature
QgF
UkylMphthalaws, Cl0 to
C20
h27 NAPHTHALENE
c 2 8 1"ETHYLNAPHTHALENE
h29 2-IIETHYLNAPHTHALENE
630 1-ETHYLNAPHTHALENE
h31 2-ETHYLNAPHTHALEYE
C32 1,2-DIIIETHYLNAUPHTHLENE
c33 1,4-DIIIETHYLLUPIflHALENE
553 2,6-DIHETHYLNAPHTHALEWE
554 2,7-DIKETHYLNAPHTHALENE
434 1-n-PROPYLNAPHTHALENE
435 2-n-PROPILNAPHTHALENE
436 1-n-BUTYLNAPHTHALENE
437 2-n-BUTYLNAPHTHALENE
438 1-n-PEWTYLNAPHTHALENE
c39 1-n-HEXYLNAPHTHALENE
440 2-n-HEXYLNAPHTHALENE
U 1 1-n-HEPTYLNAPHTHALENE
442 1-n-OCTYLNAPHTHALENE
443 1-n-YOWYLNAPHTHALENE
444 2-n-WOWYLNAPHTHALENE
445 1-n-DECILLUPHTHALENE
ClOH8
CllHlO
C
H
lO
ll
ClZH12
Cl2Hl2
c12n12
Cl2H12
C12H12
C12H12
Clu114
C13H14
C14H16
C14H16
C15H18
C16H2O
c16H20
ClM22
C 18124
C19H26
C19H26
CtOH28
701
m2
m3
?W
755
756
757
m
709
758
765
759
766
760
761
767
769
762
711
768
712
9.505
9.833
9.642
9.701
9.501
...
...
8.821
8.943
9.330
...
9.334
...
...
9.149
...
...
...
8.508
1
.
.
8.406
176.00
179.60
206.60
a1
219.20
.o0
...
226:;
P
227.93 P
236.93 P
...
262.13 P
...
3Q5:ii P
...
...
...
...
366.73 P
348.53 P
353.46
351.O2
266.67
263.90
202.07
168.45
P
l.08
230.61
188.58
-148.77
123.77
119.87
63.59
29.16
59.39
-153.77
-26.41
-80.27
-24.96
-109.23
PI
P
P
P
P
P
P
P
P
P
P
P
P
P
751.62
658.80
653.97
620.57
618.06
...
59O:ii
590.57
587.82
...
560.39
...
523:i;
...
...
...
478.72
.f.
467.02
63.75
21 .O3
36.33
...
...
...
...
..I
...
...
."
I..
...
...
."
...
...
...
...
...
..I
-
Tetrahydrenaphthalenes, C10 t o C20
1,2,3,4-TETRAHYDRONAPHTHALENE
447 l"ETHYL-C1,2,3,4-TETRAHYDROIIAPHTHALENEI
c48 l-ETHYL-t1,2,3,4-1ETRAHYDRCWAPHTHALENEI
449 2,2-DIWETHYL-t1,2,3,4-TETRAHYDRCWAPHTHALENEI
450 2,6-DIMETHYL-Cl,2,3,4-TETRAHYDROIAPHTIULENEI
451 6,7-DlltETHYL-C1,2,3,4-TETRAHYDRONAPHTHALENEI
452 l-n-PRWYL-[1,2,3,4-TETRAHYDRONAPHTHALENEI
453 6-n-PROPYL-tl.2.3.4-TETRAHYDRWAPHTHALENEI
4% l-n-BUTIL-Cl.2.3.4-TnRARYDRWPHTMLENE]
455 6-n-BUTYL- [1,2.3,4-TETRAHYDROLUPHTHALENEI
456 l-hPENTYL-(1,2,3,4-TETRAHYDRONAPHTHALENEI
446
ClOHl2
706
C11H14
m
C12H16
776
Cl2H16
m
C12H16
778
C12H16
779
C13H18
m
C13Hld
781
C14HZO
787
C14H20
788
ClSH22
789
9.452
...
...
...
...
...
...
...
...
...
...
159.53
86.54
543.41
...
...
-102.59 P
...
...
."
...
-48.83P
...
-125.26 P
...
...
...
...
...
...
...
...
-108.25 P
-43.44 P
-186.81 P
...
-196.72 P
...
...
...
...
...
.
I
I
.
40.55
...
...
...
...
...
."
...
...
...
...
Note: Footnote codes follw Table lC4.12.
1-118
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
1997
Not for Resale
S T D - A P I / P E T R O T D B CHAPTER L - E N G L 1 9 7 7 m 0732290 05bb707 TOT m
1C2.6
TABJX 1C2.6 (Contioued)
E
-
~
xff icimt
f
ASTM
Octane
t-bi\ty
UIlEtWrs
Limits
Ani 1 ine
BtSM
no.
Factor
o l a Percent in
i r Mixture
D908
hl TEL
p r gal
Clear
Lour
\lkylnapthelmes, Cl0 t o C20
3.0001w
...
...
."
...
...
...
...
...
...
...
".
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
".
...
...
...
...
...
...
...
...
...
...
...
...
...
...
."
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
-..
...
...
...
...
...
...
...
...
...
...
...
...
...
...
."
...
...
...
*..
...
...
...
...
...
...
...
...
...
....
..
...
...
...
...
...
...
...
...
-..
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
...
0.88
0.80
0.80
0.70
o.m
0.74
0.74
0.m
0.70
0.70
0.67
0.60
0.62
0.57
0.50
0.53
0.49
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
0.46 P
0.40 P
0.44 P
0.40 P
5.90
5.30
5.30
5.20
5.20
8.68
8.68
5.00
5.00
5.10
8.06
5.10
8.05
8.09
5.10
8.56
8.77
9.45
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
P
5.10 P
10.62 P
5.10 P
9.3
9.5
9.7
9.7
9.9
9.8
9.9
...
...
10.0
10.3
10.2
10.2
10.6
10.7
10.8
10.9
11.1
11.1
11.1
11.3
427
428
429
430
431
432
433
553
554
434
435
436
437
438
439
U0
u1
442
443
444
445
-
Tetrahydrmaphthalmes, C10 t o C20
D.000430
-4.0
I
81.9
84.0
96.4
100.0
0.84
5.00
9.8
446
...
...
...
...
0.77 P
7.73 P
10.1
u7
...
...
...
...
0.69 P
7.29 P
10.3
448
...
...
...
...
...
...
...
0.69 P
7.04 P
10.4
449
7.29 P
10.4
450
...
".
...
7.22 P
10.4
451
...
...
...
...
...
...
7-04 P
10.5
452
6.97 P
10.6
453
."
..-
...
...
..-
10.6
454
10.7
c55
...
...
10.8
456
-
."
...
...
...
...
...
...
...
...
...
...
...
.-.
...
...
...
...
1997
1-119
--`,,-`-`,,`,,`,`,,`---
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
...
...
Not for Resale
STD.API/PETRO TDB CHAPTER 1 - E N G L L797 M 0 7 3 2 2 9 0 U 5 b b 7 2 0 72L m
1C2.6
TABLE 1C2.6 (Continued)
Io.
~
ForruLa
Coapoud
~~~
Flash
Solubility
Point
NuPber Parameter
(C€il/cPT3)X T a p erature
deg F
search
Ideal tas
Heat of
Formation
at 77 F
BtWLb
Ideal Gas
Gibbs
k a t of
Fret :usion at
Energy of VdcgF
Formstion Itu/lb
at 77 F
Btu/Lb
~
Tetrshydr~thalenes,C10 to u0
457 6-n-PENTYL- fl,2,3,4-TETRA-
--`,,-`-`,,`,,`,`,,`---
Indmes, c9 to c10
463 INDENE
464 1"ETHYLINDENE
465 2-UETHYLINDENE
...
c16H24
E l m
?a3
...
...
C18H28
m
...
C19H30
785
s
.
.
...
...
c20H32
786
."
...
C15H22
IYDRWHTWNEI
459 1-n-HEPTYL- [1,2,3,4-ETRAWDRGUAPWTIWYEJ
460 1-n-OCTYL- t1,2.3,4-TETRllHYDRONAPHTHALENE1
U1 1-n-NCUYL- [1,2,3,4-TETRAHYDROWAPHTHALENEI
462 1-n-DECYL-[1,2,3,4-TETRAHYDRCUAPHTHALENEI
...
m
raz
nm(KIUPHTHALENE1
158 1-n-HEXYL-t1.2.3.4-TETR-
I
I
8.655
- ..
-204.47 P
425.82
-244.38 P
...
-266.78 P
...
.-2a9.26 P
...
-303.95 P
...
865.91
...
...
...
...
...
...
604.31
37.80
9.926
9.344
9.603
130.73 P
14.73 P
159.53 P
631.41 P
379.77 P
980.80
m.22
...
...
742
743
744
745
746
9.491
119.30
220.83
606.82
...
764
8.929
9.520
10.581
8.675
9.730
9.598
9.422
9.246
803
ClOH10
280.13 P
."
723
Ro
4
:
:
l
Dihydroirdenes, C9 to C10
4M 2,3-DIHYDROINDENE
467 l-HETHYL-2,3-DIHYDROINDENE
468 2-METHYL-2.3-DlHYDROlUDENE
469 4-CtETHYL-2,3-DIHYDROlNDENE
470 5-METHYL-2.3-DIHYDROlNDENE
W H 1O
ClOHlZ
ClOHl2
CIOH12
ClOHlZ
...
...
...
...
...
...
...
...
108.03
17.14
17.14
-3.67
P
P
P
P
...
...
...
...
...
...
...
."
Cwrdensed Ring Arowtics,
C12 to C18
471
472
473
474
475
476
477
478
479
480
ACENAPHTHALENE
ACEMAFMHENE
FLWRENE
ANTHRACENE
PHENAUTHRENE
PYRENE
FLWTHEYE
CHRYSENE
TRIPHEWLENE
BENUUTHRACEWE
482 WHTHACEWE
Cl2H8
C12H10
C13H10
C14H10
C14HlO
C16H10
Cl6HlO
C18Hl2
c18H12
C18H12
Cl8H12
808
738
804
805
807
717
&J6
810
811
813
1
."
...
...
244.13 P
247.73 P
...
249.53
339.53
389.93
362.93 P
...
...
...
...
m .33
432.13
483.41
555. o4
485-33
478.28
614.11
508.10
508.10
547.08
533.90
926.55
725.42
750.34
800.12
na.94
6%. 52
820.94
758.95
...
...
m.78
19.60
59.92
50.71
70.94
39.76
36.94
39.86
49.40
."
...
. f .
Note: Footnote codes follow Table 1C4.12.
1-120
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
1997
Not for Resale
S T D - A P I / P E T R O T D B C H A P T E R L-ENGL L997
0732290 05bb7LL bb8
m
1C2.6
TABLE 1C2.6 (Continued)
-
IC
lamabilty Limits
f
xpansim
t 6 O F
' o l u ~ cPercent i n
D908
Clear
YO.
Factor
l- ResearchMethod
e r deg F
ItSon
,ir Mixture
3ml TEL
per sal
Lcnur
-
TetrahydroMphthalmes, C10 t o CM
...
...
...
...
...
...
...
...
...
...
...
...
...
...
."
...
...
...
...
...
...
...
...
...
...
...
...
... I ...
...
IndencS,
...
."
."
...
10.9
L57
0.50 P
5.10 P
11.0
L58
7.75 P
11.2
459
8.39 P
11.4
CM)
...
9.29 P
11 -5
461
...
10.48 P
11.6
462
1.00 P
0.90 P
7.20 P
6.60 P
6.40 P
9.3
9.7
9.7
463
P
P
P
P
9.6
10.1
10.1
10.0
10.0
466
467
468
469
470
...
...
...
...
...
-
c9 t o c10
o. 000500
o. 000240
0.000370 R
--`,,-`-`,,`,,`,`,,`---
...
...
...
...
I
+0.7
:::
K
I
*O.&
:::
K
*2.3
...
K
1
.
.
+1.4
...
...
K
0.90 P
464
465
-
Dihydroindenes, C9 t o C10
o. ooo4zo
0.000240
0.000530
o. 000490
O .O00530
...
...
...
......
...
89. 8
90.8
...
...
...
...
...
...
...
*0.3
...
...
K
...
...
+0.5
...
...
...
...
K
1.00
0.85
0.85
0.85
0.85
P
P
P
P
P
6.10
8.42
8.42
8.39
8.39
P
-
Condensed Ring Aromatics,
c12 t o C18
".
...
...
...
...
...
...
...
...
...
".
-..
...
...
.-.
...
...
...
...
...
...
...
...
...
...
I
I
...
...
*.*
...
...
...
...
.....
...
...
...
...
...
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
...
...
...
...
...
...
...
...
...
...
...
0.80 P
0.80 P
0.70 P
0.60
0.70 P
0.60 P
0.60 P
0.50 P
...
...
...
...
5.30 P
5.30 P
5.20 P
5.20 P
5.30 P
5.30 P
5.30 P
...
...
...
11.0
...
...
...
471
472
473
474
8.9
476
...
...
cf5
&TI
... 478
... 479
... 480
482
... -
1-121
Not for Resale
1 C3.1-1
C3.3
TABLES lC3.1-1C33
ACIDS, ALCOHOIS AND PHENOLS, AND ALDEXIYDES
r
No.
Conpovd
Critical Constants
Freezing
Forsula
air at
1 atm
erature
dcoF
I
L
Table lC3.l Acids
16.03
TOO FORMIC ACID
TO1 ACETIC ACID
60.05
74.08
88.11
88.11
102.13
102.13
102.13
116.16
702 PROPIONIC ACID
703 n-BUTYRIC
ACID
704 2-HETHYLPRCPIONIC ACID
705 n-PENTANOIC ACID
?D6 2-IIETHYLBUTYRIC ACID
707 3-HETHYLBUTYRIC
ACID
708 n-HEXANOIC ACID
213.01
266 .u
266.11
325-89
310.10
366.44
350.60
367.18
402.26
Table lC3.2 Alcohols and Phenols
709 METHANOL
710 ETHANOL
71 1 n-PROPANOC
712 ISOPROPANOL
713 n-BUTANOL
714 ISOEUTANOL
715 sec-BUTANOL
716 tert-BUTANOL
717 1-PENTANOL
718 2-PENTANOL
719 2-METHYL-1-BUTANOL
720 2-METHYL-2-BUTANOL
721 3-ClETHYL-2-BUTANOL
722 2,2-DlMETHYL-l-PROPANOL
N 4-HETHYL-2-PENTANOL
RG PHENOL
725 O-CRESOL
R6 m-CRESOL
R 7 p-CRESOL
CH40
CSHlM
32.04
46.07
60.10
60.10
74.12
74.12
74.12
74-12
88.15
88.15
88.15
CSH120
88.15
C2HW
UH80
C3H80
t4H100
CCHlOO
C4H100
C4HlOO
C5Hl20
C5H120
CSHlZO
C6H140
c6w
CM80
CM80
C7H80
88.15
88.15
102.18
94.11
108.14
108.14
108.14
I
148.46
172.92
206.96
180.07
243.79
225 -79
211.19
180.36
280.04
246.20
263 -66
215.60
232.70
CSH120
235.58
269.06
359.31
375.81
396.10
395.57
842.68 P 0.0435 P
839.20
0.0479
669.65
0.0504
589.44
0.0530
536.65
0.0531
518.08
0.0527
564.21 P 0.0544 P
564.21 P 0.0527 P
479.79
0.0520
697.73 P
-173.38
-195.16
-126.17 P
-128.74
-162.40
-174.46
78-48 P
-107.66 P
-99.67 P
-477.65
557.33
518.99
16.16
...
129.20
0.0590
0.0581
750.58
0.0584
690.68
641 -51
623.67
606.12
576-24
562.76 P
538.10
562.76 P
538.10
574.36 P
562.76 P
503.29 P
889.10
726.65
661.38
746.96
526.33
505.22
451.51
595.40
549.05
P
I
891.71
1174.39
463.08
465.39
506.53
455.27
553.82
-143.82
573.53 P
530.33 P
0.0586
0.0594
0.0590
0.0581
0.0594
0.0592
0.0594
0.0594
0.0594
0.0594
0.0594
0.05%
P
P
P
P
P
P
P
0.0390
0.0418
0.0462
0.0410
0.1490
0.2110
0.2150
0.2320
0.2150
0.2260
0.2520
0.2480
o. 2280
0.3173
0.4665
0.5745
0.2240
0.2400
0.2540
o .2480
o. 2600
0.2580
0.2520
o. 2600
0.2600
0.2600
0.2700
0.2680
0.2710
0.2m
O. 2760
O. 2430
0.2440
0.2420
o. 2440
0.5640
0.6452
0.6218
0.6677
O. 5935
0.5848
O. 5722
0.6115
O. 5938
0.5625
O .6784
0.4795
0.3510
O. 6036
0.2230
0.2210
0.2390
0.2500
0.2818
0.2907
0.2559
0.2774
0.3198
0.3382
O. 2456
0.5730
O. 4435
O. 4339
0.4480
0.5072
L
Table 1C33 Aldehydes
~~~
729 ACETALDEHYDE
730 n-PROPIOWALDEHYDE
731 n-BUTYWEHYDE
732 ACROLEIN
m trans-CROTOWALDEHYDE
734 ClETHACROLEIN
CH20
C2H40
C3H&
WH80
UH40
C4H&
C4W
30.03
44 .O5
58.08
72.11
56.06
70.09
70.09
-2.38
69.53
118.40
166.64
126.84
216.00
154.40
~
-133.60
-189.40
-153.67
-141.52
-125.86
-105.70
-113.80
~
~
~~~
274.73
379.13
448.25
507.29
451.13
564.53
494.33
T
~ ~~~~
P
P
P
P
~
955.81
804.97
713.60
626.57
725.20
616.42
616.42
P 0.0614 P
P 0.0560
P 0.0563
0.0573
P 0.0563 P
P 0.0571 P
P 0.0583 P
0.2340
0.2250
0.2460
Note Footnote codes follow Table 1C4.12.
1-1 22
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
--`,,-`-`,,`,,`,`,,`---
Not for Resale
1997
S T D . A P I / P E T R OT D BC H A P T E RL - E N G L
m
L997
0732290 0 5 b b 7 L 3 430
m
1C3.1-1 C3.3
TABLES lQ.l-lC33(Continued)
API
Spccific
Gravity
Gravity
a t 60 F
deg MI
60160
H e a t Capacity
Liquid Refractive Vapor
Pressure
Density I n k x of
a t 100 F
a t 60 F theLiquid
psia
lb/gal a t 77 F
a t M F and CWtMt
Pressure
Btullb deg F
Kinematic Viscosity
of the Liquid
Heat of
Vaporit-
centistoke
Yom1
Boiling
Point
Btu/lb
Ideal Cas L i w i d a t a t 100 F
1 atm
a t 210 F
Wet Heat
Liquid
Surface
b u s t i o n a t i oTension
n at
of Liquid a t 77 F
a t 77 F
+/m
Btu/Lb
No.
of Can-
Table 1C3.1 Acids
0.224
8.785
1.36930
B. 324
8.008
7.950
7.851
7.845
7.797
7.738
-
1.40600
1.40510
1.40220
1.41480
1.4908
0.6015
0.1609
0.0388
0.0657
0.0109
0.0247
O. 0227
0.2332
0.2472
0.2816 T
0.4810
0.4735
...
...
0.3145 T
...
...
...
0.0023
0.4816
...
0.4589
1.0556
0.9049
0.8856
1.2841
1.0893
1.7208
1.5630
1.7475
2.4031
Table 10.2 Alcohols and Phenols
...
0.8122
...
1.0488
1.0380
...
45.52
46.48
43.36
47.42
42.29
44.00
41.97
4.M
41 .O0
42.50
40.57
42.34
40.39
...
42.73
...
3.42
4.82
...
1.32652
6.664
1.35941
6.628
6
-7471.36370
1.37520
6.594
1.39710
6.788
1.39380
6.722
1.39490
6.801
6.624 R 1 .B520
1.40800
6.839
1.40440
6.780
1.40860
6.856
1.40240
6.786
1.40750
6.863
1.39150
1.40900
6.771
1.54960
8.744
1 -54420
l. 53960
8.654
1 .S3910
-..
...
...
0.3236
0.3297
0.3309
0.3472
0.3380
0.3443
0.3570
0.3561
O. 3437
4-6249
2.3257
0.8819
1 .a372
0.3183
0.4865
0.8020
1 .ma
0.1221
o .2892
0.1620
0.7242
0.4297
...
0.2306
0.0252 1r
0.0159
O. 0076
0.0064
-
8096
9797
9761
11014
11282 P
1low
11957
0.4819
0.4809
37.1 1
27.04
26.20
26.15
24.54
26.82
27.03
...
...
...
...
...
...
O. 2568
0.2726
0.2651
O. 2671
1 m2
m3
704
705
706
25.04
707
27.50
708
-
c
c
0.7993
0.7950
0.8092
O. 7909
0.8142
0.8063
0.8157
0.7945
O. 8203
0.8132
o. 8223
0.8140
0.8232
!
1976
5832 P
0.5123
0.4854
0.5900
0.5918
0.5644
0.5546
0.5989
o. 5543
O. 5637
1.o995
l. 8500
1 .871 1
2.3348
2.8700
2.5100
3.0789
3.O M S
2.7499
3.3927
2.7186
2.6~98
0.6004
...
0.54%
0.6419
0.5846
0.6476
0.6423
0.6350
.."..
."
297.95
281.75
250.59
242.63
238.65
226.25
218.66
208.17
216.24
193.02
200.46
201 .a
172.90
212.32
184.04
191 -71
192.23
0.7527 T
0.5856
O .S472
0.8838
0.6351
0.8320
O .62B
0.6101
1 .O707
O. 6 9 R
1.1118
1 .O367
1.2204
1 .?a58
4.0858
6.8396
6.9781
0.4872
360.68
...
0.7417
...
3.1237
...
...
473.01
0.3269 T
0.4579
0.6152 T
8563 F
11525
13191
13092
14245
14205
14157
14059
14927
14883
14934
14823
L
I
8
8
6
15117
15398
13x4
14026
14026
I4005
~
22.22
709
22.10
71O
23.40
711
21 .o1
712
24
-37 713
714
22.56
23-01
715
19.81 T 716
717
25.30
718
23.45
719
25 .O5
22-30
720
24.67
721
722
22.63
723
724
725
36.48 726
727
...
...
...
...
Table 1Q.3 Aldehydes
0.2792
0.2941
0.3268
O -3363
O. B63
0.3128
6.268
6.567
6 693
6.732
7.047
7.147
7.034
-
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
...
I
0.5903
0.5458
0.5291
0.5017
0.4902
0.4214
...
I
1I
0.3616
0.4691
0,4534
0
.3621
0.4723
II
1
I
:::
...
I1
...
...
I
0.3702 T
0.3053
I
330.25
242.36
211.70
185.17
219.41
211.40
182.45
I
24.95
1-123
--`,,-`-`,,`,,`,`,,`---
Not for Resale
1C3.4-1 C3.6
TABLES 1C3.4-1C3.6
AMINES, OTHER NITROGEN CONTAINING COMPOUNDS, AND ESTERS
m.
Freezing
Boiling
I
C r i t i cC
a lœ s t a n t s
Point at
erature
Table 1C3.4 Amines
CH51
736 ETHYLAMINE
737 n-PROPYLAMINE
C2H7N
C3HW
738 ISCPROQYLAMINE
am
739
740
741
742
WllN
CLHllY
n-BUTYLAMINE
ISOBUTYLMINE
SS-BUTYLAMINE
tert-WTYWINE
4
t
W
H
ll
C4HllN
-
.o6
31
45.08
-136.23
20.61
61.84
118.13
89.19
171.32
153.91
145.40
111.92
59.11
59.11
73-14
73-14
73-14
73.14
-113.80
-117.40
-139.36
-56.38
-120.28
-156.10
-88.53
314.42
361 .&O
108
81
389.64
65
W
61
Se
55
434 .84
497.75
465.04 P
466.O7
41 1.35
a
O .321 O
o.mm
0.2980
0.2560
0.2940
0.3085
0.2900
0.2800
0.2814
0.2848
0.2798
O. 2759
0.3292
0.3627
0.2815
0.2748
Table 1C3.5 Other Nitrogen Containing Compounds
743 UREA
744ACETONITRILE
745 UORPHOCIYE
746 PYRIDINE
747ANILINE
CH4NZO
C2H3N
ccn9wo
748 INOOLE
CBH7N
C9H7N
749 QUINOLINE
881 IUYWILlDLINE
750 OIBENZOPYRROLE
751 ACRIDINE
CSHSN
C6WN
C9H7N
C12HW
C13H9N
60.06
377.33
41 .O5
87.12
79-10
93.13
117.15
129.16
129.16
167.21
179.22
178.88
262.40
239.47
363.20
687.40
459.68
469.85
670.49
654.80
Table 1C3.6 Esters
I
I
.a6
270
-46.89
26.42
-42.92
21.16 F
127.40
5.18
79.34
472.64
230.16 P
809.33 P
522.23
652.73 P
656.24
798.53
962.33 P
948.20
986.00
1158.53 P
1169.33 P
~~
752 METHYL FORHATE
C2H402
753 METHYL ACETATE
an602
754 ETHYL FORMATE
755 ETHYL ACETATE
aw2
UHELG!
?S6 n-PROPYL FORMATE
757 VINYL ACETATE
758 METHYLn-BUTYRATE
759 n-PROPYLACETATE
760 ISOQROPYL ACETATE
761 n-BUTYLACETATE
762 n-PENTYL ACETATE
UH&2
C4H602
C5H1002
CSHlMZ
C5W1002
C6HlZoZ
c7H1402
60.05
74.08
74.08
88.11
88-11
86.W
102.13
102.13
102.13
116.16
130.19
89-15
134.49
129.76
170.71
177.48
162.50
216.95
214.70
191-30
258.80
298.40
Note: Footnote codes follow Table 1C4.12.
1-124
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
1997
Not for Resale
--`,,-`-`,,`,,`,`,,`---
3
Formula
S T D - A P I I P E T R O T D B CHAPTER 1 - E N G L L997 m 0 7 3 2 2 9 0 O 5 b b 7 L 5 2 0 3 m
1C3.4-1 C3.6
TABLES lC3.41C3.6 (Continued)
k X
Net Heat
Gravity
Canbustion
atim at
Gravity
centistoke
1 atm
Table 1Q.4
i
i í
1.37058
1.39870
1.39450
1.39070
1.37610
O3989
78.3101
32.0621
10.1442
18.3023
3.2447
4.7487
5.8590
11 .m
0.3776
0.3787
0.3837
0.3764
...
0.3727
0.3823
6.4000
0.7044
O. 6548
0.6579
O 6252
O 5932
0.5550
0.6228
0.2566 T
-
...
0.4633
214.73
0.4208
0.6637
0.6357
0.5804
0.5611
189.19
180.61
176.39
162.28
Table lC3.5 Other Nitrogen Containing Compounds
...
.....
10.266
6.565
8.383
8.242
8.545
9.255 T
9.150
."
1.50745
1.58364
1.63000
1.62480
1.62080
...
...
...
r
."
...
...
I
Table 1C3.6 Esters
0.9817
0.9411
0.9284
0.9056
0.91 10
0.9386
0.9034
0.8932
o0"
0.8867
0.8810
12.65
18.85
20.91
24.76
23.82
19.25
25.13
26.93
29.29
28.09
29.11
8.184
7.846
7.741
7.550
7.595
7.826
7.532
7.446
7.337
7.392
7.345
1.34150
1.35890
1.35750
1.37040
1.37500
1.39340
1.
m70
1.38280
1.37500
1.39180
1.4O080
i
0.7800
0.0315
0.0008 1
O. W33
0.0036
18.3104
7.1284
7.9784
3.2609
2.8889
3.%9
1.1979
1.2482
2.1384
O -454.6
0.1806
0.2578
o. 2981
...
0.2275
O. 2753
0.2327
0.2310
0.2300
o.2iG
0.2562
0.2697 T
O. 2825
0.2901 T
0.2683
...
0.4548
...
0.3184 T
...
O. 4797
0.6871
1.5816
0.4557
0.7618
0.8660
2.5229
5.0143 T 1.4052
0.6176
2.2750
2.5155
0.9960
...
0.3595
...
...
...
0.4643
0.4497
O. 4M1
0.4569
0.4542
0.4670
0.4497
0.4544
0.4422
0.4616
0.4733
...
0.398i
0.5278
0.4759
0.3949
O. 4897
...
...
I
...
...
0.3032 T I
...
0.3718
0.3032
T
0.4778
0.3906
0.5291
0.5518
0.5399
1
0.6674
1
0.8222
0.2956 T
...
0.3222
0.3180
...
0.3871
0.4263
-
!
13498
15138
15747
116320
16293
16262
16187
I
...
~
..- I
-.- [
...
I
Amines
1 .U910
1. u m
1. W 1 0
-16.58
08-19
9.23
11.64
6.56
-4.03
-2.57
Tension
of Liquid at 77 F
at n F
dym/un
BWLb
N o ml
Boi 1 ins
1.2313
0.7874
1.0055
0.9886
1.0249
1.1101
1.0975
Liquid No.
Surface
of
316.24
187.79
191 .
T8
204 -29
183.12
157.40
157.70
151.38
137.98
19.41
19.17
17.40
21.11
16.86
...
3891
12467
735
736
737
73a
739
740
741
742
~
743
744
28.66
745
37.16
%.R r46
747
42.38
41.62 T 748
r49
42.53
881
750
751
14953
14977
15126
15090
15262
15313
...
...
...
1
201 -68
176.76
174.03
157.28 10057
157.44
157.67
144.68
143.55
137.85
135.07
127.09
6389
24.24
24.53
8479
23.08
8746
P
9959
9m
11307 P
11248 P
11189 P
12140
12860 P
23.24
23.95
22.w
24.56
2
3
.
8
6
~
21-75
24.75
25.25
T52
753
?34
755
756
757
758
759
760
761
762
1
--`,,-`-`,,`,,`,`,,`---
1-125
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
1C3.7-1C3.8
I
No.
TABLES 1C3.7=1C3.8
IrrHERs AND GASES:
PRIMARY PROPERTIES
I 11
carpand
Foraula
M.Y.
CriticalConstants
biIW
Point at
Acentric
Factor
Freezing
Point in
air at
1 atm
degF
Table 1C3.7 Ethers
~
763
764
765
766
767
865
893
768
769
~~
~~~
DIMETHYL ETHER
METHYL ETHYL ETHER
OIETHYL ETHER
METHYL-tcrt-BUTYL ETHER
METHYL-tert-MYL ETHER
DIIWPROPYLETHER
TERT-BUTYL ETHYL ETHER
TETRAHTDROFURAN
DIBENZOFLRAN
46-07
60.10
r4.12
1.15
102.18
102.18
102.18
72.11
168.20
-12.71
45.23
93 -97
131.36
187.45
1%.%
163.04
150.75
544.48
28 -95
17.03
39.95
159.81
28.01
44 .o1
-318.06
-28.17
-302.57
137.75
-312.61
-109.26 1
-58.27
-222.68
260.51
-171.67 P
-127.34
-163.48
380.39
...
-121 .90
435.11
501.53
-137.20
-163.30
180.50
465.53 P
512.60
1048.37 P
-353.20
-107.93
-308.87
18.95
-337.00
-69.83
-217.84
-149.85
-363.30
-457.85
-456.50
-434.56
-124.26
-173.52
8.17
-118.05
-121.85
-251-27
-415.48
-221 -26
270.50
-257.80
-131 -48
11-75
11.75
-361 -82
-315.40
-99.67
62.24
-169.22
-135.40
97.56
316.40
316.40
-181 .43
10.13
315.68
423.86
61.86
Tt8.87
0.0591
638.18 328.37
0.0589
0.0605
52r.95
497.49
0.0598 P
440.92 P 0.0605
417.72 440.42
440.92 P 0.0599 P
0.0498
752.76
464.13 P
P
0.2744
0.2Do2
0.2670
0.2222
0.2811
0.2630
0.2661
0.2730
0.2640
0.2981
0.2670 0.0605
0 -3387
0.2720
0.2957
0.2590
o. 2254
0.24500.0508
O. 2753
0.0506
547.38
0.0682
1636.05
0.0299
710.41 -188.12
0.0135 S
'1493.91 591.80
0.0540
507.50 -220.41
0.0342
1070.83
0.0360
920.86
11 18-26
750.21 P
P
16.97
33.00
0.2293
0.5097
190.44 -399.93
1240.38
0.0356
1205.28
781.77 362.30
0.0824
0.0552
939.86 370.40
1299.98
0.0463
0.3130
O. 0074
O. 2526
0.2420
0.2910
0.2860
o. 1290
0.0482
0.2990
0.2236
0.2740
O. W70
0.2720
0.2760 0.0280
0.0688
0.0530
-0.28700.0281
0.3080 0.3851
0.4715
0.3020
0.3900
0.3050 ,0.2160
0.0734
0.2830 0.0198
0.2490
0.1315
0 . 1 9 ~ 0.4099
o.trm 0.3823
0.2840
o * o942
0.0013
0.2880 0.0174
O. 0396
0.3000
O. 0377
0.2890 0.0510
0.5829
0.2510
0.1409
0.2740
0.8511
0.2330
l.O074
0.2330
o. 0222
0.2880
0.2119
0.2280
0.2454
0.2690
0.4240
0.2550
0.2860
Table 1C3.8 Gases
772
h
ARGON
m BRMINE
774 CARBON MONOXIDE
775 CARBOW DIOXIDE
776 CARBONYL SULFIDE
777 CHLORINE
778 FLUORINE
779 H E L I W - 3
780 HELIIM-4
781 HYDROGEN
782 HYDRCGEN B R W I D E
783 HYOROCEN CHLORIDE
784 HYDROGEN CYANIDE
785 HYDROGEN FLUORIDE
786 HYDROGEN SULFIDE
787 KRYPTON
788 N E W
789 NITROGEN
790 NITRIC OXIDE
791 NITRUJS OXIDE
792 NITROGEN DIOXIDE
793 NITROGEN TETROXIDE
794 OXYGEN
795 OZONE
796 S U L F U R OIOXIOE
797 SULFUR TRIOXIDE
798 XENON
Un3
Ar
Br2
Co
coz
cos
c12
F2
He
He
H2
HBr
HC L
HCN
HF
HZS
Kr
Ne
N2
no
N20
No2
W204
o2
o3
so2
so3
Xe
60.08
70.91
38.00
3.02
4.00
2.02
80.91
36.46
27.03
20.01
34.08
83.80
20.18
28-01
30.01
44.01
46.01
92.01
32.00
48.00
64.06
80.06
131-29
-292
.5
-306.76
-453.91
-452.07
-422.97
-88.06
-121 .o0
78.26
67.14
-76.63
-244.03
-410.91
-320.45
-241.19
-127.26
69.80
84 -33
-297.33
-168.34
13.96
112.55
-162.62
-346.00
87.91
222.17
291.20
-200.25 P
-453.71
-450.31
194.00
124.70
212.68
-82.84
-379.75
798.00
384.79
0.0331
493.14 -232.51
939.86
0.0310
1050.81
0.0354
1469.62
0.0287
0.0144 S
1469.62
0.0367
731.44
0.0297
807.87
0.0305
1143.51
0.0254
1190.78
0.0144
847.09
...
...
Note: Footnote codes follow Table 1C4.12.
1997
1-126
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
--`,,-`-`,,`,,`,`,,`---
TID AIR
771 M I
STD.API/PETRO T D B CHAPTER L-ENGL L777 m 0 7 3 2 2 7 0 0 5 b b 7 L 7 O86 m
1C3.7-1 C3.8
TABLES 1C3.7-1C3.8 (Continued)
Kinematic Viscosity
API
Livid
Gravity Density
a t 60 F a t 60 F
deg API tb/gal
Specific
Gravity
60/60
8 t u / l b deg
F
Heat of
Vaporiration at
Net Heat
of C m bustion
Livid
surf ace
Boiling
a t 77 F
Btu/Lb
*/an
Ho.
Tension
centistoke
Point
Btu/Lb
Table 1C3.7 Ethers
0.7196
0.7459
0.7311
0.7456
O. 8908
Table 1Q.8
o. 8748
0.6165
...
3.1398
...
3.8172
1.0310
1 .L236
...
...
...
...
1. W 5
0.8474
O. 6943
0.9661
0.8012
...
...
...
...
0.8175
1 A619
1 .4515
l.1421
...
~
1.29840
1.34410
1.3954
1.36430
1.38590
1 .M550
1.37290
1.4W96
1 .&mo
1 -3945
1.9269
1.4151
.f.
...
...
...
...
...
".
...
...
-53.17 1 5 .O61
35.48 7.065
72.29
5.789
14.%
8.055
45.10 6.680
-..
...
...
-
".
...
...
...
...
41 .58 6.816
-34.71 112.188
-34.02
112.102
-7.61
9.522
...
1.32500
1. m o
1 .O0031
1 .o0041
1.37850
1.37860
1.20000
1 .o0002
1 .O0003
I .O0013
1.00056
1.32870
1.25940
1.15740
1 .O0585
I 00039
1 .O0006
1.20530
1.33050
1.19300
1.40"
1.40(##,
26.177
...
1.00102
l. 00026
41.65
6.813
5.75
a. 596
-32.10 1 1.869
...
4.8946
4.1478
5.307
-
7.293 G
5.140
...
-86.43
...
22.3030
44.1257
16.5424
7.9973
2.5837
...
0.%1
0.3580
0.3677
0.3383
...
...
0.2&
0.2141
O. 59ii
0.5557
0.4998
0.4867
O A988
0.4906
0.4028
.*.
O. 2867
0.4031
".O
O. 3961
O. 4367
o. 4635
...
...
...
155.32
0.1886
0.2635
1
198.93
171.86
...
...
...
136.21
129.08
122.58
125.15
0.3098
...
177.99
116.29
12397
13817
14521
15143
15620
15580
15598
13863
14519
I
-30.03 1I l -626
-58.07 116.065
-31.51 111.798
-
1.22100
...
1.35700
1 .C0520
1
...
211.2220
...
6.9342
...
...
250.6650
1 57.8070
...
...
...
4, E .4700
9'09.2240
o .MW
0.1634
0.3216
0.1140
0.1957
1.6461
1.2404
3.4021
0.0860
22.7083
0.1909
0.3129
27.0448
3i94.9320
0.3478
0.2388
...
...
...
...
...
30.7669
20.4803
...
...
87.7647
10.4218
.Mloa - ...
...
1.1027
...
0.1144
...
0.P91
0.4950
0.1243
0.0538
0.2484
0.1994
0.0592
0.2460
0.2483
0 . W
0.2075
0.1905
0.2069
0.2187
0.1935
0.1475
O. 1490
0.0378
...
...
...
...
...
0.1802 T
...
O. 6252
0.6043
0.5063
...
...
0.1990
...
0.2815
...
...
...
...
...
...
...
."
...
0.0917
."
...
O. 1447
...
...
...
...
...
o.Tji4
O. 2424
0.3658
...
...
...
".
...
0.3259
0.16w
... 0.6409
...
...
~~
89.17
588.92
69.29
...
...
80.14
92.06
124.42
133.20
123.75
74.15
3.6
8.95
191 -21
95.14
192.93
428.35
161 -66
236.37
46.59
36.62
...
...
193.85
160.06
356.56
135.22
91.17
124.03
169.12
218.60
4'1-33
..I
m..
...
...
...
0.1166
...
...
0.0855
. . I
85.46
...
...
7998P
...
4344
...
3924
...
...
...
...
51573 P
367
337
9 9 15
3275 P
6534 P
...
...
...
1293 P
801 P
309 P
42 F
...
127B F
...
531 F
...
11 -36
15.10
16.42
19.30
22.59
17.26
19.78
26.53
763
...
no
...
40.96
...
m
764
765
766
767
865
893
760
769
... -
20.21
O .57
7.87
17.32
...
...
...
...
9.20
3.30
17.76
8.40
9.28
...
...
...
...
1.33
771
m
n4
m
776
m
m
779
m
781
782
783
784
785
786
787
788
789
790
26-38
791
792
21-69
33.08
796
797
... 793
794
...
... m
...
798
1-127
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
...
."
...
...
0.1372
...
...
...
...
...
...
...
...
...
...
...
...
...
~~
I
P
Gases
30.26
98.02
...
...
~
Not for Resale
--`,,-`-`,,`,,`,`,,`---
I !
~~
0.6719
1C3.9-1C3.10
TABLES 1C3.9-1C3.10
HAux;ENATEDcoMpouNDsANDI(FMINEs:
1;;
PRIMARY PROPERTIES
n.u.
Table 1Q.9
_."....
Freezing
Point at
Point in
a i r at
1 atm
dtoF
..
Halogenated Compounds
~
7Ç9 CHLOROTRIFLUORaETWE
800 D1CHLORQ)IFLWRCHETHANE
801 TRICHLOROFLUOROIETWE
802 CAREON TETRACHLORIDE
803 UREON TETRAELWRIDE
804 CHLORODIFLUOROIETHANE
805 DICHLDROFLWRWTHANE
806 CHLOROFORH
807 TRIFLUORWETHANE
808 DICHLORCMETHANE
809 METHYL CHLORIDE
810 HETHYL FLUORIDE
811 VINYL CHLORIDE
812 1, I , ~-TRICHLOROETHA~E
813 1.1.2-TRICHLOROETHANE
814 1,1,1-TRIFLUOROETHANE
815 1,l-DICHLDRMTHANE
816 1,2-OICHLDROETHANE
817 1,l-DIFLUOROETHbNE
818 ETHYL CHLORIDE
819 ETHYL FLUORIDE
820 1,2-DICHLOROPROPANE
CCLR
1OC.U
CCl2F2
CC13F
CC 14
CF4
CHCLF2
CHCl2F
CHCl3
CHF3
CH2Cl2
CH3CL
CH3F
c2mc 1
eZH3C13
PH3CL3
C2H3F3
C2H4C12
QtI4Cl2
C2H4F2
eZH5CL
C2H5 F
C3H6C12
120.91
153.82
8B8.00
70.01
84.93
62.50
133.40
133.40
84.04
98.96
98.96
-293.80
-114.54
-252.40
-21.62
-168.00
74.88
137.37
-9.08
169.95
-198.51
-298.46
-41
-49 -251.36
86.47
-211.o0
48.02
102.92
142.12
119.38
-82.34
-115.89
-247.32
-139.25
103.55
-11.60
50.49
-143.86
-223.24
-108.w
34.m
6.98
-244.82
-22.09 F
165.35
236.93
-33.97
-53.32
-168.39 F
135.14
-142.53
182.20
-32.19
-14.44
66-05
64.51
54.09
48-06
-35.86
112.99
205.47
-178.60
-213.52
-225.76
-148.79
83.93
233.26
561 -31
598.29
639.34
O. 0276
0.2780
D.2800
0.2790
0.2720
O 2770
O .26W
0.2710
0.0287
O. O289
388.49
0.0287
541.76
M1.38
0.0255
542.45
-50.17
0.0308
720.99
205.07
O .O305
353.17
751.89
0.0321
793.W
505.85
79-07
704.60 0.0304
0.0349 P
458.33
881.84
289.50
968.07
0.0656
0.0532
111.69
852.13
317.93 P 822.30 P 0.0659 P
0.0337 P
521.33
623.67
623.93 P 649.78 P 0.0337 P
163.58
545.08
O. 0370
O. 0388
735.35
481.73
0.0356
778.87
551.21
235.92
655.55
O.OC34
32-96
0.0697
764.36
0.0547 P
729.26
215.89
569.93 P 614.97 F 0.0413 P
0.2930
0.2600
0.2650
O. 2760
O. 2520
o. 2830
0.2670
Q.2520
0.2530
o .2800
0.2530
0.2520
0.2750
0.2640
0 -2590
0.1717
0.1797
0.1894
0.1926
0.1791
0.2192
0.2048
0.2219
0.2640
o. 19M
0.1531
0.1980
0.1001
0.2183
0.2591
0.2565
0.2339
0.2066
0.2504
o. 1902
o. 2200
0.2564
L
Table IC3.10 Ketones
821 ACETONE
822 METHYL ETHYL KETONE
823 DIETHYL KETONE
824 METHYL-n-PROPYL
KETONE
825 METHYL-n-BUTYL KETONE
826 METHYL ISbBUTYL KETONE
I
1 I _* 1 :
S90[P
~
58.08
72.11
86.13
86.13
100.16
100.16
'133.32
175.35
215.58
216.16
261.86
241 -70
-138.46
455.09
681.83
0.0576
-124.01 P 504.23
-38.15
550.04
-106.35
550.27
-68.44
597l2
-119.20
568.85
474.28
0.05W
O. 2330
601.92
542.45
535.78
0.0593
0.0625
0.0560
P
0.3065
o. 2490
O. 3234
O 2690
0.2380
0.2570
0.2540
0.3448
0.3433
O .3967
O. 3892
1
I
1
Note: Footnote codes folIow Table 1C4.12.
1-128
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
--`,,-`-`,,`,,`,`,,`---
Not for Resale
1997
1C3.9-1 C3.1 O
TABLES 1C3.9-1C3.10 (Continued)
API
Specific
Gravity
Gravity
a t 60 F
60160
deg API
Liquid Refractive
Density Index of
at M, F the Liquid
Lb/gal a t TI F
Vapor
Pressure
a t 100 F
psi8
Heat Capecity
a t 60 F end ConStant
Pressure
E t W l b deg F
KinematicViscosity
o f theLiquid
Ideal Gas
a t 100 F
ar 210 F
0.1593
0.2650
0.4879
0.1063
o. 1938
0.2688
Liquid at
1 atm
cent istoke
Heat of
Wet Heat
CanVaporization at burtion
Woml
o f LieJid
a t TI F
Boiling
Point
Btu/lb
EtV lb
Liquid MD.
Surfaceof
Tmsion
at 77 F
*/cm
Table lQ.9 Halogenated Compounds
3.9794
1.3440
1.5017
1.6022
...
1.2286
1.3921
1.5017
0.8886
1.3374
0.9332
0.6190
0.9199
1.3464
1.4513
0.9915
1.1838
1.2616
0.92’18
0.9037
o.na8
1.1m
12.98
-26.21
-37.27
-43.19
8.165
11.205
12.520
13.358
-16:ii
lo.;&
-29.86 11.606
-37.27 12.520
27.74
7.408
-25.70 11.150
7.780
20.13
97.09
5.161
22.31 7.670
-26.41 11.225
-34.00 12.099
11.21
8.266
-11.97
9.069
-19.34 10.518
22.01
7.685
25-08
62.14
7 . s
6.092
9.703
1.19900
1. m o o
1.37960
1.45730
1.15100
1.25600
1.35400
1.Cc310
1.21500
1.42120
1.33620
l. 17400
1. m o
1.43130
1. U 9 0
1.20600
1A1380
1.Cc210
1.24340
1.36520
1.262’10
1.43680
-9.91
...
13.7400
118.4880
740.6260
0.1503
0.1108
0.1339
0.1279
0.1625
0.1558
o. 1401
0.1297
0.1717
0.1417
0.1891
0.2594
82.6780
0.2012
4.1215
0.8518
252.1260
7.3585
2.7485
124.5260
35.1706
186.2890
1. m 2
0.1621
131.a160
t3.5675
3.7788
...
209.5430
40.1098
6.4028
...
0.2178
0.1798
0.1836
0.2416
0.2257
O. 2873
0.2037
...
O 2283
0.2091
0.2044
...
0.2906
.
1
...
0.1480
...
.I.
0.2186
0.3269
O. 1687
0.2ài
0.1734
0.2060
0.1225
0.1318
O . 2965
0.3350
0.3870
0.1771
0.5120
0.6217
0.1174
0.3561
O. 5429
0.1688
0.2662
O. 3270
0.5660
0.5129
0.5211
0.3540
0.4405
O. 2497
O .2258
0.3621
0.2816
0.3778
...
0.3167
0.2564
O. 2674
...
O. 3 0 3
0.3097
0.3068
...
...
...
...
...
...
...
...
0.2981
o.2om
...
...
64.16
72.28
78.24
83.22
57.29
101.58
104.20
106.25
102.94
143.61
183.62
219.49
155.22
95 -87
110.97
98.51
126.52
139.72
136.79
164.93
179.85
121.73
1294
U9
328
742
2636
163
P
P
P
P
P
0.23
8.65
17.95
26.29
...
799
BDD
801
802
803
8.09
au
P65 P 17.91
805
1369
806
26.68
1121 P
0.06
m7
808
2601
27.22
5751
15.15
809
6593 P
1.90
81O
8104 P 15.84
81 1
3143 P 25.05
81 2
3121 P 33.75
813
2115 P
5.58
814
1824 P 24.81
815
31.51 4801
816
5011 P 10.06
817
8563 18.19
818
819
loa2 P
9.25
820
6
4
% P 28.58
P
-
Table 1C3.10 Ketones
0.7980
0.8105
0.8196
0.8130
0.8162
0.8054
45.81
43.08
41.15
42.55
41.86
44.19
6.653
6.758
6.833
6.778
6.805
6.715
1.35596
1.37640
1.39002
1.38800
1.39870
1.39330
7.5201
3.1669
1.3371
1.2961
0.4204
0.7573
0.2994
0.33&7
0.3525
0.3265
0.3455
0.34-51 T
0.5250
0.4875
0.5059
0.5039
0.5007 T
0.5186
0.6228
0.58%
--`,,-`-`,,`,,`,`,,`---
0.3431
218.79
12281
13523 P
188.13
167.13
14377
166.98
14373
157.21 0.359414980
149.47
14980 P
23.04
23.96
24.71
23.85
25.28
23.50
821
822
823
824
825
826
1-129
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
...
0.2816
0.3124
0.3318
Not for Resale
1C3.11-1C3.12
TAB=
lC3~ll-lC3J2
SULFUR CONTAINING COMPOUNDS AND MISCXZLANEOUS:
PRIMARY PROPERTIES
Boi 1 ing
Point a t
1 atm
,
Freezing
Point in
air at
Critical
Constants
Pressure
mia
Volure
CU f t
erature
Ccaprcss- Factor
ibilitv
Table 1C3.11 Sulfur Containing Cornponds
827 CARBON OISULFIDE
828 METHYL MERCAPTAN
829 2.3-OITHIABUTANE
830 DIMETHYLSULFIDE
831 ETHYL MERCAPTAN
832 2-THIABUTANE
833 1-PROPANETHIOL
834 hBUTANETHIOL
835tert-BUTANETHIOL
836 2-BUTANETHIOL
857 2-METHYL-1-PRWANETHIOL
838 3-THIAPENTANE
839 2-THIAHEXAWE
840 3-THIAHEXANE
841 1-PENTANETHIOL
842 2-TRIAHEPTANE
843 1-HEXANETHIOL
844
1-HEPTANETHIOL
891 THIOPHENE
892 TETRAHYDROTHIOPHENE
Cs2
cH4s
c2n6s2
C2H6S
C2H6S
c3H8S
c3H8S
UHlOS
UHlOS
UHlOS
UH10.S
UHlOS
C5H12S
C5H12S
OH12S
C6H14S
C6H14S
CM165
UH4S
UH8S
76.14
48.11
94.20
62.14
62.14
76-16
76.16
90.19
90.19
90.19
90.19
90.19
104.22
104.21
104.22
118.24
118.24
132.27
84.14
88.17
1
Acentric
e
la
p
-
115.21
42.R
229.55
99.19
95.01
151.97
153.90
209.23
147.60
184.96
191.28
197.78
254.17
245.30
259.95
293.00
306.79
350.50
183.49
250.01
-168.83
-189.35
-120.48
-144.89
-234.20
-158.66
-171.76
-176.24
34.00
-220.23 I
-228.71 I
-155.11
-144.13 I
-178.62
-104.26
-137.20
-112.95
-45.81
-36.78
-141.09
212.00
638.33 P
2834 -33
467. 06
323.06
369.68
473.W
625.19 P
32.00
50.56
613.13
-56.56
-33.70
-76.00
13.19
23.00
50.90
82.40
9.50
-5.80
M. 16
113.00
-76.77
-11.20
65 .U
81-32
-20.00
533.93
0.0337 1145.82
0.2750
0.1107
0.1582
0.0483
0.2680
631.13 P 777.41 P 0.0429 P 0.2680
0.2652
445.80
0.0518 802.07
0.2660
0.1934
438.80
796.27
0.0534
0.2740
0.1878
499.73
0.0534 P 617.87
0.2440
0.2091
671.54 P
0.2318
506.21
P
0.2CO0.0534
566.51573.81
P 0.0545 P
0.2570
0.2714
494.33 P 588.86 P 0.0545 P 0.2830
0.1914
0.2506
537.53 P
P
0.27100.0545
P
546.53 P 588.86 P
P
0.26800.05450.2528
0.2936574.62 543.20
0.2720 0.0565
607.73 P 503.29 P 0.0553 P 0.2530
O .3229
593.33 5.08
0.0569 0.2620
616.73 P 503.29 P 0.0552 P 0.2510
0.3207
643.73 449.62 0.0576 0.2560
P 0.0558 P
0.2450
0.3ta1
661.73 P
P 0.24000.0563
O A226
701.33 P 401.76 P
0.0417
O. 1928
583.16 825.28
0.2590
6T1.84
768.41 P 0.0452 P 0.2450
O. 1979
1048.64
386.24
588.86
...
...
446.72
Table 1C3.12 Miscellaneous
845 YATER
8L6 WLFURIC ACID
847 S
C
H
0
.
I
I HYDROXIDE
848 PROPYLENE
CARBONATE
849 FURFURAL
850 1,2-PROPYLEWE
GLYCOL
851 OIETHYLENE GLYCOL
852 TETRAETHYLENE
GLYCOL
853 ~ T H A N O L A M I N E
854 OIETHANOIAMINE
855DICLYCOUCIINE
856 METHYLOIETHAWOUWINE
857 TRIETHANOLAHINE
858 DlISDPROPALIOUnINE
859 N,N-DIMETHYLFORWIDE
860 N-METHYL-2-PYRROLIDOWE
861 DIMETHYL SULFOXIOE
862 SULFOLANE
863 KLEXOL
18.02
H20
H2S04 98.08
NaOH
C3HbC03
c5Hc02
C3HBO2
CCH1003
40.00
102.09
96.09
76.10
106.12
C8Hl805
194.23
C2H7NO
61.08
U H l l W 2 105.14
UH11ND2 105.14
CSH13NOZ 119.16
C6H15N03 149.19
C6H15NOZ 133.19
73-09
c3Hh10
C5H9NO 99.13
78.14
C2HW
CCH802S 120.17
280.m
338.00
515.10
433.56
472.73 P
635.70
479.75
305.60
399.69
375.53 P
549.14
518.00 S
705.16
1203.53
4616.33
940.73
746.60
667.13
880.61
971.33
761.09
866.21
P
P
P
P
863.33 P
755.33 P
930.11
:
709.61
839.57
852.53 P
1075.73 P
...
928.26
3626.00
784.67
820.93
884.74
667.18
375.65
1033.26
619.32
855.74
562.76
397.85
522.14
0.0497 3198.86
0.2290
0.0289
P 0.0801 P
0.2130
P
P
0.0386 P
0.0420 P
P 0.0503 P
0.2800
0.0471 P
0.0465 P 0.2210
0.0590 P 0.2840
0.0532 P
0.2430
0.0517 P
0.3270
0.2540
P 0.0495 P
0.2020
P 0.0507 P
0.2930
0.0546 P
749.93
P 0.0574641.080.2140
P 0.0501693.290.2470
0.2120
819.48 P 0.0465 P
729.55 P 0.0400 P 0.2130
...
P
P
P
P
P
...
...
0.3449
0.8560 0.1470
...
0.4419 0.2060
0.3678 0.2560
1 .lo65
0.6211 0.2320
0.9174
0.4467
0.9529
0.5598
1.1649
1.2841
1.3891
0.5177
0.3950
0.2806
...
0.3823
Note: Footnote codes follow Table 1C4.12.
--`,,-`-`,,`,,`,`,,`---
1-130
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
1997
Not for Resale
1C3.11-1C3.12
TABLES 10.11-1C3.12 (Continued)
L i q u i d Refractive
Gravity Density
Gravity Index of
a t 60 F a t 60 F theLiquid
deg A P I lb/gal a t 77 F
API
Specific
60/60
Vapor
Pressure
a t 100 F
psia
Kinematic Viscosity
Heat Capacity
a t 60 F and Constant oftheLiqJid
Pressure
centistoke
Btu/lb deg F
Ideal Gas Liquid st
1 etln
a t 100 F
Heat of
Vapor ization at
Net Heat
Surf ace
of c m
Ttnsion
busticil
of Liquid
a t 77 F
BtWlb
Normal
Boi Ling
210 F Pointat
Btu/Lb
I
Table lC3.11 Sulfur Containing Compounds
1.2715
O A757
l. 0685
0.8540
O -8446
O. 8478
O. 8462
0.8460
0.8053
0.832
O. 8393
0.8421
0.8469
.-.
-20.21 10.600
30.08
7.301
8.wp
0.92
7.120
34.19
7.041
36.04
7.068
35.41
7.055
35.73
7.053
35.76
6.714
44.22
6.955
38.13
6.997
37.10
7.020
36.54
35.57
7.061
...
...
O. 8462
35 .R
.-.
...
0.8470
0.8469
l. 0708
l . 0052
7.055
...
7.061
7.061
8.927
8.381
35.56
35.58
O. 65
9.27
1.62409
...
1-52297
1.43228
1 A2-m
1.43735
1.43533
1 44033
1.42004
1.43394
1 .CM00
1 .U015
1. U 5 2 4
1.44350
1. u 3 5
1. w u
1.44720
1.44981
.
1.5257’2
1.S0213
11.O525
43.7524
1.oc29
14.9267
16.1813
5.2641
5 .o853
1.6404
5 -8642
2.7455
2.3932
2.0398
O .S925
...
O. 5267
...
0.1822
O. 0589
2.7152
0.6808
0.1421
0.2455
0.2350
o. 2795
o. 2750
0.2920
0.2913
0.3061
0.3132
0.3099
0.3076
0.3036
0.3132
...
0.3164
...
0.3235
0.3296
0.1993
0.2382
0.2387
0.4451
0 . m
0.4503
0.4487
0.4487
O
0.4506
0.4586
O. 4487
O. 4495
0.4488
0.4543
.&i83
...
0.4562
...
0.2617
...
O .4689
...
O .3&
0.4134
0.5053
0.6235
0.5199
0.5092
0.4534
0.5831
...
...
0.2642
...
...
...
...
0.3264
...
...
...
...
0.3554
...
...
0.3908
O. 6338
...
...
O. 4605
0.4642
O .3364
O .3R9
0.7321
0.8846
0.5097
1.O021
O. 7063
...
0.4191
0.4823
0.3147
...
152.50
219.71
156.73
187.76
185.46
166.64
167.06
153.40
135.94
146.18
148.23
152.54
144.25
...
144.51
...
136.09
130.34
161.66
168.76
6081
10292
9328
12073
12016
13283
13242
14088
14013
14058
14058
14114
14737
14731
14703
15209
15185
15558
12443
13484
31.63
23 .e4
33.07
24.17
228
.2
24.25
24.15
25.33
20.17
24.07
23.50
24 .M
25.83
...
25.98
I
.
.
27.01
27.25
31.44
35 .O8
827
828
a29
830
831
832
833
834
835
8%
837
838
839
840
841
042
843
844
89I
892
-
Table lC3.12 Miscellaneous
e
1 .o000
1.B93
10.00
-54.57
1.2097
l. 1654
1.o607
-14.53 10.085
-10.08
9.716
4 .46 8.677
-5.36
9.352
-6.45
9.434
7.17
8.507
...
1.1218
l. 1316
1.o204
.f.
8.324
15 -335
...
...
...
...
1.om2
1.O431
1.96
4.16
...
8.696
7.954
l. 0347
16.81
5.25
...
...
0.9541
...
...
...
...
...
...
8.627
-
...
...
...
...
0.9507
0.0000
o. oozi
0.4447
0.2019
0.2891
...
...
...
...
0.0968
0.2386
0.00760.3134
T
0.0004 0.2940
0.0000
0.0201
0.3265 T
0.0000
0.0013
O .O005
0.0000
0.3135 T
0.3875
0.5857
0.5426
0.5087
0.2977
0.1682
0.0163
0.0275 0.2671
0.0003
o.cam
...
...
...
...
...
-..
...
...
...
...
...
...
0.5705
...
...
...
...
...
...
...
a. 3397
...
1.6309
1.1465
20.W7
16.0015
23.0195
12.2663
208.3160
18.5357
45 -5386
219.a260
0.3952
0.7534
1.5556
1.4512
6.6860
...
0.0003
...
..-
0.8004
0.7023
2.8072
2.6314
...
2.1931
9.3279
2.1089
4.9058
Il .2851
...
0.4681
0.7008
O .6m7
2.1623
...
973 .a
2.55
...
21 1.76
186.42
307.81
229.80
145.93
350.32
264.18
220.71
227.50
209.58
229.38
232.59
194.47
241.28
191.73
...
...
86P
..-
7024
10096
9309
8731
9614
9593
985 7
10100 P
11040 P
10117
12008 P
10521
121 16
B B U P
0576 P
”.
~
R .82
52.42
...
41 -34
42.92
35.53
48. o9
46.61
48.37
...
40.43
39.45
47.13
.”
34.41
40.33
42.95
85.49
845
u
847
a48
849
850
85 1
852
053
854
855
a56
a5 7
858
859
860
861
1 862
863
... --`,,-`-`,,`,,`,`,,`---
...
...
...
8.839
1.33250
1.41828
1.43300 S
1.41970
1.52345
1 A3160
1 .U600
1.45700
1 A5210
1 A7470
1.46100
1.CM50
1.48350
1.45950
1.42690
1.46900
1.47730
1 A8330
1-131
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
S T D . A P I / P E T R OT D BC H A P T E R
L-ENGL
m
L777
m
0732270 05bb722 q43
1C4.1-1 C4.3
TABLES 1C4.1-1C4.3
ACIDS, ALCOHOLS AND PHENOLS, AND A
L
D
E
H
Y
D
E
S
:
SECONDARY PROPfi=RTLES
Fonula
NO. C#
ldeal Gas Ideal Gas
G i b b s Free
Heat of
F o m t i o nEnergy of
F o r m t ion
a t 77 F
Btu/ 1b
Search
Nurkr
Heat of
F l d i l t y Limits
Fusion at
Volune Pecent
in A i r Mixture
BtWLb
Table 1C4.1 Acids
1251
1252
1253
12%
1260
1258
T257
1261
1262
700 FCRKIC ACID
701 ACETIC ACID
702 PROPlONlC ACID
703n-BUTYRICAC10
704 2-METtiYLPROPlONlC ACID
705 n-PENTANOIC ACID
706 2-HETHYLBLnYRIC ACID
7073-KETHYLBUTIRIC ACID
703 n-HEXANOIC ACID
-3278.72
-2681.85
-2128.19
-1756.68
1766.93
-1454.81
-1472.91
-1544.89
-1251.00
10.49
9.31
9.n
9-86
9.21
10.31
11.o5
9.81
10.59
-
115.45
81.02
61.87
53 -95
24.53
59.69
...
30.82
55.83
Table 1C4.2 Alcohols and Phenols
~~
CH40
UH60
c3H80
c3H&
C4HlW
C4H1 W
GM00
C4HlOO
C5H120
C5H120
CSHI20
C5H120
CSHlM
C5Hl20
C6H140
724 PHENOL
C
6
w
725 O-CRESOL
726 m-CRESOL
727 p-CRESOL
Cm80
C7H&
C7H80
1101
1102
1o
l3
1104
1105
1106
1107
1108
1109
1110
1112
1111
1124
1113
1130
1181
1182
1183
1184
14.46
12.77
Il.%
11.44
11.41
11.20
11.o2
10.56
11.
o4
10.61
1o.al
10.18
10.56
9.42
9.43
12.04
11.18
11.68
11.74
51 -53
55.13
59.00
53 -33
83.93
82.13
74-93
52.00
91.O0
92.93
122.00
105.00
103.00
98.60
105.53
175.73
1T7.53
202.73
202.73
-2696.14
-2192.63
-1825.72
-1950.91
-1592.7s
-1642.63
-1698.89
-1811.99
-1457.02
-1530.49
-1473.35
-1608.04
-1532.53
-1556.20
-1451.24
-440.37
-511.15
-525.98
-498.35
-2177.95
-1566.43
-1143.94
-1241.02
-871.78
-898.46
-983.72
-1030.12
-712.19
-776.95
-715.54
-805.73
-762.60
P
-757.81
-665.66
-149.09
-140.86
-159.78
-125.87
42-86
46. 44
37.85
38.50
S4.32
36.73
34.69
38.93
47.93
41.40 F
...
21 -75
...
48-72
...
52.46
62.98
42.62
50.58
7.30
4.30
36-00
19.00
12.00
12.00
11.20
10.90
9.80
8.00
2.00
2.00
1.40
1 .m
.m
1
2.40
1.20
1.50
1.40
1.20
1.50
1.50
1.o0
1.50
1.40
1.10
1 .lo
10.00
P
9.70 P
9.00
9.00
P
P
S
9.90
9.10
5.50
9.10
7.60
7.60
7.60
P
P
P
P
P
P
Table 1C43 Aldehydes
728 FORCUILDEHYDE
729 ACETALDEHYDE
730 n-PROPIONALOEHYOE
731 n-BUTYRALDEHYOE
?'S?ACROLEIN
trens-CROTONALOEHYDE
754 HETHACROLEIN
m
1001
1002
1003
1005
n.o0
1o34
7.83 P
1OM
1037
2.10 P
60.00
16.10
12.50
31 .O0
15.50
14.60 P
Note: Footnote codes follow Table 1C4.12.
1-132
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
1997
Not for Resale
--`,,-`-`,,`,,`,`,,`---
~~
709 KETHANOL
710 ETHANOL
711 n-PROPAHOL
712 ISOPROPANOL
713n-BUTANOL
714
ISOBUTANOL
715sec-BUTANOL
716 tert-WTAROL
717 1-PENTANOL
718 2-PENTANOL
7192-IIETHYL-1-BUTANOL
720 2-HETHYL-2-BUTANOL
721 3-KETHYL-2-BUTANOL
722 Z,2-DlMEfHYL-l-PROPANOL
N 4-KETHYL-2-PENTANOL
STD.API/PETRO T D B CHAPTER L - E N G L L 9 9 7 W 0 7 3 2 2 9 0 0 5 b b 7 2 3 38T
1C4.4-1 C4.6
TABLES 1C4.4-1C4.6
AMINES, OTHER NITROGEN CONTAINING COMPOUNDS, AND E
S
T
E
S
:
SECONDARY PROPERTIES
~
Search
~~~~~
S o l b i 1 ity
Permeter
lurker
F Lash
Point
T"
(Cal/&3)%
I
i n Air Mixture
erature
BtWlb
l
Table 1C4.4 Amines
735METHYLMIWE
736 ETHYLAMINE
737 n-PROPYLAMINE
738 ISOPROPILAMIWE
739 n-BUTYLAMINE
740 ISOBUTYLMINE
741sec-WTYLAHINE
742tert-BUTYLAMINE
C4HllN
C4H11N
C4Hl1N
C4H11N
1701
1704
1711
1719
1712
1714
1726
1727
443.95
11.29
344.83
303.29
232.16
289.80
270 -99
238.82
169.71
8.63
8.45
8.90
-704.65
87.16 P
5.18
Table 1C4.5 Other Nitrogen Containing Compounds
CH4N2O
C2H3N
C4H9N0
743 UREA
744ACETONITRILE
745 MORPHOLINE
746 PYRIDINE
747 ANILINE
748 INDOLE
749 OUINOLINE
881
ISWUlNOLINE
?i0 DIBENZOPYRROLE
751 ACRIDINE
C12HW
C13HMI
lm
1765
1791
I
2784
1748
2785
2789 10.18
704
11:ii
10.65
10.54
11.79
11.45
10.72
10.74
9.66
i;
42:
100.00
68.00
158.00
1792
962.10
402.10
48.E
5.60 P
4.40
1.80
1.80
1.30
33 07
35.99
1.00 P
75.76
41 -26
0.80 P
106.19 S
93.45
45.46 P
43 .O3
...
-
... 870.87574.71
214.00
224.60
...
... 928.20538.92
-
962 19
335.93 F
...
...
35.30
16.00
10.80
12.40
11-00
8.10
7.79
7.80
5.50
6.30
P
P
P
P
P
P
--`,,-`-`,,`,,`,`,,`---
Table 1C4.6 Esters
752 METHYL
FORMATE
753 METHYL ACETATE
7% ETHYL FORMTE
755 ETHYL ACETATE
756n-PROPYL FORMTE
757 VINYL ACETATE
758 METHYLn-BUTYRATE
759 n-PROPYL ACETATE
760 ISOPROPYL ACETATE
761 n-BUTYL ACETATE
762 n-PENTYLACETATE
-~
~~
C2H402
C3H602
anta
C4H802
C4H802
' C4H602
C5H1002
C5H1002
i C5H1002
CbHl202
, C7H1402
~
1301
1312
1302
1313
1303
1321
1332
1314
1319
1315
1357
10.02
9.46
8.97
9.03
9.08
8.74
8.60
8.48
-2522.91
-2.47
-2390.52
14.00
-4.00 9.32-2253.55
24.53
-2169.01
-1988.96
26.33
-1572.59
17.33
56.93 8.81-1897.23
58.73
-1956.58
35.33 8.38-2027.72
-1797.30
71.33
-1669.36 F 1
73.40
-
53.67
P
53.48
51.25
64.49
26.85
48.47
47.21
37.63
53.37
5.46
P
P
P
P
P
P
P
5.90
3.1046.30
2.70
2.20
2.10 P
2.60
1.60 F
2.00
1.76 5
1.70
1.10
20.00
16.00
13.50
11.40
11.30 P
13.40
7.20 S
7.60
7.50
1-133
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
-2111.97
- 1881 .54
-1759.08
-1600.53
-1432.67
-1138.12
1285.16
-1348.73
-1404.71
-1156.99
-1002.28
Not for Resale
1C4.7-1 C4.8
TABW 1C4.7-lC4.8
"GASES
SECoNDmY PROPERTIES
Forrula
Search
Solubility
Ylrabtr
Parcurter
H e a t of
F u s i o n at
77 deg F
F l æ m m b i l tLyi m i t s
Volrmr P c c e n t
in A i r M i x t u r e
CcIL/d3)W
BtWLb
Table 1C4.7 Ethers
763 DIKETHYL ETHER
764 E T H Y L ETHYL ETHER
765 DIETHYL ETHER
766 M E T H Y L - t e r t - B U I Y L ETHER
767 I 1 E T n Y L - t t r t - A M Y L ETHER
865 DIISOPROPYLETHER
893 TERT-BUTYLETHYLETHER
768 TETRAHYDROFLIRAN
769 DIBENZOFURAN
II
1401
1407
1402
1405
1400
1403
lb28
1479
705
7.39
7.51
7.56
7.36
7.57
7.06
7.23
9.27
8.91
-42.07
-34.87
-49.00
-18.67
12-20
-18.67
-2.47
6.53
233.33 I
-1718.08
-1548.14
-1462.24
-1382.71
-1285.03
-1343.10
-1320.80
-1098.15
213.18
-1052.68
-837.74
-708.21
-573.08
-478.42
-525.12
-512.08
-4fs.14
508.67
46.17
57.18 P
42.10
37.13
...
...
...
52.67
3.30
2.00
1.90
2.00
1.20 P
27.30
10.10
48.00
15-10
9.10 P
21 .W
9.10 P
11.80
6.40 P
1 .&O
1.20 P
2.00
P
58.02 0.81
Table 1C4.8 Gases
R0 A I R
771 W I A
772 A
R
m
773 BROnlNE
WH3
Ar
915
191 1
914
Br2
922
774 U R B O N MONOXIDE
URBW DIOXIDE
776 CARBONYL SULFIDE
777 CHLORINE
m
T78 FLUORINE
779 HELILM-3
780 HELILM-4
F2
Ml
HYDROGEN
782 HYDROGEN B R O l l D E
783 HYDRWENCHLORIDE
784 HYDROGEN CYANIDE
coz
ms
c12
He
He
H2
HBr
nc L
HCN
785 HYDROGEN FLUORIDE
HF
766 HYDROGEN SULFIDE
H2S
Kr
787 KRYPTOW
788 NEON
789 NITROGEN
790 NITRIC OXIDE
7 9 1 NITRWSOXIDE
792 NITROGEN DIOXIDE
793 NITROGENTETROXIDE
794 O m t E N
Ne
N2
NO
N20
H02
N204
D2
795 OZONE
796 SULFUR DIOXIDE
o3
797 SULFUR TRIOXIDE
798 XENW
503
Xe
!a2
908
909
1893
918
917
923
913
902
1906
1904
1771
1905
1922
920
M9
905
912
899
900
906
901
924
910
911
959
6.23
14.28
6.91
11 .S3
3.13
7.12
8.86
9.83
7.43
...
0.60
3.25
10.21
10.75
12.13
7.62
8.80
7.47
4.61
4.44
11 .u)
9.93
16.37
...
4.00
9.16
6.00
15.21
7.78
...
...
.I.
...
...
...
...
...
...
...
...
...
-0.67
...
...
...
...
...
."
...
...
...
...
...
...
...
I..
0.00
83.16
-1696.52
-3844.18
-1016.21
0.00
-414.01
0.00
8.45
-2105.11
-3852-58
-1210.86
0.00
0.00
0.00
0.00
0.00
0.00
...
0.00
-192.83
-1088.49
2149.88
-5873.14
-260.24
0.00
...
0.00
1293.11
801 -49
310.07
42.42
0.00
1277.93
-1992.05
-2124.94
0.00
..I
0.00
-283.43
-1123.74
1984.15
-5918.27
-421.
a3
0.00
...
0.00
1240.38
1017.46
479.67
456.59
0.00
1U1.49
-2014.06
-1991.93
0.00
142:80
12-72
28.38
12.88
84.69
S.87
38.80
5.77
...
5 -37
24 .98
12.77
23.83
133.89
98.43
29.98
8.41
6.99
11-04
32.97
63.88
...
68.46
5.96
17.93 P
49.67
40.45
7.52
...
...
...
...
...
...
...
".
...
...
...
...
75.00
4.00
...
...
...
430
45':s;
... I ...
...
."
...
I
...
...
...
...
...
...
...
...
...
1
I
I
1
...
...
...
...
...
...
...
...
...
Note Footnote codes follow Table 1C4.12.
--`,,-`-`,,`,,`,`,,`---
1-134
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
1997
Not for Resale
S T D - A P I / P E T R O T D B C H A P T E R L-ENGL L 7 7 7 m 0 7 3 2 2 7 0 0 5 6 6 7 2 5 L52
1C4.9-1 C4.1O
TABLES 1C409-1C4010
HALOGENATED COMPOUNDS AND KETONES:
SECONDARY PROPERTIES
Search
Nuber
Soltbility
ParaDeter
Flash
Point
T m -
(Cal/mf3)A~ersture
Ideal Gas
Heat of
Fonnation
at 77 F
Utu/lb
deg F
Ideal Cas
G i b b s Free
Energy of
Fonnation
et 77 F
Btu/lb
Heat of
Flamrrabilty limits
Fusion at
77 deg F Volune Pecent
in Air Mixture
Btu/lb
Lower
Upper
Table 1C4.9 Halogenated Compounds
79p
CHLOROTRIFLUORMETHAWE
800 OICHLOROOIFLUORMETHANE
801 TRICHLDROFLWRMETHANE
802 CARBON TETRACHLORIDE
803 C A R B O N TETRAELUORIDE
804 tHLDRWlFLUM(METHANE
805 DICHLORDFLUORMETHANE
806 CHLOROFORM
807 TRIFLUOROnETHANE
808 DICHLORWETHANE
809 METHYL CHLORIDE
810 METHYL F L U O R I D E
811 VINYL CHLORIDE
812 1,1,1-TRICHLOROETHANE
813 1,1,2-TRItHLOROETHANE
814 1,1,1-TRIFLUOROETHANE
815 1,1-DICHLOROETHANE
816 1,2-DlCHLOROETHANE
817 1,l-OIFLUORMTHANE
818ETHYL CHLORIDE
819 ETHYL FLUORIDE
820 1,2-01CHLOROPROPANE
i t 1 F3
1606
UlZF2
CC13F
U 14
CF4
CHCl F2
CHCl2F
CHC13
CHF3
CH2C 12
CH3Cl
CH3F
CtH3C 1
CZH3Cl3
CZH3C13
CZH3F3
CZH4C12
C2H4C12
C2H4F2
CZH5Cl
CZHSF
C3H6C 12
1601
1602
1501
1616
1604
1 6%
1521
1615
1511
1502
1613
1504
1527
1524
1619
1522
1523
1640
1503
1617
1526
-2746.79
-1609.70
-780.56
-149.64
-267.79
-4340.55
-4558.73
-*9.93
-108.70 F -2394.57
1056.00
-33.10 F -1183.40
-370.59
-252.46
-169.90 F -4280.32 P -4068.84
8-64
-349.08
-483.53
9.96
-497.65
697.94
9.64
-2657.91
-2959.83
9.87
288.58
1 9 5 .71
8.68 -108.67
-245.61
-458.60
2.99 F
8.43
-260.95
89-30 I
-457.63
9.72
-3414.23
-3767.21
7.61
-315.37
-562.22
10.40
8.94
-321
-26
-563.88
9.90
55.13
-2885.ka
-3259.76
8.34
-603.17
-748.11
-58.00
8.67
-1899.17
-2365.24
8-59
-305.1 O
-619.48
55.40
8.99
6.98
7.34
7.61
8.58
6.77
8.49
8.59
9.25
.
s
".
...
...
...
-2913 -68
-1748.05
-903.56
-
...
...
...
...
...
...
...
-
...
...
21.64
7.68
3.48
20.62
".
34.47
24.93
23.28
55.80
3iGJ
7.57
36.65
31.69
3.4.18
38.34
...
29.91
...
...
...
...
...
...
.-.
...
...
..
...
15.90
8.10
...
3.60
8.00
8.60 F
9.20
5.40
6.20
3.70
3.80
...
3.40
...
...
...
...
...
26.90 R
54.70 R
...
35.30 R
19.10
17.20
22.20 P
33.00
10.50
2.78 P
18.40
11.40
16.00
18.00
15.40
17.30 P
14.50
Table 1C4.10 Ketones
821 ACETONE
822 METHYL ETHYL KETONE
823 DIETHYL KETONE
C4H80
824 METHYL-n-PROPYL KETONE
CSH100
82s HETHYL-n-BUTYLKETONE
WIZO
1 O60
1062
826 METHYL ISDBUTYL KETONE
C6H120
1 O54
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
~~
C5HlOO
1051
1052
1053
C3H609.64
9.23
9-00
8.94
8-87
8-52
-1119.98
42.34
-0.67
-1596.69
-1425.01
-876.47
20.93
-670. as
57.96
55.13
-1287.3
-690.31
44.33
-1293.78 53.03
-558.36
n.o0
-1201.12
1.40
7.50
60.53
-1236.21 P -579.47
--`,,-`-`,,`,,`,`,,`---
Not for Resale
8.00
1-135
STD.API/PETRO TDB CHAPTER L-ENGL 1777 m 0 7 3 2 2 7 0 O 5 b b 7 2 b O77 m
1C4.11-1C4.12
TABLES 1C4.11-1C4.l.2
CONTAINING COMPOUNDS AND MISCELLANl3OUS
SECONDARY PROPERTIES
E
YO.
coapwrd
Flash
Formt1a
Point
faaq
in A ï r Mixture
crature
EtWlb
Table 1C4.11 Sulfur Containing Compounds
~
--`,,-`-`,,`,,`,`,,`---
827 URBON DISULFIDE
828 METHYL BERCAPTAU
829 2,3-DITHIABUTANE
830 DIMETHYL SULFfDE
831 ETHYL MERCAPTAN
832 2-THIABUIAYE
833 1-PROPANETHIOL
8u n-BLITANETHlOL
835 tert-BUTANETHIOL
836 2-BUTAWETHlOL
837 2-METHYL-I-PROPAUETHIOL
838 3-THIAPENTANE
839 2-THIAHEXANE
840 3-THIAHEXANE
841 1-PENTANETHIOL
842 2-THIAHEPTAWE
843 1-HEXAWETHIOL
a44 1-HEPTANETHIOL
1938
Cs2
CH45
ttH6s2
SH6S
1801
1828
1820
1802
C2H6S
C3H8S
1815
C3H8S
UHlOS
1808
11541
UWlOS
1804
UHIOS
UHlOS
C4HlOS
1823
1825
1818
1816
1817
1827
1819
1826
1829
C5H12S
QHl2S
C5H 12s
C6H14S
C6H14S
C7H16S
~~~
9.97
9.91
9.83
-22.00
-69.07 P
9.05
8.92
-29.47
-51.67 P
5.00
-4.00
35 .O0
8.80
8.81
8-70
7-72
8.31
8.43
8.56
8.59
...
8.63
...
8.53
8.55
660.06
-204.65
-107.70
-257.67
-320.36
u.33
-336.44
-381 .
o3
-418.54
-521 .O3
-460.49
-461.92
-397.90
-420.79
-430.71
-452.97
-666.15
-469.77
-485.93
...
-9.40
15.80
14.00
60.53 P
ac:...ii
68.00
114.80
~~
~-
~~
377.18
-87.58
70.08
50.52
-33.31
64.75
14.58
54.30
4.80
24.41
28.52
154.76
111.01
100.25
74.42
128.35
100.32
117.73
24.86
52.88
41.w
55.37
34.50
1.30
3.90
1.90
2.20
2.80
1.80
1.80
1.40
1.40
1.40
."
...
49.87
11.83
50.00
21 -80
P
P
P
P
P
P
1.40 P
1.40 P
1.20 P
.I.
I.
I
56.75
...
...
...
R.32
...
...
...
19.70
18.00
1.20 P
...
."
."
m..
.I.
...
...
...
...
.
I
.
.
I
Table 1C4.12 Miscellaneous
891 THIOPHENE
892 TETRAHYDROTHIOPHENE
845 WATER
846 SULFURIC ACID
a47 s c o w HYDROXIDE
848 PROPYLENE CARBONATE
849 FURFURAL
850 1,2-PROPYLEWE GLYCOL
851 DIETHYLENE GLYCOL
852 TETRAETHYLENE GLYCOL
853 WOWOETHANOLAHINE
854 DIETHANOLAHIWE
855 OIGLYCOLAHIRE
856 METHYL DIETHAYOLAHIYE
857 TRIETHANOWINE
858 OIISOPROPAUOLAHINE
859 N,N-DICIETHYLFMUU)41DE
860 W-METHYL-2-PYRROLIDOWE
861 DIRETHYL SULFOXIDE
862 SULFOLANE
863 SELEXOL
1821
1843
1921
H20
H2SW
1901
YeOH
1912
C3H6W3
1185
C5H402
1889
1
C31802 121
UH1003
1202
lXH1805
1204
C2H7NO
lm
UHl lNO2
1724
1728
c4W11WO2
C5Hl3NO2
lm
1M
C6Ht5wa
C6H15W
1730
C3117wO
1876
1071
CZH60S
C4HCS
UH8S
9.83
10.00
23.37
13.88
...
12.83
11-54
14.43
13.58
I l -58
15.56
14-30
12.98
13.75
13.41
13.00
11.71
11.32
C5H9NO
13.07
12.76
...
19.94
64.13
...
".
...
589.85
-164.61
-5770 -82
-3222.74
-2125.73
-2453.07
269.33
140.00
-675.64
209.93
-2381.43
254.
93 -2314.09
384.53
-1954.55
18s.O0
-1456.83
305 .a -1670.33
-1492.57 I
254.93
-1371.00 I
260.00
-1617.97
355 -73
254 .93 -1465.48 I
136.13
1127.55
-898.61
203.00
190.13
-827.89
343.40
-1333.38 I
304.00 S
-
...
646.98
224.88
-5455.24
-2U.61
-2155.29
-1918.24
-459.97
-1717.57
-1656.97
-1239.36
-727.06
-923.10
-764.69
-609.73
."
...
143.23
~
46.95
71O
.6
...
64.27
42.82
66.52
81.11
144.4s
102.81
F
F
F
F
...
78:&F
-862.80
-694,OO
-519.95
95.14
-282.
42
76.78
-248.12
4.W
-869.72
...
...
...
...
...
...
...
...
...
".
...
1 .so
2.40
2.10
2.60
2.00
1.00
3.10
9.00
I..
P
P
P
P
1.80 P
2.60
1.40 P
1.20 P
1.20 P
2.20
2.18
2.60
...
...
18.70
19.30
12.50
17.10
11.00
21.60
13.40
11.70
10.00
9.90
9.80
15.20
12.24
28.50
P
P
P
P
P
P
P
P
...
...
Note: Footnote codes follow Table 1C4.12.
1997
1-136
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
S T D - A P I / P E T R O TDB CHAPTER L-ENGL
T25
m
KEY TO FOOTNOTE CODES
Sublimation point temperature
B = Pseudocritical value
c = Absolute values from weights in vacuum
D = Calculated from the definition
E = At saturation pressure (triple point)
F = At saturation pressure and
60F
G = At boiling point
H = Critical solution temperature instead
of aniline point
I = Interpolated
J = Evaluated at-148 F
K = The + sign and the number following signify the octane numb
of the compound corresponds to of
that
2,2,4-Trimethylpentane
of milliliters of tetraethyl lead
with the indicated number
added.
L = Evaluated at- 5 4 F
M = kTaluated at-193.3 F
N = Too volatile to run as a liquid inCFR engine
P = Predicted
Q = Specific gravity-119.2 F/60 F
R = For the undercooled liquid below the normal freezing point
S = Unknown whether predicted
or experimental
T = Extrapolated
U = Evaluated at-13.27 F
V = Predicted and Extrapolated
Y = Net heatof combustion of the gas
Z = Estimated value
a = Net heatof combustion of the solid
=
--`,,-`-`,,`,,`,`,,`---
A
1-137
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Copyright American Petroleum Institute
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No reproduction or networking permitted without license from IHS
Not for Resale
1C5.1
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Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
1997
Not for Resale
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1-139
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1-140
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Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
1997
Not for Resale
--`,,-`-`,,`,,`,`,,`---
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Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
1-141
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1997
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1-163
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ACETIC ACID
702 PROPIOilC ACID
703 n-BUTYRIC ACID
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8
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705 rrPENTANOlC ACID
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715 sec-BUTANOL
716 tert-BUTANOL
717 1-PENTANOL
718 2-PENTANOL
719 2-METHYL-1-BUTANOL
8
8
8
8
8
8
8
8
720 2-METHYL-2-BUTANOL
721 3-METHYL-2-BUTANOL
722 2,2-DICIETHYL-l-PROPANDL
723 4-METHYL-2-PENTANOL
724 PHENOL
8
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1-164
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
8
8
8
8
8
8
733 trans-CROTONALDEHYDE
73A METHACROLEIW
8
8
8
8
8
a
732 ACROLEIN
1
8
8
8
730 n-PRWIWALDEHYDE
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T
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1997
Not for Resale
1C5.2
TABLE 1CS. 2 (Continued)
1
-
1
Yeat of
4aporiration
Heat Capcity
LiqJid
Viscosity
at60F
Et
Homl
3oitingPoint
Ideal Ces Liquid
a t 1 atm a t 100 F a t 210 F
1 atm
Yet Heat of
Canbustion
of Liquid
a t 77 f
of
GibbsHeat eat of
Surface Flash
usion
Tension Point
Formation Free
o f the Tempa t 77 F
Energy of t 7 7 F
Format ion
Liquid erature
e t 77 F
atTIFat77F
imits
8
8
8
8
8
8
8
8
8
8
8
8
8
8
8
39
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8 1
8
8
8
8
8
8
8
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8
8
8
8
8
8
8
8
8
8
8
8
8
8
8
8
8
8
8
8
8
8
8
8
8
0
8
8
8
8
8
8
8
8
8
8
8
39
8
8
8
8
8
8
8
8
8
8
8
8
8
8
8
8
a
8
8
8
8
8
8
a
a
8
8
8
8
8
8
8
...
8
...
8
8
8
8
8
8
8
8
0
0
8
8
8
8
8
8
8
8
8
8
8
8
8
8
8
I
...
I
8
8
8
8
8
8
8
8
8
702
703
8
...
29
8
8
8
8
8
8
8
8
8
8
8
...
8
.._
...
...
l
8
8 I
8
8
8
8
8
8
8
8
-
8
717 I
8
719
B
R0
8
R1
8
722
723
72L
8
8
8
8
B
8
8
725
726
727
720
B
a
8
8
8
8
8
8
a
a
n
o
8
8
731
a
a
8
I
8
8
8
8
8
I I : I :a
8
8
a
8
...
...
8
23
8
8
8
8
8
...
8
8
8
8
8
8
a
8
8
8
8
8
8
8
8
a
729
8
...
-
:::
8
8
8
8
8
-
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
1-165
Not for Resale
1C5.2
-LE 1cs. z (continued)
IO.
CarpoMd
740 I S O B W Y L M I N E
741 S~C-BUTYLANINE
742 t t r t - W T Y L A U I N E
C r i t i c a lC o n s t a n t s
Liquid
B o i l i n g Freezing
P o i n t in
a t 60 F
Point
Index
at 1 atm a i r at
P r e s s u r e Votune
Tmperature
a t 77 F
1 atm
745 llOCLPHOLI Y E
746 PYRIDINE
747 M I L I N E
8
8
8
8
8
8
--`,,-`-`,,`,,`,`,,`---
881 ISWUINOLINE
irso DIBENZOPYRROLE
751 ACRIDINE
752 METHYL FORMTE
753 METHYLACETATE
8
754
755
756
757
758
ETHYL FORMATE
ETHYL ACETATE
n-PROPYL FORMATE
VINYL ACETATE
METHYL n-BUTYRATE
759
760
761
762
763
n-PROPYL ACETATE
fSOPROPYLACETATE
n-BUTYL ACETATE
n-PENTY L ACETATE
DIMETHYL ETHER
766
765
766
767
METHYL ETHYL ETHER
DIETHYL ETHER
M E T H Y L - t e r t - B U T Y L ETHER
METHYL-tert-AMYL ETHER
8 6 5 DIISOPROPYLETHER
893
768
769
770
TERT-BUTYL ETHYL ETHER
TETRAHYDROFURAN
DIBENZOFURAN
AIR
771 AMMONIA
8
8
8
8
E
8
8
8
E
8
8
8
E
8
E
E
8
E
8
E
8
8
8
8
8
8
8
8
8
8
8
8
E
8
8
8
8
8
E
8
E
a
E
a
B
E
E
8
E
8
a
E
a
a
a
a
a
E
E
a
._.
E
a
a
a
a
a
E
E
E
a
a
a
E
a
13
8
8
8
6
a
E
a
a
a
a
a
8
a
E
a
a
a
E
a
a
E
E
8
8
a
1-166
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
a
a
a
77’4 CARBON MONOXIDE
776 CARBONYL SULFIDE
8
8
8
a
8
8
772 ARGON
773 BROMINE
775 CARBON DIOXIDE
8
8
8
INDOLE
749 W I N O L I N E
8
8
8
8
763 UREA
744 ACETONlTRILE
748
8
E
8
8
8
8
8
E
8
8
8
8
8
8
8
E
8
8
8
8
8
8
E
8
8
8
8
E
E
8
8
8
8
...
...
8
a
E
a
a
a
8
...
...
E
E
8
a
a
8
8
E
a
8
8
8
8
8
:I
8
B
a
,a
8
E
E
a
a
a
a
8
a
E
E
8
E
E
a
E
E
a
a
a
a
a
a
a
a
a
a
a
a
a
...
a
E
...
a
a
8
8
a
a
a
a
a
E
8
8
8
8
E
B
8
8
8
8
8
E
a
a
a
8
8
8
a
a
E
8
8
a
8
8
...
8
a
a
8
8
8
a
13
a
a
a
a
a
a
a
a
E
E
E
E
E
...
Refractive
8
8
8
8
a
a
a
a
8
...
a
a
8
...
...
...
a
E
a
a
E
8
8
E
D eVnaspiot ry
Pressure
a t 100 F
a
a
E
a
...
...
a
...
a
...
...
a
1997
Not for Resale
1C5.2
TABLE 1CS. 2 (Continued)
a t 60 F
at
...
...
8
8
8
8
8
8
8
8
8
...
...
8
...
...
8
8
39
a
a
a
8
a
...
8
i
'
:i
a
8
8
8
8
8
8
a
...
a
..a
...
8
a
a
I
a
a
a
a
ä
a
B
a
8
8
8
8
8
8
8
...
8
a
8
8
a
a
1 :
i :
a
8
a
b
a
a
a
!"S:
8
0
a
a
8
8
8
a
a
...
...
...
...
8
-
a
...
a
a
_..
a
...
a
a
8
a
8
8
a
8
a
a
a
74F
-
752
753
-
a
754
755
756
a
a
757
758
-
a
a
a
a
a
a
a
a
a
a
8
0
762
a
t
...
L
...
...
...
._.
...
759
760
76 1
a
a
763
76L
765
766
...
...
...
n a
751
8
8
a
a
a
747
750
a
a
a
8
746
881
...
a
a
a
a
74L
- -
767
m
...
a
...
a
4a
217
0
0
8
8
B
a
a
8
a
......
865
a93
768
769
770
??l
-
n2
m
774
775
776
-
--`,,-`-`,,`,,`,`,,`---
8
-..
-
...
._.
a
_..
...
...
8
a
8
745
8
8
...
".
...
...
...
8
8
8
8
8
8
8
8
-
742
743
8
...
a
8
8
8
8
8
...
8
a
a
8
8
a
a
...
8
8
740
741
a
8
...
a
...
8
8
...
8
8
8
8
a
a
a
...
8
a
a
...
.-.
a
...
8
B
8
a
a
...
a
..a
8
B
8
8
8
8
-
8
a
1
t 7 7 F
8
8
8
8
a
...
'
...
a
a
8
8
a
a
a
a
a
8
8
8
8
8
I
8
B
...8
... l
8
8
8
...
a
a
8
.-.
a
39
8
39
...
8
8
...
...
a
a
8
8
a
...
8
8
-..
...
a
8
39
8
8
8
F
D.
8
8
8
...
...
...
...
77
eat o f
Gibbs
ormatim Free
t ?7 F
Energy of
f o r m t i or
a t 77 F
Surface Lash
lens ion c i n t
o f the
CnpLiquid
rature
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
1-167
Not for Resale
1C5.2
TABLE 1 ~ 5 . 2 (continued)
Critical Constants
No.
Denrit)
Carpovd
1
.I 1 :i
j 1 *-j
at 100 I
erature
j
777 CHLORINE
778 FLUORINE
779 HELIW-3
780 HELIUI-4
781 HYDROGEN
762 HYDROGEN ERQllDE
783 HYDROtEN CHLORIDE
8
8
8
8
8
8
8
8
8
8
8
8
8
8
8
8
7& HYDROGEN CYANIDE
785 HYDROGEN FLUORIDE
786 HYDROGEN SULFIDE
8
8
8
8
8
8
8
8
8
8
787 KRYPTON
788 NEON
789 NllROGEN
8
8
8
B
8
8
790 NlTRIC OXIDE
791 NITROUS OXIDE
8
8
7 p Z NITROGEN DIOXIDE
793 NITROGEN TETROXIDE
8
8
8
8
8
794 OXYGEN
795 OZONE
796 SULFUR DIOXIDE
8
--`,,-`-`,,`,,`,`,,`---
797 SULFUR TRlOXIDE
798 XENON
799 CHLOROTRlFLUORU4ETHANE
800 DlCHLORQ,IFLUORCHETHANE
801 TRICHLOROFLUORMETHANE
802 CARBON TETRACHLORIDE
803 CARBON TETRAELUORlDE
804 CHLOROOIFLWROMETHANE
B05 DICHLDROFLUOROMETHANE
806 CHLOROFORM
8
8
8
807 TRIFLUORCHETHANE
808 DICHLORCHETHANE
809 METHYL CHLORlDE
810 UETHYL FLKRIDE
811 VINYL CHLORIDE
a
8
I
I
8
x
8
8
8
8
I
..*
8
...
...
8
8
8
8
B
8
8
8
8
8
8 1
x1
I
8
...
".
:::
8
-
a
8
8
8
8
a
a
a
8
8
8
8
...
8
8
8
8
8
8
8
8
8
9
8
8
8
8
8
8
8
8
8
...
8
8
E
8
8
8
a
8
8
8
8
8
B
8
a
8
B
8
8
8
E
8
8
8
8
8
8
B
8
8
."
...
...
...
8
8
...
8
8
8
8
I
~
B
8
a
8
8
'
8
8
8
8
8
8
8
13
8
8
B
8
a
8
8
8
8
8
8
8
8
a
...
...
8
8
8
8
...
8
8
8
8
.
812
813
814
815
816
1,l.l-TRICHLbROETHANE
1,1,2-TRlCHLMIOETHANE
~,~,I-TRIFLUMIOETHANE
1,l-DICHLOROETHANE
1.2-DICHLOROETHANE
8
8
8
I
1-168
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
~~~~~
8
8
8
8
8
8
8
1997
Not for Resale
lC5.2
TABLE 1cS. 2 (continued)
Heat Capacity
Liprid Viscosity
F
at 60 F
Liquid
e t Heat o f Surface Flash
&stion
If Liquid
I t
...
...
...
...
I
...
~
8
E
B
8
...
0
8
8
...
etT7FatTIF
...
...
...
...
.-.
...
...
...
...
...
...
...
-..
-..
-..
8
...
...
8
8
8
8
8
8
-..
...
"_
...
...
...
...
...
...
...
-..
...
...
8
...
8
E
...
a
...
E
8
8
...
B
B
...
...
a
8
B
a
8
8
8
...
a
...
a
...
8
..
..
E
.
.
8
a
8
8
8
8
8
j
8
8
...
l
...
...
a
B
a
0
8
a
a 1
8
a
8
a
a
8
0
8
a
-..
0
8
B
8
8
24
16
u
a
a
...
...
0
8
I
:::
8
8
...
8
...
8
8
8
8
i
8
0
0
8
a
8
I
6
a
783
786
7a5
a
786
......
787
a
19
34
24
a
a
...
8
8
...
1
i; j ::: i
......
...
...
......
fpb
...
...
1 ..a I
aos
806
8
.__
...
...
a
8
1997
1-169
--`,,-`-`,,`,,`,`,,`---
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
782
...
a
a
0
......
...
a
E
...
...
I
.B
8
a
a
8
..
...
a
781
. . . . . . raa
. . . . . . 789
. . . . . . 790
. . . . . . 791
. . . . . . 792
. . . . . . 793
. . . . . . 794
. . . . . . 795
...
8
8
0
8
...
a
0
B
1-
...
1
...
8
0
B
B
8
...
I
~~
8
8
...
...
...
0
8
......
B
8
......
...
...
a
8
...
...
...
Upper
wer
I
~
0
8
Ï iI
l m m b i 1 i t y No.
imits
...
m
... ::: m
...... m
. . . . . . 780
...
...
...
8
...
...
...
...
...
...
...
8
...
...
...
...
8
S
8
8
Heat of
Gibbs
e a t of
ormation Free
Fusion
t 77 F
Energy of a t 77 F
F o r m t i on
a t T7 F
j1 L
...
...
8
...
a
Tension Point
o f the TVLiquid erature
77 F
Ideei tas a t 1 atm a t 100 F a t 210 F
-
y.
Heat of
Vaporizaticm
at N o m l
Boiling Point
Not for Resale
1C5.2
mBLg 1CS. 2 (Continued)
Critical Carstants
collpovd
Boi Ling
Point
at 1 at(
:reez i ng
'oint in
.iquid
D m s i t' Vapor
at 60 1 !cfractive Pressure
at 100 F
ndex
m
I
1t77F
818 ETHYL CHLORIDE
819 ETHYLFLUORIDE
820 1,Z-DICHLORCPROPANE
LIZ1 ACETOUE
822 METHYL n H Y L KETONE
Bu DIETHYL KETONE
824 METHYL-n-PROPYL KETONE
825 METHYL-n-BUTYL E T O U E
826 METHYL ISOBUTYL KETONE
827 CARBON DISULFIDE
828 METHYL MERCAPTAN
9 9 2,3-D1THIABUTANE
830 DIMETHYL UlLFlDE
8 3 1 ETHYL MERCAPTAN
832 2-THIABUTANE
833 1-PROPANETHIOL
8u n-BUTANETHIOL
835 tert-BUTANETHIOL
836 2-BUTANETHIDL
837 2-METHYL-1-PROPANETHIOL
838 3-THIAPEYTANE
839 2-THIAHEXANE
840 3-THIAHEXANE
841 1-PENTANETHIOL
842
843
844
891
092
8
8
0
2
:
8
0
B
0
0
0
0
B
B
0
0
0
a
0
0
0
8
0
8
4042
42
0
0
0
0
B
0
0
0
0
0
0
8
0
0
0
0
045 VATER
846 SULFURIC ACID
847 SWlW HYDROXIDE
840 PROPYLENE CARBDNATE
049 FURFURAL
8
0
8
.-.
8
0
0
0
8
0
0
0
9 42
B
0
0
a
a
0
8
a
8
0
40
42
8
42
B
a
0
0
42
0
0
a
a
8
0
0
B
B
0
0
0
0
B
B
0
0
0
0
0
0
0
a
1
8
8
8
8
0
a
0
0
0
0
8
8
...
0
B
8
B
0
0
0
8
0
...
0
._. ...
B
0
0
B
0
a
0
0
0
0
0
0
0
0
...
0
a
I
88
a
0
0
0
0
8
8
8
8
0
0
0
0
0
...
0
...
0
0
0
8
0
B
0
0
8
...
8
0
0
8
8
0
8
0
0
0
0
-i!j
0
0
1-1 70
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
:I:
8
1i !
8
0
2-THIAHEPTANE
1-HEXANETHIOL
1-HEPTANETHIOL
THIOPHENE
TETRAHYDROTHIOPHENE
850 1.2-PROPYLENE GLYCOL
DIETHYLENE
GLYCOL
851
852 TETRAETHYLENE
GLYCOL
853 LK)IIMTHAUMAMIYE
8% DIETHANOLAl4INE
8
8
...
0
0
--`,,-`-`,,`,,`,`,,`---
30.
8
1997
Not for Resale
~-
~~
S T D . A P I / P E T R O T D B C H A P T E R 1 - E N G L L777 m 0 7 3 2 2 7 UO 5 b b 7 b L
L73
m
1C5.2
(Continued)
T;;urface Flash
Heat of
Gibbs
Heat of
Fusiwl
Formation Free
'msim Point
a t 77 F
Energy of a t 77 F
,f the fmpFormat i o n
.iquid erature
a t 77 F
bt77FatTIF
8
8
8
8
8
8
...
8
8
0
...
0
8
...
8
8
8
8
8
8
B
8
8
8
8
8
8
8
8
8
8
0
...
8
...
...
8
8
0
0
8
8
0
0
8
8
0
...
0
...
8
8
8
9
8
8
0
8
0
I
0
8
8
0
0
0
...
...
..
0
8
0
8
...
0
0
...
...
...
0
...
8
0
0
0
...
...
0
0
0
0
8
8
8
0
...
8
0
8
8
8
8
0
0 1
8
...
0
8
8
8
8
8
8
...
8
8
0
0
8
8
0
8
8
8
8
8
8
0
8
0
0
8
27
8
...
...
8
8
0
0
0
8
017
0
0
0
8
018
819
820
821
8
0
0
0
822
023
024
825
026
.-.
8
8
8
0
8
0
8
0
0
0
8
8
u
8
8
0
0
8
8
8
8
8
0
0
0
8
0
8
...
_..
...
8
8
...
..I
".8
I
8
0
0
0
...
0
I
0
8
0
q
8
..
B
0
8
8
...
...
..a
...
I
8
B
i
0
44
0
0
8
0
0
0
0
-..
8
0
a
8
...
...
a
8
I
..
8
0
8
8
...
0
1
8
8
0
0
a
8
...
0
0
37
8
8
8
44
8
44
8
...
u
44
0
0
0
0
a
a
8
8
0
:::..
8
8
8
0
..
8
8
0
8
il i
8
37
34
...
I
...
...
...
a
8
8
8
...
0
0
0
0
0
...
1997
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
8
8
...
0
...
8
8
8
m
8
0
0
0
8
8
8
8
8
8
8
8
...
0
8
8
8
8
0
8
0
1-
"7-
Ideal Cas Liquid
a t 1 atm a t 100 F a t 210 F
1 atm
lmmabilityllo.
imi t s
a
0
...
...
34
...
8
".
...
...
...
0
20
0
8
8
0
19
a
18
...
0
a
...
827
028
829
0
8
8
830
831
8
8
...
...
8
...
832
033
834
835
a
a
...
._.
836
...
837
...
......
840
8
a
a
.._ 030
...
......
...
a
a
a
._.
......
8
839
841
Wb2
843
844
891
8
892
......
......
Wb5
846
847
......
a
1
85 1
05 2
0
08
8
1-171
Not for Resale
--`,,-`-`,,`,,`,`,,`---
T
A
B
U 1C5.2
1C5.2
TABLE
I
No.
Conpod
les. 2 (Continued)
Boi 1n
ig F r e e z i n g
Point in
Point
a t 1 nt1
l
tritical
Density Liquid
Vapor
a t 60 F R e f r a c t i v e P r e s s u r e
Inder
a t 100 F
a t 7? F
volune
8
8
855 DIGLYCOLAMINE
8% M€THYL DlETtlANOLAMIYE
857 T R I E T K M D W l I Y E
8
858 D I I S O P R O P A m X M I NE
8S9 N,N-DIMETHYLFDR”IDE
8
8
8
I
...
8
8
8
8
8
I : I
“i
8
“i
I
Y-METHIL-2-PYRROLIDME
DIHETHYL SULFOXIDE
SULFOLANE
SELEXOL
9
13
...
...
--`,,-`-`,,`,,`,`,,`---
MO
M1
862
843
1
I
constants
1-172
Copyright American Petroleum Institute
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No reproduction or networking permitted without license from IHS
1997
Not for Resale
~~
S T D - A P I / P E T R O T D B C H A P T E R 1 - E N G L 1 7 7 7 E 0732270 0 5 b b 7 b 3 T b b m
1C5.2
TABLE lC5.2
neat C s p c i t y
a t 60 F
~
'Ideal Gas Liquid
1 atm
...
...
...
8
...
8
...
...
a t 1 atm a t 100 F a t 210
8
...
...
...
8
...
...
...
...
Heat o f
Vaporization
at Normal
Boiling Point
Liquid Viscosity
Netneat of
Cartustion
ofLiquid
at 77 F
F
8
a
8
8
8
8
8
8
8
8
8
8
... 88
8
...
8
-..
8
8
8
...
8
8
8
...
Surface
Tension
of the
Liquid
at77F
Flash
Point
T m erature
atTIF
neat o f
Gibbs
~~~~
Formation
a t TI F
~~~
8
8
8
...
8
...
...
:I
1
Heat o1 : L m b i 1 i t y wo.
Formation Free
Fusion .imits
at 77 F
Energy of a t
i
8
8
8
.
8
8
8
(Continued)
8
8
13
8
...
I ...:
8
.wer
8
8
a
8
8
0
8
8
0
8
8
8
0
8
...
Upper
......
......
855
856
057
858
859
860
861
862
863
--`,,-`-`,,`,,`,`,,`---
1997
Copyright American Petroleum Institute
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1-173
Not for Resale
~~
S T D . A P I / P E T R O T D B C H A P T E R L - E N G L L997 m 0 7 3 2 2 9 0 0 5 b b 7 b 4 7 T 2
1
American Petroleum
Institute,
API Monograph Series, Tour-Ring Condensed Aromatic
Compounds," N
I Publication 709, Washington, D.C (March 1979).
2
American Petroleum
Institute,
MI Monograph Series, "Benzofuran, Dibenzofuran,
and
Bemnaphthofurans," API Publication 721, Washington, D.C (November 1983).
3
American Peroleum Institute, API Monograph Series, 'Carbazole, 9-Methylcarbazole, and
Acridine," API Publication 716, Washington, D.C.(June 1981).
4
Andon, M.L, Counsell, J.F., Lee, DA., Martin, J.F., 'Thermodynamic Properties of Allphatlc
Halogen Compounds,"J. Chem. SOL, Faraday Trans., 69, 1721 (1973).
5
(1973).
Boublik, T., Fried,V., Hola, E,The Vapor R m r e of A u e Substances, Elsevier, New York
6
Chang, SS,Bestul, AB., "Heat Capacity and Thermodynamic Properties of o-Terphenyl Crystal,
Glass,and Liquid," J. Chem. Phys., 56, (1) 503 (1972).
7
Danner, R.P., Dauben, T E , Manualfor Predicting Chemical Process DesignData, 1st edition, 600
pages, American Institute of Engineers, New York, N Y (extant 1987).
Daubert, T.€,Danner, R.P., Sibul, H.M., Stebbins, CC,PhysicalandThermodynamicProperties
8
of Pure Chemicals: Data Compilation, DIPPR-AIChE, Taylor & Francis, Bristol, PA (extant 1994).
10
(1956).
Davies, P., "Ammonia,"edited by F.Din, pp. 33-100, Butternorth Scientifc Publications, London
11
Ferry, J.D., Thomas, S.B., "Some Heat Capacity Data for Durene, Pentamethylbenzene, Stilbene,
and Dibenzyl," J. Phys. Chem., 37,253 (1957).
Finke, H.L., Messerly,
J.F.,
Todd, S.S., 'Thermodynamic Properties of Acrylonitrile, 112
Aminopropane, 2-Aminopropane, and 2-Methyl-2-Aminopropane,"J. Chem. Thermo., 4,359 (1972).
Gas Processors Association, "Standard Tables of Physical Constants of Paraffin Hydrocarbons and
Other Components of Natural Gas,' Publication No. 2145-94, Tulsa, Oklahoma, (1994).
13
14
Giauque, W.F., Kemp, J.D.,"The Entropies of Nitrogen Tetroxide and Nitrogen Dioxide. The
Heat Capacity from 15 K to the Boiling Point. The Heat of Vaporlzation and Vapor Pressure. The Equilibria
N204 2N02 = 2N0+05" J. Chem. Phys., 6,40(1938).
15
Gray, D.€,American Institute of Physics Hnndbook, 3rd ed., McGraw-Hill, New York (1972).
16
Horvath, AL,Physical Propertics of Inorganic Contpounds, Crane Russak, New York (1975).
17
IUPAC, "Atomic Weights of the Elements 1991,"J. Phys. Chem. Ref. Data, 22 (6), 1571 (1993).
18
JANAF Thermochemical Tables, 1974 Supplement, J. Phys. Chem. Ref. Data, 3,(2) 311 (1974).
19
JANAF Thermochemical Tables, 1982 Supplement, J.Phys. Chem. Ref. Data, 11, (3) 695 (1982).
--`,,-`-`,,`,,`,`,,`---
1-174
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
1997
~
STD.API/PETRO
~~~
~
T D B C H A P T E R L-ENGL L797 m 0 7 3 2 2 9 0 0 5 b b 7 b 5 837
20
Keenan, J.H., Keyes, F.G., S t e m Tables, S.1, Wiley, New York (1978).
21
Kirk-Othmer Encyclopedia of Ckmical Technology, 3rd ed., Interscienœ, New York (1978).
24
Matheson Company, Inc,Matheron Gar Data Book,unabridged e&, 4 VOIS, East Rutherford, New
Jersey (1974).
25
Matheson Company, Inc,Matheson Gar Data Book, 6th d.,
Lyndhurst, New Jersey (1980).
26
Messerly, J.F., Todd, S.S., Gutherie, G.B., 'Chemical ThermodynamicProperties of Pentadienes,"
J. Chem. Eng. Data, 15, (2) 227 (1970).
27
Oetting, EL, 'Absolute Entropies of the Methyl AlkylKetones at 298.15 K,"J. Chem. Eng. Data,
10, 122 (1%5).
29 Riddick,
J A , Bunger, W.B., Organic Solvents: Physical Propstes and Methods of Auificatian, 3rd
ed., Wiley Interscience, New York (1970).
30
Rossini, F.O.,Wagman, D.D., Evans, W.H., Levine, S., Jaffe, I., Selected Values of Chemical
T
h
m
o
d
y
n
a
r
n
i
c Prop&,
National Bureau of Standards Circular No. SOO, Washington, D.C. (1952).
31
Seaton, W.H., Freedman, E., Treweek, D.N., "CHETAH - The ASTM Chemical Thermodynamic
and Energy Release Evaluation Program, AST" DS 51,' American society for Tasting and Materials (1974).
32
S e l e c t e d Values of Hydrocarbons and Related Compounds, Thermodynamic Research Center,
American Petroleum Institute Research Project 44, Texas A&M University, College Station, Texas (1980).
33
Selected Values of Propenies of Chemical Compounds, Thermodynamic Research Center, Data
Project, Texas A&M University, College Station, Texas (1980).
34
Selected Values of Properties of Hydrocarbons and Related Compounds, Thermodynamic
Research Center, Thermodynamic Research Center Hydrocarbon Project, Texas A%M University, College
Station, Texas (1984).
35
*rijan, KT., Wise, P.H.,'Dicyclic
C15,' J. Am. Chem. Soc, 73,4766 (1951).
Hyudrocarbons.III.Diphenyl and Dicycloalkanes Through
36
Shebeko, Yu.N., Ivanov, AV., Dm-trieva, TM., 'Methods of Calculation of Lower Concertration
Limits of Combustion of Gases and Vapors in Air: The Soviet Chemical Industry, 15, (3) 311 (1983).
37
Stull, D.R, Westrum, €E, Jr.,Sinke,
Wiley and Sons, New York (1%9).
G.C, Tlte Chemical Tltmodynnmics of Organic
Compounds, John
38
Touloukian, Y.S., Ho,CY., ed., Properties ojNonmetallic Fluid Elements, McGraw-Hill Book Co.,
1-175
1997
Copyright American Petroleum Institute
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No reproduction or networking permitted without license from IHS
Not for Resale
--`,,-`-`,,`,,`,`,,`---
28
Pitzer, K.S., Guttman, L, Westrum, EF., Jr., T h e Heat Capacity, Heats of Fusion and
Vaporization, Vapor Pressure, Entropy, Vibrational Frequencies and Barrier to Internal Rotation of Styrene,'
J. Am. Chem. S o c , 68,2209 (1946).
--`,,-`-`,,`,,`,`,,`---
New York (1981).
39
-
TRC Thermodynamic Tables Non-Hydrocarbons, Thermodynamic ResearchCenter, The Texas
A&M University System, College Station, Texas (1985).
40 TRC Thermodynamic Tables- Hydrocarbons, ThermodynamicResearch Center, The Taras A&M
University System, CollegeStation, Texas (1986).
TRCThermodynamic Tables- Hydrocarbons, Thermodynamic ResearchCenter, The Texas A&M
41
University System, College Station, Texas (1987).
42
TRCThermodynamicTables - Hydrocarbons, Thermodynamic ResearchCenter, The Texas A&M
University System, CollegeStation, Texas (1988).
43
TRCTbemodynamic Tables - Hydrocarbons, ThermodynamicResearch Center, The Texas A&M
University System, CollegeStation, Texas (1989).
-
44 TRCThermodynamic Tables Hydrocarbons, Thermodynamic ResearchCenter, The Tags A&M
University System, College Station, Texas (1990).
-
45
TRC Thermodynamic Tables Hydrocarbons, Thermodynamic Research Center,The Texas A&M
University System, College Station, Texas (1991).
-
46
TRC Thermodynamic Tables Hydrocarbons, Thermodynamic ResearchCenter, The Texas A&M
University System, College Station, Texas (1992).
-
47
TRCThermodynamic Tables Hydrocarbons, Thermodynamic ResearchCenter, The Texas A&M
University System, College Station, Texas (1993).
49
Weast, RC,"Handbook of ChemistryandPhysics,"62nd
d.,The Chemical Rubber Cu.,
Clevland, Ohio (1981).
50
Wilhoit, R.C., Zwolinski, BJ., "Physical and Thermodynamic Properties of Aliphatic Alcohols,"
J. Phys. Chem. Ref. Data, 2,(Suppl. No. l), (1973).
51
NationalBureau of Standards (US.), CODATA Bulletin, No. 63, (1986).
1997
1-176
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~~~
~
STD.API/PETRO TDB CHAPTER
~~
~
~~
2-ENGL L777 W 0732270 Ob39530 888 W
CHAPTER 2
CHARACTERIZATION OF
HYDROCARBONS
--`,,-`-`,,`,,`,`,,`---
Revised Chapter 2 to First Edition (1966), Second Edition
(1970), Third Edition (1976), Fourth Edition (1982), Fifth
Edition (1992), and Sixth Edition (1997)
Copyright American Petroleum Institute
Provided by IHS under license with API
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--`,,-`-`,,`,,`,`,,`---
Copyright O 1999 American Petroleum Institute
Copyright American Petroleum Institute
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No reproduction or networking permitted without license from IHS
Not for Resale
CHAPTER 2
PREFACE
This revised chapter is based on an expanded experimentaldata base for petroleum characterizing
parameters. Existing correlations were evaluated andnew correlations for predicting some characterizing
properties were developed. Correlations
for aniline point, smoke point, freezing point, cloud point, and cetane
index wereadded to the chapter. Existing correlations for flash
point, pour point, and refractive index were
evaluated and revised. Detailed results of
the COlTelations addedto this chapter are provided in Documentation
Report 2-98available fiom Global Engineering Documents.
The work on this revision was primarily carried out by Research Assistant Paul M.Hinderliter with
Research Aides Tony
B. Hollobaugh and DouglasM.Ruhe underthe direction ofproject Director Thomas E.
Dubert. The Technical Data Committee chapter coordinatorwas Dr. S.J. Kramer, Bechtel Corporation.
Thomas E. Daubert
Department of Chemical Engineering
The PennsylvaniaState University
University Park, PA 16802
June 1998
1999
iii
--`,,-`-`,,`,,`,`,,`---
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STD*API/PETRO TDB CHAPTER
2 - E N G L L777
0 7 3 2 2 7O
0 kl7533
577 M
CHAPTER 2
CHARACTERIZATION OF HYDROCARBONS
PAGE
................................................... 2-1
petroleum Product Blending . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 2-3
2-0 Introduction
2-1
2A Characterization of Pun Hydrocarbons
2A1. Characterimion Factors of Pure Hydrocarbons
proCCdure 2Al.1 Acentric Factors of Pure Hydrocarbons
Figure 2A1.2
Acentric Factors of Pure Hydrocarbons
.. . . . . . . . .
. . . . . . .. . .
2-7
2-9
2B Characterization of Petroleum Fractions
2B1.
CharacterizingBoiling Pointsof Petroleum Fractions
procedure 2B l.1 Characterizing Boiling Points
of Petroleum
Fractians
Figwe 2B1.2
2-10
CharacterizingBoilingPoints of Petroleum
Fractions
2B2.
. . . . . . . . . . . . . . .. . . . . . .. . . . . . . . . .
. . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. .
2-12
Molecular Weightof Petroleum Fractions
ProCadure 2B2.1 Molecular Weight of Petroleum Fractions . . . . . . . 2-13
Figure 2B2.2
MolecularWeight of PetroleumFractions . . . . . . . 2-15
procedure 2B2.3 Molecular Weight of Heavy Petroleum Fractions
2B3.
2-16
. 2-18
Figure 2B2.4
MolecularWeight of Heavy PetroleumFractions
Figure 2B2.5
API Gravity-ViscosityRelationship . . . . . . . . . . . 2-19
Aœntric Factor of Petroleum Fractions
Procedure 2B3.1 Acentric Factor of Petroleum Fractions
2B4.
.
. . . . . . . ..
2-20
Molecular Type Compositionof Petroleum Fractions
Procedure 2B4.1 Molecular Type Compositionof Petroleum Fractions2-22
2B5.
Refractive Indexof Petroleum Fractions
procedure 2B5.1 Refractive Index of Petroleum Fractions
2B6.
Watson Characterization Factor
of Petroleum Fractions
Figure 2B6.1
WatsonCharacterizationFactor of Petroleum
Fractions
2B7.
................................
2-28
Flash Pointof Petroleum Fractions
Procedure 2B7.1 Flash Point of Petroleum Fractions
2B8.
. . . . . . . . 2-26
. . . . . . . . . . . . 2-30
Pour Pointof Petroleum Fractions
--`,,-`-`,,`,,`,`,,`---
Procedure 2B8.1 Pour Point of Petroleum Fractions . . . . . . . . . . . . . 2-32
1999
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~~~
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S T D - A P I / P E T R O T D B C H A P T E R 2-ENGL I997 m 0 7 3 2 2 9 00 b I 9 5 3 44 2 3
PAGE
2B9. Aniline Point
of Petroleum Fractions
Racedure 2B9.1 A n i l i n e Point of Petroleum Fractions
. . . . . . . . . . 2-34
2B10. Smoke Point of Petroleum Fraction
...........
procedure 2B10.1 Smoke Point of Petroleum Fractions
2-36
2B1l. Freezing Pointof Petroleum Fractions
Racedure 2Bll.l Freezing Pointof Petroleum Fractions ......... 2-38
2B12. Cloud Point of Petroleum Fractions
Procedm 2B12.1 Cloud Point of Petroleum Fractions
............
2-40
2B13. Cetane Index of Petroleum Fractions
procedure 2B13.1 Cetane Index of Petroleum Fractions
........... 2-42
2B14. Intercorrelationsof Petroleum Fractions
-
Procedure 2B 14.1 Smoke Aniline Point Intercorrelation . . . . . . . . . 2-44
-
Procedure 2B 14.2 Pour Point Cloud Point Intercorrelation . . . . . . . 2-46
2B15. Flash Point Blendingof Petroleum Fractions
procedure 2B15.1
...................................................
. . . . 2-48
2-50
--`,,-`-`,,`,,`,`,,`---
References
Flash Point Blending of Petroleum Fractions
vi
Copyright American Petroleum Institute
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1999
Not for Resale
CHAPTER 2
CHARACTERIZATION OF HYDROCARBONS
2-0 INTRODUCTION
properties and acentricfixtors adequately characterize
the system.Formorecomplex
mixtures such as
petroleum fractions, it is impractical and not always
For correlational purposes,it is often necessaryto
possible to analyze the entire mixture to define the
designate the individual hydrocarbons in the various
series by numerical parameters which chaxacterizethem.concentration of all the components. These undefíned
Hydrocarbom are partly characterizedby such physical mixtures are usually characterized by parameters that
properties as the boiling point, critical point, and the
are derived from the n o d inspection te
sts, an ASTM
D86orD1160distillation,andthespeci6cgravityofthe
liquiddensity. Their molecular size and shape are
mixture. Many characterizing parameters have been
simultaneously indicated by the acentric factor
(1O, 11).
proposed, but very few are generally useful.
The acentric factoris useful fbrwmlatingphysical and
Among the usefulparameters are five Werent
thedynamic properties and is defined as o
boilingpointsand the Watson (19) characterization
factor, K. Each boiling point reduces to the normal
o = -log p r* 1.000
(2-0.1)
boiling point for pure hydrocarbonsis significant
and
for
a different group of correlations. These five quantities
Where:
are defindby the following equations (16):
p ,* = reduced vapor pressure, p*lpc.
Volumetric average boiling point:
P* = vapor pressure at T = 0.7 T,,in pounds per
n
square inch absolute.
(2-0.3)
pF = critical pressure, in pounds per square inch
absolute.
Where:
T = temperature,indegreesRankine
x, = volume fraction of component i.
T, = criticaltemperature,indegreesRankine.
T,
= normal
boilingpoint
of component i.
-
"I
The acentric factoris used in hydrocarbon correlations
in several chaptersofthis book. Accordingly, Procedure
2A1.1 is presented as a general method of estimation
if
consistentwithProcedure5A1.10.Alternately
experimentalvaporpressure data are available,the
defíning equation (2-0.1) shouldbe used.
Formixtures of identifiablehydrocarbons,the
acentric factor is given bythe following equation:
n
o
= Cxp1
(2-0.2)
Either Fahrenheitor Rankine unitsmay
be used for volumetric average boiling
and
point, molal average boiling point,
weight averageboiling point to give the
same units for the averageboiling
point. Rankine units must be used for
cubic average boilingpoint, however.
The MABP andCABP must be inthe
Same units to calculate mean average
boiling point.
i-l
Where:
n = number of componentsin the mixture.
x, = mole fiaction ofcomponent i.
ai = acentric factor of component i.
This equation is an oversimplification, but it is quite
satisfactoryin most cases. No bettersubstitute is
currently available.
For
hydracarbon
mixtures
for which
the
composition is known, thepure-componentphysical
Molal average boiling point:
c x,Xb,
n
MBP =
(2-0.4)
i- 1
Weight average boiling point:
n
WBP
c x s b ,
i- I
(2-0.5)
Where:
x, = weight fraction of component i.
2-1
1999
--`,,-`-`,,`,,`,`,,`---
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for the Watson K. However, if the viscosity of the
210 F, Figure2B2.4 can
fraction is known at 100 F and
CABP =
xv,.2'~~]
(24.6)
be used to determine the molecular weight which, with
i- 1
gravity, defines the Watson
K from Figure2B2.2.
Mean Average Boiling Point:
Forheavypetroleumfractionssomeanalyhcal
U.QBP+CABP
correlations
int
e
m of specific gravity,
flash point and
MeABP =
n
(2-0.7)
L
r e M v e index are proposed by Woodle (22).
Inasmuch as volume, mole, and weight fractions
are
The Watson characterization
factor is a satisfactory
are
not known for undefined mixtures, the boiling points
approachforcorrelatingthephysicalandthermal
convenientlycorrelated in an empiricalplot(Figure
properties of parafìïnic or naphthenicstraight-run
2B1.2) based on the ASTM D86 distillation curve.
petroleum M o n s . However, the WatsonK dues not
Analytical correlationsdeveloped by Zhou
(23) are also
accuratelycharacterize fractions containing appreciable
included for use on a digital computer.Forhighamounts of olefinic,
diolefinic,
or aromatic
molecular-weight fractions which are vacuum distilled hydrocarbons. Examplesof such fractionsare catalytic
the results mustbe converted
by ASTM Method D 1 160,
cracker recycle oils, catalytic reformer streams, and
to an AST" D86 basis before obtaining a boiling point hydrocarbon streams from other synthesis processes.
(see Chapter 3).
Molecular weight is an important input parameter
The Watson characterization factor,
K, is defined by
a
formanycorrelations.Procedure2B2.1provides
the equation:
method usefil for both desk and computer to estimate
fractions, given only
the molecular weight of petroleum
(2-0.8)
K = (MeABP)'"
the mean average boiling point of the fractionand the
sp gr, 60 FI60 F
where MeABP mustbe in degrees Rankine. The boiling specific gravity. This method is usefil in the range of
molecularweightof70-700.
An altemate, but less
point for the Watsoncharacterizationfactorwas
to
be
used
only when the mean
accurate,
procedure
originally takenas the molal average(19) and was later
unknown
is given by Procedure
average
boiling
point
is
changed to the cubic average(16). Later usage(9,2 1)
involves the mean average,or the arithmetic average of 2B2.3. This procedurerequiresspecificgravityand
viscosity at both 1O0 F and 2 1O F to predict molecular
the two earlier boiling points, as used in equation (2weights
from 200-800.
0.8).
Acentric factorsfor petroleum fractionsfor use with
TheWatson
K is an approximateindexof
analytical
and generalized equations of state can be
paraffinicity, with high values corresponding to high
estimated
byProcedure 2B3.1 whichcombines the
degrees of saturation. A number of Watson K-values
Maxwell-Bonne11
procedure
for
estimating
vapor
for pure hydrocarbons are listed in Table 2A1.3. For
pressure
with
the
defínition
pf
acentric
factor
(Equation
identifiable hydracarbon mixtures, the Watson
K is
2-0.1).
Required
primary
input
parameters
are
mean
given bythe equation:
average
boiling
point
and
specific
gravity.
n
Molecular type distribution aofpetroleum fraction
K =
(24.9)
i=l
is estimable for straight-run petroleumhctions using
where K, is the Watson K for the component i. For
are
Procedure 2B4.1. . Requiredinputparameters
in
petroleum fi-actions, equation (2-0.8) is given
molecular weight, specifíc
gravity, refractive index, and
nomographic formin Figure 2B6.1 where aniline point, one value of viscosity. Molecular typeanalysis, using
molecular weight, and carbon-to-hydrogen ratio are also
theproceduresofChapters7and
11 for defined
correlated.
mixtures ratherthan specialized methodsfor undefined
The MeABP and specific gravity
may also be used
mixtures, allows calculation of enthalpy, heat capacity,
to estimate the Watson K. For high-molecular-weight
and
viscosity
of
petroleum
fractions. Improved
petroleum fkctions, thermal cracking interferes with
d
i and
accuracy is obtained, as substantiated by R
distillations at atmospheric pressure,so it is difficult to
Daubert (15).
obtain a reliable MeABP ufor
se in the defining equation
Refractive index of a petroleum fraction can be
Cubic average boiling point:
[2
3
--`,,-`-`,,`,,`,`,,`---
ExJi
2-2
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--`,,-`-`,,`,,`,`,,`---
disappear as the temperatureis raised.
estimated by usingProcedure 2B5.1. Mean average
Procedure 2B 1 l. 1 provides a method
for predicting
boiling point and specific gravity of the fi-action are
the freezing point
of petroleum fractions using the mean
required input parameters.
average boiling point and specific gravityas the input
K
Figure 2B6.1 can be used for estimating Watson
from specific gravity andmean average boilig point,
parameters.
Cloudpoint is the temperatureof a petroleum
molecular weight,or aniline point.Thisfigure, although
usable for estimation of molecular weight, should
be notfiaction at which its solid paraffin content begins to
solid@ and form crystalsmaking the fraction cloudy.
used if the mean average boiling point and specific
Procedure 2B12.1provides a method for predicting
gravity are both known whereProcedure 2B2.1 is
the cloud point of petroleum
fractons from the specific
preferable.
gravity
and
the
mean
average
boiling If
point.
the cloud
Flash point is the lowest temperature at which
point is known, the pour point can be predicted by
application of a test flame causes the vapor of the
Procedure 2B14.2.
specimen to ignite at test conditions corrected to
Cetane index is the percent of cetane in a blend of
standard pressure.
cetaneand alpha methyl naphthalene which
has the same
Procedure 2B7.1 can be usedto predict thePenskyMartens closed cup and Cleveland open cup flash points ignition qualityas a sample of the petroleum fraction.
Procedure 2B 13.1 provides a method for predicting
of petroleum M o n s . The ASTM D86 10%
thecetaneindex of petroleum fractions using N I
temperature is the input parameter.
gravity and the mean average boiling point
as the input
Pour point is the lowesttemperature at which
parameters.
petroleum fiaction will
flow or can be poured.
Procedure 2B 14.1provides a method for predicting
The choice of pour point procedure isdictated by
the smoke point of petroleum fì-actions using specific
the available parameters in
the priority ordershown.
gravity and aniline point
as the input parameters.
Known Information
Euuation
Procedure 2B14.2provides a method for predicting
pour point of a petroleum fraction using
cloud point as
2B8.1-1
M&P, S,v100
the input parameter.This procedure can also be usedto
2B8.1-2
MeABP, S
predict the cloud point
given the pour point.
Procedure 2B 15.1 provides a methodto predict the
Cloud Point
2B14.2-1
flash point of blends of petroleum fractions using the
where
Wickey-Chittenden (20)blending model.
S = specific gravity,60 F/60F
vloo= kinematic viscosityat 100 F
2-1 Petroleum Product Blending
Aniline point isthe lowest temperatureat which a
petroleum fraction is completely miscible
with an equal
Themixing of unfinished stocks to formmore
volume of aniline.
is accomplished through aprocess
valuable end products
Procedure 2B9.1 provides a method for predicting
known as product blending. Petroleum product blending
the aniline pointof petroleum M o n s using the mean
remainsone of the
most cost effective methods available
average boiling point,specific gravity, and Watson K
to the refiner to meet ever changing product demands.
Edctor as input parameters.
To meet these specialized demands, the refiners now
Smoke pointis the height in millimeters of a flame have various blending proceduresat their disposal. To
that is produced in a lamp burning
a petroleum fraction
be cost effective, blending procedures must optimize the
at standard conditions without causing smoking.
use of blending stucks. Although it is the ultimate
Procedure 2B10.1 can be usedto predict thesmoke
responsibility of the refiner
to detennine the recipe for
point of petroleum fractions from the mean average
the specific blend, blending procedures can provide a
boiling and specific gravity.
useful means
to determinethe appropriate proportions
of
Freezing point is the temperature of a petroleum
each component inthe blend.
m i o n at whichsolid crystals formedoncooling
Of the available blending procedures, most blend
2-3
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murces (1’3) without evaluation.
Blending Procedums for Cloud, Pour, and
Fmezing Points
--`,,-`-`,,`,,`,`,,`---
whm:
PB
propertyodtbttotalblead
Pi = property ofcampent i
x,
weight, molar, or volumetric fiaction of
component i
Most properties do not blcnd linearly, however. For
t&st propertits, a somewhat more cornplex model is
used. Tbese models often q u i r e blading indices, or
blending Mrs. Blending indices an anpirical
quantititsthatproduccfunctionswhichtbenareblended.
’Ihtsc fbnctions CBIl be cxprtsscd as follows:
(2-1.2)
m:
le=blading index of the total blend
& = blendmg index of component i
Tben are numerous reports sumwking
proctdurts for petroleum product blending. Baird (1) as
well as Gary a d Handwerk (3) art two that haw proven
to be the most helpful. Each report summarizes
blending proCCdures, developed byvarious authors,for
pmpelties of interest to petroleum refining.
Prcscatcd in the fóllowing scabns arc p d m
most oommonly uscd for pctrolaxn productbl-.
It
shouldbcDotcdthatbccauscalmostnodataarc
8vailablC, &Idtesting of CaCh P d U n Was d
conducted by t
h Data Book project of thc Amcricau
PetroleumInstitutc. R#.ammcndcdprocedurtsgivtnan
bascd m cacb equation’s m
r
s (asreported by the
author) and cast of mputatim. Whcn models were
dwadtfiatproductnodistiactrrdvantagebetwecnapair
of comla!jons, both or multiple correlations arc given.
l’be procedures were taka directly from the literature
PPBI= pour point blendingiadex number
PP =pourpoint(F)
BP = ASTM 50% boiling tanperazure0
a
b
C
d
The ASTM distillation metbod was not given m the
article, but is assumed to be D86. Once the blending
~fbrcach~isdckmkd,tkirKiexofthctotal
blend can be found by taking a Vdumctric weighted
average of each stock’s pour point index (
v
i
aeq. 2-1.2).
Rearranging equation 2-1.3,the pour point ofthe blend
can be determined, fiom theblend’s index and mid
boiling point, bythe following equation:
- -
PP = [In(PPBIB) a c BPI / It,+ d BP)(2-1.4)
Where:
PPBI, = pour point blending index of total
b l d (h
e ~ 2-1.2)
.
Onc disadvantageof the Reid-Alla p d u n is that the
fatal blcnd’smid boiling point must be known to
determine the pour point of the blead. 7 k authors
ovcfcamt this problem by suggesting the mid boiling
point ofthe b l d could be stimatcd by volurnctrically
averaging the 50% boding temperatures of each blend
dock. Out O f II to5al Of 90 b l d , Rcid-Alla m
rted
pour point predictions witbin 5 F for over 90% of all
cases tested. ”be methodis applicableto any number of
components.
2-4
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æ4.05334
1.5657E-2
4.2928E-3
= 5.084OE-5
1999
Not for Resale
significant with less than 60% falling within 4 F. As
The Hu-Bum method forpetroleumproduct
blending uses a different approach in modeling pour andmentioned above,the recommended procedure for each
property should includea c u s t o d value of k. Hucloud points of blends. The general fonn of the HuBurns model does not require
a blending index value for Burns evaluated the accuracy of the Procedure using
customized values of kfor 5 different refineries. Their
prediction of properties specificto the blended product.
findings wereas follows:
The general form oftheHu-Burnsequation
is as
follows:
Percent within ASTM
Remtabilitv
T;"=E\pi)'"
(2-1S)
ASTM
Repeatability
Where:
TB
Ti
X.¡
k
=pour M cloud point of the total blend (R)
= pour or cloudpointofcomponent i (R)
= volume fraction ofcomponent I
= constantspecific to a givenrefinery
o
Cloud
4
ASTM
General
RepNxluc- value
ibility (F) for k
Customized
Value for
k
8
57
85
Point
--`,,-`-`,,`,,`,`,,`---
94
97
Pour
5
10
The valueof the constantk is specificto a given refinery
Point
and should, under most circumstances, be found by a
trial-and-emr procedure from experimentaldata. For
Very little research
has been conducted for blending
best results,Hu-Burnsrecommendsdetermining
the
freezing points. Maurin (8) proposesamethod for
constant
from
experimental
data. However, if
weight blendingof fieezjng points. However, thereare
insufficientdata exists, the authors
reportedthat a value
not any data or test results for the model. Therefore,
of k 4 . 0 8 for pour point and b0.05 for cloud point
this correlation shouldbe used with caution.
gave the best results on an industry wide basis. For
k
most practical applications, the value of the constant
Blending Procedures forFlash Points
ranges fiom 0.04 to O. 15 for both pour and cloud point
blendmg procedures.
Other blending procedures in addition
to Procedure
TheHu-Burns blendingmodelgivesverylarge
2B15.1 exist for flash point. The Wickey-Chittenden
blending
numbers.
Hu-Burns
accounted
for this
model is recommended because of its ease, accuracy,
problem by developing a blending index. According
to
and vast acceptance by the industry. Hu-Burns (4),
Baird, pourand cloud points with a value
of 140F were
Thiele(17),Chevron
(2), and Maurin (8) offer
arbitrarily assigned an
index valueof 10,000. With 140
alternativeblending methods forflashpoint.The
F taken as the upper limit, the index covers the practicalpetroleum refineris advised to consult these articlesto
range of pour and cloud points of distillate íùel
blends
determine which procedureworks best for a given
and components.
refíning process.
A cloud and pour point index curve
is provided in
the Hu-Burns article forvarious values of k. The HuBlending Proceduresfor Aniline Point
Burns blending index procedure
is similar to that ofthe
Reid-Allen procedure. The blending index from each
Baird (l), reporting
on
work
conducted
by
component(readfromthecurve)
is volumetrically
Unzelman (18) and Jackman (6),indicates aniline points
averaged to obtain thetotal blend's index. The blended
of stocks blend linearly by volume. The observation
is
product's property is then obtained fiom the curve.
based on 53 blends.Thestudyfound
an average
When using a general value Mof. O 8 for pour point
deviation of 0.22 F for the 53 blends. These reports
blending, Hu-Burns found 94% of
97 total blends were
suggest equation 2-l. 1 is adequate for blending aniline
predicted within 5 F of laboratory testdata. For cloud
points.
point blendingand H.05,errors were noticeably more
Work conducted by Chevron (2) contradicts this
2-5
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theory and
suggests
blending
indices
are more
appropriateforanilinepointprediction.Chevron
proposes calculating an aniline pointblendingindex
fiom the following equation:
A ~ B=I e(0.w3652 .W
(2-1 .S)
NOTE:A report documenting the basis upon which
the material in this chapter was s e l e c t e d has been
Petroleum Institute as
publishedbytheAmerican
Documentation Report No.2-98 and is available fiorn
Global Engineering Documents.
Where:
APBI = aniline point blending index
AP = d i n e point (F)
Once the aniline point blending indexis calculated for
the volumetric average is then
each blend stock,
computed to determinethe index of thetotal blend (via
equation 2-1.2). The aniline point of the blendis then
found from its blending indexby the following equation:
AP = 273
.S23 h (AF'BIB)
(2-1.9)
Where:
APBIB = aniline point blending index for total
blend (fiorn equation 2-1.2)
Use these equationswith caution.
2-6
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~~
STD-API/PETRO TDB CHAPTER 2-ENGL
1997
0732290 Ob19541 b b 3
PROCEDURE 2Al.1
ACENTRIC FACTORS OF PETROLEUM FRACTIONS
Discussion
The acentric factor defined by equation (2-0.1) is a usehl characterizing parameter for several
prediction methods. The following equationis used to estimate the acentric factor
of pure hydrocarbons.
.I
o =
- 5.92714 + 6.09648/Tr + 1.28862 InT, - 0.169347T:
15.2518 - 15.6875/Tr - 13.4721 In TR + 0.43577T:
Pr
(2Al.l-1)
Where:
W
'P:
P*
PS
T,
T
Tc
= acentric h r .
= reduced vapor pressure at the reduced temperature, p*/pc.
= vapor pressure at T, in pounds per square inch absolute.
= criticalpressure,in pounds persquareinchabsolute.
= reduced
temperature, T&
= temperature, in degrees
Rankine.
= criticaltemperature, indegreesRankine.
Procedure
--`,,-`-`,,`,,`,`,,`---
Step 1: To determine the acentricfactor for a hydrocarbon that is not listed in Table 2A1.3, first
obtain the critical temperature and pressure fkom Chapter 1 or predict the latter values from methods of
Chapter 4.
Step 2: Ifthe normal boiling point is available
from chapter 1, set T equal to the normal boiling point
at a reduced
and pLequal to 14.7 psia. Ifthe normal boiling pointis not available, predict the vapor pressure
temperature of 0.7 by the methodsof Chapter 5 .
Step 3: Use Equation(2A1.1-1)or its equivalent, Figure 1Al.2, to estimate the acentric factor.
2-7
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COMMENTS ON PROCEDURE 2A1.1
Purpose
Procedure 2A1.1 is a general method for obtainingthe acentric factors of pure hydrocarbons for use in the correlations of other chapters. Use this procedure forpure hydrocarbons
which are not listed in Table 2A1.3 or in Chapter 1. For undefined hydrocarbon mixtures,
use Procedure 2B3.1.
Reliability
The reliability of the acentric factors calculated with this procedure is a direct function of
the reliability of the inputcritical properties and vapor pressures. Large discrepancies can be
detected by comparison with the values in Table 2A1.3. Equation 2A1.1-1 can reproduce the
values in Table 2A1.3 with an average deviation of 1.3% when the normal boiling point is
used.
Special Comments
Because reliable normal boiling point temperatures are usually available, this point is
generally used. However, other vapor pressure data in the same temperature range may be
used.
For mixtures of identifiable hydrocarbons, the acentric factor, o,is given by the following
equation:
"
o=
E x , o,
(2Al.l-2)
i- 1
Where:
n = number of components in the mixture.
xi = mole fraction of component i.
oi = acentric factor of component i.
This equation is an oversimplification, but it is quite satisfactory in most cases. No better
substitute is currently available.
Literature Source
Lee, B. I., Kesler, M. G., AZChE J . 21 510 (1975).
Example
Calculate the acentric factor of l-butene.
From Chapter 1, T, = 295.6 F, p,=583 pounds per square inch absolute, and the boiling
point is 20.7 F. The reduced vapor pressure at the boiling point is 14.7583 = 0.0252, and the
20 7 + 459 7
corresponding reduced temperature is
= 0.636.
29i.645i.7
+
o=
+
+
ln (0.0252) - 5.92714 6.09648/0.636 1.28862 In (0.636) - 0.169347(0.636)6
15.2518 - 15.6875/0.636- 13.4721 In (0.636) + 0.43577(0.636)6
=
"
-Oh1@
0.188
-3.2884
The value listed in Table 2A1.2, which was derived from data at T, = 0.7, is 0.1867. Alternately, using Figure 2A1.2,
I; = 0.636, In P?
o = 0.19
= -3.6809
2-8
1999
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S T D - A P I I P E T R O T D B C H A P T E R 2 - E N G L L997 m 0732290 ObL95V3 g3b m
2A1.2
hl (ACENTRIC FACTOR)
O
0.1
0.2
0.3
0.4
0.5
0.6
0.7
0.8
0.9
1.0
O
O. 5
1.0
1.5
2.0
In
P';
2.5
3.O
3.5
--`,,-`-`,,`,,`,`,,`---
4. O
4.5
2-9
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PROCEDURE 261.1
CHARACTERIZING BOILING POINTS OF PETROLEUM FRACTIONS
Discussion
Figure 2B1.2 is useful for estimation of various average boiling points when the ASTM D86
distillation properties are available.
Procedure
Step 1: Obtain the volumetric average boiling point of a petroleum fraction using ASTM
D86 distillation temperatures at each of the 10, 30, 50, 70, and 90 volume percent distilled
points, ¡.e. VAPB =
O '
+
O
'
O+ '
5
+
"
+
Tw,where all temperatures arein degrees Fahren-
heit.
Step 2: The slope is calculated assuming a linear ASTM D86 distillation curve between the
Tw - To
10- and 90-percent points, with a slope, SL = 90 - 10 , in Fahrenheit degrees per percent
distilled.
Step 3: Using the VABP and theslope, read corrected values to VABP for various average
boiling points from Figure 2B1.2.
This procedure may also be used with a digital computer using the following correlations
generated from Figure 2B1.2 (13).
(2Bl.l-1)
(2Bl.l-2)
tMc
= fv-A4
In Al = -3.062123 - 0.01829(f,-32)0,6667+ 4.45818 SLo.*'
(2Bl.l-5)
ln A2 = -0.56379 - 0.007981(t,-32)0~6667
+ 3.04729 SL0.333
(2B1.1-6)
ln As = -0.23589 - 0.06906(t,-32)0.45+ 1.8858 SL0.45
(2Bl.l-7)
--`,,-`-`,,`,,`,`,,`---
(2Bl.l-3)
(2Bl.l-4)
tcy = f v - A 3
In A4 = -0.94402 - 0.00865(f,-32)0~6667
+ 2.99791 SL0.333
(2Bl.l-8)
where t,, t,,, , t,,, , tMc, and t, are WABP, MABP, CABP, MeABP and VABP, respectively,
in degrees Fahrenheit, and SL is the 10-90 percent slope in (Fahrenheit degrees)/(% distilled).
2-1o
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261.1
COMMENTS ON PROCEDURE 281.1
Purpose
The various average boiling pointswhich are used to characterize petroleum fractionsare
correlated in Figure2B1.2 withthe ASTM D86 distillation properties of the fraction. Ifthese
boiling pointsare required for mixtures (or portions of a mixture) for which the composition
is known, use the defining equations (2-0.3) through (2-0.7) given in the introduction.
Reliability
The reliability is unknown.
Notation
The relationships between the various average boiling points given in Figure 2B1.2 for
petroleum fractions are analogous to those defined by equations (2-0.3) through (2-0.7) for
mixtures of identifiable hydrocarbons.
Special Comments
If the available distillationdata are not from ASTM Method D86, they must be converted
by the methods of Chapter 3 to calculate the volumetric average boiling point.
Literature Sources
This figure was developed by Smith and Watson, Ind. Eng. Chem. 29 1408 (1937). Equations (2Bl.l-l) through (2Bl.l-8) weredeveloped by P. Zhou, Int. Chem. Eng., 24(4),
731-741 (1984).
Example
Determine the molal average boiling point, weight average boiling point, cubic average
boiling point, and mean average boiling point of a petroleum fraction having the following
ASTM D86 distillation properties:
Distillation, percent by volume . . . . .30
.....
Temperature, degrees Fahrenheit . . . . . 230
...
VABP =
10
90
149
371
70
325
50
282
149 + 230 + 282 + 325 + 371 = 271 F
5
Fahrenheit degrees
Slope = 371 - 149 = 2.78
80
percent distilled
Using Figure 2B1.2,the average boiling pointsare calculated from the volumetric average
boiling pointby first readingthe boiling point corrections from the figure and then calculating
the various average boiling points fromthe VABP.
MABP = 271 - 30 = 241 F
CABP=271- 7=264 F
WABP = 271 + 7 = 278 F
MeABP = 271 - 19 = 252 F
Alternately, using equations (2Bl.l-1) through (2Bl.l-8), the average boiling pointsare:
MABP = 240.6 F
WABP = 278.3 F
CABP = 264.0 F
MeABP = 252.1 F
2-1 1
1999
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S T D - A P I / P E T R O T D B C H A P T E R 2-ENGL 1 7 7 7 M 0732290 Ob1954b 1 4 5 M
R
O
3 .2
4
Lß
--`,,-`-`,,`,,`,`,,`---
2-12
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2B2.1
PROCEDURE 282.1
MOLECULAR WEIGHT OF PETROLEUM FRACTIONS
Discussion
The following equation is used to estimate the molecular weight of petroleum fractions.
M=20.486[exp(1.l6Sx1O4Tb-7.787123
+ 1.1582 x
TbS ) ] Tb1~26007S4.98308
(2B2.1-1)
Where:
M = molecular weight of petroleum fraction.
Tb = mean average boiling point of petroleum fraction in degrees Rankine.
S = specific gravity, 60 F/60 F.
Procedure
Step 1: Obtain the specific gravity of the petroleum fraction.
Step 2: Obtain the mean average boiling point from Figure 2B 1.2.
Step 3: Calculate the molecular weight using equation (2B2.1-I).
Alternately Figure 2B2.2, the equivalent of equation (2B2.1-1) in terms of Watson characterization
factor and API gravity, can be used with slightly lower accuracy.
Where:
141.5
API gravity = -- 131.5
S
K =c/3/S
2-13
1999
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2B2.1
COMMENTS ON PROCEDURE 262.1
Purpose
The purpose of this procedure is to predict the molecular weight of petroleum fractions
from specific gravity and mean average boiling point, both of which are usually available.
Limitations
Equation (2B2.1-1) was evaluated over the following range of molecular weight, mean
average boiling point, and gravities:
Range of Data
Molecular weight
Boiling point, degrees Fahrenheit
API gravity
Specific gravity
70-700
90-1050
14.4-93.1
0.63-0.97
The equation may be safely extrapolated to a boiling point of 1500 F.
Reliability
The equation reproduced experimental values of molecular weight to within an average
error of 3.4 percent whenM < 300 and 4.7 percent for M > 300 when tested against 635 data
points.
Literature Sources
The equation is a 1986 modification of a correlation developed by M. R. Riazi, “Prediction
of Thermophysical Properties of Petroleum Fractions,” Ph.D. Thesis, Department of Chemical Engineering, The Pennsylvania State University, University Park, Pa., 1979.
Special Comment
For heavy fractionsor if the mean averageboiling point is not available,Procedure 2B2.3
should be used.
Example
Determine the molecular weight of a petroleum fraction havinga specific gravity (60F/60
F) of 0.8160 and the following ASTM D86 distillation properties:
Distillation, percent by volume . . . . . . . . . .
10
30
50
70
90
Temperature, degrees Fahrenheit.. . . .. . . 227
276
340
413
509
Using Procedure 2Bl.l the volume averageboiling point is 353 F, the 1 6 9 0 slope is 3.53,
and the correction from Figure 2B1.2 is -24 F. The mean average boiling point is then
353 - 24 = 329 F (788.67 R).
Using equation (2B2.1-1), the molecular weight is:
M = 20.486 exp(1.165 x
x 788.67 - 7.78712 x 0.8160 + 1.1582 x
x 788.67
x 0.8160)(788.67)’~26M7(0.816)4~98308
= 134
An experimental value is 137.0.
Alternately using Figure 2B2.2:
K = (788.69)’”/0.8160 = 11.32
141 5 - 131.5 = 41.9
API gravity = 0.8160
M=140
2-14
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--`,,-`-`,,`,,`,`,,`---
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1999
2B2.2
700
600
500
400
300
--`,,-`-`,,`,,`,`,,`---
200
1O 0
-20
O
20
40
60
80
100
API G R A V I T Y
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282.3
PROCEDURE 282.3
MOLECULAR WEIGHT OF HEAVY PETROLEUM FRACTIONS
Discussion
The following equation is used to determine the molecular weight of a heavy petroleum
fraction.
M = 223.5~v~-1.2435+1.1228S)(3.4758-3.038s)~-0.6665
(2B2.3-1)
100
v210
Where:
M = molecular weight of petroleum fraction.
vlW= kinematic viscosity of petroleum fraction at 100 F, in centistokes.
u210= kinematic viscosity of petroleum fraction at 210 F, in centistokes.
S = specific gravity, 60 F/@ F.
Procedure
Step I : Obtain the kinematic viscosities at 100 and 210 F from experimental dstta or usin
estimation methods of Chapter 11.
Step 2: Obtain the specific gravity of the petroleum fraction. When API gravity is given,
S = 141.5/(API + 131.5). If a gravity is unknown use equation (2B2.3-2) or Figure 2B2.5 to
estimate.
Step 3: Calculate the molecular weight using equation (2B2.3-1) or, alternately, Figure
2B2.4.
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2B2.3
COMMENTS ON PROCEDURE 282.3
Purpose
This procedureis used to determine molecular weight of a high-boiling petroleum fraction
when viscosities at 100 F and 210 F are known. The molecular weight can be used with Figure
2B6.1 to estimate the Watson characterization factor for the fraction.
Llmltatlons
The viscosities at 100 F and 210 F do not characterize petroleum fractions as well as an
AST" distillation; thus, when a choice exists, use Procedure 2B2.1 instead of this procedure
for estimating molecular weights.
Use this procedure only for petroleum fractions as erroneous values may be obtained for
synthetic hydrocarbon mixtures, for which it was not designed.
Use this equation in the molecular weight range of 200 to 800.
Reliablllty
Molecular weights obtained from this procedure differ by an average of 2.7 percent from
experimental data.For the few data points for which both Procedure 2B2.1 and 2B2.3 could
be used to estimate molecular weights, the predictions differed by 8.5 percent.
Speclal Comments
For petroleum fractions for which specific gravity is not available, the following equation
can be used to estimate the specific gravity.
S = 0 7717vn.~~s7-0.1616
100
v210
(2B2.3-2)
This equation is also shown in Figure 2B2.5 in terms of API gravity. If predicted values of
specific gravity from equation 2B2.3-2 are used instead of experimental values, errors in
equation (2B2.3-1) increase from 2.7 to 3.5 percent.
Literature Source
Riazi, M.
R.,private communication (1985).
Example
Determine themolecular weight and Watson K for an oil having an API gravity of 22.5 and
kinematic viscosities of 55.1 centistokes at 100 F and 5.87 centistokes at 210 F.
S=
141S
- 0.9188
22.5 + 131.5 -
A. Using equation (2B2.3-1).
M
= 223.56(55.~)(-1.2435+"228X0.91sr() (5.87)(3.4758-3.n3~
X
n.Ylm)
(0.9188)-"."
= 340
An experimental molecular weight is 349.
B. Using Figure 2B2.4, the molecular weight is about 332.
C. Assuming the API gravity is unknown, use of equation (2B2.3-2) gives S = 0.9219 and
an API gravity of 22.0. Figure 2B2.5 also would yield an API gravity of 22.
Using a value of molecular weight of 340 and API gravity in Figure 2B6.1, the Watson K
is 11.58.
2-17
1999
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STD.API/PETRO
TDB CHAPTER
2-ENGL
L997
0732290 Ob19552 4q9
m
6
--`,,-`-`,,`,,`,`,,`---
262.4
3000
I2Ooo
1 O00
000
000
700
600
500
400
300
E200
F I G U R E 2B2.4
MOLECULAR WEIGHT OF
HEAVY PETROLEUM FRACTIONS
@
T E C H N I C A L D A T A BOOK
JUNE lQ86
Approved: TED
- 1
2-1a
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STD-API/PETRO TDB CHAPTER 2-ENGL 1777 9 0732270 Ob19553 385 9
282.5
O
O
O
v)
d
O
o
O
Cu
1999
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O
r
O
2B3.1
PROCEDURE 283.1
ACENTRIC FACTOR OF PETROLEUM FRACTIONS
Dlscussion
Equation (2-0.1) and Procedure5A1.13 are used to calculate acentric factors for petroleum
fractions.
Procedure
--`,,-`-`,,`,,`,`,,`---
Step I : Obtain the mean average boiling point and specific gravity (60 N60 F) of the
petroleum fraction.
Step 2: Obtain the Watson K from defining equation (2-0.8).
Step 3: Calculate the pseudocritical temperature, using Procedure 4D3.1.
Step 4: Multiply the pseudocritical temperature obtained in Step 3 by 0.7.
Step 5: Use Procedure 5A1.13to determine the vapor pressure of the petroleum fraction
at the temperature calculated in Step 4.
Step 6: Calculate the pseudocritical pressure, using Procedure 4D4.1.
Step 7: Calculate the acentric factor of the petroleum fraction, using equation (2-0.1).
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S T D - A P I / P E T R O T D B C H A P T E R 2-ENGL L977 E 0732270 Ob17555 L58
m
263.1
COMMENTS ON PROCEDURE 263.1
pwoThe purpose of this procedure is to calculate the acentric factorof petroleum fractions for
use in &e correlations of other chapters. The method WS a reliable correlation for vapor
pressure and tbe defining quation for acentric factor.
Umltatlons
Procedure 5A1.19,when used by itself to determine vapor pressures, is strictly applicable
only to pure hydrocarboas and narrow-boiling petroleum fractions. However,
when the
procedure is used in conjunction with equation (2-0.1)to calculate acentric factor, it is also
applicable to wide-boiling petroleum fractions.
Special Comment
Procedure 2Al.l should be used to calculate the acentric factor of pure hydrocarbons.
-m*
Determine the acentric factor of a petroleum fractionhaving a specific gravity(60 FI60 F)
of 0.8160 and the following ASTM D86 distillation properties:
Distillation, percent by volume . .. ......
10
30
50
70
90
Temperature, degrees Fahrenheit.. .. . ... 227276
340
413
M9
Correcting the calculated VABP using Figure 2B1.2, the meanaverageboiling
point = 329.0 F. Using equation (2-0.8)the Watson K is 11.32.Using Procedure 4D3.1,the
pseudocritical temperature is calculated to be 683.7F.Since the reduced temperature is 0.7,
the temperature for which the vapor pressure is determined is
T = 0.7(683.7+ 459.7)
= 800.4 R
= 340.7 F
From Procedure5A1.19,the vapor pressureat 340.7 F is 897mm Hg. By Procedure 4D4.1.
the pseudocritical pressure is 400 pounds per square inch absolute.
By definition, equation (24.1),the acentric factor is:
--`,,-`-`,,`,,`,`,,`---
.
2-21
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264.1
PROCEDURE 284.1
MOLECULAR TYPE COMPOSITION OF PETROLEUM FRACnONS
Dimuion
Equations 2B4.1-1 through 2B4.1-3 are w d to predict the fractional composition of
and aromatics contained in both light and heavy petroleum fractions.
V i i t y , specific gravity, and refractive index of the desired fraction are w d as input
parameters.
t,=~+b(Ri)+c(VG)
(2B4.1-1)
x. = d + e ( R i )+ f ( V C )
(2B4.1-2)
r.=g+h(R,)+i(VG)
(2B4.1-3)
Where:
u, b, c , . , ,i = constants varying with molecular weight rangeas given below.
Constants
Fractions
Fractions
Heavy
Light
Molecular weight range
70-200
u)(Moo
a
-13.359
+2.5737
b
+14.4591
.+1.0133
C
1.41344
-3.573
d
+23.9825
+2.464
e
-23.333
-3.6701
+ 1.%312
+0.81517
f
-4.0317
-9.6235
g
h
+8.8739
+2.6568
+ 1.m88
i
+OS9827
paraffins, naphthenes,
--`,,-`-`,,`,,`,`,,`---
.
-
x,, x., x, = mole fraction of paraffins, naphthenes, and aromatics, respectively.
R,= refractivity intercept as given by equation (2B4.1-4).
VG =viscosity gravity constant (VCC) as givenby equations 2B4.1-S for heavy
fractions or viscosity gravity function(VGF)as given by equations 2B4.1-6 for
light fractions.
d
Ri = n -(2B4.1-4)
2
Where:
n = refractive index at 68 F and 1 atmosphere.
d = liquid density at 68 F and 1 atomosphere in grams p e r cubic centimeter.
(2B4.1-5.1)
or
VGC =
S
- 0.24 - 0.022 log (V,,-,35.5)
(2B4.1-5.2)
0.755
Where:
S = specific gravity at 60 FI60 F.
V = Saybolt universal viscosityat 100 or 210 F, in Saybolt universal seconds.
Note: For interconversion of viscosity units see Chapter 11.
VGF= -1.816 + 3.484s
-0.1156
InUlm
or
VGF -1.948 + 3.535s 0.1613 In ~ 2 1 0
Where:
Y = kinematic viscosity at 100 or 210 F,centistokes.
-
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(2B4.1-6.1)
(2B4.1-6.2)
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S T D - A P I / P E T R O T D B C H A P T E R 2-ENGL L777 E 0732270 Ob19557 T 2 0
m
2B4.1
Procedure
Step 1: Obtain the specifíc gravity (60 F/60F), density at 68 F (20 C),,and refiactive indexat 68
F (20 C)of the fiaction. Estimate the r e w i v e index, if unknown, fiom Procedure 2B5.l. Estimate the
density, ifunknown, from methods of Chapter 6 or from equation (2B4.1-10)
ifappropriate.
Step 2: Estimatethe molecular weight,ifunknown,fiomProcedure2B2.1or Figure2B2.2to establish
whether the fractionis light or heavy.
Step 3: Obtain the correct viscositiesto use equations (2B4.1-5)or (2B4.1-6)as appropriate.
though (2B4.1-6).
Step 5: Calculate the mole fractionof paraflins, naphthenes, and aromatics from equations
(2B4.1-1)through (2B4.1-3)respectively. The sum must equal 1.00.
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--`,,-`-`,,`,,`,`,,`---
Ifexperimental values areunknown, use the methodsof Chapter 11 for estimation.
Step 4: Calculate VGC or VGF as appropriate and calculate R,from equations (2B4.1-4)
Not for Resale
~
~~
S T D * A P I / P E T R O T D B CHAPTER 2 - E N G L L997 m 0732290 U b L 9 5 5 8 7b7
2B4.1
COMMENTS ON PROCEDURE 284.1
Equations are given for calculating the molecular type distribution of straight run petroleum fractions.
Llrntt.tion8
This proCCdure was evaluated with petroleum fraction data having the following ranges of
molecular weight, refractivity intercept, viscosity gravity constant or viscosity gravity function, and composition.
Range of Data
Light fraction
Heavy fraction
Molecular weight
7&214
233-571
1.04-1.08
Ri
I .04-1.06
VGC or VGF
0.57-1.52
0.7W.98
O.024.93
0.1M.81
x,
0.02-0.46
0.13-0.64
X"
0.014.93
0.0-0.31
X.
The method may be used for petroleum fractions of molecular weight as low as 70.
However, it should not be used outside the range of evaluated data.
~llabllity
For the 85 tight petroleum fractions tested, average deviations for x, and x. are 0.04 and
0.06 mole fraction, respectively. For the 72 heavy fractions evaluated, average deviations of
0.02 and 0.04 mole fraction occurred for x, and x., respectively.
Speclot Comments
A. For highly aromatic fractions where detailedknowledge of aromatic t y p e s is required,
the following equation is proposed to estimate monoaromatic content of the fraction
x,,,, = -62.8245 + 59.90816R,- 0.0248335m(2B4.1-7)
Where:
R,= refractivity intercept as given by quation (2B4.1-4).
x- = mole fraction of monoaromatin.
m = a factor given by equation (2B.4.1-8).
m = M(n
- 1.4750)
(2B4.1-8)
--`,,-`-`,,`,,`,`,,`---
in which M is the molecular weight. Equation 2B4.1-7is applicable to fractions with molecular weights less than 250.
Mole fraction of other t y p e s of aromatics (di- and polyaromatics) can be determined by
difference between x. from equation (2B4.1-3)and x,,,, from equation (2B4.1-7).
+=x.
-xm.
(2B4.1-9)
Where:
x, = mole baaion of di- and polyaromatics.
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2B4.1
B. For petroleum fractionsfor which density at 68 F (20 C ) needed for quation (2~4.14)
h not available, insteadof using methods of Chapter 6, it could be more convenient to obtain
this PtopenY Using the following equations for fractions of molecular weight greater than 300:
d æ 2,83085MO.-I'.'35'3
(2B4.1-10)
Where:
d * liquid density at 68 F m d 1 atmosphere, in g r a m s per cubic antimeter.
I = Huang (1) characterization parameter a t " F.
nz- 1
-
I n ' *
n = refractive index at 68 F and 1 rtmosphere.
M molearlar might of petroleum fraction.
source
R i a d , M.R.,"Prediction of Thennophysical Properties of Petroleum Fractions," Ph.D.
Tbesis, Dtpartment of CbemicalEngineering, The Pennsylvania State University. University
Pprk, Pa., 1979.
Riad, M.R.,Daubert, T.E.,I n d . Eng. Chcm. Proms DLS.Dev. 19 289 (1980).
Riad, M.R.,private communication (1985).
--`,,-`-`,,`,,`,`,,`---
Example
Calculate the molecular type distribution of a petroleum fraction of specific gravity 0.9046
at 60 F/60F,a refractive index of 1.5002,a liquid density of 0.90 at 68 F,a mean average
boiling point of 798 F, and a viscosity of 336 Saybolt universal. secondsat 100 F.
From equation (2B2.1-1).the molecular weight is:
M * 20.486 exp (1.165 x IO" x 1258 - 7.78712 x 0.9046
+ 1.1582 x
x 1258 x 0.9046)(1258)'~-"(0.9046)'~euoB
M = 378
mus, the fraction is heavy and the viscosity gravity constant shouldbe used for correlation.
From equation (2B4.1-5.1).the viscosity gravity constant is:
(10)(0.9046) - (1.0752)log(336- 38)
VGC =
[ 10 - log (336 - 38)]
VGC = 0.6485
From quation (2B4.1-4), t h e refractivity intercept is:
Ri = 1.5002 - 0.90 = 1.05
2
From equations (2B4.1-1),(2B4.1-2)and (2B4.1-3), using heavy fraction constants, the
mole fractions are:
~ ~ ~ 2 . 5+
7 (1.0133)(1.05)
37
- (3.573)(0.8485)
x, = 0.606
X.
2.464 (3.6701)(1.05) + (1.%312)(0.8485)
x, = 0.275
X.
-4.0377 + (2.6568)(1.05) + (1.60988)(0.8485)
x. = 0.1 19
2x = 1.000
Experimental values of x p , x., and x. are 0.59, 0.28, and 0.13, respectively.
-
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285.1
PROCEDURE 2B5.1
REFRACTIVE INDEX OF PETROLEUM FRACTIONS
Discussion
Equation (2B5.1-1)is to be used to predict the rehctive index of petroleum fractions.
.=I1
(2B5.1-1)
1 - I
Values of I may be calculated from equation (2B5.1-2).
--`,,-`-`,,`,,`,`,,`---
I = 2.266
-5.704
exp(3.905
x
x
x
MeABP
1O-4 MeABP S) MeABP
+
2.468 S
S
(2B5.1-2)
Where:
n
= r e W v e index at 68F.
I
= modified Huang characterizationparameter at 68F.
MeABP= mean average boiling point, D86,R.
S
= specific gravity, 60F/60F.
Procedure
Step 1:
Step 2:
Step 3:
Obtainthe mean average boiling point from equation (2-0.7)or Figure 2B1.2 and specific
gravity of the fiaction.
Calculate the modified Huang characterizationparameter fiorn equation (2B5.1-2).
Calculate the refiadve index of the M o n fiom equation (2B5.1-1).
2-26
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2B5.1
COMMENTS ON PROCEDURE 2B5.1
Purpose
The purpose ofthis procedure is to predict the refractive index of petroleum
fractions at 68F from themean
average boiling pointand specific gravity.
Limitations
Equations (2B5.1-1)and (2B5.1-2)were usedtoevaluate refractive index
data for petroleum fiactions
with
mean average boiling point, specificgravity, and refractive indices in the following
ranges listed.
Range ofData
100 950
0.63 - 0.97
1.35 1.55
-
Mean average boiling point,F
Specific gravityy60F/60F
Refractive indexat 68F
The method may also be used to predict the reftactive
index for purehydrocarbons by using the n o d boiling
point in place of the mean average boilingpoint.
Reliability
indexan average absolute percent
Equation (2B5.1-1)reproduced experimental values for refractivewithin
emor of 0.3%.
Literature Source
R.iazi, M.R., “PredictionofThemophysicalProperties ofPetroleum Fmctionsyy’Ph.
D. Thesis, Department
of Chemical Engineering, The Pennsylvania State University, University
Park PA 1979.
Riazi, M.R., private communication(1985).
API Documentation Report API-2-98.
Calculate the refractive index of
a fraction at 68F with specific gravity of
0.732 and mean average boiling
point of 656 R
Using equation (2B5.1-2), the Huang parameter is:
I= 2.266 X
-
e ~ p [ 3 . 9 0 5lo4
~ (656)+ 2.468 (0.732) 5.704 X lo4 (656)(0.732)] (656)0.0Sn(0.732)~0.no
--`,,-`-`,,`,,`,`,,`---
Example
I= 0.246
From equation(2B5.1-1)¶the r e W i v e index is:
L
J
The experimental value for the refractive index offracton
the is 1.4074.
2-27
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2B6.1
-3-
90
FIGURE 286.1
L
85
WATSON
=t
753
65
CHARACTERIZATION
~1100
:ACTOR OF PETROLEUM FRACTION:
4-
TECHNICAL DATA BOOK
June
Approved:
1980
RPD 8 TED
4
0O'[
L
50
0.80V
E
z
P:
0
200
P
4 0 3
8
d
-L
i
W
400
U
loo]
50
2-28
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Lu
z
1999
--`,,-`-`,,`,,`,`,,`---
Not for Resale
COMMENTS ON FIGURE 2B6.1
266.1
Purpose
The Watson characterizationfktor, K, of petroleum fraction whichis used to estimate many other
properties in subsequent chapters,has been correlated with many properties suchas mean average boiling
point, molecular weight, carbon-to-hydrogen weight
ratio, and aniline point with
either API or specificgravity.
Figure 2B6.1 is provided for estimating the Watson K factor fiom the gravi@ and any one of the other
APO
v
t
i
y
a
r
ehewn, use the defining equation
properties. Ifthe mean average boiling point and specific (orp
(2-0.8)given in theintroductionfor calculating the Watson
K.
Please note that the prediction ofproperties other
thanWatson K using this plot will most likelybe less
accurate than using other specific methods given various
in
procedures of this chapter. For example, aniline
point is much better predicted by Procedure2B9.1 while molecular weight proceduresof Section 2B2 are
recommended.
Reliability
The reliability depends on the
accuracy of input parameters.
Special Comments
For heavy petroleum fiactions
(MW>300) distillation data for determinationof mean average boiling
point usuallyare not available. For such fiactions molecular weight
A P I gravity
and may be used to determine
Watson K from Figure2B6.l. Ifmolecular weightis unknown, use Procedure2B2.3to estimate molecular
weight fiom kinematic viscositiesat 100 F and 210 F. However, the use of API gravity with carbon-tuhydrogen weight ratio or aniline point is not recommended for determining Watson
K factor.
For heavy fiactions when
this figure cannotbe used to determine WatsonK, simple correlations given
by W d e (1 2)in terms of M I gravity, flash point, aniline point,or refractive index maybe used to estimate
the WatsonK factor.
Literature Source
This figure was given by Winn, F. W., Petrol. ReJiner 36[2] 157 (1957).
Detennine the WatsonK factor of a petroleum fraction having an API gravity of 34.5,kinematic
viscosity of 5.27 cStat 100 F and 170 cSt at210 F.
Using Procedure2B2.3,to predict molecular weight,
M = 247
--`,,-`-`,,`,,`,`,,`---
Example
Using Figure2B6.1,with M = 247 and API gravity of 34.5,
K = 11.85
Using its definition, equation(2-0.8),the WatsonK is 11.89.
2-29
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2B7.1
PROCEDURE 2B7.1
FLASH POINT OF PETROLEUM FRACTIONS
Discussion
For closed cupflash point:
FP = 0.69 Tlph 118.2
-
(2B7.1-1)
- 109.6
(2B7.1-2)
For open cup flash point:
FP = 0.68 T
l
,
where:
FP = flash point, F.
Tlph= ASTM D86 10% temperature for petroleumfrslction, F
Procedure
Step 1: Determine the correct prediction method for
flash
thepoint type required (open or
closed cup).
Step 2: Obtain the ASTM D86 10% temperature.
Step 3: Calculate theflash point using equation(2B7.1-1), or equation (2B7.1-2) depending on the
flash point method to be predicted.
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--`,,-`-`,,`,,`,`,,`---
The following equations areused to estimate the flash point of a petroleum fraction.
~
-
~~
~~
~
~~
~
S T D - A P I i P E T R O T D B C H A P T E R 2-ENGL L777 E 0732290 ObL95b5 U T 7 W
2B7.1
COMMENTS ON PROCEDURE 2B7.1
Definition and Purpose
Flash point is defined as the lowest temperature corrected to 14.7 psia (1 atm) at which application
of a test flame causes the vaporof a specimen to ignite underspecific conditions of testing. The purposeof
this procedure is to predict Pensky-IMartens Closed
Cup (ASTM D93) and Cleveland Open Cup
(ASTMD92)
flash points of petroleum fractions from theASTM D86 10% temperature.
Limitations
Equatiom (2B7.11) and (2B7.1-2)
were evaluatedover the following range
of flash points and ASTM
D86 10% boiling temperatures.
Range of Data
-
Flash Point, F
O 450
ASTM D86 10% boiling temperatures,F.
150 to 850
The equationscan be reasonably extrapolated beyond the tested
data range to a limited extent. The
to the ASTM D86 5% boiling point
flash point of a petroleum fiaction should be more accurately correlated
as the light end determines the
flash point. A lack of data prevented the development of the correlation.
Reliability
Equation (2B7.1-1)and w o n (2B7.1-2) reproduced experimental values
for flash point within an
average absolute deviation
of 9.6 and 3.2 F, respectwely.
Literature Source
American PetroleumInstitute, Documentation Report 2-98.
--`,,-`-`,,`,,`,`,,`---
Example
Determine the o p e n a p flash point of a fiaction having an ASTM D86 10% temperature of 403 F.
From equation (2B7.1-2)
FP = 0.68(403) - 109.6= 164 F
An experimental valueis 165 F.
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288.1
PROCEDURE 2B8.1
POUR POINT OF PETROLEUM FRACTIONS
Discussion
The followingequations are used to estimate the pour point of a petroleum fraction.
PP = 753 + 136 [ l - exp (-0.15 vlo0)] - 572 S + 0.0512vloo+ 0.139 MeABP
(2B8.1-1)
If only the cloud pointis known, pour point may be predicted usingProcedure 2B14.2.
mere:
PP
v100
S
MeABP
= pour point of petroleum
fraction, R.
= kinematic viscosity at 100 F, cSt.
= specific gravity, 60F/60F.
= mean averageboiling point, D86, R.
Procedure
Step 1: Obtain the specific gravity,mean average boiling point, and kinematic
viscosity at 1O0 F
(if available) of the petroleum
Mon.
Step 2: Use equation(2B8.1- 1) to calculate thepour point if kinematic viscositydata are
available. When experimental viscositydata are not available, use equation(2B8.1-2).
2-32
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--`,,-`-`,,`,,`,`,,`---
Ifthe experimental kinematic viscosityis available:
COMMENTS ON PROCEDURE 2B8.1
288.1
Definition and Purpose
(2B8.1-1) md (2B8.1-2)wuc evaluated OW t
k following ranga.
Pour po& R
420 to 590
Mean average boiling point, R
800 to 1500
KinaMtic v;scoSity, cSt
2 to 960
Specificgravity, (60F/60F)
0.8 to 1.0
Equat~oas(2B8.1-1)and (2B8.1-2)may be reasoMbly extrapolated to a limited extent.
Reliability
Equation (2B8.1-1) reproduced experimental values of pour point to within an average dewation of
6.9 R for 280 data points. Kinematic viscosity data should not be tstimatcd when using quation
(2B8.1-1). Ifviscosity data are not available use equation (2B8.1-2). Equation (2B8.1-2) reproduced
experimental values of pour point to within an average deviation of 9.9 R for 428 data points.
Literature Source
Example
specific
Dctcnniot the pour p i n t of a of a petroleum fr;rctimwith mtan average b o i point of 972 R,
of 0.839, and ldnanatic viscosity at I 0 0 F of 3 cSt.
g
r
a
*
F m -00 (2B8.1-1)
PP = 753 + 136 (lcl~p[-O.l5(3)])-572(0.839)+ (0.0512)3 +0.139(972)
PP = 458 R
Aa qcnmaml pour point of the fiaction is 455 R.
1999
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2-33
S T D - A P I / P E T R O T D B C H A P T E R 2-ENGL L777 M 0732270 ObL75b8 8Db m
PROCEDURE 2B9.1
269.1
ANILINE POINTOF PETROLEUM FRACTIONS
Discussion
The following equation is usedto estimate the aniline point
of a petroleum M o n .
AP = -1253.7- 0.139MeABP + 107.8K + 868.7S
(2B9.1-1)
Where:
AP
S
= aniline point of petroleum fizti04 R
= mean average boiling point, R.
= specific gravity, 60F/60F.
K
=Watson K factor.
MeAJ3P
Procedure
Step 1: Obtain the the mean average boiling pointand specific gravity.
Step 2: Ob& the WatsonK of the petroleum fiaction; if unknown calculate fiom Equation (2-0.8).
Step 3: Calculate the aniline point using Equation
(2B9.1-1).
2-34
1999
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~
~
STD.API/PETRO TDB C H A P T E R 2-ENGL L717 H 0732270 ObL75b9 7 q 2 H
2B9.1
COMMENTS ON PROCEDURE 2B9.1
Definition and Purpose
The aniline point
is the lowest temperature
at which a petroleum fractionis completely misciblewith
an equal volume of distilled aniline.ASTM Procedure D61
1 is used to determine experimental aniline points.
of a petroleum fiaction fiom mean average boiling
The purposeof this procedure is to predict the aniline point
point, specific gravity, and the Watson K factor.
Limitations
Equation (2B9.1-1)
was evaluated over the following
data ranges.
Range of Data
200 to 1100
0.7 to 1.0
100 to 240
Mean average
boiling
point,
F
Specific gravity, 60F/60F
Aniline point, F
Reliability
The equation reproduced experimental values of aniline pointto within m average deviationof4.2 R
for 343 data points havinga mean average boiling point lessthan 750 F. Including datawith mean average
boiling points grater than 750 F, the equation reproduced experimental values of aniline point within an
average deviationof 4.7 R for 475 data points. The equation should
be used with caution when estimating pure
compound aniline points and petroleum
h t i o n s with a mean average boiling point
greater than 750 degrees
Fahrenheit.
with an average deviationof 8.6 F for
Aniline pointcan also be easily estimated using Figure 2B6.1,
48 data points.
Literature Source
American Petroleum Institute, Documentation Report API-2-98.
Example
459.67)'" = 12.16
0.8304
Calculate the aniline pointfìom equation (2B9.1-1).
Using Equation(2-0.8):
K = (570.2
+
--`,,-`-`,,`,,`,`,,`---
Determine the aniline point
of a petroleum fìactionhaving a specificgravity of 0.8304 and a mean
average boiling pointof 570.2 F.
AP = -1253.7 - 0.139(570.2+ 459.67) + 107.8(12.16)+ 868.7(0.8304)
AP = 635.4 R
An experimental value is 639.1
R.
2-35
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2B10.1
PROCEDURE 2B10.1
SMOKE POINT OF PETROLEUM FRACTIONS
Discussion
The following equation is used to estimate the smokepoint ofpetroleum íÌactions.
(2B10.1-1)
Where:
MeABP
= smoke point of petroleum fracton, mm.
= mean average boilingpoint, R.
K
= Watson K factor
SP
Procedure
Step I : Obtain the specific gravity and mean average boiling pointof the petroleumhction.
Step 2: Obtain the Watson K factor; if not available calculateusing Equation(2-0.8).
Step 3: Calculate the smoke point using Equation(2B10.1-1).
2-36
1999
--`,,-`-`,,`,,`,`,,`---
Copyright American Petroleum Institute
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Not for Resale
COMMENTS ON PROCEDURE 2B10.1
2B10.1
Definition and Purpose
--`,,-`-`,,`,,`,`,,`---
The smoke point is the height in millimeters of the flame that is produced in a lamp at standard
anditions without causing smoking. The purpose
of this procedure is to predict the smoke point
of petroleum
fractions fiom mean averageboiling point and specificgravity data. ASTM Procedure D1322is a standard
method for experimental determination.
Limitations
-
Equation (2B1O. 1 1) was evaluated over the following smoke point, gravity,
specificand mean average
b o i point ranges.
Range of Data
-
Smoke point, mm
15 33
- 0.86
Specific gravity,60F/60F
0.7
-
Mean average
boiling
point,
F
200 550
This equation is not recommendedfor the unlikely case of a fractionof low specific gravity (S<0.8)
with a mean boiling point greaterthan 1000 F.
Reliability
The equation reproduced experimental values
of smoke pointto within an average error 6.3
of percent.
Literature Source
American Petroleum Institute, Documentation
Report API-2-98.
Example
Determine the smoke point of a petroleum M o n having a specific gravity of 0.853 and a mean
average boiling point of 414.5F.
459.6)'"
= 11.21
0.853
Calculate the smoke point fiom equation
(2B 10.1-1):
Using equation (2-0.8):
K =
(414.5
+
In SP = -1.028 + 0.474(11.21) - 0.00168(414.5 + 459.6) = 2.817
SP = 16.7 mm
An experimental valueis 17 mm.
1999
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2811.1
PROCEDURE 2B11.1
FREEZING POINT OF PETROLEUM FRACTIONS
Discussion
The following equation is used to estimate thefreezing point of petroleum fractions.
FRP = -2390.42 + 1826 S +122.49 K - 0.135 MeABP
(2Bll.l-1)
Where:
FRP
MeABP
K
S
= freezing point of petroleum M o n , R
= mean averageboiling point, R.
=Watson K factor.
= specific gravity of petroleum fraction, 60F/60F.
Procedure
Step 1: Obtain the specificgravity and mean average boiling point of the fraction.
Step 2: Calculate the WatsonK fixtor using Equation (2-0.8).
Step 3: Calculate the freezing point of the fraction using Equation (2B1 l . 1-1)
1999
2-38
--`,,-`-`,,`,,`,`,,`---
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Not for Resale
COMMENTS ON PROCEDURE 2B11.1
2B11.1
Equation(2Bll.l-l)wasevsluatadovclthc~~~raqgesab~points,mcanavaogc~~
points,andspacificgravities.
Range O f D a t a
- 0.90
725 - 1130
Freezing poing R
320 510
Specific grav
tiy,60F/60F
0.74
Mean avenge boiling poing R
Reliability
Literature Source
American Petroleum Institute, Documentation Report API-2-98.
--`,,-`-`,,`,,`,`,,`---
Tbe equation nproduccd experimental values of freezing point to within 7.2 depes Rankiae.
Example
Determine the freezing point ofa petroleumM o n with a mean average b o i point of 874.5R and
spccific gravity of 0.799at 60 F.
From equation (2-0.8), the Watson K factor is as follows:
-
FRP = -2390.42+ 182q0.799)+ lU.49(11.97) 0.135(874.5)
FRP= 417R
An expimental value is 409 R
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2B12.1
PROCEDURE 2B12.1
CLOUD POINT OF PETROLEUM FRACTIONS
Discussion
The following equationis used to estimate the cloud pointof petroleum íì-actions.
log CP = -7.41
+ 5.49
log MeABP - 0.712 MeABP0*315
- 0.133 S (2B12.1-1)
mere:
CP
MeABP
S
= cloud
point of petroleum fracton, R
= mean average boiling point, R.
= specific gravity, 60F/60F.
Procedure
Step I: Obtain the mean average boiling point and specificgravity.
Step 2: Calculate the cloud point
using Equation (2B12.1-1).
2-40
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Not for Resale
STD.API/PETRO T D B CHAPTER 2-ENGL L 7 9 7 M 0 7 3 2 2 9 0 Ob17575 Tqb M
COMMENTS ON PROCEDURE 2B12.1
2B12.1
Definition and Purpose
The cloud pointof a petroleum productis the temperature at which its solid paraffin content, normally
the oil to appear cloudy. The purpose
held in solution, begins to solid@ and separate in tiny crystals, causing
of this procedure is to predict the cloud pointof petroleum fractionsfiom the specificgravity and the mean
average boiling point. ProcedureASTM D97 is used to determine experimental valuesof cloud point.
Limitations
Quation (2B12.1-1) was evaluated with 834points of experimental data over the following ranges
of cloud point andmean average boilingpoint.
Range of Data
R
375 to 560
Specific gravity,60F/60F
0.77 to 0.93
point, Cloud
Mean average
boiling
point,
R
800 to 1225
The equationcan be reasonably extrapolated beyond
the tested data range.
Reliability
The equation reproduced experimental values
of cloud pointto within 7.4 degrees Rankine.
Literature Source
American PetroleumInstitute, Documentation Report API-2-98.
Example
Determine the cloud point
of a petroleum fraction
having a mean average boiling point
of 8 1 1.5 R and
specific gravity of 0.787.
-
Calculate cloud point using equation
(2B 12.1 1)
-
log CP = -7.41 + 5.49 log (811.5) 0.712(811.5)0.3’5
- 0.133(0.787) = 2.584
CP = 383.7 R
The experimental valueis 383.4 R.
2-41
1999
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2613.1
PROCEDURE2B13.1
CETANE INDEX OF PETROLEUM FRACTIONS
Discussion
The following equation
is used to calculate the cetane index
of petroleum fractions.
CI = 415.26- 7.673 API + 0.186 MeABP + 3.503 API log MeABP
(2B13.1-
- 193.816 log MeABP
Where:
CI
API
MeABP
= cetane
index of petroleum fraction.
= API gravity.
= mean averageboiling point, F.
Procedure
--`,,-`-`,,`,,`,`,,`---
Step 1: Obtain the APIgravity and mean average boiling pointof the petroleum fiaction
Step 2: Calculate the cetaneindex using Equation(2B13.1-1).
1999
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2B13.1
COMMENTS ON PROCEDURE 2B13.1
Definition .ad Purpose
The cetane index is the number cqual to the percentage of cetane in a blend of cetane and alpha methyl
naphthalene having the same ignition quality as a sample of the petroleum hction. The purpose of this
procedure is to predict the cetane index of petroleum fiactions fiom the A P I gravity and the mean average
--`,,-`-`,,`,,`,`,,`---
bolhg point.
T k equation is not recommended for mean average b
o-
points 250 F.
Reliability
Tbc quation reproducedvalues ofcetane index to within an average mor of 29 % for 150 data p o i n t s .
Literature Source
American Petroleum Institute, Documentation Report API-2-98.
Example
Dcterrnine the cetane index of a petroleum M o n having an API gravity of 32.3and ASTM D86
mean average b o i g point of 6 17 F.
Using equation (2B13.1- I),
CI=415.26 7.673 (32.3) + 0.186(617) + 3.503 (32.3)1% (617) 193.816 i q ( 6
= 57.1
An txptrimcntal value is 56.
-
-
2-43
1999
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~~
~
~
~
STD.API/PETRO T D B CHAPTER E'-ENGL 1797 W 0732270 Oh19578 7 5 5 W
2614.1
PROCEDURE 2B14.1
SMOKE POINT - ANILINE POINT INTERCORRELATION
Discussion
The following equations are used to estimate the smoke point
or aniline pointof petroleum friictions.
SP = -3500+ 3522 S (1 + 8.234x lo5 Ap) - 3021 ln@)
AP
=
1.214 x
lo4
[
+
3500 + 3021 ln S
35228
-4
(2B14.1-1)
(2B14.1-2)
Equation (2B14.1-2)is simply an algebraic rearrangementofEquation (2B14.1-1).
Where:
SP
S
AP
=
=
=
smokepoint, mm.
specific gravity, 60F/60F.
anilinepoint, F.
Procedure
--`,,-`-`,,`,,`,`,,`---
Step 1: Obtain the specific gravity and aniline pointor smoke pointof the petroleumfraction.
Step 2: Calculatethesmokepoint or aniline point usingEquation (2B14.1-1)or (2B14.1-2),
respectwely.
1999
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2B14.1
CoMMENTS ON PROCEDURE 2B14.1
Rmge OfDara
15 to 42
112 to 170
0.76 to 0.86
The equation reproducedexperimental values of smoke point to within an average absolute
deviation and average absolute percent errorof 1.7mm and 7.3%, respectively. Note that Equations
(2B14.1-1)and (2B14.1-2)should be used only when Procedure2 2B10.1or 2B9.1are applicable.
Liraturc Source
Amcrican PetroIeum Institute, Documentation Report API-2-98.
Example
Determine tbe smoke point of a petroleum fraction given a specific gravity of 0.839 and aniline point
of 128.2 F.
Using equation (2B14.1):
-
SP -3500 + 3522(0.839)(1+ 8.234 X 1Vs(128.2)] 3021 ia (0.839) 16.5
2-45
1999
--`,,-`-`,,`,,`,`,,`---
Copyright American Petroleum Institute
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Not for Resale
~
~~~
~
STD*API/PETRO TDB CHAPTER 2-ENGL
~~
L997
~~~~
0 7 3 2 2 9 0 O b 1 7 5 8 0 303
PROCEDURE 2B14.2
CLOUD POINT POUR POINT INTERCORRELATION
2B14.2
-
Discussion
Tbc fillowing equation is UECd to estimate the cloud point or pour point of petroleum fi.actioasifthe
mdhodsofProceduns2B8.1.Dd2B12.1uurnaCbcusad.
PP = 0.9895 CP + 1.4
(2B14.2-1)
P P = paupoint,R
CP= ckudppoinSR
Procedure
step I : Obtain the pour point or cloud point of the petroleum fraction.
Step 2: Calculate the pour point or the cloud point of the petroleum W o n using Equation (2B14.2-1).
2-46
--`,,-`-`,,`,,`,`,,`---
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S T D . A P I / P E T R O T D B C H A P T E R 2-ENGL L997 E 0732290 ObL958L 2 q T
COMMENTS ON PROCEDURE 2B14.2
2B14.2
Purpose
The purposeof this procedure is to predict cloud point
or pour point fÌom the other when
pameters
are not available fordirect prediction from Procedures 2B 12.1 or 2B8.1, respectively.
Limitations
Equation (2B14.2-1) was evaluated over thefollowing data ranges of pour points and cloud
points.
Range of Data
point,
Cloud
R
370 to 570
Pour point, R
370 to 570
The procedure should not
be used to predict pour point unless parameters
are not available to use Procedure
2B8. l. In this case useProcedure 2B12.1 to predict cloud point and then
this procedure to predict pour point.
Reliability
The equation reproduced experimental values of cloud point and pour point to within an average
absolute deviationof 2.2 degrees Rankine for2 13 data points.
Literature Source
American PetroleumInstitute, Documentation Report API-2-98.
Example
--`,,-`-`,,`,,`,`,,`---
Determine the pour point of a petroleum fraction having a cloud point of574 Rankine.
Using equation (2B14.2-1):
PP = 0.9895(574) + 1.4 = 569.4 R
An experimental pour point value
is 565 R.
2-47
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2815.1
PROCEDURE 2B15.1
FLASH POINT BLENDING
Discussion
The Wickey-Chittenden blending model
is used to calculate theflash point of a petroleum blend. The
model requires flash point indices calculatedí?om the following equation:
1% FBP4 = -6.1 188 +
4345.2
+ 383.0)
(FP,
(2B15.1-1)
mere:
FPBI, = flash point blending indexfor component i.
FP,
= flash point for component i, F
The blend's index can be calculated by volumetrically averaging the flash point blending indices of each
component using equation2B15.1-2.
FPBI,
=
2 xviFPBI,
(2B15.1-2)
--`,,-`-`,,`,,`,`,,`---
i- 1
Where.
FPBI, = flash point index of the total blend
X
vi
n
= volumetricfraction of component I
= number
components
of
Rearranging equation(2B15.1-1), the flash point ofthe blend is found using equation(2B15.1-3).
FP,
=
4345.2
- 383.0
[log(FBPI,) + 6.1 1881
(2B15.1-3)
Procedure
Step 1:
Step 2:
Step 3:
Step 4:
Determine theflash point and volumetric fì-action for
each component in the blend.
Calculate theflash point blending indexfor each fraction from equation (2B15.1-1).
Determine the total blend's index from equation (2B15.1-2).
Determine theflash point of the blend from the total blend's index using equation
(2B15.1-3).
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COMMENTS ON PROCEDURE 2B15.1
Purpose
2615.1
The purpose of
this procedure is to predict the flash point
of blends of petroleum fractions using the
Wickey-Chittenden blending model.
Limitations
Wickey and Chittenden evaluated the blending procedure
for binary andternary systems, with blended
flash points rauging from 78 F to 543 F. Although good results were reported for blends of components
varying by as much as 345 F,the procedure is not recommended for blends of very lightnaphtha and asphalt.
The procedureis not recommended for interblending open and closed cup flash points. Caution also should
be taken with systems containing morethan 3 blend components.
Reliability
The procedure reprodud values of flash points
to within an average absolute deviation
of 6 F for 162
blends. The authors noted,71% of the deviations were within the reproducibility of the flash test.
point No
further testingwas conducted by theAPI project e.
Literature Source
--`,,-`-`,,`,,`,`,,`---
Wickey, R O., and Chittenden, D. H., "Flash Points of Blends Correlated," Hydrocarbon Processing
and Petroleum Refiner, 42(6), 157 (1963).
Example
Determine thefinalblend's flash point when combiningstreams X and Y in the following proportions:
25% by volume ofstream X with a flash pointof 172 F
75% by volume ofstream Y with a flash point of
325 F
Using equation(2B15.1-1) for stream X,
log (FPB1,J = -6.1188 + [4345.2/(172+383)] = 1.710
FPBI, = 5 1.33
Similarly for stream Y,
FPBI, = 1.04
The flashpoint blending indexfor the total blend is then calculatedfrom equation (2B15.1-2).
FPBIB = (0.25)(53.11) + (0.75)(1.04) = 13.61
Using equation(2B15.1-3), the flash point of the blend is,
-
FPB = [4345.2hog (13.61 + 6.1188)] 383 = 216 F
1999
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~~
2-49
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S T D - A P I / P E T R O T D B C H A P T E R 2-ENGL L797 D 0732290 Ob19584 T 5 7 m
1.
Baird, C. T., "Guide to Petroleum Product Blending," HP1 Consultants, Inc., Austin,
TX (1989).
2.
Chevron Research Company, Private Communication
(1971).
3.
Gary, J. H.,
and Handwerk, G. E.,"Petroleum Reíïning, Technology and Economics," M. Dekker,
New York (1975).
4.
Hu, J., and Burns, A. M.,"New Method PredictsCloud, Pour, and Flash Points
ofDistillate Blends,"
Hydrocarbon Processing, 49( 11) 2 13 (1970).
5.
Huang, P. K., "CharacterizationandThermodynamicCorrelations for Undehed Hydrocarbon
Mixtures," Ph.D. Thesis, Departmentof Chemical Engineering,The Pennsylvania State University,
University Park, PA 1977.
6.
Jackman, J. R., "Are Aniline Points Additive?," Ethyl
Cop., memorandum (1982).
7.
Lee, B. I., Kesler, M. G.,"A Generalized "hemodynamic Correlation Based on Three-Parameter
Corresponding States,"AZChE Journal 21 510 (1975).
8.
Maurin, Henri, "Programmation Lineaire Appliquee,"Editions Technip. Paris,353 (1967).
9.
Maxwell, J. B., Data Book on Hydrocarbons,D.Van NostrandCo., Inc., Princeton,NJ (1950).
10.
Pitzer, K. S.,"The Volumetric and Thermodynamic Propertiesof Fluids-I: Theoretical Basis and
Virial Coefficients,"J Am. Chem. Soc. 77 3427 (1955).
11.
Pitzer, K. S.,Lippmann, D. Z., Curl, R.F.,Jr., Huggins, C. M., Petersen, D.
E., "The Volumetric and
Thennodynanuc Properties of Fluids-II: Compressibility Factor, Vapor Pressure, and Entropy of
Vaporization,"J Am. Chem. Soc. 77 3433 (1955).
12.
Reid, E. B., Allen, H. I,, "EstimatingPour Pointsof Petroleum Distillate Blends,"
Petroleum RejTner
30(5) 93 (1951).
13.
M. R., "Prediction of Thennophysical Properties of Petroleum Fractions," Ph.D. Thesis,
Deparhnent of Chemical Engineering, The Pennsylvania
State University, University Park, PA1979.
14.
Riazi, M.R.,Private Communications (1985,1986).
15.
Riazi, M.R., Daubert, T.E.,"Prediction of the Composition of Petroleum Fractions,"Zd. Eng.
Chem. Process Des. Dev. 19 289 (1980).
16.
Smith, R. L.,Watson, K. M., "Boiling Points
and Critical Properties of Hydrocarbon Mixtures,"Id.
Eng. Chem. 29 1408 (1937).
Riazi,
2-50
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--`,,-`-`,,`,,`,`,,`---
REFERENCES
17.
Thiele, E.W., "Predictionof Flash Points of Blends of Lubricating Oils," lnd.Eng. Chem. 19 259
(1927).
18.
Unzelman, G. H., "NewCetane Data Reveals Surprises, Challenges,"Oil Gas Journal Sl(46) 178
(1983).
19.
Watson, K.M.,Ne.lson,E. F., "improvedMeth& for ApproximatingCriticaland The& Properties
of Petroleum Fractions,"I d . Eng. Chem. 25,880 (1933).
20.
Wickey, R.O., Chittenden, D.H., "Flash Pointsof Blends Correlated,"Hydrocarbon Processingand
Petroleum Refiner42(6) 157 (1963).
21.
Winn, F., W., "PhysicalProperties by Nomogram,"Petrol. Refiner 36(2) 157 (1957).
22.
Woodle, R.A., "New Ways to Estimate Characterization of Lube Cuts,"Hydrocarbon Processing
59(7) 171 (1980).
23.
Zhou, P.,"Correlationof theAverageBoilingPoints
Constants," Inf. Chern. Eng. 24 731 (1984).
of PetroleumFractions With Pseudocritical
--`,,-`-`,,`,,`,`,,`---
2-51
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1.155 W
CHAPTER 3
PETROLEUM FRACTION
DISTILLATION INTERCONVERSIONS
Revised Chapter 3 to 5th Edition (1992)
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PREFACE
The subject of distillation has been of continuing concern in the design and operation of
petroleum refineries and related industries. Most of the procedures for interconversion of
various distillation data in the previous editions were developed in the 1940s and 1950s.
During the past two years, continued interest has led to the development of new analytical
correlations for conversion of various distillation data. Detailed results of the methods tested and developed in the course of this work, together with the rationale for inclusion of the
procedures in this chapter, are available in Documentation Report No. 3-93 available from
University Microfilms, Inc., Ann Arbor, Michigan.
The majority of work on thischapter was carried out by Thomas E. Daubert assisted by
Nancy Crane Dauben. The chapter coordinating committee for the Technical Data
Committee was Arthur E. Ravicz of Chevron Research and Technology Company, Chair;
Sheldon J. Kramer of Amoco Oil Company, Dale Embry of Phillips Petroleum Company,
and Peter Nick of Unocal.
Thomas E. Daubert
Department of Chemical Engineering
The Pennsylvania State University
University Park, PA 16802
June 1993
...
111
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CHAPTER 3
PETROLEUM FRACTION DISTILLATION INTERCONVERSIONS
PAGE
3.0 Introduction . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .
Figure 3-0.1TypicalASTM
D86 and Simulated Distillation
Curves for a Petroleum Fraction . . . . . . . . . . . .
Figure 3-0.2
ASTM, True Boiling Point, and Equilibrium
Flash Vaporization Distillation Curves for a
Naphtha-Kerosine Blend . . . . . . . . . . . . . . . . . .
Figure 3-0.3
Distillation Conversion Routes . . . . . . . . . . . . .
Table
3-0.4
Summary of Correlations for Converting
Distillation Data .........................
3A ASTM, True Boiling Point and Simulated Distillation Relationships
3A1. ASTM and True Boiling Point Distillation Relationships at
Atmospheric Pressure
Procedure 3Al.l Interconversion of ASTM D86-TBP
Distillations at Atmospheric Pressure . . . . . . . .
3A2. ASTM and True Boiling Point Distillation Relationships at
Subatmospheric Pressures
Figure 3A2.1
Subatmospheric ASTM Distillation and True
Boiling Point Distillation Relationship at
lOmmHg(1.33Wa) . . . . . . . . . . . . . . . . . . . .
3-1
3-1
3-2
3-3
3-5
3-7
3-11
3A3. ASTM, TBP, and Simulated Distillation Relationships at
Atmospheric Pressure
Procedure 3A3.1 Conversion of Simulated (ASTM D2887) to
TBP Distillations at Atmospheric Pressure . . . . 3-13
Procedure 3A3.2 Conversion of Simulated (ASTM D2887) to
ASTM D86 Distillation at Atmospheric
3-17
Pressure ...............................
3-21
Bibliography . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .
3-23
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3A4. Distillation Interconversions
Procedure 3A4.1 Interconversion of Distillation Data for
Petroleum Fractions at Subatmospheric
Pressures ..............................
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CHAPTER 3
PETROLEUM FRACTION DISTILLATION INTERCONVERSIONS
3.0 INTRODUCTION
ASTM and true boilingpoint
(TBP) analytical distillations are used to define the volatility characteristics of
petroleum fractions and other complex mixtures. Both are
batch distillations which differ mainly in the degree of
fractionation obtained during the distillation.
ASTM D86 and D l 160 distillations are run in an Engler
flask. No packing is employed, and reflux results only from
heat losses through the neck of the flask. ASTM distillations
are more widelyusedthan TBP distillations because the
former are simpler, less expensive, require less sample, and
require only approximately one-tenth as much time. ASTM
distillations are standardized. TBP distillations vary appreciably in procedure and apparatus.
ASTM distillation methods in use today are:
ASTM Method 086: This method is used for the distillation
of motor gasolines, aviation gasolines, aviation turbine
fuels, naphthas, kerosines, gas oils, distillate fuel oils, and
similar petroleum products. It is carried out at atmospheric
pressure. An exposed thermometer is used, andtemperatures are reported without stem corrections. ASTM D86
distillations are plotted in volume percent.
of 5. The method is a form of true boiling point distillation
for any petroleum mixture boiling above light naphthas and
mixtures with finalboiling points below 750 F.
ASTM Method 03710: This method isusedto
determine
the boiling range distribution of gasolines which do not
exceed an atmospheric pressure final boiling point of 500 F.
It is a gas chromatographic method otherwise similar to
D2887.
In ASTM D86, Dl 160, and D2892 distillations there may
be a residue left in the distillation equipment as well as a
difference between the volume of the original charge and the
sum of the distillate and residue. This difference is usually
termed “loss” and is generally thought of as volatile components of the charge which have not been recondensed. For
preparation of an ASTM distillation for conversion to a TBP
distillation, the percent distilled at the reported temperature
is thesum of the distillate collected and the loss.
When heated sufficiently hot,petroleum fractions undergo
thermal cracking. Although a function of chemical composition, the amount and severity of thermal cracking increase
800
ASTM Method 01160: This method is used for heavy
petroleum products whichcan be vaporized partiallyor
completely at a maximum liquid temperature of 750 F at
absolute pressures down to 1 mm Hg and condensed at the
pressures of the test. It is carried out at pressures between
1 mm Hg and 50 mm Hg, absolute. Temperatures are measured with a thermocouple. ASTM D1160 distillations are
plotted in volume percent.
ASTM Method 02887: Simulated distillation (SD) by gas
chromatography appears tobe the most simple, reproducible, and consistent method to describe the boiling range
of a hydrocarbon fraction unambiguously. This method is
applicable to all petroleum fractions with a final boiling
point of 1000 F or less at atmospheric pressure. The method
is also limited to samples having an initial boiling point of
at least 100 F. Figure 3-0.1 shows a typical relation between
ASTM D86 and ASTM D2887 distillations for a petroleum
fraction. Simulateddistillationsareplotted
inweight
percent.
ASTM Method 02892: This method is used for distillation
of stabilized crude petroleum defined as having a Reid
vapor pressure less than 12 psi. It employs a fractionating
column of 14-18 theoretical stages operated at a reflux ratio
700
W‘
3
ta
E
ec
500
400
300
200
O
20
40
60
80
100
PERCENT VAPORIZED
Figure 3-0.1-Typical ASTM
D86 and Simulated Distillation Curves for a Petroleum Fraction
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with increasing boiling point, contact time, pressure and
temperature. Early editionsof this chapter included acorrection for cracking for observed ASTM
D86 temperatures above
475 F. No correction forcracking is now recommended.
TBP distillations are performed in columns with 15to 100
theoretical plates at relatively high reflux ratios (i.e., 5 to 1
or greater). The high degree of fractionation in these distillations gives accurate component distributions for mixtures.
The lack of use of a standardized apparatus and operational
procedure isa disadvantage, butthevariations
between
various laboratories are small because a close approach to
perfect separation by boiling point is usually achieved. A
TBP curve is also shown in Figure 3-0.2 for comparison with
an ASTM D86 distillation.
An equilibrium flash vaporizationis an experiment carried
out at constant pressure to determine the temperaturevolume percentdistilled relation. The EFV curve is a plot of
temperature against percent by volume of liquid distilled, at
a constantpressure. Each point on the EFV curve represents
a separate equilibrium experiment. The number of equilibrium experiments needed to define all portions of the EFV
curve varies with the shape of the curve. Normally, at least
five such experiments are required. Figure 3-0.2 also shows
the EFV curves of a naphtha-kerosine blend at atmospheric
and several superatmosphericpressures compared to ASTM
D86 and TBP distillations. The tedious procedures necessary
to obtain experimental EFV data have madethis type experiment quite rare at this time. Thus, correlations involving
EFV have been eliminated from this chapter.
Users are emphatically cautioned against relyingheavily
on results obtained from these correlations. Because of a
lack of standardization and other inherent inadequacies in
the methods, the existing ASTM, TBR and SD data on the
same fractions are not suficiently precise or consistent to
developaccuratecorrelations.Consult
the Comments on
each Procedurefor the accuracyof euch method beforeuse.
The correlations of this chapter were developed usingdata
for hydrocarbon stocks and fractions which included many
components and exhibited smooth distillation curves. The
correlations do not apply to mixtures of few compounds with
widely differentboiling points.
A schematicdiagram of the interconversionprocedures is
shown in Figure 3-0.3.
Correlations are summarized in Table
3-0.4.
Correlations in this chapter are empirical in nature andare
arranged according tothevariouspairsbetween
ASTM,
TBP, and SD relations.
Section
ASTM-TBP
3A1
(Atmospheric)
Section
ASTM-TBP
3A2
(Subatmospheric)
Section 3A3
SD-TBP-ASTM (Atmospheric)
Section 3A4
Interconversionsat Subatmospheric
Pressures
Use of Procedures
20
40
60
80
VOLUME PERCENT DISTILLED
1 O0
Source: Edmister and Pollock, Chern. Eng. Progr. 44 905 (1 948)
Figure 3-0.2-ASTM, True Boiling Point, and Equilibrium
FlashVaporizationDistillationCurvesforaNaphthaKerosine Blend
Procedures in this chapter are interconnected and are in
most respects consistent. In addition, all predicted distillation curves are of the correct shape. Careful study of Figure
3-0.3 and Table 3-0.4 gives the method(s) to be used
for each
conversion. It should be noted that in somecases alternative
paths are possible. The narrative belowdescribes the procedures to be used in each case.
Procedure 3A l. 1 (Step 1) allows interconversion between
ASTM D86 and TBP distillations. Expected average errors
are given inthe Comments.
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API TECHNICAL DATA BOOK
92
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m
m
07322900552724759
API TECHNICAL DATA BOOK
ASTM D2887lD371O
SIMULATED
DISTILLATION
(GAS CHROM.)
I
3
ASTM D86
760 m m
*
TBP
760 m m
5
'I
TBP
5
+
TBP
5
Subatmospheric
10 m m
b
-
2
I
1
--`,,-`-`,,`,,`,`,,`---
ASTM D l160
I
ASTM D l 160
5
Subatmospheric
10 m m
L
STEP
1
2
3
4
5
PROCEDURE
3A1.1
3A2.1
3A3.1
3A3.2
3A4.1
ASTM D1160
reported
at
760 mm
Figure 3-0.3-Distillation
Conversion Routes
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API TECHNICAL DATABOOK
Procedure 3A3.1 (Step 3) allows direct interconversion of
ASTM D2887 (Simulated) and TBP distillations with excellent accuracy as shown in the Comments.
ommended for development of a TBP distillation curve if
neither an ASTM D86 or simulated distillation are available
as the curve, though reasonably shaped, was not able to be
verified since insufficient experimental data were available.
Procedure 3A3.2 (Step 4) relates ASTM D2887 (Simulated) and ASTM D86 distillations with accuracy as given
in the Comments. This conversion route should not be used
for fractions with D86 distillation temperatures above
600 F.
Equilibrium flash data, while probably more reproducible
thanASTMand
TBP data, are obtained usingdifferent
types of apparatus and many variations in procedure. A
computer method for flash calculations and estimation of
equilibrium K-Values for petroleum fractions using a modified Soave-Redlich-Kwong (6) equation of state is included
in Chapter 8.
--`,,-`-`,,`,,`,`,,`---
The conversion of Simulated to TEP distillations can also
be carried out in two steps (4and 1 ) with little degradation
of the prediction. See discussion in Procedure 3A3.1.
NOTE: A report which documents the basis upon which material
the
in all editions of this chapter was selectedhas been published by the
American Petroleum Institute as Documentation Reports No. 3-66,
No. 2.3-86, and No. 3-93. All data used for development of prediction methods are referencedin these reports.
Figure 3A2.1 (Step 2) allows conversionofASTM
Dl 160 to TBP distillations at 10 mm mercury total pressure
after which Procedure 3A4.1 (Step 5 ) can be used to convert
the TBP to atmospheric pressure. This method is only rec-
TABLE 3-0.4”SUMMARY OF CORRELATIONS FOR CONVERTING
DISTILLATION DATA
Data Available
Data Desired
Pressure,
Type
ASTM D2887 (SD)
ASTM D86
ASTM D1 160
ASTM
10
1601 D
ASTM Dl 160
TBP
ASTM D2887 (SD)
ASTM Dl 160
ASTM D1 160
ASTM D 1 160
ASTM D1 160
mm Hg
760
760
10
10
10
760
Type
ASTM D86
TBP
TBP
TBP
ASTM D86
TBP
TBP
Pressure,
mm Hg
Conversion Method
Steps in Fig. 3-0.3
760
4
760
1
10
2
760
2,5
760
2,5, 1
760
5
760
3
1
TBP
760
5,2,5
1
ASTM D86
TBP
ASTM D86
760
5,2,5, 1
760
5,2,5
760
5,2,5, 1
1O0
1O0
Note: All ASTM D86 temperatures at 760 mm Hg are observed values.
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3A1.1
PROCEDURE 3A1.1
INTERCONVERSION OF ASTM D86-TBP
DISTILLATIONS AT ATMOSPHERIC PRESSURE
Discussion
The following equation is used to convert an ASTM D86 distillation 50% point temperature to a
true boiling pointdistillation 50% point temperature.
TBP ( 5 0 ) = 0.87
180
(ASTh4 D86 (50) )
(3Al.l-1)
Where:
TBP (50) = true boilingpoint distillation temperature at 50 volumepercent distilled,
degrees Fahrenheit.
ASTM D86 (50) = observed ASTM D86 distillation temperatureat 50 volumepercent
distilled, degrees Fahrenheit.
To determine the difference between adjacentcut points, use the followingequation:
y
B
= AX,
(3Al.l-2)
Where:
Yi= difference in true boiling point distillation temperature between two cut points, degrees
Fahrenheit.
Xi= observed difference inASTMD86
distillation temperature between two cut points,
degrees Fahrenheit.
A,B = constants varying for cut point ranges, described as follows.
Maximum
Cut Point
Allowable
1
Range
A
B
X;, (F)
1
100% - 90%
O. 11798
1.6606
2
90% - 70%
3.0419
0.75497
I O0
3
70% - 50%
2.5282
0.82002
150
4
50% - 30%
3.0305
0.80076
250
4.9004
0.71644
250
5
30% - 10%
7.4012
0.60244
1O0
6
10%- 0%
TBP
TBP
TBP
TBP
TBP
TBP
(O)
(10)
(30)
(70)
(90)
(100)
= TBP(50j-Yq-Yg-Y6
= TBP (50)-Y4-Y5
= TBP (50) -Y4
= TBP (50) +Y3
= TBP (50) -k Y3 +Y2
= TBP (50) +Y3+Y2 +Y1
(3Al.l-3)
--`,,-`-`,,`,,`,`,,`---
To determine the true boiling point temperature at any percent distilled, add or subtract the proper
difference(s)from the predicted 50% true boilingpoint temperature.
Procedure
Step I : Use equation (3Al.l-1) to calculate theTBP distillation temperature at 50% distilled.
Step 2: Use equation (3A1.1-2) to calculate necessary TBP differences.
Step 3; Use equation(s) (3A1.1-3) to calculate desired TBP distillationtemperatures.
To determine the ASTM D86 distillation temperatures from the TBP distillation temperatures,
reverse theprocedure. Thus, equation (3A1.l- 1) becomes
(ASTM D86 (50)1 = exp
[ In (TBP (50) / 0.87 180)3
(3Al.l-4)
Similarly, all equations (3Al.l-2) can be reversed, and all equations (3Al.l-3) can be modified by
changing TBP toASTM.
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4b8
m
3A1.1
COMMENTS ON PROCEDURE 3A1.1
Purpose
The purpose of this procedure is to predict a TBP distillation at atmospheric pressure from an
ASTM D86 distillation or the reverse by hand or by computer.
Limitations
Because expenmental data on higher boiling fractions are quite scattered, all derivations were
carried out on fractions having an ASTM 50% point temperature of 480 F and below. However, the
correlation extrapolates well to fractions with ASTM 50%point temperatures up to 600 F. Care should
be taken in extrapolating above this point. In addition, initial and final boiling point data are scarce
and inaccurate. Thus, values for these points should be taken as rough approximations.
Reliability
Differences between the estimated and experimental TBP values at various volume % distilled
points are given below.
TBP (predicted) -TBP (experimental)
Volume % Distilled
Average
Bias
O
21.9 F
-7.8 F
10
9.0
-1.8
30
5.7
-0.4
50
4.7
-0.1
70
5.6
1.1
90
2.3
7.1
1O0
4.0
4.2
Seventy-one sets of data were used in development, although fewer points were available at the O and
100% points. Average error is defined as the sum of the absolute values of the differences between
predicted and experimental temperatures divided by the number of data points, while bias error sums
the actual values of the differences.
Special Comment
This method was derived from all data available to the project and was judged to be the most
appropriate form for interconversion among the various types of distillations. As additional data
become available, the constants in equations (3A1.1- 1 and 3A1.I-2) can easily be improved. In
addition, users may wish to check the correlation with their proprietary data before using it.
Literature Source
This method was developed by the M I Technical Data Book Project at The Pennsylvania State
University.
Example
Volume percent distilled ............
10
ASTM D86 temperature, F . . . . . .380
. . . . 350
TBP temperature, F . . . . . . . . . . . . . . . . 37321
50
404
49
1 447 409
30
70
433
--`,,-`-`,,`,,`,`,,`---
Estimate theatmosphericTBP
distillation temperatures for a petroleum fraction having the
experimental ASTM D86 distillation temperatures given in the following table. The experimental
TBP temperatures are given for comparison with the predicted temperatures.
90
469
1
Using equation (3Al.l-I)
TJ3P (SO) = 0.87180 (404)1~0258
= 41 1.2 F
Using equation (3A1.1-2) at the 30% point
Y4 = 3.0305 [X4]o.80076
where X, = 404 - 380 = 24 F
therefore, Y4 = 38.6 F
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3A1.1
Using equation (3A1.1-3) at the 30% point
TBP (30) = TBP (50) -Y4
= 41 1.2- 38.6 = 372.6 F
Similarly, using equations (3A1.1-2) and (3A1.1-3) at the other cut points,
Y2 = 45.5, Y, = 40.0, Y, = 56.0
TBP (10) = 372.6 - 56.0= 316.6 F
TBP(70) = 411.2+40.0=451.2F
TBP (90) = 451.2 + 45.5 = 496.7 F
The reverse conversion from experimental TBP temperatures to ASTMD86
illustrated only for the 50% and 30% points.
temperatures is
( 1 ) Use equation (3A1.1-4) to convert the experimental TBP SO% point temperature.
ASTM D86 (50) = exp
In (409/0.87180) = 401.9 F
1.0258
1
[
(2) Use equation (3A1.1-2) to determine the 50 to 30% ASTM increment.
X, = exp
[ln (Y4 /3.0305
,80076
)I
= 23.5 F
where Y4 = 409 - 37 1 = 38
(3) ASTM D86 (30) = ASTMD86 (50) - X ,
= 401.9 - 23.5
= 378.4 F
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3A2.1
240
ASTM D l 160 and TBP Distillation
220
50% TemperaturesAssumed
200
--`,,-`-`,,`,,`,`,,`---
180
LL
W
o
z
160
u
9
LL
140
k
W
u
3
120
L
a
n
W
a 100
SUBATMOSPHERIC
5
ASTM DISTILLATION
I-
CL
80
TRUE BOILING POINT
DISTILLATION RELATIONSHIP
60
ASTM D 1160 TEMP. DIFFERENCE
40
TECHNICAL DATA BOOK
20
O
O
20
40
60
80
1O0
120
140
160
180
200
220
240
ASTM D 1160 TEMPERATURE DIFFERENCE, F
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3A2.1
COMMENTS ON FIGURE 3A2.1
Purpose
This figure relates ASTM D1 160 and TBP distillationdata at 10 mm Hg absolute pressure.
Reliability
No quantitative evaluationof the correlation could be made becauseof lack of data. The original
reference indicates that temperatures from this method will be within
25 F of the actual values.
Special Comment
at mm Hg are assumed to be equal.
The ASTM D 1 160 and TBP 50-percent points 10
Literature Source
Adapted from Edmister and Okamoto,Petrol. Refiner 38 [9] 271 (1959); copyrightedin 1959 by
Gulf Publishing Company, Houston, Texas.
Example
Estimate the TBP curve at 10 mm Hg fora petroleum fraction having the following ASTM
D 1 160
distillation temperaturesat 10 mm Hg:
Distillation,
percent
Temperature,
F deg
volume
by
............
.....................
First, from Fig. 3A2.1, find the temperature differences
10 mm Hg:
Segment of Curve
(Percent by Volume)
10 to 30
30 to 50
50 to 70
70 to 90
30
400
10
300
70
550
50
475
90
650
for each segment of the TBP curve at
mm
Hg
10
ASTM D 1160
Temperature
Difference
(Degrees Fahrenheit)
100
75
75
1O Hg
mm
TBP
Temperature
Difference
(from Fig. 3A2.1)
Degrees Fahrenheit)
106
82
75
100
100
The TBP temperatures
are then calculated. The ASTM 1D160 and TBP distillation 50-percent temperatures are assumedto be equal at 10 mm Hg absolute pressure. Here, the 50-percent temperature
is 475 F:
--`,,-`-`,,`,,`,`,,`---
30-percent temperature = 475 - 82 = 393 F 70-percent temperature= 475 + 75 = 550 F
10-percent temperature= 393 - 106 = 287 F 90-percent temperature= 550 + 100 = 650 F
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3A3.1
PROCEDURE 3A3.1
CONVERSION OF SIMULATED (ASTM D2887)
TO TRUE BOILING POINT DISTILLATION
AT ATMOSPHERIC PRESSURE
Discussion
The true boiling point temperature at 50 volume percent distilled is taken to be equal to the
simulated distillation temperature at 50 weight percent distilled.
TBP (50)= SD (50)
(3A3.1-1)
Where:
TBP (50) = true boiling point temperature at 50 volume percent distilled, degrees Fahrenheit.
SD (50) = simulated distillation temperature at 50 weight percent distilled, degrees Fahrenheit.
To determine the difference between adjacent cut points, use the following equation.
wi
=
cyD
(3A3.1-2)
Where:
Wj = true boiling point temperature difference between two cut points, degrees Fahrenheit.
F = simulated distillation temperature difference between two cut points, degrees Fahrenheit.
C,D = constants varying for cut pointranges, described as follows.
Approximate
Maximum
Cut Point
Allowable
D
1
Range
C
y (F)
0.02 172
1.9733
30
1
100% - 95%*
0.97476
0.8723
2
95% - 90%
40
1.2938
75
90%3
- 70%
0.31531
4
70% - 50%
0.19861
1.3975
15
0.05342
1.6988
15
5
50% - 30%
15
0.01 1903
2.0253
6
30% - 10%
O. 15779
40
1.4296
1
10%- 5%
7
*approximate-use
with care
To determine the true boiling point temperature at any percent distilled, add or subtract the proper
difference(s) from the predicted 50% true boiling point temperature.
TBP
TBP
TBP
TBP
TBP
TBP
TBP
(5)
(10)
(30)
(70)
(90)
(95)
(100)
= TBP(50)-W5-Wg-W,
= TBP (SO) - W5 - W6
= TBP(50)-W5
= TBP(50)cWq
= TBP(50)+Wq+W3
= TBP(50)+ Wq+W3 +W,
= TBP (50) +W, + W3 + W2 +W,
(3A3.1-3)
Procedure
--`,,-`-`,,`,,`,`,,`---
Step 1: Use equation (3A3.1-1) to calculate the TBP at the 50% distilled point.
Step 2: Use equation (3A3.1-2) to calculate necessary TBP differences.
Step 3: Use equation(s) (3A3.1-3) to calculate desired TBP temperatures.
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~.
A P I C H A P T E R * 3 92
0732290 0552732 825
3A3.1
COMMENTS ON PROCEDURE 3A3.1
Purpose
The p u p s e of this procedure is to predict a TBP distillation at atmospheric pressure from a
simulated distillationby hand or by computer.
Limitations
700 F were used in deriving this correlation.
Data sets with TBP 50% points between 250 and
Although the correlation extrapolates well, useof the resulting temperature-% distilleddata outside
the limits is not encouraged. Also, as final boiling point data are not generally accurate, values for
these points should onlybe taken as rough approximations.
Reliability
Differences between the predicted and experimentalTBP temperatures at various % distilled points
are given below.
TBP (predicted)-TBP (experimental)
% Distilled
Bias
Average
2.1 F
5
21.7 F
0.2
10
19.7
.o
301
12.3
0.6
50
9.6
70
11.0
-1.4
-1.4
90
12.6
-2.6
95
12.1
1O0-8.0
8.1
Twenty-one data sets were used in development
of this procedure, except at the 100% point where
only 8 sets were available. The initial boiling point is not included,
as the data scatter isso great that
the correlation is meaningless.
Special Comment
This method was derived from all data available
to the project and was judged to be the most
appropriate formfor interconversion among varioustypes of distillations. As additional data become
available, the constants in equations (3A3.1-2) can easily be improved. In addition,users may wish
to check the correlation with their proprietary data before using it.
A two step procedure giving essentially equivalent results for materials with TBP temperatures
below 600 F consists of step 4 followed by step 1 of Figure 3-0.3. The table below shows an error
analysis, canied out on 19 sets of data for which ASTM D86, TBP, and SD were available, which
confirms this conclusion.This method should be limited to fractions boilingbelow 600 F.
Conversion of Simulated to TBP Distillation
Comparison of Two-step Procedure with One-Step Procedure-Error Analysis
%
Distilled
O
10
30
50
70
90
100
Data
Points
-29.0
18
19
19 -2.7
190.3
19
19
8
Conversion of SD to ASTM
D86 by Step 4 followedby
Conversion of Calculated
ASTM D86 to TBP by Step 1
Conversion of SD to
TBP by Step 3
Errors, F
Errors, F
Ave
32.3
12.2
8.4
7.4
9.0
11.3
5.6
Bias Bias
Ave
-9.20.2
19.7
12.3
9.6
11.0
12.6
8.1
0.6
2.3
3.0
4.5 -8.0
-1.4
-1.4
1994
3-14
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A P CI H A P T E R * 3
92
m 0732290 0552733 761W
3A3.1
Literature Source
This method was developed by the API Technical Data Book Project at The Pennsylvania State
University.
Example
Estimate the atmospheric TBP distillation temperatures for a petroleum fraction having an experimental simulated distillation as given in the following table. Experimental TBP temperatures are
given for comparisonwith the calculated temperatures.
% distilled . . . . . . . . . . . . . . . .
5
SD temperature, F . . . . , . . . . . 293
TBP temperature, F . . . , . . . . . 321
10
305
322
30
324
326
50
336
332
70
344
337
90
359
345
95
369
348
Using equation (3A3.1-1)
TBP (50) = SD (50) = 336 F
Using equation (3A3.1-2) at the 30% point
W5 = 0.05342[ V5]'.698*
whereV5 = 336 - 324 = 12
therefore W, = 3.6 F
Using equation (3A3.1-3) at the 30% point
TBP (30) = TBP - W5
= 336 - 3.6 = 332.4 F
Similarly, using equations (3A3.1-2) and (3A3.1-3) at other cut points
W, = 7.3 F
W, = 10.5 F
W,= 3.6 F
W6 = 4.7 F
W7 = 5.5 F
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TBP (95) = 350.1 + 7.3 = 357.4 F
TBP (90) = 339.6 + 10.5 = 350.1 F
TBP (70) =336 + 3.6= 339.6F
TBP (10) = 332.4 - 4.7 = 327.7 F
TBP ( 5 ) = 327.7 - 5.5 = 322.2 F
--`,,-`-`,,`,,`,`,,`---
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3-15
A P I CHAPTERN3 7 2
m
0732290 0552734 bT8
m
3A3.2
PROCEDURE 3A3.2
CONVERSION OF SIMULATED (ASTM D2887)
TO ASTM D86 DISTILLATION
AT ATMOSPHERIC PRESSURE
Discussion
The ASTM D86 temperature at the 50 volume percent distilled point may be calculated from the
simulated distillation temperature at the 50 weight percent distilled point.
ASTM (50) = 0.77601 (SD (50)
(3A3.2-1)
Where:
ASTM (50) = ASTM D86 temperature at 50 volume percent distilled, degrees Fahrenheit.
SD (50) = simulated distillation temperatureat 50 weight percent distilled, degrees Fahrenheit.
To determine the difference between adjacent cut points, use the following equation.
= ET
F
(3A3.2-2)
Where:
U i = ASTM D86 distillation temperature difference between two cut points, degrees Fahrenheit.
Ti= SD temperature difference between two cut points, degrees Fahrenheit.
E,F = constants varying for cut point ranges,described as follows.
Approximate
Maximum
Cut Point
Allowable
I
Range
E
F
T , (F)
1
100%- 90%
2.6029
0.65962
1O0
2
90% - 70%
1.2341
1O0
0.30785
1.4287
3
70% - 50%
O. 14862
1O0
4
50% - 30%
1 S386
0.07978
1O0
5
30% - 10%
0.06069
1.5176
150
6
10%- 0%
0.30470
1.1259
150
To determine the true boiling point temperature at any percent distilled, add or subtract the proper
difference(s)from the predicted 50% true boiling point temperature.
ASTM
ASTM
ASTh4
ASTM
ASTM
ASTM
(O)
(10)
(30)
(70)
(90)
(100)
AST" (50)-U4-U,-U,
= ASTM (50) -U4- U,
= AST" (50) -U4
=
= ASTM(50)+U3
= ASTM(50)+U3+U2
= ASTM(SO)+U3+U*+U1
(3A3.2-3)
Procedure
Step I: Use equation (3A3.2-1) to calculate the TBP at the 50% distilled point.
Step 2: Use equation (3A3.2-2) to calculate necessaryTBP differences.
Step 3: Use equation(s) (3A3.2-3) to calculate desired TBP temperatures.
1994
3-17
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92
m
07322900552735
534
m
3A3.2
COMMENTS ON PROCEDURE 3A3.2
Purpose
The purpose of this procedure is to predict ASTM D86 distillation temperature from simulated
distillation data by hand or by computer.
Limitations
Data sets with ASTM D86 50% points between 150 and 600 F were used in deriving this correlation. Although the correlation extrapolates well, use of the resulting temperature-% distilled data
outside the limits is not recommended. Some evidence shows errors to be significantly higher above
a 600 F boiling point. As initial and final boiling point data are inaccurate,values for these points are
only rough approximations and should not be used for design.
Reliability
Differences between the predicted and experimental ASTM D86 temperatures at various %
distilled points are given below.
% Distilled
3.2
0.9
O
10
30
50
70
90
100
TBP (predicted) -TBP (experimental)
Average
Bias
21.5 F
8.0 F
8.6
5.3
<o.1
7.8
4.5
-0.1
9.6
-1 .S
19.5
-9.6
Approximately 125 data sets were used in development.
Special Comment
This method was derived from all data available to the project and was proven to be the most
accurate form for interconversion amongalltypes
of distillations. As additional data become
available, the constantsin equations (3A3.2-1 and 3A3.2-2) can easily be improved. In addition, users
may wish to check the correlation with their proprietary data before using it.
Literature Source
This method was developed by the API Technical Data Book Project at The Pennsylvania State
University.
Example
................ O
SD temperature, F .......... 77
ASTM D86 temperature, F ... 104163
% distilled
10
93
134
30
50
148360285215
208
Using equation (3A3.2-1)
ASTM (50) = 0.77601 (215)1.0395 = 206.3 F
Using equation (3A3.2-2) at the 30% point
U4 = 0.07978 T41.5386
where T4 = 215 - 148 = 67
therefore U4 = 5 1.5 F
Using equation (3A3.2-3) at the 30% point
ASTM (30) = 206.3 - 51.5 = 154.8 F
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70
269
90
100
335
408
390
--`,,-`-`,,`,,`,`,,`---
Estimate the atmospheric ASTM D86 distillation temperature of a petroleum fraction having an
experimental simulated distillation as given in the following table. Experimental ASTM D86
temperatures are given for comparison with the calculated temperatures.
~~
A P I CHAPTERx3 92
m
0732290 0552736 470
3A3.2
Similarly, using equation (3A3.2-2) and (3A3.2-3) at other cut points
ASTM (100) = 334.0 + 28.6 = 362.6 F
ASTM (90) = 270.6 + 63.4 = 334.0 F
ASTM (70) = 206.3 + 64.3 = 270.6 F
ASTM ( I O ) = 154.8 - 26.5 = 128.3 F
ASTM (O) = 128.3 - 6.9 = 121.4 F
--`,,-`-`,,`,,`,`,,`---
U, = 28.6 F
U2 = 63.4 F
U, = 64.3 F
U, = 26.5 F
U6 = 6.9 F
1994
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A P I CHAPTER83 9 2
0732290 0552737
307
3A4.1
PROCEDURE 3A4.1
INTERCONVERSION OF DISTILLATION DATA FOR PETROLEUM
FRACTIONS AT SUBATMOSPHERIC PRESSURES
Discussion
The following procedure is recommended to convert ASTM or TBP distillation data between
subatmospheric pressures (usually 1, 10, 1 0 0 mm Hg) and between subatmospheric pressures and
atmospheric pressure (760 mm Hg).
Procedure
A. Data at Subatmospheric Pressure
Step I: Assume the Watson K of the petroleum fraction is 12, and convert the data using Procedure
5A1.19.
B. Data at Atmospheric Pressure
Step I: If the specific gravity and mean average boiling point are known or can be calculated,
determine the Watson K from the defining equation (2-0.8). Otherwise assume K = 12.
Step 2: Follow Procedure 5A1.19.
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--`,,-`-`,,`,,`,`,,`---
Step 2: Since the Watson K is set at 12, no Watson K correction isnecessary.
3-21
Not for Resale
3A4.1
COMMENTS ON PROCEDURE 3A4.1
Purpose
The purpose of this procedure is to convert petroleum fraction ASTM orTBP distillations from
one pressure to another up to atmospheric pressure. This procedureis intended for both desk and
computer use.
Limitations
Limitations are the same as given for Procedure 5A1.19.
Reliability
Reliability is the same as given for Procedure 5A1.19. If the Watson K is taken to be 12, larger
errors will result, especiallyfor highly aromatic fractions.
Example
Consider a 31.4' API Saudi Arabian crude for which extensive TBP data are available. Four
experimental TBP distillation data pointsare:
Measured TBP
Temperature, F
Pressure,
mm Hg
450
252
463
403
760
10
10
1
Volume
API
Gravity
% Distilled
30
34
58
62
44.5
40.8
26.3
24.7
Interconvert thesedata to distillation temperaturesat each of 1, 10, and 760 mm Hg pressure.
Although it is not necessary in this case, assume K = 12 and read results directly from Figure
5A1.20b.The measured temperature at one pressure canbeconverted to each of the other two
pressures. Theresults are given below:
Volume % Distilled
30
Pressure,
Hg mm
450*
760
10
403*
1
34
58
Temperature,
TBP
218
370 144
492
782
252*
175
62
F
742
463*
498
*Experimental values.
Each tabulation shows good consistency.
In this case, note that the actual Watson
K is calculablefor
For example, for the first point:
the first point and could be used with the full Procedure 5A1.19.
[ 141.5/(131.5
+ 44.31
= 12.06
The Watson K for the entire crude, assuming a MeABP of617 F, is 11.8 and could beused as an
estimate for all fractions distilled at subatmospheric pressure.
3-22
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--`,,-`-`,,`,,`,`,,`---
K = (450 + 460)
A P I CHAPTER*3 92
0732290 0552739
LBT
API TECHNICAL DATA BOOK
BIBLIOGRAPHY
--`,,-`-`,,`,,`,`,,`---
1. Dauben, T. E., Daubert, N. C., “Documentation of the Basis for Selection of the Contents of Chapter 3” in Technical Data Book-Petroleum
Refining. Documentation Report No. 3-93, University Microfilms, Ann
Arbor, Michigan.
2. Dauben, T. E.,Riazi, M. R., Danner, R. P., “Documentation of the
Basis for Selection of the Contents of Chapters 2 and 3” in Technical Data
Book-Petroleum Refining, Documentation Report No. 2,346, University
Microfilms, Ann Arbor, Michigan.
3. Edmister, W. C., Okamoto, K. K., “Applied Hydrocarbon Thermodynamics-Part 13: Equilibrium Flash Vaporization Correlations for Heavy
Oils Under Subatmospheric Pressures,” Perrol. Refiner38 [9] 271 (1959);
Applied Hydrocarbon Thermodynamics, 133, Gulf Publishing Company,
Houston, (1961).
4. Edmister, W. C., Pollock, D. H., “Phase Relations for Petroleum
Fractions,” Chem. Eng. Pmg,: 44 905 (1948).
5. Maslanik, M. K., Daubert, T. E., Danner, R. P., “Documentation of the
Basis for Selection of the Contents of Chapters 2 and 3 including Portions
of Chapters 3.4,and 8” in Technical Data Book-Petroleum Refining, Documentation Report No. 2-81, University Microfilms, Ann Arbor, Michigan.
6. Soave, G., Chem. Eng. Sci. 27 1197 (1972).
1994
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CHAPTER 4
CRITICAL PROPERTIES
--`,,-`-`,,`,,`,`,,`---
Revised Chapter 4 to First Edition (1966),
Second Edition (1970), Third Edition (1976),
and Fourth Edition (1982)
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Copyright O 1988 American Petroleum Institute
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0732290 0536433 T93
PREFACE
--`,,-`-`,,`,,`,`,,`---
In 1966 the first edition of the Technical Data Book-Petroleum Refining was
published by the American Petroleum Institute and
includeda chapter on the
estimation of the critical properties of hydrocarbons. The Subcommittee onTechnical Data of the Division of Refining, which was responsible for the publication,
noted at that time that there was a paucity of both data and correlations for the
criticalproperties of mixtures.Thisresulted
in aprojectbeinginitiatedunder
Professor Webster B. Kay at The Ohio State University to determine critica! properties of hydrocarbon mixtures. This project continued for six years and obtained
data on 120 different systems and in itself dwarfed all previous data available.
From 1970 to 1973, using all new data and correlations available, the Data Book
group in the Department of Chemical Engineering atThe Pennsylvania State University revised and extended Chapter4. Detailed results of the methods and of the
evaluations using the experimental data areavailable in Documentation Report No.
4-73 available from University Microfilms, Ann Arbor, Michigan. In 1980 Figures
4D3.1, 4D3.2, and 4D4.1 were replaced with Procedures 4D3.1 and 4D4.1. These
procedures are documented in Documentation Report No. 2-81 also available from
University Microfilms.
Themajor work on this chapter was carriedout by Mr. Calvin F.Spencer,
Research Assistant in Chemical Engineering, reportingto Drs. ThomasE. Daubert
in Chemical
andRonaldP.Danner.
Miriam K. Maslanik,ResearchAssistant
Engineering, aided in preparing the 1980 update. The chapter coordinator for the
Subcommittee on Technical Data was Joseph E. Wolfof Amoco Oil Company.
From 1983 to 1985, methods for prediction of critical properties for pure hydrocarbons and defined hydrocarbon mixtures were reevaluated leading to the current
revision. Mr. J. Richard Elliott, Research Assistant in Chemical Engineering, carged outmuch of the work. The revisions are documentedin Documentation Report
No. 4-85 available from University Microfilms. Dr. J. G. Spiro, Gulf Canada, Ltd.
was the chapter coordinator for the Technical Data Committee.
of critical properties of undefinedmixtures
In 1985 methodsforprediction
of Chemical
were reviewed and revised. Dr. M. R. Riazi,AssistantProfessor
Engineering,carriedoutthiswork.Revisionsaredocumented
in Documentation Report No. 2,3-86 available from University Microfilms. Dr. T. E. Daubert
directed the work and Dr. J.G. Spiro was coordinator for this portion of the work.
Thomas E. Daubert
Ronald P. Danner
Department of Chemical Engineering
The Pennsylvania State University
University Park, Pennsylvania 16802
September 1986
iii
1987
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CHAPTER 4
CRITICAL PROPERTIES
PAGE
4-0 Introduction .......................
Figure 4-0.1
Figure 4-0.2
Figure 4-0.3
Figure 4-0.4
Figure 4-0.5
Figure 4-0.6
Figure 4-0.7
Figure 4-0.8
Critical Locus for the Methane-n-Decane
System .........................................................
Critical Locus for the Ethyne-Ethene
(Acetylene-Ethylene) System and Envelopes for Four Binary Mixtures ...................
P-T Critical Loci of Binaries Containing a
Common Component and a Representative from a Homologous Series ...................
Excess Critical Temperature vs Composition for Representative Binary Systems .............................................................
4- 1
4-3
4-4
4-5
4-7
4-8
The Effect of Relative Size and Absolute
Molecular Weight on the Excess Functions .............................................................
4-9
Excess Critical Pressure vs Composition
for Representative Binary Systems ............. 4- 10
Critical Properties for Pure Hydrocarbons
Group Contribution Method for CalcuProcedure 4A 1.1
lating the Critical Temperature, Pressure,
and Volume of a Pure Hydrocarbon ............ 4- 13
Table4A1.2
Procedure 4A2.1
Table 4A2.2
Procedure 4A3.1
4B
Pressure-Temperature Diagram for a Mixture of Constant Composition Near the
Critical Point ...............................................
Critical Locus for the Ethane-n-Heptane
System and Envelopes for Three Binary
Mixtures ......................................................
Group Increments for Equations 4A l. 1 - 1
Through 4A 1. l-3 .........................................
Equation for Calculating the Critical Temperature of a Pure Hydrocarbon ..................
Values
of Coefficients for Equation 4A2.1- 1
for Calculating the Critical Temperature
of a Pure Hydrocarbon ................................
Equation for Calculating the Critical Volumeof a Pure Hydrocarbon ........................
4- 17
4-19
4-19
4-21
Critical Properties of Defined Mixtures
Procedure 4B l . 1
Method for the Critical Temperature of a
Mixture of Defined Composition ................ 4-23
Procedure 4B2.1
Method for the Critical Pressure of a Mixture of Defined Composition .......................
4-27
Figure 4B2.2
Critical Pressures of Binary Systems ContainingMethane ..........................................
4-3 1
--`,,-`-`,,`,,`,`,,`---
4A
4- 1
V
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W 0732290 053b415 Bbb
m
PAGE
Figure 4B2.4
Procedure 4B3.1
Procedure 4B4.1
Figure 4B4.1~
1
Figure 4B4.1-2
Figure 4B4.1-3
Figure 4B4.1-4
Figure 4B4.1-5
4C
Critical Pressures of Binary Systems ContainingCarbonDioxide ...............................
Critical Pressures of Binary Systems ContainingHydrogenSulfide ............................
Method for the Critical Volume of a Mixture of Defined Composition .......................
Alternate (Computer) Method for Critical
Properties of a Mixture of Defined Composition ........................................................
Critical Locus for Ethene-Ethyne
System .........................................................
Critical Locus for n-Octane Benzene
System .........................................................
Excess Critical Temperature .......................
Excess Critical Pressure ..............................
Excess Critical Volume ...............................
Critical Properties of Natural Gases
Figure4C 1 .1
True Critical Temperature of NaturalGas
Mixtures ......................................................
4D Critical Properties of Petroleum Fractions
Method for the Critical Temperature of
Procedure 4Dl . 1
Petroleum Fractions ....................................
True Critical Pressures of Petroleum FracFigure 4D2.1
tions .............................................................
Procedure 4D3.1
Figure 4D3.2
Procedure 4D3.3
Procedure 4D4.1
Figure 4D4.2
Procedure 4D4.3
Figure 4D4.4
Method for the Pseudocritical Temperature of Petroleum Fractions .........................
Pseudocritical Temperatureof Petroleum
Fractions ......................................................
True andPseudocritical Temperatures of
Mixtures Containing Both Identified
Hydrocarbons and Petroleum Fractions ......
Method for the Pseudocritical Pressureof
PetroleumFractions ....................................
Pseudocritical Pressure of Petroleum
Fractions ......................................................
True and Pseudocritical Pressuresof Mixtures Containing Both Identified
Hydrocarbons and Petroleum Fractions ......
True Critical Pressures of Petroleum
Fractions for Use Only withProcedure
4D4.3 ...........................................................
Bibliography ............................................................................................................
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4-32
4-33
4-35
4-38
4-42
4-43
4-44
4-45
4-46
4-49
4-53
4-55
4-57
4-59
4-61
4-65
4-67
4-69
4-71
4-73
--`,,-`-`,,`,,`,`,,`---
Figure 4B2.3
A P I TDB C H A P T E R * 4
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0732290 053b4Lb 7T2 H
CHAPTER 4
CRITICAL PROPERTIES
4-0 INTRODUCTION
baric or an isothermal path across the envelope so that
both bubble-pointanddew-pointcurves
are crossed.
For example, the constant pressure path of Case I between points I and 2 in Figure 4-0. l crosses the bubblepointcurve at A . Starting at I in thehomogeneous
liquid region, increasing the temperatureof the system
causesnochange
in the state of aggregation of the
mixture until the temperature corresponding topoint A
is reached. At this point vaporization begins,
and, as
the temperature is increased further, the liquid in the
system decreases in quantity while the vapor phase increases. Following the same path in the reverse direction, from point 2 in the homogeneous vapor region
towardpoint I , nochangetakes place in the vapor
phase until the dew-point curve is crossed at B, where
condensation of vapor commences. As the temperature
is reduced further, more vapor condenses until,
at point
A on the bubble-point curve, the system is completely
liquid.
The actual experimental or true critical temperature
and pressure of pure compounds andof mixtures are of
importance in determining existing phaseconditions
and permissible operating ranges of reactors and mass
transfer equipment such as distillation columns andextractors. Critical propertiesof pure compounds arealso
essential to calculatepseudocriticalproperties
used
throughout the Technical Datu Book in the theorem of
corresponding states(54) for the estimationof thermodynamic and volumetric properties
of mixtures. A pseudocritical or molaraverage propertyis a calculatedvalue
that cannot be measured under any circumstances.
Critical temperatures and pressures for pure hydrocarbons and a number of nonhydrocarbons are given in
Chapter 1. Critical compressibility factors are given in
Chapters 1 and 2.
The Critical State of Mixtures and
the Two-Phase Envelope
The conditions of equilibriumfor coexisting vapor
and liquid phases of a pure substance are defined on a
pressure-temperaturediagram by the vaporpressure
curve. This curve starts at the triple point,
where vapor,
liquid, and solid phases are in equilibrium, and ends at
the critical point. As the critical point is approached by
the coexisting phases, their properties approach each
other until they become identical
at the critical temperatureandpressure,where
a single homogeneous
phase is present.
In the case of homogeneous mixtures of liquids, vaporization at aconstantpressuretakesplaceovera
range of temperatures instead of at the single temperature associated with the vaporpressure
of pure
substances.Consequently,thevaporization
of multicomponent liquids requires two curveson the pressuretemperature diagram to define the boiling characteristics instead of a single vaporpressurecurve.To
illustrate,Figure 4-0.1 showsa part of apressuretemperature diagram for a hypothetical liquid mixture.
In this diagram, the two-phaseregion is enclosed by the
envelope L p M CT, which consists of the “bubble-point’’
curve, L p M C,and the “dew-point” curve,VT, C. Their
commonpoint, C, is the criticalpointat
which the
coexisting liquid and vapor become asingle homogeneous phase.
The significance of the bubble-point and dew-point
curves may be demonstrated by following either an iso-
~
~~~~
1
I CASE
IV
I
Figure 4-0.1-Pressure Temperature Dlagram for a
Mixture of Constant Composition Near the Critical Point
Not for Resale
~
8
TEMPERATURE
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~~~
I
LIQUID
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4
CASE II 1
A P I TDB CHAPTERa11 X * M 0 7 3 2 2 9 0 05361137 6 3 9
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Case II shows a typical example of vaporization or
condensation at constant temperature. In this case, between points 3 and D, the path is in the homogeneous
vapor region. Between D on the dew-point curve and E
onthebubble-pointcurve,condensationtakes
place
with rising pressure until, at E, the system is entirely
liquid. From E to point 4, the stateof aggregation of the
mixture is notchanged by theconstantly increasing
pressure.
One of the important characteristics of the pressuretemperaturediagrams of mixtures is thatthe curve
defining the envelope enclosing the two-phase region
can have maximum values of pressure and temperature
thatare notnecessarilycoincident
with the critical
point. This is illustrated in Figure 4-0.1, where a maximum pressure occurs at p M and a maximum temperature at T M .The maximum pressure, pM , is frequently
referred to as the cricondenbar, which is an abbreviation for the critical condensation pressure. Similarly,
the maximum temperature, T M ,is known asthe cricondentherm to indicate the critical condensation temperature. Etter andKay (16), Grieves and Thodos(19),
and Silverman and Thodos (54) have presented correlations for estimating these maximum values.
The points pM and TMon the bubble-point and dewpoint curves of Figure 4-0.1 make it possible to:
1. Follow an isobaric path at a pressure higher than the
III, which crosses the
critical pressure,suchasCase
bubble-pointcurve twice without crossing the dewpoint line.
2. Follow an isothermal path at a temperature
higher
than the critical temperature, such as Case IV, which
crosses the dew-point curve twice without crossing the
bubble-point curve.
These possibilities give rise to vaporizationandcondensation phenomena which differ from those of Cases
I and II, whose paths are respectively at a pressure and
a temperature lower than the critical pressure and temperature. In Case III, for example, the
isobaric path
between points 5 and 6 is at a pressure intermediate
between the critical
and
maximum
pressures
and
crosses the bubble-point curve at F and G. Because of
this, whether the temperature rises or falls, the initial
point of intersection with the bubble-point curve coincides with the beginning of vaporization for the path
being followed. Inasmuchas the pathmust return to the
homogeneous liquid phase without crossing the dewof
point curve, if it is continued to the second point
intersection, it is evident that vaporization must first
increase from zero, go through a maximum, and then
decrease to zero again upon its second crossing of the
bubble-point curve. In these circumstances, the part of
the isobaric path between points F and G which lies
between the point of maximum vaporization and G involves either condensationwith a rising temperature or
vaporization with a falling temperature,depending
upon the direction it takes. This anomalous behavior is
termed “isobaric retrograde vaporization”by Sage and
Lacey (60).
In Case IV, an isothermal path at a temperature between the critical temperature of the system and the
maximum onthe dew-pointcurve is takenbetween
points 7 and 8, in the homogeneous vapor region. This
path crosses the dew-point line at H and J giving rise to
somewhat similar anomalous vaporization and condensation phenomena as that illustrated by Case III. Because this case is associated with the dew-point curve,
Sage and Lacey refer to this anomaly as “isothermal
retrogradecondensation.” Foramoredetailed
discussion of the retrograde phenomena associated with
the two-phase region near thecritical point of mixtures,
the readeris referred to Katz and Kurata (24), and Sage
and Lacey.
The Critical Locus
The two-phaseenvelopeillustrated in Figure 4-0.1
representsthepressure-temperaturerelationships
in
the critical region for a mixture having a defined composition. Any change in the composition of the mixture
is reflected in changes in the curves enclosing the twophase region. Thecritical temperature and pressure will
change, and the maximum pressure and temperature
and the slopes of the bubble-point and dew-point lines
will all be different.
Figure 4-0.2 illustrates the effects of changes in composition on the shapeof the two-phase envelope and its
associated variables.The figure represents the pressuretemperaturediagrams of Kay (26) forethaneand
n-heptane and three mixtures in the critical region. Of
the three two-phase envelopes
given in Figure 4-0.2, the
one indicated by the symbol C, for the binary mixture
containing 9.78 percent by weight ethane is the one that
approaches most closely the diagram presented in Figure 4-0.1 for a hypothetical mixture.In those labeled C,
and C, there are conspicuous differences in all of the
varibles mentioned previously. The change of position
of the critical point relative to the maximum values of
temperature and pressure found on the three envelopes
shown is of concern here. Comparison of the three envelopes presented in Figure 4-0.2 with that of Figure
4-0.1, for example, shows that the critical point apparently can be located anywhere around the
closed end of
the envelopebetween the vicinities of A and H in Figure
4-0. l . When the mixture containsa relatively high proportion of the light component, the critical point will
probably be found between points A and E in Figure
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--`,,-`-`,,`,,`,`,,`---
TEMPERATURE, F
Curve
c
2
C,
C,
C C
C,
Ethane
(Percent
by Weight)
100.0
90.22
50.25
9.78
0.00
Symbols:
C = critical point.
B = bubble-point line.
D = dew-point line.
Figure 4-0.2-Critical Locus for the Ethane-n-Heptane
(23)
System and Envelopes for Three Binary Mixtures
4-0.1. Whentheconcentration
of the volatilecomponent is smaller than that of the less volatile one, the
critical point will probably lie between E and H in Figure 4-0.1. One of the consequences of this variation in
the relative positions of critical points, cricondenbars,
and cricondentherms is that the character of the retrograde phenomena described previously varies for each
case. The types of retrograde phenomena described in
association with Figure 4-0.1, for example, are onlytwo
out of a totalof eight possibilities describedby Sage and
Lacey, if the full range of compositions between light
and heavy components is considered.
The broken line of Figure 4-0.2, connecting the critical point of ethane with that of n-heptane and drawn
tangenttoeach
compositionenvelope at its critical
point, is known as the critical locus. On such a locus
only one critical pressure occurs for each critical tem-
perature, and each critical point is associated with only
one composition.
In practice, critical loci for multicomponent systems
are of greater concern than are those
of binary systems.
The aforementionedprinciplesdevelopedforbinary
systems with the aid of Figure 4-0.2, however, caneasily
be shown to apply for multicomponent systems. It
is
only necessary to imagine one or both of the vapor
pressure curves of the binary system to have been replaced by envelopes representing pressure-temperature
diagrams of mixtures of fixed composition. Then each
terminus of the critical locus that represents thecritical
point of a mixture, such as pointC of Figure 4-0.1, may
be considered to be the criticalpoint of a“pseudocomponent.’’
As long as the pseudocomponents involved in the
substitution remain unchangedin composition, the critical locus associated with them will be fixed, and the
pressure-temperatureenvelopes
of all intermediate
compositions can be defined as binary mixtures of the
two. In a mixture of several pure componentsof varying
volatility, for example, the two pseudocomponents required to establish the termini of the critical locus for
the mixture may be chosen so that the vapor pressure
the
curve of the mostvolatilecomponentprovides
pressure-temperature relationship of one of the compoThe other
nents of thehypotheticalbinarymixture.
component needed to establish the critical locus then
becomes the two-phase envelope that defines pressuretemperature relations of the multicomponent mixture
consisting of all the remaining components of the mixture under consideration. This means
that in a pressuretemperature diagram, such as Figure 4-0.2, the vapor
pressure curve of the heavy component in the binary
system is replaced by the two-phase envelope of a certain mixture of the combined heavier components considered as a pseudocomponent. At the same time, the
vapor pressure curve of the light pure component continues to represent the pressure-temperature relationship for the more
volatile component of the pseudo
binary system usedas a more tractable substitute for the
entire multicomponent system considered.
Mixturesconsideredaspseudocomponentsmust
have rigidly fixed compositions so that the envelopes
representing the intermediate compositions can be defined as binary mixtures of the two terminal pseudocomponents. Any changeof composition in the pseudocomponent mixtures obviously will displace the critical
point to be used as a terminus of the critical locus for
what is, in effect, a different system.
The critical locus illustrated in Figure 4-0.2 is typical
of manycommonly known systems. For this reason,
most
present
methods
of
predicting
critical temperatures and pressures of hydrocarbon mixtures pre-
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X*
suppose systems which form that type of critical locus.
For convenience, this common type of critical locus is
referred to in this chapter as Type I.
There are at least four other types of critical loci to
which the available correlations for predicting critical
temperatures and pressures donot apply. So far, two of
these four reported types of critical loci are for binary
systemscontainingmethane,butthesephenomena
have not yet been explored sufficiently to exclude with
certainty such compounds as ethane, propane, butane,
and ethylene from similarbehavior under analogous
conditions. Kay (28) has stated thatsuch deviant behaviorexists in binarysystemscontaining methane with
n-hexaneandhigher
homologs.With ethaneasthe
common component, loci other than Type I occur only
20 or more carbon
when the second component has
atoms. For propane and n-butane, thebehavior begins
at higher molecular weights.
In the absence of experimental data, at least in the
case of binary mixtures, it may be expected that, when
the heavy component has a melting point equal to or
greater than the critical temperature of the light component, thecritical locusof the mixturewill depart from
the Type I form. Whether or not this departure continues to exist when components of intermediate volatility are added tosuch a binary mixtureis not certain.
It is suspected, however, that the presence of components of intermediate volatility tends to normalize the
critical locus of a mixture whose terminal components
would form an anomalous critical locus when they constitute a binary mixture. If the components of intermediate volatility are present in sufficient numbers and
concentrations, the critical locus of the resulting multicomponent mixturemight even appear tohave the Type
I form.
The following are thesystems known to form anomalous types of critical loci:
Type II: Methane-n -heptane system (6,32). The critical locus extends from the
critical pointof n -heptane to
lower temperatures and ends at a temperature below
the critical temperature of methaneand apressure
above the critical pressure of methane. The end of this
critical locusis its intersectionwith another critical locus
of two liquid phases and asolid phase. Themethane-noctane and methane-n-nonane systems are expected to
behave similarly.
Type III: Methane-n-decane system (5). The critical
locusextendsfromthecriticalpoint
of n-decane to
lower temperatures and ends at both
a higher temperature and a higher pressure than the critical values for
methane.This critical locus ends in a critical point
which is also the terminus of a gas-liquid-solid locus.
Figure 4-0.3 is the pressure-temperature diagramfor
this system showingthe anomalous behavior described.
-200
O
200
400
600
TEMPERATURE, F
Figure 4-0.3-Critical Locus for the Methane-n-Decane
System (52)
Analogous behavior should be expected for all binary
systems containing methane and a component with a
higher freezing point than n-decane.
Type IV: Azeotropic binary systems. Some, but not
all, form critical loci with a minimum critical temperature, such asthatillustrated in Figure 4-0.4forthe
acetylene-ethylene system (9).
Type V: Benzene-watersystem ( 5 ) . The gas-liquid
critical locus extends from thecritical point of benzene
andendsatthethree-phase
critical endpoint.The
three-phase critical end point
is the highest temperature
at which all three phases coexist; above that, the
hydrocarbon rich liquidphasedisappears.Experimental
valuesfor threephase critical endpoints of several
hydrocarbon-water systems are tabulatedin Chapter 9.
Effect of Size, Shape, and Chemical Nature of the
Components on the Critical Locus
An excess critical property is defined as the difference between the value of the true critical property of
a mixture and the molar averageof the critical properties of the pure components. The excess property, the
deviation of the critical locus from ideal mixture behav-
4-4
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____
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X*
m
0732290 05361)20 123
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ior, is useful in studying trends in critical properties
because difference quantities magnify the effects of the
factors being studied.An increase in the excess critical
properties indicates a greater nonideality of a mixture
and a greater curvature of the critical locus curve.
Studies by Kay (30) have shown that excess critical
propertiesare affected in somecomplex manner by
differences in molecular size, molecular structure, and
chemical nature of the components.
By examining a largeamount of binary data, Kay (30)
noted the following trends in the critical loci and excess
criticalproperties in systemscontainingacommon
component.
P-T Critical Loci for Systems Whose Components
Belong to the Same Homologous Series
Where the components of the system are about the
samemolecularweight,
the critical locus curveap4-0.5-a.)
As the
proaches a straight line. (See Figure
relative size difference
increases,
the locus curve
changes to a curvedline, concave downward,anda
maximumpressurepointappears.
With further increases in the relative size difference,the maximum
pressureincreasesand may attaina very high value
relative to the critical pressures of thepurecomponents.
94c
90C
86C
82C
.-O
111
n
W'
3
78C
v)
W
P:
&
74c
70C
66E
62C
10
20
30
50
40
60
70
80
90
100
TEMPERATURE, F
Curve
C
Cb
C
C
Cd
Figure 4-0.4-Critical
1987
Ethane
Percent)(Mole
Unknown
18
Unknown
30
Locus for the Ethyne-Ethene (Acetylene-Ethylene) System and Envelopes
for Four Binary Mixtures (6)
4-5
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4-0
P-T Critical Loci for SystemsWhose Components
Belong to Different Homologous Series
The trends are generally thesame as homologous
systems with regard to size althoughdifferences in
chemical nature andmolecular structure play a part that
is not clearly discernible. (See Figure
4-0.5-b and -c.)
Becausethe critical temperatures of n-hexaneand
n -heptane are lower than that of cyclohexane, the critical loci crossoverfrom one side of cyclohexane to
the other side as the molecular weight of the paraffin
is increased. The samerelation
is observed in the
benzene-paraffin series. However, this series is different from the cyclohexane-paraffinseriesbecause the
critical locus of benzene-n -octane has a minimum temperature point that suggests the presence of a critical
azeotrope.Approximately of thesame size butbelonging to completely different homologous series are
n-hexane, cyclohexane,
and
benzene.
(See
Figure
4-0.5-d.) Therefore, differences in their loci with a commoncomponent may be considered to be due, principally, to the differences in their molecular structure
and chemical nature. The sameis true for o -xylene and
ethylbenzene which have thesame molecular weight
but different molecular structures.
Excess Critical Temperaturefor Systems
Whose Components Belong to the Same
Homologous Series
A plot of excess critical temperature, T,', as a function of composition is not necessarily symmetrical. (See
Figure 4-0.6-a.)The maximum T,' are shifted towardthe
more volatile component. For a constant difference in
molecular weight, the lower the molecular weight of the
components, the greater themaximum T,'. (See Figure
4-0.7b.) As the difference in molecular weight between
components increases, the maximum T,' is greater, the
lower the average molecular weight.
Excess Critical Temperaturefor Systems
Whose Components Belong to Different
Homologous Series
The plots are asymmetrical and show the transition
from a minimum T,' (negative) to a maximum T,' (positive)as the difference in the size of the components
increases. (See Figure4-0.6-b and -c.)Maximum T,' are
approximatelythesamewhencomponent
molecules
are of the samesize even though the molecular structure
and/or chemical naturearedifferent.
(See
Figure
4-0.6-d.) This indicates that the effect of size is greater
than that of structure and chemical nature.
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Excess Critical Pressure for Systems
Whose Components Belong to the Same
Homologous Series
The same trends asgiven for excess critical temperatureapply.(SeeFigure
4-0.7-c and-dand
Figure
4-0.8-C.)
Excess Critical Pressure for Systems
Whose Components Belong to Different
Homologous Series
The plots are highly asymmetric for the systems of
cyclohexane and benzene with n-paraffins. (See Figure
4-0.8-a and -b.)As the molecularweight of the paraffin
decreases, the P,' becomes more negative and then reverses after the n-heptane binary to become less negative. As the size difference gets larger, the curves show
a transition in which both a minimum P,' and a maximum P,' exist. Systems of czs-decalin with n -hexane,
cyclohexane, and benzene exhibit a maximum p: (positive). (See Figure 4-0.8-d.) The maximum P,' tends to
shift toward the higher mole percentof the lower molecular weight component as observed in other binary systems. The maximum P,' value is greatest for n-hexane
but is almost the same for benzene and cyclohexane.
This is to be expected because n-hexane differs from
czs-decalin in size, structure,and chemical nature,
ciswhereasbenzeneandcyclohexanedifferfrom
decalin in size but have a ring structure. Thedifference
in chemical naturebetweenbenzeneand
cis-decalin
seems to be negligible. The excess critical pressures are
practically thesameforthe
physicalisomersethylbenzene and o -xylene.
Pseudocritical Temperature and Pressure
The use of the theorem of corresponding states for
the correlation of the properties of hydrocarbon mixtures requires the correlating parametersknown as the
For
reducedtemperatureandthereducedpressure.
pure substances, these are the quotients
of the temperatureandpressure
of interestdivided by the critical
temperature and the critical pressure of the pure compound. For hydrocarbon mixtures, the correspondingstates correlations apply when pseudocritical temperatures
and
pressures
are
used.
The
pseudocritical
propertiesarenotexperimentallydetermined
values
but are obtained by Kay's empirical equation (25).
A pseudocritical property of a defined hydrocarbon
mixture is the sum of the products of the mole fraction
of eachpurecomponentand
itsrespective critical
property value.
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A P I T D B C H A P T E R t 4 t t W 0 7 3 2 2 9 0 O536922 T T 6 W
4-0
CRITICAL TEMPERATURE,F
n-hexane-n-heptane
e
f n-hexane-n
-octane
g n-hexane-n-decane
h n -hexane-n-tridecane
i n-hexane-n-tetradecane
j cyclohexane-n-hexane
Figure 4-0.5-P-T
k
I
m
n
o
p
Legend
cyclohexane-n
-heptane
cyclohexane-n-octane
cyclohexane-n-nonane
cyclohexane-n-decane
cyclohexane-n-trldecane
benzene-n-hexane
q benzene-n-heptane
r benzene-n
-octane
S
benzene-n-nonane
x
t benzene-n
-decane
u benzene-n-tridecane
W
y
z
cis-decalin-benzene
cis-decalin-cyclohexane
cis -decalIn- hexane
cls-decalin-o-xylene
cir-decalin-ethylbenzene
Critical Lociof Binaries Containing a Common Component and
a Representative
from a Homologous Series
4-7
1987
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--`,,-`-`,,`,,`,`,,`---
MOLEFRACTIONCOMMONCOMPONENT
e
f
g
h
i
j
n-hexane-n-tetradecane
n-hexane-n-tridecane
n-hexane-n -decane
n-hexane-n-octane
n-hexane-n-heptane
cyclohexane-n-tridecane
Figure 4-0.6-Excess
k
I
m
n
o
p
Legend
cyclohexane-n -decane
cyclohexane-n -nonane
cyclohexane-n -octane
cyclohexane-n-heptane
cyclohexane-n -hexane
benzene-n-tridecane
q benezene-n-decane
r benzene-n-nonane
S
benzene-n-octane
t benzene-n-heptane
u benzene-n-hexane
W
x
y
z
cis-decalin-cyclohexane
cis-decalin-benzene
cis-decalin-n-hexane
cis-decalin-ethylbenzene
cis-decalin-o-xylene
Critical Temperature vs Composition for Representative Binary Systems
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4-0
M
M
(16
as
MOLEFRACTIONLOWERMOLECULARWEIGHTCOMPONENT
e propane-n-pentane
f n-butane-n-octane
g n-hexane-n-octane
h n -decane-n-dodecane
propane-n-heptane
i
Figure 4-0.7-The
Legend
n-butane-n -octane
o n-butane-n-hexane
k n -pentane-n-nonane
n-hexane-n-octane
p
I
n -hexane-n -decane
q n-decane-n
-dodecane
m n-nonane-n-trldecane
propane-n-heptane
r
n propane-n -pentane
J
t
u
v
n-butane-n-octane
n -pentane-n
-nonane
n -hexane+
-decane
n-nonane-n-tridecane
Effect of Relative Size and Absolute Molecular Weighton the Excess Functions
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053b425
705
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W
110
100
m
60
40
20
O
-?o
00
a4
u)
(16
MOCE ERACTION COMMON CWPONENT
benzene-n-tridecane
benzene-n -decane
benzene-n-hexane
benzene-n -nonane
benzene-n-octane
benzene-n -heptane
Figure 4-0.8-Excess
Legend
cyclohexane-n-tridecane
1 cyclohexane-n -decane
m cyclohexane-n-nonane
n cyclohexane-n-hexane
o cyclohexane-n -octane
p cyclohexane-n -heptane
k
q n-hexane-n-tetradecane
r n-hexane-n-tridecane
S
n -hexane-n-decane
t n -hexane-n-octane
u n-hexane-n-heptane
W
x
y
z
cis-decalin-n-hexane
cis-decalin-benzene
cis-decalin-cyclohexane
crs-decalin-ethylbenzene
crs-decalin-o-xylene
Critical Pressure vs Composition for Representative Binary Systems
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n
Jpc =
c
I=
XLJ,,
(4-0.1)
1
Where:
Jpc= pseudocritical property (temperature, pressure,
or volume) of the mixture.
n = number of components in mixture.
x, = mole fraction of pure component i in the mixture.
J,, = critical property of pure component i.
Because of these methodsof calculation, the pseudocritical temperatures and pressures arealways less than
the so-called true critical values of the same mixture
with mixtures following a Type 1locus. In Figure 4-0.1,
for example, the point
( p P cT,,J
, might represent the
pseudocritical temperature and pressure of the mixture
whose true critical value is at point C in thesame
pressure-temperaturediagram.Forthesamereason,
the locus of the pseudocritical point is a straight line for
the full range of composition of a mixture such as that
illustrated in Figure 4-0.2.
Forundefinedmixtures,apseudocriticalproperty
may be defined by a particular correlation. The pseudocritical temperature defined by Procedure 4D3.1 is an
example of such a correlation.
Other rules for obtaining “pseudo” values for the
critical properties are available, and some
of these rules
have been used in other chapters of the Technical Data
Book, However, when the temperature or pressure is
predicted by some rule other than equation (4-O,l), the
resulting values are referred to as the mixture correspondencetemperatureand
mixturecorrespondence
pressure and are useful only in their specific procedure.
Critical Temperature
A list of experimental critical temperatures formany
pure compounds is given in Chapter 1. To predict the
critical temperature of other pure compounds,use Procedure 4Al.l or Procedure4A2.1.Procedure
4Al.l
may be more useful when all the critical properties of a
compoundaredesired.Procedure4A2.1
is asimple
regression equation.
Procedure 4 B l . l and an optional computer method
(Procedure 4B4.1) aregiven for calculating thetrue critical temperature of adefinedmixture.Specific
recommendations
and
restrictions
are
given for binary hydrocarbon-hydrocarbon, binaryhydrocarbonnonhydrocarbon, and multicomponent mixtures.
The true critical temperature of natural gas mixtures
canbecalculatedfromFigure
4 C l . l . Anatural gas
contains a large amount of methane and sometimes an
appreciable amountof hydrogen, helium, nitrogen, and
carbon dioxide.
The method for obtaining the true critical temperature of petroleum fractions is described in Procedure
4D1.1. Pseudocritical temperatures of petroleum fractions can be estimated from Procedure 4D3.1
using specific gravity and mean average boiling point as input
parameters.
The method of obtaining the true and pseudocritical
temperatures of mixtures of known hydrocarbons and
one or more petroleum fractions is described in Procedure4D3.2.Thismethodshouldnotbe
usedasan
alternative for Procedure 4B1.1 or 4D1. l .
Critical Pressure
A list of experimental critical pressures is givenin
Chapter 1. Topredict the criticalpressure of a pure
compound, use Procedure 4A1. l . This is a group contribution method and the required increments are
given
in Table 4A1.2.
The true critical pressure of defined mixtures may be
calculated by hand from Procedure 4B2.1. The procedure is mostaccurateformixturescontaining
only
hydrocarbons. Restrictions are stated for mixtures containing methane andinorganic gases. An alternatecomputer method, Procedure 4B4.1,
is more reliablefor
critical pressures.
Use Figure 4D2.1 to calculate the true critical pressure of petroleum fractions. The ASTM slope, ASTM
volumetric average boiling point, and the API
gravity of
the fraction, all of which are needed for this method,
are usually directly determined from standard inspection tests or can be calculated from standard inspection
tests. Chapter 2may be helpful whenusing this method.
The pseudocritical pressure of a petroleum fraction
can be estimated from Procedure 4D4.1 using specific
gravity and mean average boiling point as input parameters. The method for obtaining the true and pseudocriticalpressure of mixtures of known hydrocarbons
and one or more petroleum fractions is described in
Procedure 4D4.2 andis illustrated by a numerical example. This method should not be used as an alternative
for Procedure 4B2.1 or Figure 4D2.l.
Critical Volume
A list of some experimental critical volumes is given
in Chapter 1. The critical volume of pure compounds
may be estimated by Procedure 4A1.1 or 4A3. l . Procedure 4Al.l may be more useful when all the critical
properties of a compound are desired. However, Procedure 4A3.1 is muchsimpler if critical temperature
and critical pressure are known.
--`,,-`-`,,`,,`,`,,`---
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0732290 0536427 588
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--`,,-`-`,,`,,`,`,,`---
4-0
tt
Procedure 4B3.1 is used to predict the critical volume
of a defined mixture. Procedure 4B4.1 may also be used
asa computer method. No methodsare recommended
forthe critical volume of natural gases or petroleum
fractions.
A method for predicting the critical volume of petroleum fractions isgivenby Hall and Yarborough (22).
Sincefew experimental data exist, this method could
not be evaluated in the preparation of this chapter.
4-1 2
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A P I TDB C H A P T E R 8 4
**
m
0732290 0536428 414
m
4A1.1
PROCEDURE 4A1.1
GROUP CONTRIBUTION METHOD FOR CALCULATING THE CRITICAL
TEMPERATURE,PRESSUREANDVOLUMEOFAPUREHYDROCARBON
Discussion
The following equation is to be used to calculate the critical pressure of a pure hydrocarbon. Since the technique uses the group contribution method, the structure of the compound must be known.
=
14.5M
(0.339 + ZAP - 0.026 A Platt #)'
(4Al.l-1)
Where:
p . = critical pressure of pure hydrocarbon, in pounds per square inch absolute.
= molecular weight.
ZAP = summation of critical pressure group contributions.
A Platt # = the Platt number of any alkyl chains in the compound minus the Platt number
of the n-alkane with the same number of carbons. The Platt number is the
number of pairs of carbon atoms which are separated by three carbon-carbon
bonds andis an indicator of the degree of branching in the molecule. The Platt
number of an n-alkane is equal to thenumber of carbons minus three. Further
discussion of the Platt number is given by Wiener, J . Am. Chem. Soc., 69, 17
(1947).
M
[
T , = % Ir
+
1
(1.242 Z A T - 0.023 A Platt #)
1
V ,= 0.01602 [40 + EA,]
--`,,-`-`,,`,,`,`,,`---
Procedures consistent with this method are given below for critical temperature and critical
volume of a pure hydrocarbon. These procedures are of practically equivalent accuracy to
procedures 4A2.1 and 4A3.1.
(4A1.1-2)
(4Al.l-3)
Where:
T, = critical temperature of pure hydrocarbon, in degrees Rankine.
V , = critical volume of compound in cubic feet per pound-mole.
6 = boiling temperature of compound in degrees Rankine.
Procedure
Step 1: Obtain the molecular weight and boiling temperature from Chapter 1.
Step 2: Determine the structure of the compound.
Step 3: Obtain the needed group contributions from Table 4A1.2.
Step 4: Sum these group contributions to obtain ZAP, ZA, or ZAv.
Step 5: Compute the desired critical property from equation (4Al.l-I), (4Al.l-2) or
(4A1.1-3).
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CHAPTER*4
**
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0732290 0536429 350
m
4A1.1
COMMENTS ON PROCEDURE 4A1.1
Purpose
Equations are given for calculating the critical properties of pure hydrocarbons. For many
hydrocarbons, Chapter 1lists experimental critical properties; these are tobe preferred when
available. However, for compounds containing 12 carbon atoms or more, including an alkyl
chain, even “measured” critical properties may not be reliable, because of thermal decomposition at elevated temperatures.
Limitations
The equations are applicable to all hydrocarbon families provided the structure of the
compound is known. The equation was evaluated for C1-C2”paraffins and for C&, compounds forall other families. The accuracy of results for critical pressure and critical volumes
of compounds with more than twelve carbons may be questionable. Maximum deviations
should be expected for cycloalkanes.
Reliability
r,
P,
Average percent deviation
Average deviation
Maximum percent deviation
Maximum deviation
2.2
3.4
10.2 psia
18.7
165.8 psia
v,
0.7
7.6 R
8.0
98.1 R
0.2 ft3/lb-mole
15.6
1.4 ft3/lb-mole
--`,,-`-`,,`,,`,`,,`---
Literature Source
Adapted from Ambrose, D., “CorrelationandEstimation
of Vapor-Liquid Critical
Properties, I. Critical Temperatures of Organic Compounds,” NationalPhysical Laboratory,
Teddington, NPL Report 92 (Sept. 1978korrected Mar. 1980b), and Ambrose, D., “Correlation and Estimation of Vapor-Liquid Critical Properties, II. Critical Pressures and Critical Volumes of OrganicCompounds,”National Physical Laboratory, Teddington, NPL
Report 98 (May 1979).
Examples
1. 2,2,3 Trimethylpentane
From Chapter 1, the molecular weight is 114.230 and the boiling point is 229.72 F. From
Table 4A1.2, the increment contributions are:
Group #
# of occurrences
1
5
2
1
3
1
4
1
The summations are:
ZAP
5(0.226)
0.226
0.220
0.196
1.772
ZAT
5(0.138)
O . 138
0.095
0.018
0.941
ZA”
5(55.1)
55.1
47.1
38.1
415.8
A Platt # = 8 - 5 = 3
From equation (4A1,l-1):
P,=
(14.50)(114-230)
= 4 0 . 7 5 psis
[0.339 + 1.772 - 3(0.026)12
From equation (4Al.l-2):
1
1
= 1015.50 R = 555.83 F
[1.242 + 0.941 - 0.023(3)]
From equation (4Al.l-3):
V ,= (40 + 415.8)(0.01602) = 7.302 ft3/lb mole = 0.0639 CU ft per lb
Experimental values are:
T, = 554.63 F
P, = 395.91 psia
V ,= 0.0611 CU ft per lb
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A P I TDBCHAPTER*4
m
0732290 053bY30 O72 9
4A1.1
2. 2-Methyl-1-butene
From Chapter 1, the molecular weight is 70.13 andthe
From Table 4A1.2, the increment contributions are:
Group #
# of occurrences
2
1
1
2
1
5
7
1
The summations are:
ZAO
2(0.2260)
0.2260
O. 1935
0.1875
1.O590
boiling point is 88.09 F.
U r
2(0.138)
O. 138
0.113
0.070
0.597
ZA"
2(55.1)
55.1
45.1
37.1
247.5
A Platt = 2 - 2 = O
From equation (4Al.l-1):
P,=
(14.5)(70.13)
= 520.3 psia
[0.339 + 1.059 - 0.026(0)]z
From equation (4Al.l-2):
1
(1.242 + 0.597 - 0.023(0))
1
= 845.61
R = 385.93 F
From equation (4A1.1-3):
V , = (40 + 247.5)(0.01602) = 4.606 ft3/lb mole = 0.0657
Experimental values are:
T, = 378.0 F
P, = 493.0 psia
CU
ft per lb
--`,,-`-`,,`,,`,`,,`---
[
T, = 547.76 1 +
V , = 0.0667 CU ft per lb
3. cis-Decalin
From Chapter 1 the molecular weight is 138.25 and the boiling point is 384.47 F. From
Table 4A1.2, the increment contributions are:
Group #
# of occurrences
11
8
13
2
The summations are:
No alkyl side chains, therefore A Platt
ZAP
8(0.1820)
2(0.1820)
1.S20
ZAr
S(0.090)
2(0.030)
0.780
U"
8(44.5)
2(44.5)
445
= O.
From equation (4Al.l-1):
From equation (4A1.1-2):
r
1
T, = 844.06 1 +
1
(1.242 + 0.780)
= 1261.50
R = 801.83 F
From equation (4A1.1-3):
V ,= (445 + 40)(0.01602) = 7.770 ft3/lb mole = 0.0562 CU ft per lb
Experimental values are:
T, = 804.38 F
P, = 470.27 psia
V ,= 0.0556 CU ft per lb
4. tert-Butyl benzene
From Chapter 1, the molecular weight is 134.22 and the boiling point is 336.41 F. From
Table 4A1.2, the increment contributions are:
# of occurrences
Group #
3
1
1
4
1
18
The summations are:
ZAP
3(0.2260)
O. 1960
O. 9240
1.7980
8Ar
3(0.138)
0.018
0.458
O. 890
8A"
3(55.1)
38.1
222
425.4
APlatt=O-1=-1
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A P I TDB CHAPTERv4
**
0732290 0 5 3 b 4 3 L T09
4A1.1
From equation (4A1.1-1):
P,=
(134.221)(14.5)
[0.339 + 1.7980 - 0.026(-1)12
= 415.98
psia
From equation (4Al.l-2):
r
1
T, = 796.08 1+
1
[1.242 + 0.890 - 0.023(-l)]
1
= 1165.50
R = 705.82 F
From equation (4A1.1-3):
V , = [425.4 + 40](0.01602)
= 7.456 ft3/lb mole = 0.0555 CU ft per lb
Experimental values are:
T, = 728.33 F
V , = 0.0587
P, = 430.80 psia
CU
ft per lb
5. Anthracene
From Chapter 1, the molecular weight is 178.23 and the boiling point is 646.16 F. From
Table 4A2.2, the increment contributions are:
Group #
# of occurrences
19
0.448
1
29
2
The summations are:
ZAP
0.894
2(0.515)
1.924
EAT
2(0.220)
0.888
ZA"
222
2(148)
518
A Platt # is zero because there are no alkyl chains.
From equation (4Al.l-1):
From equation (4A1.1-2):
[
T, = 1105.83 1 +
I
1
= 1625.00 R = 1165.3 F
(1.242 + 0.888)
From equation (4A1.1-3):
V , = (518 + 40)(0.01602) = 8.939 ft3/lb mole = 0.0502 CU fi per lb
Experimental values are:
T, = 1104.53 F
P, = 484.43 psia
V , = 0.0498 CU ft per lb
--`,,-`-`,,`,,`,`,,`---
4-16
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API TDB CHAPTERx4
m 0732270
X*
0536432 945
m
4A1.2
TABLE 4A1.2
GROUP INCREMENTSFOR EQUATIONS 4A1.1-1 THROUGH 4A1.1-3
Group
Group
Number
Description
APi
AT
AV^
1
-CH,
0.138
0.2260
55.1
2
\
,CH2
0.138
0.2260
55.1
3
)CH-
0.2200
4
5
6
=CH-
47.1
0.018 O. 1960
38.1
0.1935
45.1
0.1935
45.1
=CH,
0.113
13
0.095
0.1
/
O. 1875
0.070
37.1
=C=
0.1610
0.088
35.1
9
=CH
0.038
0.1410
35.1
10
=C-0.038
0.1410
35.1
\
/CH2
O. 1820
7
=C
8
\
Ring Increments
12
\
/CH-
13
‘CH-*in
14
\C/
/ \
15
=CH-
16
=C,
17
=C=
/
/
44.5
44.5
0.090
O. 1820
fused ring
0.1820
0.030
44.5
0.1820
0.090
44.5
0.075
O. 1495
37.0
0.075
O. 1495
37.0
170
O. 1
0.060
29.5
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0.090
--`,,-`-`,,`,,`,`,,`---
11
Not for Resale
A P I TDB CHAPTER+4
X+
m
0732290 O536433 B B l
m
4A1.2
Aromatic Compounds
0
0.9240 222
0.458
0.8940
0.448
222
0.9440
0.488
222
0.9440
0.488
222
22
o.8640
222O. 438
23
0.9140
222O. 478
24
0.8340
222O. 428
25
O. 8840
222O. 468
26
O. 8840
222O. 468
27
0.8040
0.418
222
28
0.7240
0.368
222
18
19
cz
20
0-
21
29
-0
ring* in fused
* Group contributions for
/
0.5150
fused
rings
148
0.220
have been
calculated
from
minimal
data
and
may
--`,,-`-`,,`,,`,`,,`---
be less reliable than the other values in Table 4A1.2.
4-18
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A P I TDBCHAPTERx4
**
m
0732290 0536434 718
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4A2.1
PROCEDURE 4A2.1
EQUATION FOR CALCULATING THE CRITICAL
TEMPERATUREOFAPUREHYDROCARBON
Discussion
The following equation is to be used to calculate the critical temperature of pure hydrocarbons. It is applicable for all families of hydrocarbons.
logloT, = A
+ B log,, (sp gr) + C log,, Tb
(4A2.1-1)
Where:
T, = critical temperature of pure hydrocarbon, in degrees Rankine.
A, B, C = empirically derived constants (specific for each family).
sp gr = specific gravity, 60 F/60 F.
Tb = normal boiling point, in degrees Rankine.
Procedure
Step I : Obtainthe normal boiling point and specific gravity of the compound from
Chapter 1.
Step 2: Obtain the values of A, B, and C from Table 4A2.2.
Step 3: Calculate the critical temperature using equation (4A2.1-1).
TABLE 4A2.2
VALUES OF COEFFICIENTS FOR EQUATION 4A2.1-1 FOR CALCULATING
CRITICAL TEMPERATURE OF A PURE HYDROCARBON
A
1987
B
Type Compound
Paraffin . . . . . . . . . . . . .
Naphthene. . . . . . . . . . .
Olefin. . . . . . . . . . . . . . .
Acetylene . . . . . . . . . . .
Diolefin . . . . . . . . . . . . .
Aromatic. . . . . . . . . . . .
0.43684
-0.07165
0.27749
0.30381
-0.39618
O. 22732
1.47115
0.70612
l.18325
0.79782
O. 14890
1.14144
4-1 9
--`,,-`-`,,`,,`,`,,`---
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C
O. 56224
0.81196
0.65563
0.79987
0.99481
O . 66929
Not for Resale
A P I TDB C H A P T E R t 4 t t
m
0732290 0536435654
m
4A2.1
COMMENTS ON PROCEDURE 4A2.1
Purpose
An equation is given for predicting the critical temperature of a pure hydrocarbon. For many
hydrocarbons, Chapter 1 lists experimental critical temperatures; these values are preferable when
available. However, for compounds containing 12 carbon atoms or more, including an alkyl chain,
even “measured” critical properties
may not bereliable becauseof thermaldecomposition at elevated
temperatures.
Limitations
The equation is applicable to all hydrocarbon families. Equation (4A2.1-1) was tested, however,
using only experimental boiling points and specific gravities. Estimated valuesof these parameters
may lead to larger errors. The equation
was tested using data in the range C1-C20 for paraffins and in
the range C3-CI4 for all other families. Higher molecular weight hydrocarbons may yield less accurate results.
Reliability
The average deviation from experimental data is about 5.0 deg F or 0.84 percent. To retain this
accuracy the untruncated valuesof A, B, and C in Table 4A2.2 shouldbe used. The maximum deviF or 7 percent.
ation expected is 100 deg
Special Comment
For naphthenes and aromatics with paraffinic side chains, use the coefficients given in Table 4A2.2
for the naphthene or aromatic. Densities for these compounds can be estimated by methods in
Chapter 6.
Literature Source
Adapted from Nokay, R., Chem. Eng. 66 [4] 147 (1959).
Example
Calculate the critical temperature
of n-octane.
From Chapter 1:
6 = 258.21 F
sp gr = 0.7070
From Table 4A1.2:
A = 1.47115
B = 0.43684
C = 0.56224
Tb = 258.21 + 459.67 = 717.88
log T, = 1.47115 + 0.43684 loglo (0.7068)+ 0.56224 loglo (717.88)
log T, = 1.47115 +0.43684 (-0.1506) + 0.56224 (2.85605)
log T, = 3.0111
T, = 1025.89 R = 566.22 F
The experimental value from Chapter1 = 564.22 F.
4-20
1992
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CHAPTER*:4
ff
m 0732290
053bY3b 590
m
4A3.1
PROCEDURE 4A3.1
--`,,-`-`,,`,,`,`,,`---
EQUATION FOR CALCULATING THE CRITICAL
VOLUME OF A PURE HYDROCARBON
Discussion
The following equations are to be used to calculate the critical volume of a pure hydrocarbon. It is applicable for all families of hydrocarbons.
RT,
(4A3.1-1)
V,= pJ3.72 + 0.26(a
- 7.00)]
(4A3.1-2)
a = 5.811 + 4 . 9 1 9 ~
Where:
V , = critical volume of pure hydrocarbon in cubic feet per pound-mole.
R = gas constant = 10.731 (psia) (CUft) per (Ib-mole) (deg R).
T, = critical temperature, in degrees Rankine.
p . = critical pressure, in pounds per square inch absolute.
a = Riedel factor.
W = acentric factor.
Procedure
Step 1: Obtainthe critical pressure and critical temperature of the compound from
Chapter 1.
Step 2: Obtain the acentric factor from Chapter 2 or by Procedure 2 A l . l .
Step 3: Calculate a using equation (4A3.1-2).
Step 4: Calculate the critical volume using equation (4A3.1-1).
4-21
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API TDB C H A P T E R t 4 t t M 0732290 O536437 427 M
4A3.1
COMMENTS ON PROCEDURE4A3.1
Purpose
--`,,-`-`,,`,,`,`,,`---
An equationisgivenforcalculatingthecriticalvolume
of apurehydrocarbon.Formany
hydrocarbons, Chapter 1 lists experimental critical volumes; thesebeare
preferred
to when available.
However, for compounds containing 12 carbonatoms or more,includinganalkylchain,even
"measured" critical properties may not be reliable because of thermal decomposition at elevated
temperatures.
Limitations
The equation is applicable to all hydrocarbon families. Equation (4A3.1-1) was tested using
experimental values for the critical temperatures and critical pressures. Estimated values of these
parameters may yield larger errors in the critical volume. Also, the equation
was evaluated for C3-C18
paraffins and for C3-CI1for each of the other families. Heavier materials may give less accurate
results.
Reliability
The average error from experimental
data is about0.24 cubic feet per pound-mole or 3.26 percent.
This method is least reliable for
Maximum deviation is 1.83 cubic feet per pound mole or 20 percent.
cycloalkanes and aromatic compounds.
Literature Source
Adapted from Riedel,L., Chem. Ingr.-Tech. 26 679 (1954).
Equation (4A3.1-2)is adapted from Riedel,L., Chem. Zngs-Tech. 28 557 (1956).
Example
Calculate the critical volume
of n-nonane.
From Chapter :1
T, = 610.68 F
p, = 331.8 psia
= 610.68 + 459.7 = 1,070.35 R
From Chapter 2:
W =
0.4368
From equation (4A3.1-2):
a = 5.811 + (4.919) (0.4368)
a = 7.960
By equation (4A3.1):
v, =
(10.731) (1,070.35)
(332) [ 3.72 + 0.26 (7.960 - 7.00) ]
V, = 8.72 CU ft per lb-mole = 0.0680 CU ft per lb
The experimental value from Chapter1 = 0.0684 CU ft per lb.
4-22
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A P I TDB CHAPTER+4 * X W 0732290 053b438 363 W
4B1.1
PROCEDURE 4B1.1
METHOD FOR THE CRITICAL TEMPERATURE
OF A MIXTURE OF DEFINED COMPOSITION
Discussion
The Li equation (4B1.1-1) is to be used to calculate the critical temperature of a mixture
of defined composition. For this purpose the critical volumes of the pure components must
be known or estimated. The following equation is applicable for most hydrocarbons over the
entire composition range.
--`,,-`-`,,`,,`,`,,`---
T,,
= C e, T,,
I=
(4Bl.l-1)
I
Values of 8, may be calculated from equation (4Bl.l-2) and (4Bl.l-3).
(4B1.1-2)
(4B1.1-3)
Where:
7&, =true critical temperature of mixture, in degrees Rankine.
e, = volumetric fraction of component i.
T,, = critical temperature of component i, in degrees Rankine.
x , = mole fraction of component i.
V,, = molar critical volume of component i, in cubic feet per pound-mole.
V,= molar average critical volume, in cubic feet per pound-mole.
Procedure
Step I: Obtain the critical temperature, critical volume, and molecular weight of each
component from Chapter 1. If values of the critical temperature and critical volume are not
available, they may be calculated from methods given in Section 4A of this chapter.
Step 2: Convert each critical temperature and critical volume to the units specified in the
discussion.
Step 3: Compute the molar average critical volume using equation (4B1.1-3).
Step 4: Compute the volumetric fractions from equation (4Bl.l-2).
Step 5: Calculate the critical temperature from equation (4Bl.l-1).
4-23
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A P I TDB C H A P T E R t 4
**
M 0732290 053b439 2 T T M
4B1.1
COMMENTS ON PROCEDURE 4Bl.l
Purpose
Procedure 4Bl.l is to be used to predict the truecritical temperature of a mixture containing any number of components. It is intended for use both as a desk and a computermethod.
Limitations
This procedure was evaluated using experimental critical temperatures and critical volumes. If estimated values of these parameters are used, some loss of accuracy should be
expected.
--`,,-`-`,,`,,`,`,,`---
A. Defined Binary Hydrocarbon-Hydrocarbon Systems
The equation is not reliable for mixtures containing more than 0.5 mole fraction methane.
If the ratio of the molecular weights of the components is greater than 2.5 the expected
error is increased.
B. Defined Binary Hydrocarbon-Nonhydrocarbon Systems
The procedure should not be used for mixtures containing hydrogen, more than 0.3 mole
fraction carbon dioxide or carbon monoxide, or more than 0.45 mole fraction nitrogen.
Procedure 4B4.1 should be used for these cases.
C . Defined Multicomponent Systems
This method has been evaluatedprimarily with binary data although it can be extended to
higher-order systems. Very few experimental data are available for critical temperatures of
multicomponent systems, but equation (4Bl.l-1) has been applied to mixtures containing as
many as nine components. For even higher order systems, it would be more appropriate to
use either Procedure 4Cl.l for natural gases or Procedure 4Dl.l for petroleum fractions.
This procedure can be used for multicomponent systems containing a small amount of
methane (0.10 to 0.15 mole fraction). At higher methane concentrations Procedure4Cl.l for
natural gases should be used.
Reliability
A. Defined Binary Hydrocarbon-Hydrocarbon Systems
Errors in the calculated critical temperature average about 0.6 percent (5.2 deg F). For
non-methane mixtures the maximum deviation expected is 15 deg F. For mixtures containing
more than 0.5 mole fraction methane, errors as high as 100 deg F have been obtained, with
an average deviation of 5.7 percent (31 deg F).
B. Defined Binary Hydrocarbon-Nonhydrocarbon Systems
For binaries containing at least one nonhydrocarbon, the errors in the calculated critical
temperatures average about 5.0 percent (36 deg F). If the procedure is used for mixtures
containing hydrogen or more than 0.45 mole fraction nitrogen, absolute deviations in the
range of 100 to 200 deg F should be expected. For mixtures containing in excess of 0.3 mole
fraction carbon dioxide, deviations in the order of 50 deg F have been found.
C. Defined Multicomponent Systems
Average deviations in the calculated critical temperatures are 1.2 percent (8 deg F) for
non-methane systems. Generally the error is higher for a system containing methane and
increases as the number of components increases.
Special Comments
This procedure may be used for defined binary hydrocarbon mixtures, defined binary
mixtures containing one or more nonhydrocarbons, and defined multicomponent systems.
The evaluation of the Li equation with the binary hydrocarbon-hydrocarbon data was the
most extensive with a data set of 1,230 points representing 135 systems. For hydrocarbonnonhydrocarbon systems, a data set of 430 points representing 69 systems was evaluated
while 235 data points representative of 35 multicomponent systems were tested in the multicomponent portion of the study (see Documentation Report No. 4-73).
Literature Source
Adapted from Li, C. C . , Can. J . Chern. Eng. 49 709 (1971); Errata 50 152 (1972).
4-24
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A P I TDB
CHAPTERx4
0 7 3 2 2 9 0 O536440 TIIL
*X
m
4B1.1
Example
Estimate the critical temperature of a mixture containing 30 mole percent 1-hexene, 41.5 mole
percent n-octane, and 28.5 mole percent n-decane.
From Chapter 1:
2
3
1
n-Decane
1-Hexene
n-Octane
Critical temperature, deg F . . . . . . . . . . . . . . . .
Critical volume, CU ft per lb. . . . . . . . , , . . . , . .
Molecular weight. . . . . . . . . . . . . . . . . . . . . . . .
447.08
0.0673
84.16
564.22
0.069
114.23
Conversion to absolute units:
T,,
= 447.08 + 459.7 = 906.78 R
652.0 + 459.7 = 1,111.7 R
VCl = (0.0673) (84.16) = 5.66 CU ft per lb-mole
V, = (0.069) (114.23) = 7.88 CU ft per lb-mole
V, = (0.0679) (142.28)= 9.66 CU ft per lb-mole
T,3 =
From equation (4Bl. 1-3):
’V = (0.300) (5.66)+ (0.415) (7.88)+ (0.285) (9.66)
= 1.70 + 3.27 + 2.75 = 7.72 CU ft per lb-mole
By equation (4B l . 1-2):
--`,,-`-`,,`,,`,`,,`---
0, =
(0.300) (5.66)
= 0.220
7.72
0, =
(0.415) (7.88)
= 0.424
7.72
=
(0.285) (9.66)
7.72
=
0.357
The true critical temperature is then calculated from equation (4B1.1-1)
= (0.220) (906.78) + (0.424) (1,023.92)+ (0.357) (1,111.7)
Tm = 199 + 434 + 397 = 1,030 R
T,,,,
The experimental value (30) = 1,O31.85 R.
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652.00
0.0679
142.28
A P I TDB CHAPTERx4
*X
m 0732290 0536441 958
482.1
PROCEDURE 4B2.1
METHOD FOR THE CRITICAL PRESSURE
OF A MIXTURE OF DEFINED COMPOSITION
Discussion
Equation (4B2.1-1) is to be used to calculate the critical pressure of a defined mixture. For
this purpose the critical pressure and critical temperature of the pure components, as well as
the true critical temperature of the mixture, must be known or estimated. The equation,
which is generally applicable over the entire composition range, is as follows:
[
P,, = p p c+ pPe 5.808 + 4.93
(,:,c
X,W,
-
(4B2.1-1)
Values for the pseudocritical temperature and pseudocritical pressure are calculated as
molar average values.
(4B2.1-2)
(4B2.1-3)
Where:
pcm =true critical pressure of mixture, in pounds per square inch absolute.
ppc= pseudocritical pressure of mixture, in pounds per square inch absolute.
n = number of components in mixture.
x, = mole fraction of component i.
W , = acentric factor of component i.
=true critical temperature of mixture, in degrees Rankine.
T,,= pseudocritical temperature of mixture, in degrees Rankine.
T,, = critical temperature of component i, in degrees Rankine.
pc,= critical pressure of component i, in pounds per square inch absolute.
r,,,
Procedure
Step I : Obtain the critical temperature and critical pressure of each component from
Chapter 1. Obtain the values of the acentric factor of each component from Chapter 2. If
values of the critical pressure and critical temperature are not available, they may be calculated from methods given in Section 4A of this chapter.
Step 2: Compute the pseudocritical temperature from equation (4B2.1-2).
Step 3: Calculate the pseudocritical pressure from equation (4B2.1-3).
Step 4: If, as is generally true, the critical temperature of the mixture is unknown, calculate
it using Procedure 4 B l . l or Procedure 4B4.1.
Step 5: Calculate the true critical pressure from equation (4B2.1-1).
1987
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4-27
--`,,-`-`,,`,,`,`,,`---
Not for Resale
A P I TDBCHAPTERr4
m
0732290 053b442 8 9 4
m
--`,,-`-`,,`,,`,`,,`---
482.1
**
COMMENTS ON PROCEDURE 482.1
Purpose
Procedure 4B2.1 is to be used to predict the true critical pressure of a mixture containing any
number of components. It isintended for use both as a desk and a computer method.
Limitations
This procedure was evaluated using the experimental critical temperature and critical pressure of
each component. If estimated values of these parameters are used, errors may be higher.
A. Defined Binary Hydrocarbon-Hydrocarbon Systems
The equation should not be used for mixtures containing methane. Instead, Procedure 4B4.1
should be used.
The procedure is less reliable for mixtures of ethaneandaromatics as well as mixtures of
naphthenes with higher molecular weight paraffins (C, and above).
B. Defined Binary Hydrocarbon-Nonhydrocarbon Systems
The procedure should not be applied for mixtures containing nonhydrocarbon gases like carbon
dioxide or hydrogen. Instead, Procedure 4B4.1 is recommended.
C. Defined Multicomponent Systems
Equation (4B2.1-1) yields reasonable results for methane-free multicomponent systems. The
method has been evaluated primarily with binary data, but it has been applied to mixtures containing
up to eight components. For even higher order systems. it would be more appropriate to use Figure
4D2. l .
Very few experimental data areavailable on the critical pressures of multicomponent systems.
Reliability
A. Defined Binary Hydrocarbon-Hydrocarbon Systems
Errors in thecalculated critical pressures are about 3.8 percent (30 psia) for non-methane systems.
For methane-hydrocarbon mixtures the maximum deviation expected is approximately 50 percent
(710 psia).
B. Defined Binary Hydrocarbon-Nonhydrocarbon Systems
For binary systems containing at least one nonhydrocarbon (inorganic gas), the average error in the
calculated critical pressure is about 22 percent (760 psia).
C. Defined Multicomponent Systems
Average deviations in the calculated critical pressures are 4.6 percent (74psia).
Special Comments
This method should not be applied to predict the critical pressure of systems containing methane
or inorganic gases. A number of diagrams representing experimental data for representative methane,
carbon dioxide, and hydrogen sulfide systems are given in Figure 4B2.2 to 4B2.4.
Literature Source
Adapted from Kreglewski, A. and Kay, W. B., J. Phys. Chem. 73 3359 (1969).
Examples
A. Estimate the critical pressure of an ethylbenzene-n-octane mixture containing 30 mole percent
ethylbenzene. The experimental critical temperature of this mixture is 584.4 deg F (27).
From Chapter 1:
Ethylbenzene
n-Octane
Critical temperature, deg F. ...........
651.24
564.22
360.7
Critical pressure, psia ................ 523.5
4-28
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A P I TDBCHAPTERt4
m
tt
0732290 0536443 720
m
482.1
From Chapter 2:
o1(ethylbenzene) = 0.3036
y (n-octane) = 0.3962
By equation (4B2.1-2):
TF = (0.30) (651.24)+ (0.70) (564.22)
= 195.37 + 394.95 = 590.33 F
Conversion to absolute units:
Tm= 584.4 + 459.7 = 1,044.1 R
Tpc
= 590.3 + 459.7 = 1,050.0 R
From equation (4B2.1-3):
pPc = (0.30) (523.5)+ (0.70) (360.7)
= 157.1 + 252.5 = 409.6 psia
The molar average acentric factor is
n
C 5 y = (0.30) (0.3036) + (0.70) (0.3962)= 0.3684
i= 1
The critical pressure is then calculated from equation (4B2.1-1)
pcm = 409.6 + 409.6 [ 5.808
+ 4.93 (0.3684)] X
1,044.1 - 1,050.0
1,050.0
+ (409.6) (7.62)(-0.0056)
= 392.1 psia
= 409.6
The experimental value (27) is 403.6 psia.
B. Estimate the critical pressure of a n-hexane-n-decane mixture containing 40 mole percent
n-hexane. The experimental critical temperature is unknown.
From Chapter 1 :
n-Hexane
n-Decane
652.1
Critical temperature, deg F . . . . . . . . . . , . 453.6
Critical pressure, psia . . . . , , . . . . . . . . . . 436.9
305.20
From Chapter 2:
o1(n-hexane) = 0.3047
y (n-decane) = 0.4842
By equation (4B2.1-2):
Tpc
= (0.40) (453.6)+ (0.60)(652.1)
= 181.4 + 391.3 = 572.7 F
Conversion to absolute units:
Tpc
= 572.7
+ 459.7 = 1,032.4 R
Using Procedure 4B 1 . 1 the estimated critical temperature equals 1,054.3 deg R.
From equation (4B2.1-3):
pPc = (0.40) (436.9)+ (0.60) (305.2)
= 174.8 +183.1 = 357.9 psia
The molar average acentric factor is
n
2 3 y = (0.40) (0.3047) + (0.60) (0.4842)= 0.4124
I =
1
The critical pressure is then calculated from equation (4B2.1-1)
+ 357.9 [5.808 + 4.93 (0.4124)] X
= 357.9 + (357.9) (7.841) (0.021)
= 357.9
1,054.3 - 1,032.5
1,032.5
1
--`,,-`-`,,`,,`,`,,`---
P,,
= 416.8 psia
The experimental value (30) is 405.8 psia.
4-29
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A P I TDB CHAPTERM4
**
0732290 0536444 667 M
--`,,-`-`,,`,,`,`,,`---
482.2
ao
a1
a 2 0 3
0.4
o5
a6
Q7
a8
a9
10
MOLE FRACTION METHANE
1987
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4-31
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A P I TDB CHAPTERS4
SS
m
0732290 053b445 5T3
m
482.3
28
i
I
!
i
l
26
CRITICALPRESSURES OF
24
.-i
BINARY SYSTEMS
CONTAINING CARBON DIOXIDE
TECHNICAL DATABOOK
22
July 1973
J
Approved: TED 8. RPD
20
18
16
14
"
"
"
!
CARBON DIOXIDE 'HYDROGEN SULFIDE
CARBON DIOXIDE-METHANE
12
10
8
6
4
2
l
i
l
l
8
0.1
0.2
I
1
l
0.3
OA
0.5
06
a7
0.8
3
MOLE FRACTIONCARBONDIOXIDE
4-32
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--`,,-`-`,,`,,`,`,,`---
Not for Resale
A P I TDB
CHAPTERJ4
J*
m 07322r90 0536446
43T
m
462.4
21
20
19
--`,,-`-`,,`,,`,`,,`---
18
17
16
15
14
13
12
11
10
9
a
FIGURE 482.4
CRITICALPRESSURES OF
7
1
BINARY SYSTEMS
CONTAINING HYDROGEN SULFIDE
6
TECHNICAL DATA BOOK
July 1973
5
Approved. TED L RPD
4
4-33
1907
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A P I TDB CHAPTERt4 f t W 0732290 053611117 37b
482.2-482.4
COMMENTS ON FIGURES 482.2 THROUGH 4B2.4
Purpose
Critical pressure loci are presented for binary systems containing as one component methane, hydrogen sulfide, or carbon dioxide. Other systems are covered by Procedure 4B2.1.
Reliability
The maximum error to be expected from experimental data over the entire locus of each
curve is 1.0 percent.
Data Sources
Methane-ethane (13)
Methane-propane (1, 44, 48, 52)
Methane-n-butane (14, 50)
Methane-2-methylpropane (40)
Methane-n-pentane (7, 50)
Methane-n-heptane (42)
Methane-ethene (20)
Carbon dioxide-methane (51)
Carbon dioxide-propane (41, 51)
Carbon dioxide-n -butane (39)
Carbon dioxide-n -pentane (41)
Carbon dioxide-n -decane (43)
Carbon dioxide-hydrogen sulfide (5)
Hydrogen sulfide-methane (51)
Hydrogen sulfide-ethane (29)
Hydrogen sulfide-propane (31)
Hydrogen sulfide-n-pentane (51)
Hydrogen sulfide-n -decane (51)
Hydrogen systems show inconsistencies among sources of experimental data. For the
convenience of the user, the following references are available.
Hydrogen-methane (4)
Hydrogen-propane (51)
Hydrogen-n -hexane (37)
4-34
--`,,-`-`,,`,,`,`,,`---
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1987
A P I TDB CHAPTER+4
+f
m 0732290
0 5 3 b 4 4 8 202
m
453.1
PROCEDURE 483.1
METHOD FOR THE CRITICAL VOLUME
OF A MIXTURE OF DEFINED COMPOSITION
Discussion
The Chueh-Prausnitz equation (4B3.1-1) is to be used to calculate the critical volume of
of the pure components must be
a defined mixture. For this purpose the critical volume
known or estimated. The equation,which is applicable over the entire composition range,is
as follows:
For binaries,
v
,
,
= $1
K I
+ $2 v,,+ 241 $ 2 V l 2
(4B3.1-1)
In general,
(4B3.1-2)
(4B3.1-3)
, =I
(4B3.1-4)
(4B3.1-5)
(4B3.1-6)
Where:
--`,,-`-`,,`,,`,`,,`---
C
C
= 0.1559 if component i or j is a nonhydrocarbon.
= O if components i and j are hydrocarbons.
V,
=,true critical volume of mixture, in cubic feet per pound-mole.
V, = molar critical volume of component i, in cubic feet per pound-mole.
n = number of components in mixture.
i, j = any two of the components.
ut, , V;, , = correlation parameters.
C = empirically derived constant.
Procedure
Step 1: Obtain the critical volume and molecular weight of each component from Chapter
1. If values of the critical volume are not available, they may be calculated from methods
given in Section 4A of this chapter.
Step 2: Convert each critical volume to the desired units.
Step 3: Compute the value of C$ for each component from equation (4B3.1-3).
Step 4: Compute each qtl from equation (4B3.1-6).
Step 5: Obtain the value of C and compute each
using equation (4B3.1-5).
Step 6: Calculate the corresponding values of uir from equation (4B3.1-4).
Step 7: Compute the critical volume from equation (4B3.1-2).
v,
4-35
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API TDB CHAPTERt4
tf
m 0732290
053b449 L49
m
--`,,-`-`,,`,,`,`,,`---
463.1
COMMENTS ON PROCEDURE 483.1
Purpose
Procedure 4B3.1 can be used to predict the true critical volume of a mixturecontaining any number
of components. It is intended for use bothas a desk and acomputer method.
Limitations
This procedure was evaluated using the experimental critical volume of each pure component. If
estimated values of these parameters are used, errors may be higher.
This method has beenevaluated primarily with binarydata although it can be extended to higherorder systems. Very few experimental data are available for critical volumes of multicomponent
systems.
Reliability
Average errors in the calculated critical volume are about 8 percent (0.302cubic ft per lb-mole)for
non-methane hydrocarbon-hydrocarbon binary mixtures and
11 percent (O. 176 cubic ft per lb-mole)
for methane mixtures. The maximum deviation expected is approximately 40 percent.
For binary mixtures containing at least one nonhydrocarbon, the errors in the calculated critical
volume are about 9percent (0.1 cubic ft per lb-mole).
Special Comments
Although this procedure is not so accurate as the procedures for predicting other critical properties
of defined mixtures, it has been
included because it is the most accurate method available. Equation
(4B3.1-1)was evaluated with acomparatively small data set since only a small amount of critical volume data are available. The problem is further complicated bythe nonideality of most ofthe systems
considered. For mixtures having components of similar size, shape, and chemical family, it would
probably be better to use a simple molar average of the pure components as an estimate for the true
critical volume. Inthe Chapter 6 introduction, the discussion of excess volume of mixing may offer
additional guidelines.
Literature Sources
Adapted from Chueh, P. L. and Prausnitz, J. M., AIChE Journal 13 1107 (1967).
Example
Estimate the critical volume of a n-butane-n-heptanemixture containing 63 mole percent n-butane.
From Chapter 1:
1
2
n-Heptane
n-Butane
0.0704
0.0691
Critical volume, CU ft per lb ..............
Molecular
weight
......................
58.12
100.20
Conversion to molar units:
v, = (0.0704) (58.12)= 4.09
CU
ft per lb-mole
y2 = (0.0691) (100.20) = 6.92 CU ft per lb-mole
From equation (4B3.1-3):
01 =
(3.63)
(0.37)
(2.56)
-
(0.63) (4.09) 2/3
(0.63) (4.09) 'I3 + (0.37) (6.92) 2/3
(0.63)
(0.63) (2.56) + (0.37) (3.63)
e2 =
-
= 0.546
(0.37) (6.92) 2/3
(0.63) (4.09) 2/3
(0.37) (3.63)
= 0.454
By equation (4B3.1-6):
= 0.258
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+ (0.37) (6.92) 2/3
+ (0.63)
(2.56)
STD*API/PETRO TDB CHAPTER
4-ENGL
1982
0732290 O b 1 9 5 8 b 821 D
483.1
Using equation (4B3.1-5)
VI2 = -1.4864(0.258)
VI2 = 4.3835
The valueof y2 is now determined from equation
(4B3.14):
"12 =
VIZ
-0.3835 (4.09 + 6.92)
2.0
= -2.11
The critical volumeis then calculated from equation
(4B3.1-1):
V, = (0.546)(4.09)+ (0.454) (6.92)
+ (2.0)(0.546)(0.454) (-2.11)
V, = 4.33 CU ft per Ib-mole
--`,,-`-`,,`,,`,`,,`---
The experimental value(27) equals 4.53CU ft per lb-mole.
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4B4.1
PROCEDURE 4B4.1
ALTERNATE (COMPUTER) METHOD FOR CRITICAL
PROPERTIES OF A MIXTURE OF DEFINED COMPOSITION
In this procedure, the Soave equation of state and rigorous thermodynamicrelationships
are used to calculate the critical points of defined mixtures. The use of an equation of state
is considerably more complicated than the empirical methods. The application is only practical on a computer but does offer two important advantages.
First, the method offers versatility in representing anomalous critical behavior. Figure
4B4.1-1 illustrates that the critical behavior of the ethene-ethyne system discussed in the
introduction of this chapter can be accurately represented by the Soave equation with a
nonzero interaction coefficient. Figure 4B4.1-2 shows that a minimum temperature critical
locus is predicted for the n-octane-benzene system with a zero interaction coefficient.
Figures 4B4.1-3 through 4B4.1-5 show excellentreproduction of the qualitative features of
Figures 4-0.k and 4-0.8a. Furthermore, the empirical methods cannot predict the opposite
signs of the excess criticaltemperature and excess critical pressureof the benzene-n-decane
mixture or the changingsignof the excess critical pressure of the benzene-n-tridecane
mixture. Thus the equation of state method appears to be much more reliable than empirical
methods.
Second, the combined use of the equation of state method for critical points and vapor
liquid equilibrium, as described in Chapter 8, permits explorationof phase equilibria over a
wide range of conditions. Direct calculation of the critical locus before carrying out phase
equilibrium calculations may save considerable effort near the critical region.
Critical points of defined mixtures are estimated using the Soave modification of the
Redlich-Kwong equation of state. In order to compute the critical point of a mixture, the
equation of state must be solved to satisfy the following relationships:
det Q = det
.
ndZA
anman,
a3A
=O
. . .
anidnian,
flraZA
an,'
ANipNjAlv*=o
Where:
ANi
(4B4.1-1)
,i = 1, n are normalized components of a composition change vector whichare calculated as described below.
A = the Helmholtz free energy of the mixture.
ni = the mole number of component i in the mixture.
nr= the total number of moles in the mixture.
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--`,,-`-`,,`,,`,`,,`---
Discussion
484.1
PROCEDURE 484.1 (Continued)
PROCEDURE DIAGRAM FOR CRITICAL POINT CALCULATIONS
u
Calculate
No
g
Procedure
A flow chart for the calculation isshown inthe procedure diagram. The algorithm has been
adapted from Heidemann and Khalil (seeliterature sources below). Briefly,the calculational
steps are as follows:
Step 1: Obtain critical properties and acentric factorsof pure compounds from Chapter 1
or from one of the Procedures in Chapter 4.
Step 2: Calculate the initial guesses of V,and T,,.
(4B4.1-2)
(484.1-3)
--`,,-`-`,,`,,`,`,,`---
Correct
Where:
xi = mole fraction of ith component.
R = gas constant.
Step 3: Holding V,constant, iterate on T , to find det Q = O using a Newton iteration
scheme. Det 8 should be calculated according to subprocedure A.
4-39
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4B4.1
(4B4.1-5)
(4B4.1-6)
g4B4.14)
(4B4.1-9)
S,, =0.48508+l.55171~,
-0.1561hwf
(4B4.1-10)
S* un be f w d in Table 8D1.3
b, = O.O8664RT, /P,
(4B4.1-Il)
(4B4.1-12)
--`,,-`-`,,`,,`,`,,`---
+e+
abb
B,
Ba v + b
ba(v + b) +Th?
b
(4B4.1-13)
(4B4.1-14)
(4B4.1-15)
(4B4.1-17)
4-40
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484.1
n
mi=
-2 mjqi.jlqi,i
(4B4.1-19)
i+
1
--`,,-`-`,,`,,`,`,,`---
Where: q is the result of upper triangularization of Q.
This vector should then be normalized according to:
mi= A N ~ I ( Z A N)la;
(4B4.1-20)
Finally,
(4B4.1-21)
Where:
(li=j=k
3i=)#k, i=k#j, j=k#i
i#j#k, i#k
h,'(6
The factor
(9
y
has been added to improve the convergence of the algorithm.
+ b z (Dv + b ) Z + Eb 3 ( v +E b ) - v~+hb( ~ )
8.. =
[lOi i=#jj =j #kk o r i # k
F = bi bjbn
(4B4.1-23)
(4B4.1-24)
(4B4.1-25)
(4B4.1-26)
(4B4.1-27)
4-41
1999
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No reproduction or networking permitted without license from IHS
(4B4.1-22)
Not for Resale
484.1
900
890 880 870 860 -
I
I
I
l
I
1
f
I
1
I
I
FIGURE 4B4.1- 1
CRITICAL LOCUS FOR
ETHENE-ETHYNE SYSTEM
-
TECHNICAL DATA BOOK
June 1986
Approved
TED
.-m
Q
-
830
020 810
-
. 800 a"
790
780
770
-
--`,,-`-`,,`,,`,`,,`---
+ EXPERIMENnTAL
-.- SOAVE ( k i i - 0 )
- - KAY'S RULE
SOAVE (k;i : -1.5)
-
-
720
710
700
35
I
I
I
I
I
40
45
50
55
60
I
65
70
Tc, F
4-42
Copyright American Petroleum Institute
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No reproduction or networking permitted without license from IHS
I
Not for Resale
f
75
I
80
I
85
I
1
90
95
~~
STD.API/PETRO TDB CHAPTER q - E N G L 1982 W 0732270 Ub17592 0 2 5 W
--`,,-`-`,,`,,`,`,,`---
4B4.1-2
750
700
--
I
l
I
I
I
I
I
I
1
1
1
1
I
1
1
I
I
I
FIGURE 4B4.1-2
CRITICAL LOCUS FOR
---
SYSTEM
n-OCTANE BENZENE
TECHNICALDATA
June 1986
m
Approwad
TED
BOOK
I
-
---
-
L
-
.-
m
v)
Q
-550
--
lï
’. \
W.
-
\
*\
---
-
c
450
1
EQUATION
OF STATE WITH
- LI + KREGLEWSKI 8
5545
65
56
50
KAY
555
Tc, F
4-43
1999
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Not for Resale
STD.API/PETRO TDB CHAPTER
q-ENGL
0732290 Ob17573 T b 1
L782
m
--`,,-`-`,,`,,`,`,,`---
454.1-3
FIGURE 4B4.1-3
EXCESS CRITICAL'TEMPERATURE
TECHNICAL DATA BOOK
J u n e 1986
Approved TED
MOLE FRACTION BENZENE
SOAVE EQUATION FOR THE
BENZENE-n-PARAFFIN MIXTURES
OF HEXANE THROUGH TRIDECANE
1999
4-44
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--`,,-`-`,,`,,`,`,,`---
Copyright American Petroleum Institute
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Not for Resale
464.1 -5
FIGURE 4B4.1-5
EXCESS CRITICAL VOLUME
TECHNICALDATA
BOOK
June1 986
Approved TED
y - -
0.0 0.1 0.2 0.3 0.4 0.5
0.6 0.7
0.8
0.9 1.0
MOLE FRACTION BENZENE
SOAVE EQUATION
FOR THE
BENZENE-n-PARAFFIN MIXTURES
OF HEXANE THROUGHTRIDECANE
4-46
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--`,,-`-`,,`,,`,`,,`---
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COMMENTS ON PROCEDURE 484.1
4B4.1-5
?he procedure is presented as M optional computer method to dculate the true aitical
propcrrics of mixnrres. The procedure is consistent with the procedure for vapor liquid
equilibrium drvussed in Chapter 8. Binary interaction coefficients should k calculated as
described in Chapter 8.
Umit+tiOnS
A. Single variable Newton iteration schemes with numerical derivatives ( t g . , Secant
metbod or forward differencing) have k e n used oucmsfullyin the iterations on Z, and V,.
Multivariable methods appear to be ulvtliable becaw of undesired multiple roors.
B. Although infrequent, the following emon may k encountered and should k detected
by using counters and c ~ n d i t i resting.
~~l
1. Iteration on
' T may not converge.
2. Iteration on V, may not converge.
3. V, may converge to a vplue leu than the excluded volume b.
4. "
P m y k kzs thrn zero.
Rsrurtty
96
System Type
Methane-hydrocarbon
Hydrocarbon-hydrocarbon
Hydrocarbon-
%
ØUD
6.9
0.8
1.7
96
~ ~ ~ [ p s i a AAD
]
AAD
[ft3flwmolel
AAD(R)
AAD
32.8
4.9
2.0
86.7
13.9
16.0
6.3
9.3
0.35
11.6
5.3
76.0
18.22
0.45
0.3 1
mnhydrocarbon
This method has considerably better accuracy than the handcalculation procedures for
critical pressures.?be nccuracy is also better than that ofthe hand calculation proœdura for
all the Critical properries of assymmemc *es.
Special Comments
Tbc znraccive parameter "a" and my temperature dependent b i n q interaction
coefficients (cg., hydrogen mixnua)must k calculated in the same step as calculation of
det Q because of their temperature dependence.
B. A more recent algorithm has been published by Michelsen and Heidemann. The
Michelsen and Heidemann algorithm is less than twiceas fast as the algorithm recommended
here, howevtr, and d d e r a b l y more dif6cult to implement.
Lner8ture soumes
(1980).
Michckn, M.L..Heide-,
R. A.. "Calculation of Critical Points from Cubic TwoEquations of State." AIUlE J.,
521 (1981).
Constant
€xampk
Compute th¿ critical point of a mixture of 10 mole percent methaneand 90 mole percent
ethane.
,
T = 538.79R;,P = 770.54
psia; V,
= 2.1929
lbmol
ft3
--`,,-`-`,,`,,`,`,,`---
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4-47
4B4.1
Final iteration:
Tm= 538.96R ; V, = 2.621 ft3Ab mol
From Chapters 1 and 2:
e
--`,,-`-`,,`,,`,`,,`---
Component
T, (R)
(psial
1 Methane
343.00
666.40
2 Ethane
549.59
706.50
From equations (4B4.1-6) through (4B4.1-12):
= 6619.8
u22 = 21323.9
bl = 0.4785
b2 = 0.7235
U = 19477.1
b = 0.6990
U; = 22710.0
a> = 40759.2
V, ft3Ab mol
W
1 S90
0.0 108
0.0990
2.337
From equations (4B4.1-13) through (4B4.1-17):
a2A
nTaz
n$2A
= 2.3156
~
"1
n -
a2A
.
= 0.003149
a2"2
= -0.08538
.
From equation(4B4.1-I):
Upper triangularizing:
-
r
From equation (4B4.1-18):
detQ = detq-= (2.3156) X 9(10-7) = 2.1(104) = O
From equation (4B4.1-19):
AN2= 1
AN1 = 0.0853812.3156 = 0.036869
From equation (4B4.1-20):
AN2 = 1/(1 + 0.0368692)"2 = 0.999321
A N 1 = 0.0368694 1+ 0.0368692)1n= 0.036844
From equations (4B4.1-23) through (4B1.1-27):
From equations (4B4.1-21) and (4B4.1-22):
= 1.899 [- 1.988 + 0.818 + 33.464 - 32.501 = 0.0836
Note: This isreasonablyclosetozerobecause
From equation (4B4.1-5):
( )
is very large.
em= 772.34 psia
From equation (4B4.1-4):
ft
vm(corrected) = 2.2281 __
lb mol
4-48
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1992
Not for Resale
A P I TDBCHAPTERs4
**
m
0732290 0 5 3 b 4 b 2 6 8 2 D
4C1.1
260
0.36
0.35
E
FIGURE 4Cll
TRUECRITICALTEMPERATURE
OF NATURAL GAS MIXTURES
0.34Z 2 , 0
TECHNICAL DATA BOOK
July 1973
300
f
Approved: TED & RPD
1
I
r0
0.32
f 320
--`,,-`-`,,`,,`,`,,`---
0.30-$340
+'
0'29E360
Z
Ti
o,
0.28
Lu
i 3 * 0
0.27-$
d
6L
$400
0.26
-$
L 440
4-49
1987
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m
A P I TDB CHAPTERx4 X *
4C1.1
07322900536463
519 W
COMMENTS ON FIGURE 4C1.1
Purpose
The critical temperature of a natural gas mixture in which methane is the predominant component
is estimated from thisfigure.
Limitations
The API gravity and the molal average boiling point (MABP) must be known or estimated by
methods given in Chapter 2. The method was evaluated only with experimental data for mixtures
containing more than 60 mole percent methane. For mixtures of lower methane content, errorsmay
be larger. The method should not be used for natural gas mixtures containing more than 10 mole
percent nitrogen or 3 mole percent carbon dioxide.
Reliability
The average error in estimating the critical temperature of a natural gas is about one percent or
k4 deg F. The maximum deviation expected is about 30 deg F.
Special Comments
The molal average boiling point, in degrees Fahrenheit is
n
C x,Gi
MABP =
i= 1
Where:
MABP = molal average boiling point, in degrees Fahrenheit.
n = number of components.
xi = mole fraction of component i.
Tb; = normal boiling point of component i, in degrees Fahrenheit.
The specific gravity at 60 deg F may be converted to API gravity by using Table 6Al.l or by
rearranging equation (6-0.2) from Chapter6.
In general, the liquid specific gravities (60 F/60 F) used in calculating the weight average for the
mixture are taken from Chapter l. For methane, ethane, carbon dioxide, and nitrogen, however, the
following values must be used.
Effective
Effective
Specific Gravity
API Gravity
60 FI60 F
Methane0.300
....................
340
Ethane .....................
265.76
0.3562
Carbon dioxide. . . . . . . . . . . . . . .
41.48
0.8180
Nitrogen ....................
43.32
0.8094
The weight fraction of each component may be obtained from the mole fraction using the following
equation:
x .=W1
x; Mi
n
C XiY
i= 1
(4Cl.l-2)
Where:
xwi = weight fraction of component i.
Mi = molecular weight of component i.
The following equations can be used instead of Figure 4Cl. 1:
Tl = Axexp[BxTMBP+CxSG+DxSGxTMBP]
= (T~JIBP)~
T3 =
T = T1 x h x T3
T = Critical Temperature (Rankine)
SG = Specific Gravity
TMBP = Molal Average Boiling Point (Rankine)
A = exp (-5.624853)
D = 0.013200830
B = -0.01058520
E = 2.4289880
c = -1.44011260
F = -0.2998080
4-50
1992
--`,,-`-`,,`,,`,`,,`---
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Not for Resale
A P I TDB CHAPTERx4
X*
m
0732290 0 5 3 b 4 b 4 455
m
4C1.i
Literature Source
This figure was adapted with permission from the Engineering Dura Buok, Mobil Oil Company,
Inc.
Example
Estimate the true critica1 temperature of a natural gas mixture having the following composition:
--`,,-`-`,,`,,`,`,,`---
Mole
Fraction
Methane. . . . . . . . . . . . . . . . . . . . . . . . . 0.868
Ethane ..........................
0.065
Propane .........................
0.025
n-Butane . . . . . . . . . . . . . . . . . . . . . . . . 0.007
Nitrogen . . . . . . . . . . . . . . . . . . . . . . . . 0.034
1.o00
From Chapter 1:
Methane
Molecular weight . . . . . . . . . . . . .
16.04
Normal boiling point, deg F. . . . -258.73
API gravity. . . . . . . . . . . . . . . . . . 340"
I
Ethane
30.07
-127.49
265.76"
Propane
44.10
43.75
147.60
n-Butane
58.12
3 1.O8
110.79
Nitrogen
28.01
-320.45
43.32*
The molal average boiling point is computed using equation (4Cl.l-1):
MABP = (0.868) (-258.73) + (0.065) (-127.49)
+ (0.025) (-43.75) + (0.007) (31.08)+ (0.034) (-320.4)
= -224.6 -8.3 -1.1 + 0.2 -10.9
= -244.7 F
The average molecular weight of the mixture is:
MW, = (0.868) (16.04) + (0.065) (30.07)+ (0.025) (44.10)
+ (0.007) (58.12)+ (0.034) (28.01)
= 13.92+1.95+1.1+0.41+0.95
= 18.33
The weight fraction of each component is calculated from equation (4Cl.l-2).
(0.868) ( 16.04)
18.33
= 0.760
xZ,
= O. I07
~~3 = 0.060
xw4 = 0.022
x,g = 0.052
XWI
=
The weight average gravity in degrees API is:
API gravity = (0.760) (340)+ (0.107) (265.76)+ (0.060)(147.60)
+ (0.022) (110.79)+ (0.052) (43.32)
= 300.38 API
From Figure 4C l. 1,
T, = -84.0 F.
Literature value ( 18) = -8 1.3 F.
*Taken from Special Comments.
1992
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4-51
Not for Resale
A P I TDB CHAPTER84
**
m
0732290 0536465 391
m
--`,,-`-`,,`,,`,`,,`---
4D1.1
PROCEDURE 4D1.1
METHOD FOR THE CRITICAL TEMPERATURE
OF PETROLEUM FRACTIONS
Discussion
The Roessequation (4D1 .l-1) is to be used to calculate the true critical temperature of apetroleum
fraction. For this purpose the specific gravity and volumetric average boiling point (VABP) of the
fraction must be known or estimated. The equation is asfollows:
T ,= 186.16 + 1.66676 -0.7127(10”) A’
A = (sp gr) x (VABP + 100.0)
(4Dl.l-1)
(4Dl.l-2)
Where:
T,= true critical temperature of fraction, in degrees Fahrenheit.
sp gr = specific gravity, 60 F/60 F.
VABP = volumetric average boiling point (defined in comments on Figure 2Bl.l), in degrees
Fahrenheit.
Procedure
Step 1: If values of VABP and specific gravity are not known, obtain these parameters from methods given in Chapter2. The average molecular weight and an ASTM D86 distillation for thefraction
should be known if these estimates are required. If a true boiling point (TBP)or ASTM D l 160 distillation is given, it should be converted to an ASTM D86 distillation by the methods of Chapter 3.
Step 2: Compute the value of A using equation (4D1.1-2).
Step 3: Calculate the true critical temperature from equation (4D1.1-1).
4-53
1992
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Not for Resale
**
A P I TDBCHAPTER*9
m
0732290 0536966 228
m
4D1.1
COMMENTS ON PROCEDURE 4D1.1
Purpose
An equation is given for calculating the true critical temperature of a petroleum fraction
(a mixture of undefined composition). This method is intended for use both as a desk and
a computer method.
Limitations
This equation was evaluated with petroleum fractions characterizedby the following physical property ranges:
Critical temperature, deg F. . . . . . . . . . . . . . 550 to 1,000
Critical pressure, psia.. . . . . . . . . . . . . . . . . . 250 to 700
Specific gravity, 60 FI60 F. . . . . . . . . . . . . . . 0.660 to 0.975
Most of the fractions were made up by blending base stock such as: Mid-Continent straight
run gasoline, cracked naphtha, Mid-Continent kerosine, Mid-Continent gas oil, naphthene
base gas oil, Pennsylvania crudes, and the more recent data from North Slope fractions. If
the aforementioned physical property ranges are exceeded, errors may be larger.
Reliability
Errors in the calculated critical temperatures are about one percent ( k 6 deg F) using this
procedure. The maximum deviation expected is 22 deg F.
Special Comments
The Edmister-Pollock chart (12) which is as accurate as equation (4Dl.l-1) for predicting
the critical temperature of petroleum fractions, may also be used. However, since an equation form is convenient forboth desk calculation and computerusage, the Roess equation has
been selected.
The critical temperature of mixtures for which other procedures of this chapter do not
apply may be calculated by this procedure. However, the errormay be higher than indicated
under Reliability.
Literature Source
Adapted from Roess, L. C., J . Inst. Petrol. Tech. 22 665 (1936)
Example
Estimate the critical temperature of the following NorthSlope naphtha. The specific
gravity is 0.7762 at 60 F/60 F and the volumetric average boiling point is 290.4 deg F.
From equation (4D1.1-2):
A = (0.7762)(290.4 + 100.0)
= 303.0
By equation (4Dl.l-1):
T ,= 186.16
= 625.7
+ (1.6667)(303.0) - 0.7127(10-3)(303.0)2
F
The experimental value (30) = 632.7 F.
4-54
1987
--`,,-`-`,,`,,`,`,,`---
Copyright American Petroleum Institute
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Not for Resale
A P I TDB
CHAPTER*4
*X
m
0 7 3 2 2 9 0 053b4b7 Lb4
m
4D2.1
'
c
900
900
800
800
700
700
600
600
z
B
.-O
0
8
z1
Lu
E
S
æ
500
500
p.
m
2
u<
t
Y?
um
cd
U
l-
Lu
z
93
400
400
300
300
20c
200
1oc
1 100
1987
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
--`,,-`-`,,`,,`,`,,`---
Not for Resale
4-55
A P I TDBCHAPTERt4
tt
m
0732290 053bYb8 O T O
m
4D2.1
COMMENTS ON FIGURE 402.1
Purpose
The true critical pressure
of a petroleum fraction is estimated from Figure 4D2.1, which relates the
true critical pressureof petroleum fractions to theASTM slope, ASTM volumetric average boiling
point. and the API gravity of the fraction. This figure was developed by plotting all available
(9) data
for the true critical pressures
of fractions, and smoothing the resulting curves.
Limitatlons
This method was evaluated with petroleum fraction data characterized
by the following physical
property ranges:
Critical temperature, deg F ............. 550 to 1,OOO
Critical pressure, psia.................. 50 to 700
Specific gravity,60 F/60 F. ............. 0.660 to 0.975
Most of the fractions were made upby blending base stocks such as: Mid-Continent straight run
gasoline, cracked naphtha, Mid-Continent gas oil, naphthene base gas
oil, Pennsylvania crudes, and
the more recentdata from NorthSlope fractions. If the aforementioned physical property ranges are
exceeded, errors may be larger.
Reliability
Errors in the calculated critical pressuresare about three percent (*16 psia) using this procedure.
The maximum deviation expected
is 60 psia.
Special Comments
--`,,-`-`,,`,,`,`,,`---
An advantage of this figure is that the correlating parameters can be determined directly from
standard inspection tests. If all of the parameters are not available, they may be estimated from
methods given in Chapter 2.
Figure 4D2.1 has been computerized and
is listed asP X 2 of Chapter 16.
Literature Source
Adapted from Edmister,W. C., and Pollock, D. H.,Chem. Eng. Progr. 44 905 (1948).
Example
Estimate the critical pressure
of a North Slope naphtha having the following properties:
VABP = 497.4 deg F
A P I gravity = 41.8
ASTM slope = 0.35 deg F/percent distilled
Locate 497.4 deg F on the left-hand vertical temperature axis. Draw a horizontal line from this
point until it intersects the 41.8 deg API gravity line.
Construct a vertical line from this point of intersection until it reaches an ASTM slope value
of 0.35.
A horizontalline from this point intersectsthe critical pressure axis at a value
of 342 psia.
The experimental value (30) is 342 psia.
4-56
Copyright American Petroleum Institute
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1992
Not for Resale
**
A P I TDBCHAPTER*4
m
0732290 O536469 T 3 7
m
--`,,-`-`,,`,,`,`,,`---
403.1
PROCEDURE 4D3.1
METHOD FOR THE PSEUDOCRITICAL TEMPERATURE
OF PETROLEUM FRACTIONS
Discussion
Equation (4D3.1-1) is used to calculate the pseudocritical temperature of petroleum fractions. For this purpose, specific gravity and mean average boiling point must be known or
estimated. The equation is as follows:
T,,= 10.6443 [exp(-5.1747
x T,"81067 S O 53691
x
G -0.54444s + 3.5995 X
GS)]
(4D3.1-1)
Where:
Tpc
= pseudocritical
temperature of petroleum fraction, degrees Rankine.
= mean average boiling point, degrees Rankine.
S = specific gravity, 60 FI60 F.
Equation 4D3.1-1 is also shown in Figure 4D3.2 in terms of the Watson K and API gravity.
Where:
Watson K
TL"
S
=-
141.5 - 131.5
API gravity = S
Procedure
Step I: Obtain the specific gravity of the petroleum fraction.
Step 2: Obtain the mean average boiling point using Figure 2B1.2.
Step 3: Calculate the pseudocritical temperature using equation (4D3.1-1) or read it from
Figure 4D3.2 after converting specific gravity to API gravity.
4-57
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Not for Resale
++ m
A P I TDBCHAPTER+4
0732290 053bY70 759
m
4D3.1
COMMENTS ON PROCEDURE 403.1
Purpose
An equation is givenfor calculating the pseudocritical temperature of a petroleum fraction
(a mixture of undefined composition).Thisequation is intendedas both a desk anda
computer method.
Limitations
Equation (4D3.1-1) is valid over the following range of molecular weight, normal boiling
point, and API gravity:
Range of Data
70-295
80-650
6.6-95.0
Molecular weight
Normal boiling point,
degrees
Fahrenheit
API gravity
In Figure 4D3.2 dotted lines represent extrapolated values and should be used with caution.
Reliability
Equation (4D3.1-1) can reproduce pure hydrocarbon critical temperature data to
within an
average error of 0.8 percent. T i e correlation was not evaluated using petroleum fraction data
as pseudocritical temperature is defined rather than measured.
--`,,-`-`,,`,,`,`,,`---
Literature Source
Equation (4D3.1-1) is a 1985 modification of the correlation developed by M. R. Riazi,
Fractions," Ph.D. Thesis, De"Prediction of Thermophysical PropertiesofPetroleum
partment of Chemical Engineering, The Pennsylvania State University, University Park, Pa.,
1979.
Example
Calculate the pseudocritical temperature of a petroleum fraction with specific gravity (60
F/60 F) of 0.8160 and the following ASTM D86 distillation properties.
Distillation, percent by volume
Temperature, degrees Fahrenheit276
30
9010
70
227 509 413
50
340
From Figure 2B1.2, the mean average boiling point is 329 F or 789 R.
By equation (4D3.1), the pseudocritical temperature is:
T,,= 10.6443 exp("5.1747 X
x 789 - 0.54444 x 0.8160
+ 3.5995 x
x 789 x 0.8160)(789)""O6'
(0.8160)" 536y'
= 1145 R
The pseudocritical temperature of this petroleum fraction is, therefore, 685 F. No experimental value is available because pseudocritical temperature is defined rather than measured. To estimate the pseudocritical temperature from Figure 4D3.2, first calculate the
Watson K and API gravity.
141 5
141 5
API gravity = -- 131.5 = -- 131.5 = 41.9
S
0.8160
K="= 789''3
0.8160
.3
Using Figure 4D3.2:
G,= 1148 R = 688 F.
4-58
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TDB CHAPTER*L)
X*
0732290 0536473 b 9 5
4D3.2
2000
1800
a
d
1600
a
U
1400
3
W
I-
<
1200
O
W
800
600
-30-20-10
O
10 20 30 40 50 60 70 8090100110
4-59
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--`,,-`-`,,`,,`,`,,`---
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**
0732290 0536472 521
m
4D3.3
PROCEDURE 403.3
TRUE AND PSEUDOCRITICAL TEMPERATURESOF MIXTURES CONTAINING BOTH
IDENTIFIED HYDROCARBONS AND PETROLEUM FRACTIONS
Discussion
This procedure estimatesthe true andpseudocritical temperatures of mixtures containing
both identified hydrocarbons and petroleum fractions. The procedure is applicable where
several of the more volatile components of a mixture are identified as pure hydrocarbons.
The remainder is described as one or more petroleum fractions, each of which is characterized only by an ASTM D86 distillation curve and an API gravity.
Procedure
Step I : Obtain the necessary input data. A mole percent analysis must be available for the
entire fraction, with the unidentified portion treated as a pseudocomponent. An ASTM D86
distillation curve and the API gravity are also necessary for the unidentified portion as well
as the molecular weights, which can be estimated using the methods of Chapter 2. Use the
molecular weights and API gravities for the pure components that are required for the
calculations from the tables in Chapter 1, but the following effective gravity values must be
used for the light hydrocarbons:
Effective
Effective
Specific Gravity
API Gravity
60 F/60 F
440
O. 247
Methane. ...................
Ethane .....................
213
0.41
213
0.41
Ethene (ethylene) . . . . . . . . . . .
Step 2: If the available characterizing distillations differ from ASTM Method D86, convert
using the methods in Chapter 3.
Step 3: For each unidentified portion, calculate the volumetric average boiling point as the
weighted average of the ASTM D86 distillation temperatures after 10, 30, 50, 70, and 90
+
-k
' O
5
+
T,n
+-
Tw. Also, calculate the slope
assuming a linear distillation curve between the 10- and 90-percent points,
Tu0 m,
in
K O
--`,,-`-`,,`,,`,`,,`---
percent by volume have been distilled, "
degrees Fahrenheit per percent distilled.
Step 4: Using the figures in Chapter 2, obtain the mean, molal, and cubic average boiling
points for the unidentified portions.
Step 5: Using the component molecular weights and mole fractions, calculate the mixture
average molecular weight. Determine all the component weight fractions by dividing the
product of the molecular weight and mole fraction forthe component by the mixture average
molecular weight.
Step 6: Using the component weight fractions and API gravities, calculate the weight
average API gravity and specific gravity for the entire mixture.
Note: Skip Steps 7 and 8 if only the true critical temperature is desired.
Step 7: Using the component weight fractions and component specific gravities, calculate
the component volume fractions by dividing the quotientof the component weight fractions
and specific gravities by the sum of the quotients for all components
Step 8: Using the component mole fractions and volume fractions, respectively, together
with the molal average and cubic average boiling points of each component [normal boiling
points for purehydrocarbons), calculate themolal and cubic average boiling points from the
definitions in the Chapter 2 introduction. Calculate the mean average boiling point from its
definition.
Note: Skip Step 9 if only the pseudocritical temperature is desired.
Step 9: Using the componentvolume fractions and the volume average boiling point of each
component, calculate the volume average boiling point from the definition in Chapter 2.
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CHAPTER*4
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0732290 053b473 468
m
4D3.3
Step 10: Calculate the truecritical temperature using the volume average boiling point from
Step 9 and the specific gravity for the mixture from Step 6 in Procedure 4D1.1.
Step 11: Calculate the pseudocritical temperature using the mean average boiling point
from Step 8 and the specific gravity for the mixture from Step 6 in Procedure 4D3. l.
COMMENTS ON PROCEDURE 4D3.3
Purpose
True and pseudocritical temperatures of mixtures containing both identified hydrocarbons
and petroleum fractions are estimated by this procedure. For the true and pseudocritical
pressures of these mixtures, use Procedure 4D4.3.
Limitations
This method is limited to mixtures containing both identified hydrocarbons and petroleum
fractions and is applicable only to Type I critical loci (see introduction).
Reliability
Data are not available to evaluate the reliability of this procedure.
Special Comments
--`,,-`-`,,`,,`,`,,`---
The various average boiling points are defined and correlated in Chapter 2.
When ASTM D86 distillation data are used to obtain the boiling points, temperatures
above 475 F must be corrected for cracking by equation (3Al.l-1).
Literature Source
The procedure was developed by Hadden, S. T., Chem. Eng. Progr. 44 135 (1948).
Example
Calculate the true andpseudocritical temperature of a Conroe crude oil that is characterized by the following data:
Mole Fraction
0.3223
0.0424
0.0335
0.0108
0.0148
0.0218
.
0.5544
1.o000
Methane .................................
Ethane ..................................
Propane .................................
2-Methylpropane. .........................
n-Butane ................................
Pentanes. ................................
Hexane and heavier.. .....................
The hexane-and-heavier portion has an API gravity of 38.0, molecular weight of 172, and
the following ASTM D86 distillation properties:
10
Distillation, percent by volume ........
Temperature, degrees Fahrenheit ...... 372234
30
50
592*
478
70
90
722*
From the distillation, the volumetric average boiling point is 480 F and the 10-percent to
degrees Fahrenheit
90-percent slope is 6.10 percent distilled .
From Chapter 2, Procedure 2Bl.1, the mean average boiling point for the hexane-andheavier portion is 423 F, the molal average boiling point is 386 F, and the cubic average
boiling point is 457 F.
To calculate the various average properties of the entire crude oil, the
following tabulation
is convenient. The average boiling points of pure substances are equal totheir normalboiling
points.
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TDB CHAPTERS4
tt D 0732290 053b474 3T4 D
4D3.3
(2)
(3)
MABP
(Degrees
Mole
Mole FahrenFraction
Weight heit)
Methane . . . . . . . . . . . 16.04
Ethane. . . . . . . . . . . . . 30.07
Propane. . . . . . . . . . . . 44.10
2-Methylpropane . . . . 58.12
n-Butane . . . . . . . . . . . 58.12
Pentanes . . . . . . . . . . . 72.15
C, + fraction. . . . . . . . 172
0.3223
0.0424
0.0335
0.0108
0.0148
0.0218
0.5544
-258.73
-127.49
-43.75
10.678
3 .O8
1
89
386
0.0486
0.0120
0.0139
0.0059
0.0081
0.0148
0.8967
Total . . . . . . . . . . . . . . .
Calculated mixture
average . . . . . . . . 106.3
1.o00
...
1.o00
...
API
SPG
Gravity
0.247
340
0.410
265.76
0.508
147.6
0.563
119.89
0.585
110.79
0.628
93.9
0.835 0.7808 38.0
Weight
Fraction
126.2
0.727 1
O. 1431
0.0213
0.0 199
0.0076
0.0101
0.0172
...
...
63.1
.o00
...
...
Volume
Fraction
(8)
(9)
CABP
VAPB
(Degrees (Degrees
FahrenFahrenheit)
heit)
-259
-127
-44
11
31
89
457
268.8
-259
-127
-44
11
31
89
480
336.1
From columns 1 and 2,the mixture average molecular weight is 106.3. This value was used with
each pairof entries in columns 1 and 2to calculate the weight fractions listed in column 4by Step 5.
Step 6 was followed to determine mixture average API and specific gravities in columns 5 and 6.
Volume fractions in column 7 were determined
by the procedures of Step 7.
From the procedures of Step 8, the mixure molal average and cubic average boiling points in
columns 3 and 8are calculated.
MeABP =
MABP + CABP
2
- 126.2+268.8
= 197.5 F
2
--`,,-`-`,,`,,`,`,,`---
The mixture volumeaverage boiling point in column is
9 calculated from Step 9.
The true critical temperature is calculatedfrom the VABP andspecific (API) gravity for the mixture
using Procedure 4D1.l. The result is 643 F.
The pseudocritical temperature is calculated from the MeABP and specific (API) gravity for the
mixture using Procedure4D3.1 or Figure 4D3.2. The result readfrom the figure is 990 R or 530 F.
*From vacuum assayconverted by the methods in Chapter3.
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W 0732270 05361175 230 W
4D4.1
PROCEDURE 404.1
METHOD FOR THE PSEUDOCRITICAL PRESSURE OF PETROLEUM FRACTIONS
Discussion
Equation (4D4.1-1) calculates the pseudocritical pressure of petroleum fractions. For this
purpose, specific gravity and mean average boiling point must be known or estimated. The
equation is as follows:
P,.
= 6.162 x
lo6 [exp(-4.725 X
S)] T;" 4844 S
- 4.8014s
+ 3.1939 X
(4D4.1-1)
Where:
cc= pseudocritical pressure, pounds per square
inch absolute.
Tì,= mean average boiling point, degrees Rankine.
S = specific gravity, 60 F/60 F.
Equation 4D4.1 is also shown in Figure 4D4.2 in terms of the Watson K and API gravity
where
Tl3
141.5
Watson K = -and API gravity = -- 131 S .
S
S
Procedure
Step 1: Obtain the specific gravity of the petroleum fraction.
Step 2: Obtain the mean average boiling point using Figure 2B1.2.
Step 3: Calculate the pseudocritical pressure using equation (4D4.1-1) or read it from
Figure 4D4.2.
--`,,-`-`,,`,,`,`,,`---
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A P I TDB CHAPTERS4 SS
0732290 0536476
L77
m
4D4.1
COMMENTS ON PROCEDURE 4D4.1
Purpose
An equation is given for calculating the pseudocritical pressure of a petroleum fraction (a
mixture of undefined composition). This equationis intended as both a desk and a computer
method.
Limitations
Equation (4D4.1-1) is valid over the following range of molecular weight, normal boiling
point, and API gravity:
Range of Data
Molecular weight
70-295
Normal boiling point,
degrees
Fahrenheit
80-650
API gravity
6.6-95.0
In Figure 4D4.2 dotted lines represent extrapolated values and should be used with caution.
Reliability
Equation (4D4.1-1) can reproduce pure hydrocarbon critical pressure data to within an
average error of 2.6 percent. The correlation could not be evaluated using petroleum fraction
data because pseudocritical pressures are defined rather than measured.
Literature Source
Equation (4D4.1-1) is a 1985 modification of a correlation developed by M. R. Riazi,
“Prediction of Thermophysical Properties of Petroleum Fractions,” Ph.D. Thesis, Department of Chemical Engineering, The Pennsylvania State University, University Park, Pa.,
1979.
Example
Calculate the pseudocritical pressure of a petroleum fractionwith specific gravity (60 FI60
F) of 0.8160 and the following ASTM D86 distillation properties:
Distillation, percent by volume
Temperature, degrees Fahrenheit 276
10
227
70
30
509 413
50
340
90
From Figure 2B1.2, the mean average boiling point is 329 F or 789 R.
By equation (4D4.1-1), the pseudocritical pressure is:
PVC= 6.162 x lo6 [exp(-4.725
+ 3.1939 x
X
x 789.0 - 4.8014 x 0.8160
x 789.0 x 0.8160)](789.0)-’ 4844 (0.816~1)~
= 396 psia
To estimate the pseudocritical pressure from Figure 4D4.2 first calculate the Watson K and
API gravity.
141.5 = -131.5
API = S
=
“
141 5
0.8160
131.5 =41.9
Using Figure 4D4.2:
&c
= 400
psia
No experimental value is available because pseudocritical pressure is defined rather than
measured.
--`,,-`-`,,`,,`,`,,`---
1987
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A P I TDBCHAPTER*4
**
W 0732290 O536477 003 W
4D4.2
PSEUDOCRITICAL PRESSURE
OFPETROLEUM FRACTIONS
I
TECHNICAL DATA BOOK
Approved TED
800
700
W
a
--`,,-`-`,,`,,`,`,,`---
500
1O 0
O
-10
O 10 2 0 30 40 50 6 0 7 0 80 90 100110
API GRAVITY
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m
0732290053b478
T4T
m
4D4.3
PROCEDURE 4D4.3
TRUE AND PSEUDOCRITICAL PRESSURES OF MIXTURES CONTAINING BOTH
IDENTIFIED HYDROCARBONS AND PETROLEUM FRACTIONS
Discussion
This procedureshould be used to estimate thetrue and pseudocritical pressures of mixtures
containing both identified hydrocarbons and petroleum fractions. For example, the procedure is applicable where several of the morevolatile components of a mixture are identified
as pure hydrocarbons and the remainder are described as oneor more petroleum fractions,
each of which is characterized only by an ASTM D86 distillation curve and an API gravity.
Figure 4D4.4 is included in this procedure.
Procedure
Step 1: Obtain the true and pseudocritical temperatures of the mixture using Procedure
4D3.3. Convert these to absolute temperatures, and calculate the value of the ratio of true
to pseudocritical temperatures. Retain all intermediate calculations from Procedure 4D3.3.
Step 2: Use the weighted average specific gravity and the mean average boiling point for
the entiremixture in Procedure 4D4.1 to calculate the pseudocritical pressure of the mixture.
Step 3: With the pseudocritical pressure and the critical temperature ratio from Step1, use
Figure 4D4.4 or Equation 4D4.3-1 to determine the true critical pressure of the mixture.
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m
0732290 O536479 9Bb
m
404.3
COMMENTS ON PROCEDURE 4D4.3
Purpose
True andpseudocritical pressures of mixtures containing both identified hydrocarbons and
petroleum fractions are estimated by this procedure. For true and pseudocritical temperatures of these mixtures, use Procedure 4D3.3 (which is also required in this procedure).
Limitations
--`,,-`-`,,`,,`,`,,`---
The procedure is limited to mixtures containing both identified hydrocarbons and petroleum fractions and is applicable only to Type I critical loci (see introduction).
Reliability
Data are not available to evaluate the reliability of this procedure.
The errorsin true critical pressures of defined hydrocarbon mixtures estimated from Figure
4D4.4 are within an average of 5 percent for critical pressures less than 1000 pounds per
square inch absolute. The magnitude of error in estimating true critical pressures above 1000
pounds per squareinch absolute by this figure is unknown. Severe errors occur for methanerich systems having critical pressures greater than 2000 pounds per square inch absolute or
critical temperatures less than 100 F.
Special Comments
The various average boiling points are defined and correlated in Chapter 2. Figure 4D4.4
may be replaced by the following regression equation:
logPC= 0.050052 + 5.656282 lOg(T,/T,,) - 1.001047 log&,
(4D4.3-1)
Literature Source
The procedure was developed by Hadden, S . T., Chem. Eng. Progr. 44 135 (1948).
Figure 4D4.4 was adapted with permission from the Engineering Datu Book, Mobil Oil
Company, Inc. It was based on Smith, R. L., and Watson, K. M., Ind. Eng. Chem. 29 1408
(1937).
Example
Calculate the true and pseudocritical pressures of the Conroe oil of the example of
Procedure 4D3.3. From this example the true critical temperature is 643 F, and the pseudocritical temperature is 530 F.
Step 1:
- 643 + 460 - 1103 T,, 530 + 460 - 990 -
"
Step 2: Using Procedure 4D4.1 or Figure 4D4.2 the pseudocritical pressure is 450 psia.
Step 3: Using Figure 4D4.4, the true critical pressure is 910 psia.
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A P I T D BC H A P T E R t 4
tt
m
0732290 0536480 bT8
m
4D4.4
FIGURE 4D4.4
TRUE CRITICAL PRESSURES
OF PETROLEUM FRACTIONS
TECHNICALDATA
BOOK
June 1888
Approved
TED
a
--`,,-`-`,,`,,`,`,,`---
c
I
L
FOR
USE
ONLY WITH
I
PROCEDURE 4D4.3
I-
L1.0
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**
m
0732290 053b48L 5 3 4
m
BIBLIOGRAPHY
1. Akers, W. W., Bums, J. F., Fairchild, W. R., “LowTemperature Phase Equilibria. Methane-Propane System,”
Znd. Eng. Chem. 46 2531 (1954).
2. Ambrose, D., “Correlation and Estimation of VaporLiquid Critical Properties-I. Critical Temperatures of Organic Compounds,” Nat’l.Phys. Lab. Report,Chem. 92,
Sept. (1978).
3. Ambrose, D., “Correlation and Estimation of VaporLiquid Critical Properties-II. Critical Pressures and Critical
Volumes of Organic Compounds,” Nat’l Phys. Lab. Report,
Chem. 98, May (1979).
4. Benham, A. L., Katz, D. L., “Vapor-Liquid Equilibria
for Hydrogen-Light Hydrocarbon Systems at Low Temperatures,” AIChE Journal3 33 (1957).
5. Bierlein, J. A., Kay, W. B., “Phase Equilibrium Properties of System Carbon Dioxide-Hydrogen Sulfide,” Znd.
Eng. Chem. 45 618 (1953).
6. Chang, H. L., Hurt, L. J. and Kobayashi, R., “VaporLiquid Equilibria of Light Hydrocarbons at Low Temperatures and High Pressures: The Methane-n-Heptane System,”
AZChE J . 12 1212 (1966).
7. Chen, R. J., Chappelear, P. S . , Kobayashi, R., “Dew
Point Loci for Methane-n-PentaneBinary System,” J . Chem.
Eng. Data 19 58 (1974).
8. Chueh, P. L., Prausnitz, J. M.,‘Vapor-Liquid Equilibria at High Pressures: Calculations of Critical Temperatures, Volumes, and Pressures of Nonpolar Mixtures,”
AlChE Journal 13 1107 (1967).
9. Churchill, S. W., Collamore, W. G., Katz, D. L.,
“Phase Behavior of the Acetylene-Ethylene System,” Oil Gas
J . 41 [13]
33 (1942).
10. Edmister, W. C., “Applications of Thermodynamics to
Hydrocarbon Processing-Part XXII: Convergence Correction to Vapor-Liquid Equilibrium Ratios,” Petrol. Refiner 28
[9]95 (1949).
11. Edmister, W. C., “Applications of Thermodynamics to
Hydrocarbon Processing-Part X: Pseudo-Critical for Mixtures,” Petrol. Refiner 27 [4]
213 (1948).
12. Edmister, W. C., Pollock, D. H., “Phase Relations for
Petroleum Fractions,” Chem. Eng. Progr. 44 905 (1948).
13. Ellington, R. T., Eakin, B. E., Parent, J. D., Gami, D.
C., Bloomer, O. T., “Vapor-Liquid Phase Equilibria in the
Binary Systems of Methane, Ethane, and Nitrogen,” Thermodynamic and Transport Properties of Gases, Liquids, and
Solids, 180-5, McGraw-Hill Book Publishing Co., Inc., New
York (1959).
Chen,
R.
J., Chappelear,P.
S.,
14. Elliot, D.G.,
Kobayashi, R., “Vapor-Liquid Equilibrium of the Methanen -ButaneSystem at Low Temperatures and High Pressures,”
J . Chem. Eng. Data (submitted for publication, March 1973).
15. Engineering Data Book, Mobil Oil Co.,Inc., New
York.
16. Ettar, D. O., Kay, W. B., “Critical Properties of Mixtures of Normal Paraffin Hydrocarbons,” J . Chem. Eng. Data
6 409 (1961).
17. Forman, J. C., Thodos, G., “Critical Temperature and
Pressure of Hydrocarbons,’’ AZChE Journal 4 356 (1958).
18. Gonzalez, M. H.,Lee,A.L.,
“Dew- and BubblePoints of Simulated Natural Gases,” J . Chem. Eng. Data 13
172 (1968).
19. Grieves, R. B.,Thodos, G., “TheCricondentherm and
Cricondenbar Temperatures of Multicomponent Hydrocarbon Mixtures,” Soc. Petrol. Eng. J . 3 287 (1963).
20. Guter, M., Newitt, D.M.,Ruhemann,M.,
“TwoPhase Equilibrium in Binary and Ternary Systems-II: The
System Methane-Ethylene, III: TheSystem Methane-EthaneEthylene,” Proc. Roy. Soc. (London) 176A 140 (1940).
21. Hadden, S. T., “Vapor-Liquid Equilibria in Hydrocarbon Systems, Part II,” Chem. Eng. Progr. 44 135 (1948).
22. Hall, K. R., Yarborough, L., “New Simple Correlation
for Predicting Critical Volume,” Chem. Eng. 78 [25]76
(1971).
23. Heidemann, R. A., Khalil, A. M., “TheCalculation of
Critical Points,” AZChE J . , 26 769 (1980).
24. Katz, D. L., Kurata, F., “Retrograde Condensation,”
Znd. Eng. Chem. 32 817 (1940).
25. Kay, W. B., “Density of Hydrocarbon Gases and Vapors at High Temperature and Pressure,” Ind. Eng. Chem. 28
1014 (1936).
26. Kay, W. B., “Liquid-Vapor Phase Equilibrium Relations in the Ethane-n-Heptane Systems,” Znd. Eng. Chem. 30
459 (1938).
27. Kay, W. B., “Liquid-Vapor Equilibrium Relations in
Binary Systems: n -Butane-n -Heptane System,” Znd. Eng.
Chem. 33 590 (1941).
28. Kay, W. B., “The Critical Locus Curve and the Phase
Behavior of Mixtures,” Accounts Chem. Res. 1 344 (1968).
29. Kay, W. B., Brice, B. D., “Liquid-Vapor Equilibrium
Relations in Ethane-Hydrogen Sulphide System,” Ind. Eng.
Chem. 45 615 (1953).
30. Kay, W. B., Pak, S. C., “Critical Properties of Hydrocarbon Mixtures,” The Ohio StateUniversity Research Foundation, Rep. [6]API Project No. PPC 15.8 (1971).
31. Kay, W. B., Rombasek, G. M., “Vapor-Liquid Equilibrium Relations in Binary Systems: Propane-Hydrogen Sulphide System,” Ind. Eng. Chem. 45 221 (1953).
32. Kohn, J. P., “Heterogeneous Phase and Volumetric
Behavior of the Methane-n-Heptane System at LowTemperatures,” AZChE Journal 7 514 (1961).
33. Kreglewski, A., Kay, W. B., “The Critical Constants
of Conformal Mixtures,” J . Phys. Chem. 73 3359 (1969).
34. Li, C. C.,“Critical Temperature Estimation for Simple
Mixtures,” Can. J. Chem. Eng. 49 709 (1971); Errata 50 152
(1972).
35. Lydersen, A. L., “Estimation of Critical Properties of
Organic Compounds by the Method of Group Contributions,” Coll. Eng., Univ. of Wisconsin, Eng. Expt. Sta.
Rept. 3, Madison, Wisc. (1955).
36. Michelsen, M. L., Heidemann, R. A., “The Calculation of Critical Points from Cubic Two-Constant Equations of
State,” AZChE J., 27 521 (1981).
37. Nichols, W. B . , Reamer, H. H.,Sage, B. H., “Volumetric and Phase Behavior in the Hydrogen-n-Hexane System,” AZChE Journal 33 262 (1957).
38. Nokay, R., “Estimate Petrochemical Properties,”
Chem. Eng. 66 [4]147 (1959).
39. Olds, R. H., Reamer, H. H., Sage, B. H., Lacey, W.
N., “Phase Equilibrium in Hydrocarbon Systems,” Znd. Eng.
Chem. 41 475 (1949).
40. Olds, R. H., Sage, B. H., Lacey, W. N., “MethaneIsobutane System,” Znd. Eng. Chem. 34 1008 (1942).
41. Poettmann, F. H., Katz, D.L., “Phase Behavior of
Binary Carbon Dioxide-Paraffin,” Znd. Eng.Chem. 37 847
(1945).
42. Reamer, H. H., Sage, B. H., “Phase Equilibria in Hydrocarbon Systems: Volumetric and Phase Behavior of the
4-73
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A PTI D BC H A P T E R w 4
*X
Methane-n-HeptaneSystem,” Chem. Eng.Data Ser. 1 29
(1956).
43. Reamer, H. H., Sage, B. H., “Phase Equilibria in Hydrocarbon Systems. Volumetric and Phase Behavior of the
n-Decane-C02 Systems,” J. Chem. Eng. Data 10 49 (1965).
44. Reamer, H. H., Sage, B. H., Lacey, W. N., “Phase
EquilibriainHydrocarbon Systems: Volumetric and Phase
Behavior in the Methane-Propane System,” Ind. Eng. Chem.
42 534 (1950).
45. Riazi, M. R., “Prediction of Thermophysical Properties of Petroleum Fractions,” Ph.D. Thesis, Department of
Chemical Engineering, The Pennsylvania State University,
University Park, Pa., 1979.
46. Riedel, L.,“Eine
Neue Universelle Dampfdruckformel,” Chem. Ingr. Tech. 26 679 (1954).
47. Riedel, L., “The Equation of State of Real Gases,”
Chem. Ingr. Tech. 28 557 (1956).
48. Roess, L. C., “Determination of Critical Temperature
and Pressure of Petroleum Fractions by a Flow Method,” J.
inst. Petrol. Tech. 22 665 (1936).
49. Roof, J. G., Baron, J. D., “Critical Loci of Binary
Mixtures of Propane with Methane, CarbonDioxide,and
Nitrogen,” J . Chem. Eng. Datu 12 292 (1967).
50. Sage, B. H., Lacey, W. N., Volumetric and Phase Behavior of Hydrocarbons, 291 -4, Stanford University Press,
Palo Alto, Calif. (1939).
51. Sage, B. H., Lacey, W. N., Monograph for API Research Project Number 37: Thermodynamic Properties of the
Lighter Paraffin Hydrocarbons and Nitrogen, Am. Petrol.
Inst., Washington, D.C. (1960).
W 0732290 0536482 470 W
52. Sage, B. H., Lacey, W. N., Monograph for API Research Project Number 37: Some Propertiei of the Lighter
Hydrocarbons, Hydrogen Sulfide, and Carbon Dioxide, Am.
Petrol. Inst., Washington, D.C. (1955).
53. Sage, B. H., Lacey, W. N., Schaafsma, J. G., “Phase
Equilibria in Hydrocarbon Systems-II: Methane-Propane
System,” Ind. Eng. Chem. 26 214 (1934).
54. Silverman, E. D., Thodos, G., “Cricondentherms and
Cricondenbars,” Ind. Eng. Chem. Fund. 1 299 (1962).
55. Sliepcevich, C. M., Finn, D., Kobayashi, R., Leland,
T. W., Perry’s Chemical Engineers’ Handbook, 4th edn. (edited by Perry, R. H., Chilton, C. H., Kirkpatrick, S. D.),
4-49-4-55, McGraw-Hill Book Co., Inc., New York (1963).
56. Soave, G., “EquilibriumConstants from a Modified
Redlich-Kwong Equation of State,” Chem. Eng. Sci., 27 1197
(1972).
57. Smith, R. L.,Watson, K. M., “Boiling Points and Critical Properties of Hydrocarbon Mixtures,” Ind. Eng. Chem. 29
1408 (1937).
58. Stalkup, F. I., Kobayashi, R., “High-Pressure PhaseEquilibriumStudies by Gas-LiquidPartitionChromatography,” AlChE Journal 9 121 (1963).
59. Tsonopoulos, C., Wilson, G. M., “High-Temperature
Mutual Solubilities of Hydrocarbons and Water. Part 1: Benzene, Cyclohexane and n-Hexane,’’ AIChE J . 29 990 (1983).
60. Winn, F. W., “Physical Properties by Nomogram,”
Petrol. Refiner 36 [2] 157 (1957).
--`,,-`-`,,`,,`,`,,`---
4-74
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A P I CHAPTERS5 92 W 0732290 0 5 5 2 7 4 0 9 T l
m
CHAPTER 5
VAPOR PRESSURE
Revised Chapter 5 to Fifth Edition (1992)
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0732290 0552743 8 3 8
Copyright 0 1994 American Petroleum Institute
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A P I CHAPTER*S
92
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0732290 0552742 774 W
--`,,-`-`,,`,,`,`,,`---
PREFACE
This revised chapter is based on a much expanded and verified experimental data base
used both to evaluate
prediction methods and topresent correlating equations for individual
compounds. The inclusion of correlating equations for vapor pressure is new to the chapter
and substantially enhances its use. Revised consistent vapor pressure plots are retained for
desk use. Both previousmethods for prediction of vapor pressure are retained with expanded evaluations. A method for prediction of Reid vapor pressure has been included. Detailed
results of the evaluations that serve as a basis for the selection of the material inthis chapter
are available in Documentation Report W 9 3 available from Xerox UniversityMicrofilms,
Ann Arbor, Michigan.
The work on this chapter was carried out by Thomas E. Daubert assisted by Michael J.
Thonvart and several undergraduate scholars. The chapter coordinating committee for the
Technical Data Committee was Peter Nick of Unocal, Chair; Dale Embry, Phillips Petroleum; and Calvin Spencer, M. W. Kellogg with assistance from B. I. Lee, Mobil; C. K.
Shen-Tu, Brown & Root-Braun; and B. Kouzel, Unocal.
Thomas E. Daubert
Department of Chemical Engineering
The Pennsylvania State University
University Park, PA 16802
June 1993
...
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A P I C H A P T E R t 5 92 M 0732290 0 5 5 2 7 4 3 b o 0 W
CHAPTER 5
VAPOR PRESSURE
PAGE
5.0 Introduction . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . , . . . . . . . . . . .
Table 5-0.1
Comparison of Prediction Methods . . . . . . . . . .
--`,,-`-`,,`,,`,`,,`---
5A Vapor Pressures
5A1. Vapor Pressures of Pure Hydrocarbons and Narrow-Boiling
Petroleum Fractions
Procedure 5A1.1 Correlation of the Vapor Pressure of
Pure Compounds . . . . . . . . . . . . . . . . . . . . . . . .
Table 5A1.2
Coefficients for Procedure 5A l . 1 . . . . . . . . . . .
Procedure 5A1.3 Alternate Correlation of the VaporPressure
of Pure Compounds . . . . . . . . . . . . . . . . . . . . . .
Table 5A1.4
Coefficients for Procedure 5A1.3 . . . . . . . . . . .
Figure 5A1.5
Vapor Pressureof Normal Paraffin Hydrocarbons (High-Temperature Range) . . . . . . . . .
Figure 5A1.6
Vapor Pressureof Branched Paraffin
Hydrocarbons . . . . . . . . . . . . . . . . . . . . . . . . . .
Figure 5A1.7
Vapor Pressureof Paraffin Hydrocarbons
(Low-Temperature Range) . . . . . . . . . . . . . . . . .
Figure 5A1.X
Vapor Pressureof Naphthene Hydrocarbons . . .
Figure 5A1.9
Vapor Pressure of Olefin Hydrocarbons . . . . . .
Figure 5A1.10
Vapor Pressureof Diolefin, Cycloolefin,
and Acetylene Hydrocarbons . . . . . . . . . . . . . . .
Vapor Pressureof Lighter Unsaturated
Figure 5A1.11
Hydrocarbons . . . . . . . . . . . . . . . . . . . . . . . . . .
Vapor Pressureof Alkylbenzene
Figure 5AI. 12
Hydrocarbons . . . . . . . . . . . . . . . . . . . . . . . . . .
Figure 5A1.13
Vapor Pressureof Miscellaneous Aromatic
Hydrocarbons . . . . . . . . . . . . . . . . . . . . . . . . . .
Vapor Pressure of Heavy Hydrocarbons . . . . . .
Figure 5A1.14
Vapor Pressure of Oxygenated Compounds . . .
Figure 5A l. 15
Procedure 5A1.16 Prediction of Vapor Pressure of Pure
Hydrocarbons . . . . . . . . . . . . . . . . . . . . . . . . . .
Table 5A1.17
Correlation Terms for Usein Procedure
5A1.16 . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .
Correlation Terms for Use in Procedure
Figure 5A1.1X
5A1.16 . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .
Procedure 5A1.19 Prediction of Vapor Pressure of Pure
Hydrocarbons and Narrow-Boiling
Petroleum Fractions . . . . . . . . . . . . . . . . . . . , . .
5-1
5-3
5-5
5-7
5-15
5-17
5-25
5-26
5-27
5-28
5-29
5-30
5-31
5-32
5-33
5-34
5-35
5-39
5-41
5-43
5-45
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A P I CHAPTERLS 9 2 W 0732290 0552744 547 W
Figure 5A 1.20
Figure 5A1.21
Vapor Pressure of Pure Hydrocarbons and
Narrow-Boiling Petroleum Fractions . . . . . . . . 5-47
Watson K-Correction for Procedure 5A1.19 . . . 5-53
5B Reid Vapor Pressure and True Vapor Pressure
True Vapor Pressure of Gasolines and
Figure 5B l. 1
Finished Petroleum Products . . . . . . . . . . . . . . 5-55
Figure 5B 1.2
True Vapor Pressure of Crude Oils . . . . . . . . . . 5-57
Procedure 5B1.3 Prediction of Reid Vapor Pressure . . . . . . . . . . 5-59
Bibliography . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 5-63
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CHAPTER 5
VAPOR PRESSURE
5.0 INTRODUCTION
Vapor pressureis the pressure at which thevapor phase of
a substance is in equilibrium with the liquid phase of that
substance at a specified temperature. The term is commonly
applied to pure substances, but it is also used occasionally
with mixtures. Apart from the temperature effect, the composition of the vapor and liquid phases (when not pure) also
influencesthe equilibrium pressure. Therefore, to use the
term vapor pressure with mixtures, the composition effect
must be taken into account, either by holding liquid, vapor,
or overall composition constant or by focusing attention on
a portion of the liquid mixture which is sufficiently closeboiling that composition changes with temperature have a
negligible effect on pressure.
Specific vapor pressure correlation equations are recommendedinProcedures 5Al.l and 5A1.3.For compounds
covered in this section these equations will give more accurate vapor pressures
over the range specified for the particular
compound than the generalized predictive procedures. The
approximate average error to be expected and the range of
applicability for each compound for each correlating equation deemed satisfactory are given together withthe correlationcoefficientsinTables5A1.2and5A1.4.Procedure5Al.l
istheprimarymethod
and is of a form that can be
extrapolated slightly abovethe critical point when necessary.
Procedure 5A1.3 is the alternate method which is constrained
at the exact critical point and cannot be extrapolated higher.
The experimental vapor pressure-temperature relationships of a number of the more common hydrocarbons and a
few important nonhydrocarbons are plotted directly in
Figures 5A1.5 through 5A1.15. The scales of most of these
figures are the logarithm of the vapor pressure and a
--`,,-`-`,,`,,`,`,,`---
modified reciprocal temperature scale , where r is
r + 382
temperature in degrees Fahrenheit.
An accurate generalized method of predicting pure hydrocarbon vapor pressures is given as Procedure 5A1.16. This
procedure requires the critical temperature, critical pressure,
and acentric factor of a hydrocarbon. A slightly less accurate
alternate prediction method is given for use for pure hydrocarbons only when these critical properties are not available.
This alternate method, Procedure 5A1.19, requires only the
normal boiling point andthespecific gravity and also is
applicable to narrow-boiling petroleum fractions. The procedure, which includes Figures 5A1.20 and 5A1.21, also can
be used to convert a known boiling point from one pressure
to another. Table 5-0.1 gives average andbias percent errors
for each family of compounds tested for Procedures 5A1.16
and 5A1.19.
The Reid vapor pressure (Rvp) is the absolute pressure
exerted by a mixture (in pounds per square inch) determined
at 100 F and at a feed vapor-to-liquid volume ratio of 4.
(Defined and specified in ASTM Method D 323, the apparatus and procedures are standardized under the auspices of the
American Society for Testing andMaterials.) Frequently, the
Rvp is used to characterize the volatility of gasolines and
crude oils. It also provides a convenient approximation of the
absolute vapor pressure of a partly vaporized sample at
100 F. Two figures which relate the Rvp and ASTM D 86
boiling characteristics to true vapor pressure over a wide
range of temperatures for crude oils (Figure 5B 1.2) and for
gasolines and other finishedpetroleum products (Figure
5B 1.1) are given. Procedure 5B 1.3 gives a new computer
method for predicting the Reid vapor pressure for both pure
compounds and petroleum fractions.
NOTE: A report which documents the basis upon which the material in this chapter has been selected has been published by the
American Petroleum Institute as Documentation Report No. 5-93
available fromUniversityMicrofilmsInternational,
Books and
Collections, Ann Arbor, Michigan.
1994
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A P I CMAPTER*5
92
0732290 055274b 3 L T
5-0.1
TABLE 5-0.1"COMPARISON OF PREDICTION METHODS
No.
of
Family
Cpds
n-Alkanes
Methyl alkanes
Dimethyl alkanes
Other
branched
alkanes
Cycloalkanes
22
16
1.516
1.620
2.04
Procedure 5A1.I6
(Lee Kesler)
Percent Error
Bias
Average
0.5
3.1
-0.1
1.S
-1.2
-1.3
-1.5
Procedure 5A l . 19
(Maxwell Bonnell)
Percent Error
Bias
Average
3.8
-0.9
0.2
1.4
O. 1
3.0
-0.4
4.6
1.3
3.1
~~
--`,,-`-`,,`,,`,`,,`---
Sub. cyclopentanes
-2.9
Sub. cyclohexanes
Decalinshicyclohexyl
n-Alkenes
Other linear alkenes
~~~~~~
2.9 10
13
3
18
13
-1.9
-3.5 1.9
10.6
-0.3
0.6 -0.8
4.0
3.5
14.7
2.3
1.2
Methyl alkenes
-1.1
Other branchedalkenes
Cycloalkenes
Alkadienes
Alkynes
13
10
4
13
8
1.8
-1.9-2.2
3.9 12.7
-1.1
2.0 2.8
3.8
3.7
14.5
5.3
1.1
0.4
-1.9
n-Alkylbenzenes
Substituted alkylbenzenes
Aromatics with
unsaturated side chains
Naphthalenes & tetralin
14
25
-0.6
2.9
3.3
3.4
-0.2
1.3
Fused ring aromatics
Multiple aromatic rings
Indenelindane
ThiophenemHT
Nitrogen rings
13
8
6
17.1
6
2
2
5
Total 264
4.7 -0.5
-1.92.0
-12.9
-16.5
5.2
-6.0
2.3
-4.4
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4.6
-1.5
1.o
3.7
13.7
12.7
6. I
2.6
5.2
5.4
13.7
3.9
1.9
1.8
3.6
4.5
8.0
1.9
1.9
6.0
3.3
-4.0
3.8
3.0
4.1
15.6
4.3
3.7
10.0
5-3
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~
A P I CHAPTERaS 92 D 0732290 0552747 25b
m
PROCEDURE 5A1.1
CORRELATION OF THE VAPOR PRESSURE
OF PURE COMPOUNDS
Discussion
The following equation is recommended for calculating thevapor pressure of any pure compound
over the temperature range specified for the compound.
B
' ) E
ln P= A + - + C l n T+DT-+-*
T
T
(5Al.l-I)
Where:
P = vapor pressure of compound, psia.
T = temperature, degrees Rankine.
A,B,C,D,E = derived coefficients from Table 5A 1.2.
Table 5A1.2 gives the coefficients for the above equation together with the applicable temperature
range and the maximum and average percent errors from the comparison with experimental data
carried out during regression.
Procedure
Use the coefficients from Table 5A1.2 in equation (5A1 .l-1) to calculate the vapor pressure within
the temperature range specified.
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5-5
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72
m
0732270 0552748 L92
m
5A1.1
COMMENTS ON PROCEDURE 5A1.1
Purpose
This procedure is to be used to calculate the vapor pressureof specific compounds as a functionof
temperature.
Limitations
This procedure only is valid over the temperature limits listed in Table 5A1.2. The procedure can
be extrapolated slightlyabove the critical where notedby the limits given in Table 5A1.2.
Special Comments
The vapor pressures calculatedby this procedurein the experimentaldata range are totally consistent with the vapor pressure plotsfor common compoundsof Figures 5Al .S through 5A1.13.
Errors given in the correlation coefficienttables should be noted when using this procedure.
The triple point temperatureand critical temperature listedin Table5A1.2 are taken from the 1992
version of the Chapter1 database. Therefore,slight discrepanciesmay be found for some compounds.
Literature Sources
Procedure 5A1.1 is a modification of the Riede1 (272) method and was developed by the project
staff at The Pennsylvania State University.
It has been testedby the project staff at The Pennsylvania
State University and evaluated
by the API Technical Data Committee.
Example
Determine the vapor pressure of n-octane at a temperatureof 100 F.
The necessary parameters are obtained
from Table 5A1.2 for n-octane (compound number 36).
A = 76.793
B = -11700.
C = -8.8309
D = 0.0000020086
E = -395420.
and
T = 100 F = 559.7 R
Using equation (5Al.l-1)
ln P = -0.62159
P = 0.5371 psia
The experimental value listed in Chapter1 is 0.5369 psia.
--`,,-`-`,,`,,`,`,,`---
1994
5-6
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~~
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1994
5-7
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m
0732298 8552750 840
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--`,,-`-`,,`,,`,`,,`---
API CHAPTERlk5 92
5-8
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~
A P I CMAPTER*5
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~~~~
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API CHAPTERtS 92 9 0732290 0552752 b L 3 9
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A P I CHAPTER85 92
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5A1.2
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A P I C H A P T E R t S 92
m
0 7 3 2 2 9 00 5 5 2 7 5 7l T 5
m
5A1.3
PROCEDURE 5A1.3
ALTERNATE CORRELATION OF THE VAPOR PRESSURE OF
PURE COMPOUNDS
Discussion
The following alternative equation is recommended for calculating the vapor pressure of any pure
compound over the temperature range specified for the compound. This equation should be used,
where applicable, when an exact match at the critical is desired.
ln
9 = ax, + bX, + cX, + d X ,
.3-1)
Where.
.3-2)
X,=
( 1 - T,)
'S
(5A1.3-3)
T,
X, =
( 1 - T,) 2'6
(5A 1.3-4)
'r
5
(1 T r )
x,= -
(5Al.3-5)
Tr
T, = T/T, = reduced temperature.
P, = P/P, = reduced pressure.
T, = critical temperature, in degrees Rankine.
P, = critical pressure, in psia.
T = temperature, in degrees Rankine.
P = vapor pressure, of compound, in psia.
--`,,-`-`,,`,,`,`,,`---
Table 5A1.4 gives the coefficients for the above equation together with the applicable temperature
range and the maximum and average percent errors from the comparison with the experimental data
carried out during regression. Compounds shown without coefficients had insufficient data to correlate by this method.
Procedure
Step 1: Obtain the critical temperature and pressure of the compound from Chapter 1.
Step 2: Calculate the reduced temperature and pressure at the desired conditions using the definitions above.
Step 3: Use the Coefficients in Table 5A1.4 in equations (5A1.3-1) through (5A1.3-5) to calculate
the vapor pressure within the range specified.
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A P I CHAPTER*5
92
m
07322900552758
O31
m
COMMENTS ON PROCEDURE5A1.3
Purpose
This procedure is to be used
to calculate the vapor pressureof specific compounds as a function of
temperature.
Limitations
Table 5A 1.4.The procedure will exactly
This procedure is valid over the temperature limitsinlisted
match the critical temperature and pressure used in the equation. Howevel; the equation cannot be
extrapolated to temperatures above the critical point.
Special Comments
The vapor pressures calculatedby this procedure in the experimental data range
are generally consistent with the vaporpressure plotsfor common compoundsof Figures 5A1.5 through 5A1.15.
Errors given in the correlation coefficient tables should be noted when using
this procedure.
The triple point temperature and critical temperature listed in Table
5A1.4 are taken from the
1992
version of theChapter 1 database. Therefore, slight discrepancies
may be foundfor some compounds.
Literature Sources
Procedure 5A1.3 is a linearized formof the Wagner(341) method developedby C.Shen-Tu (294).
It has been tested by the project staff at the Pennsylvania State University and evaluatedby the API
Technical Data Committee.
Example
Determine the vapor pressureof n-octane at a temperature of 100 F.
The necessary parameters are obtained from Table
5A1.4 forn-octane (compound number36).
a = -8.0092
b = 1.8442
C = -3.2907
d = -3.5457
From Chapter 1 T, = 564.22 F. The reduced temperature is
--`,,-`-`,,`,,`,`,,`---
Using equations(5A1.3-2) through (5A1.3-5)
X , = 0.8295
X , = 0.5585
X , = 0.2340
X, = 0.03505
Using equation (5A1.3- 1)
In P, = -6.5079
P, = 0.001492
From Chapter 1, the critical pressureis 360.7 psia. Therefore, the predicted vapor pressure is
P = 0.001492 X 360.7 psia
= 0.5380 psia
The experimental value listed in Chapter 1 is 0.5369 psia.
1994
5-16
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A P I CHAPTER*5
92
m
07322900552759T78
m
5A7.4
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1994
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No reproduction or networking permitted without license from IHS
--`,,-`-`,,`,,`,`,,`---
5-17
Not for Resale
A P I CHAPTERx5 9 2
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5-18
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Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
1994
Not for Resale
A P I CHAPTERg5 92
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API CHAPTERJ5 72
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1994
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
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Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
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A P I CHAPTERS5 92
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No reproduction or networking permitted without license from IHS
1994
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5-23
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1994
Not for Resale
A P I CHAPTER*5
92 m 0 3 3 2 2 9 0 0552367 0 4 4
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5A1.5
1994
--`,,-`-`,,`,,`,`,,`---
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Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
5-25
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Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
1994
Not for Resale
A P I CHAPTER*S
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1994
5-27
--`,,-`-`,,`,,`,`,,`---
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Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
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1994
5-28
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Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
..
A P I CHAPTERmS 92 W 0732290 0552773 575
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5A7.9
1994
--`,,-`-`,,`,,`,`,,`---
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
5-29
Not for Resale
A PC
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92
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0732290O552772
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5A1.10
--`,,-`-`,,`,,`,`,,`---
5-30
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
1994
Not for Resale
A P I CHAPTERrS 92
0732290 0552773 348
m
5A1.11
1994
5-31
--`,,-`-`,,`,,`,`,,`---
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
A P I CHAPTERxS 9 2
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1994
--`,,-`-`,,`,,`,`,,`---
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
A P I CHAPTERx5 92
0 7 3 2 2 9005 5 2 3 7 5
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--`,,-`-`,,`,,`,`,,`---
5A1.13
1994
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
5-33
Not for Resale
~~~
A P I CHAPTERa5 7 2
m
0 7 3 2 2 7 00 5 5 2 7 7 6
057
m
5A1.14
O
5-34
1994
--`,,-`-`,,`,,`,`,,`---
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
A PCI H A P T E R + S
92
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07322900552777
T93
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5A1.15
--`,,-`-`,,`,,`,`,,`---
1994
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
5-35
Not for Resale
A PC
I HAPTER*5
92
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0732270055277872T
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5A1.5 - 5A1.15
COMMENTS ON FIGURES 5A1.5 THROUGH 5A1.15
Purpose
--`,,-`-`,,`,,`,`,,`---
Experimental vapor pressure data are presented for selected pure hydrocarbonsin Figures 5A1.5
through 5A1.15.
Reliability
various sources to within two percent. Dashed
The curves reproduce the experimental data from the
portions of the curves represent extrapolations that are not supported
by experimental data.
Notation
O = critical point
Special Comment
For clarity, the portions of the curves that arenot supported by experimental data were deleted for
2-methylpentane and methylcyclohexane.
Data Sources
5 are listed below. These sources were used
The data sources for every compound listed in Chapter
to generate Figures 5A1.5 through 5A1.15 and the correlations
in Procedures 5Al.l and 5A1.3.
Oxygen (70,274,320,361,332)
Hydrogen (211,320,313,216)
Water (318, 179, 154,324, 349)
Nitrogen dioxide (21 1, 171,313, 145, 268)
Nitric oxide(313,320,211,272)
Nitrous oxide(3 13,320,21 1,95)
Ammonia (362, 153,320, 155,210,256, 171,
147)
Chlorine (320, 146, 313)
Hydrogen chloride (320, 171, 155,210,350)
Hydrogen sulfide(320,313,211, 150,98)
Carbon monoxide(320,3 13,90,230,211,331,
227)
Carbon dioxide (313, 129, 172,331)
Sulfur dioxide(313,331,211, 320)
Methane (267)
Ethane (152)
Propane (101,259,73,159,270,279,280,205,
104, 185,326,264,151,318)
n-Butane (247,339,47,265, 160, 134, 187,318)
Isobutane (55,61,75,224,293,327,92,
101,
278, 170,344)
n-Pentane (170,259,327,20,235,244,353,278,
167, 102, 186)
Isopentane (287,296,354)
Neopentane (45,56,22,61,346,221)
n-Hexane (109,148,195,162, 176,304,311,
318)
2-Methylpentane (318,353)
3-Methylpentane(353,318, 104)
2,ZDimethylbutane (182,244,353, 104)
2,3-Dimethylbutane (353, 176,318, 104)
n-Heptane (195,243,304,93, 138,175,213,
301,354,220, 104,318)
2-Methylhexane (169,220,3 18)
3-Methylhexane (138,220,318)
2,4-Dimethylpentane (318, 127, 138,220)
2,2-Dimethylpentane (127,354,3 18)
2,3-Dimethylpentane (318, 127, 138, 19)
3,3-Dimethylpentane (318,24,220)
2,2,3-Trimethylbutane (3 18,69, 127, 138, 300,
220)
3-Ethylpentane (3 18, 138,300,220)
n-Octane (93, 128,354,220, 167)
2,2-Dimethylhexane (3 18,354,220)
2,3-Dimethylhexane (318,220, 354)
2,4-Dimethylhexane (3 18,220,354)
23-Dimethylhexane (318,220,354)
3,3-Dimethylhexane (354)
3,CDimethylhexane (318,220,354)
2-Methylheptane (23,220,318)
3-Methylheptane (22, 220,318)
4-Methylheptane(220,318)
2,2,4-Trimethylpentane (93,244,345,54, 177,
301,354, 220, 318)
2,2,3-Trimethylpentane (220,318)
2,3,3-Trimethylpentane (354,220,318)
2,3,4-Trimethylpentane(318,21,220)
2,2,3,3-Tetramethylbutane(325,77)
3-Ethylhexane (318,354,220)
2-Methyl-3-ethylpentane(318,220,354)
3-Methyl-3-ethylpentane(318, 156,313,299)
n-Nonane (86, 138,354,318)
2-Methyloctane (3 18)
3-Methyloctane (318)
4-Methyloctane (318)
2,2-Dimethylheptane(3 18)
26-Dimethylheptane (3 18)
3,3-Diethylpentane (3 18)
2,2,5-Trimethylhexane (3 18)
2,4,4-Trimethylhexane (3 19)
2,2,3,3-Tetramethylpentane(318, 138)
2,2,3,4-Tetramethylpentane(318, 138)
2,2,4,4-Tetramethylpentane(318, 138)
2,3,3,4-Tetramethylpeentane
(319, 158)
3-Ethylheptane(3 18)
1994
5-36
Copyright American Petroleum Institute
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Not for Resale
A P I CHAPTER*5 92
m
07322700552779
Bhh
m
5A1.5-5A1.15
--`,,-`-`,,`,,`,`,,`---
2.2-Dimethyl-3-ethylpentane(318)
2.4-Dimethyl-3-ethylpentane(3 18)
n-Decane (354,278,3)
2-Methylnonane (318)
3-Methylnonane (3 18)
4-Methylnonane (318)
5-Methylnonane (318)
2,2-Dimethyloctane(3 18,83)
n-Undecane (318,80)
n-Dodecane (354,318)
n-Tridecane (3 1 8 , 3 13)
n-Tetradecane (318,80)
n-Pentadecane (3 18,80)
n-Hexadecane (170,3 18,78)
n-Heptadecane (3 18)
n-Octadecane (3 18,33 207)
l.
n-Nonadecane (318)
n-Eicosane (3 18,207)
n-Tetracosane (233,25)
n-Octacosane (233,318,89,25)
Cyclopentane (3 18,46,340)
Methylcyclopentane (104, 307, 318)
Ethylcyclopentane (104,313,307,318)
1,l-Dimethylcyclopentane(318,331)
cis- 1,2-Dimethylcyclopentane (138,318)
truns- 1,2-Dimethylcyclopentane(138, 3 18)
cis-I ,3-Dimethylcyclopentane(3 18,328)
rruns-l,3-Dimethylcyclopentane(318)
n-Propylcyclopentane(318)
Isopropylcyclopentane(3 18, 119, 158)
Cyclohexane (148, 353,269,48,276, 181)
Methylcyclohexane (3 18, 353,306,208)
Ethylcyclohexane (318, 353)
1,l-Dimethylcyclohexane(138,318)
cis- 1,2-Dimethylcyclohexane(353, 3 18)
truns- 1,2-Dimethylcyclohexane(353,3 18)
cis-1,3-Dirnethylcyclohexae (353, 318)
truns-l,3-Dimethylcyclohexane(353, 3 18)
cis- 1,4-Dimethylcyclohexane(353,318)
tmns-l,4-Dimethylcyclohexane(353, 3 18)
n-Propylcyclohexane (3 18, 353)
Isopropylcyclohexane( 1 19, 138)
n-Butylcyclohexane(318)
n-Decylcyclohexane (318, 119)
I-Methyl-l-ethylcyclopentane(252, 318, 113)
Cycloheptane (318, 131)
Cyclooctane (131,299, 157, 1)
Ethylene (74, 228,76,240, 361, 323)
Propylene (85,126,229,140,270,191,279,334,
173,323,299)
I-Butene (164,224,57,44,61, 191, 279,310,
170,193,255,350)
cis-2-Butene (61, 291, 134, 335)
truns-2-Butene (6 1, 134,335)
Isobutene (19 1,262,283)
1-Pentene (290, 106,318, 136,313, 356, 323)
cis-2-Pentene (104,3 18,289)
trans-2-Pentene (104, 318, 289)
2-Methyl-1 -butene (3 18,290,363)
2-Methyl-2-butene (318, 191,290)
3-Methyl-1-butene (3 18,289)
1-Hexene (137, 323)
cis-2-Hexene (3 18, 8 1 )
truns-2-Hexene (318, 81)
cis-3-Hexene (3 18, 1 18)
truns-3-Hexene (3 18, 1 18)
2-Methyl-1 -pentene (3 18, 8 1 )
2-Methyl-2-pentene (3 18, 8 1)
3-Methyl-1 -pentene (3 18, 1 18)
3-Methyl-cis-2-pentene (3 18, 1 18)
4-Methyl-1 -pentene (3 18, 8 1)
4-Methyl-cis-2-pentene(3 18)
4-Methyl-truns-2-pentene (318)
2.3-Dimethyl-1 -butene (3 18, 81)
2.3-Dimethyl-2-butene (3 18.5 1, 8 1, 288)
3,3-Dimethyl-l-butene (3 18, 122,51, 299)
2-Ethyl-l-butene (318, 81)
l-Heptene (1 37,201,62,318)
cis-2-Heptene (3 18)
tmns-2-Heptene (3 18,66)
cis-3-Heptene (3 18)
truns-3-Heptene (3 18.66)
2-Methyl-I-hexene (3 18, 286)
3-Methyl-I-hexene (3 18)
4-Methyl-I-hexene (318)
2-Ethyl-l-pentene (318)
3-Ethyl-l-pentene (318)
2,3,3-Trirnethyl-l-butene (318,299)
I-Octene (318, 137)
truns-2-Octene (318)
trans-3-Octene (318)
truns-4-Octene (3 18)
2-Ethyl-1-hexene (3 18)
2,4,4-Trimethyl-l-pentene
(318. 358, 82)
2,4,4-Trimethyl-2-pentene (82, 3 18)
l-Nonene (318)
l-Decene (318, 137)
1-Undecene (318)
1-Dodecene (3 18)
1-Tridecene (3 18)
1-Tekadecene (3 18)
I-Pentadecene (321)
I-Hexadecene (3 18)
I-Heptadecene (323,2, 158,284)
l-octadecene (318)
l-Nonadecene (323)
1-Eicosene (3 18)
Cyclopentene (33 1 )
Cyclohexene (27 1,33 1)
Cycloheptene (299,202,94,337)
Cyclooctene (94, 202, 135)
Cyclopentadiene(196,49, 163, 356)
1,3-Butadiene(61, 192, 143, 161, 164,232,262,
292,333,212, 134, 193,255,349)
Isoprene (65,3 18)
3-Methyl-l,2-butadiene (318, 104,251, 299)
1SPentadiene (3 18,25
1)
cis-1,3-Pentadiene(3 18,25
1)
truns- 1,3-Pentadiene(318,25 1)
1,4-Pentadiene (3 18)
2,3-Pentadiene (3 18, 25 1, 299,3 16)
1,3-Cyclohexadiene(226, 197, 120,308)
2,3-Dimethyl-l,3-butadiene(99, 123)
15Hexadiene (99, 299, 197)
1994
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
5-37
Not for Resale
A P I CHAPTERx5 92
m 0732290 0552780 588 m
5A1.5-5A1.15
fruns,trans-2,4-Hexadiene(197, 123)
1.5-Cyclooctadiene (66)
Acetylene (219,336, 15, 318)
Methylacetylene (318,246,330)
Dimethylacetylene (331,324)
3-Methyl-1 -butyne (324)
I-Pentyne (324)
1-Hexyne (149,157,324)
2-Hexyne (324)
3-Hexyne (324,275)
Benzene (60,312,364,360,6,322,7)
Toluene (53, 8, 353,364, 115,3 13, 322)
Ethylbenzene (8,20, 189, 253,322,7)
m-Xylene (263, 138, 175,8, 322,7)
o-Xylene (148,263,353,8,322,7)
p-Xylene (263, 19,322,239,7,349)
n-Propylbenzene (136,353,322, 199)
1,2,3-Trimethylbenzene (318,65,322)
1,2,4-Trimethylbenzene (148, 165,318,65, 322)
m-Ethyltoluene (318, 328, 322)
o-Ethyltoluene (318,328, 322)
p-Ethyltoluene (3 18,328, 322,204, 105)
n-Butylbenzene (318,33 1, 199)
Isobutylbenzene (318)
sec-Butylbenzene (3 18,271)
tert-Butylbenzene (318,271)
m-Diethylbenzene (318, 138)
o-Diethylbenzene (318, 138)
p-Diethylbenzene (3 18)
m-Cymene (318,37)
o-Cymene (318,37)
p-Cymene (318,328,37)
2-Ethyl-m-xylene (1 32,3 1S)
2-Ethyl-p-xylene(121,314,318)
3-Ethyl-o-xylene(3 18)
4-Ethyl-m-xylene ( 121,3 14,3
18)
4-Ethyl-o-xylene ( 121,318)
5-Ethyl-m-xylene ( 121,3 14,3
18)
1,2,3,5-Tetramethylbenzene(3 18,64,302)
1,2,4,5-Tetramethylbenzene(3 18)
n-Pentylbenzene(3 18)
n-Hexylbenzene (318)
m-Diisopropylbenzene (1 13,223)
p-Diisopropylbenzene(223,237)
n-Heptylbenzene (3 18)
n-Octylbenzene (3 18,3)
Styrene (67)
ufpha-Methylstyrene (313,319,236,338,342,
50)
m-Methylstyrene (91)
o-Methylstyrene (91,299)
p-Methylstyrene (91)
n-Nonylbenzene (318,3)
n-Decylbenzene(3 18,79)
n-Undecylbenzene (318)
n-Dodecylbenzene (318, 105,3,248,214,329)
n-Tridecylbenzene (318)
Cumene (209,322,37)
Mesitylene (318, 322)
5-38
Ethynylbenzene ( 1 1 1,203,266)
cis-1-Propenylbenzene(319,222)
trans-I -F’ropenylbenzene (258,59)
m-Divinylbenzene (313, 114)
2-Phenylbutene- 1 (277,242)
Cyclohexylbenzene (355,295, 125, 142,200)
cis-Decahydronaphthalene (32)
zrans-Decahydronaphthalene(32)
1,2,3,4-TetrahydronaphthaIene(28, 178, 355,
239,28 I , 133,245)
Indane (315, 112, 13, 166)
Indene (31,72)
Biphenyl (232, 88, 1 4 4 , 148,281)
Naphthalene (3 18,4, 80, 96,97, 130, 139, 174,
241,343,27, 107,27)
I-Methylnaphthalene(148, 237,355, 207,348)
2-Methylnaphthalene (80,39)
2,6-Dimethylnaphthalene (250)
2,7-Dimethylnaphthalene (157,250)
1-Ethylnaphthalene (318, 113, 190, 198,234)
1-n-Butylnaphthalene (42,52)
Anthracene (33, 320)
Phenanthrene (29,250)
Pyrene (170,303,328, 318)
Chrysene (1 70, 108,30)
Acenaphthene (34)
Fluorene (297, 235)
Bicyclohexyl(271,347)
Fluoranthene (34)
cis-Stilbene (110,71,68, 100,63,316,84,352,
272)
1,l-Diphenylethane (1 10,284)
1,2-Diphenyiethane (253)
m-Terphenyl ( 1 16)
o-Terphenyl ( 116)
Pyridine (184,217,254,36)
Isoquinoline (41)
Quinoline (35)
Dibenzopyrrole (171,313,65,282,235)
Acridine (313,26,309)
Indole (40)
Thiophene (318,313,65,271, 16,238)
Tetrahydrothiophene (271, 168,318, 16)
Methyl mercaptan(318,2 12,3 13,3
16)
Carbonyl sulfide (211,273,209,313, 180)
Ethylmercaptan (318, 313,218,249,316)
Methanol (351,320,313, 11, 12,206,5, 305,
255)
Ethanol (320, 171, 351, 11, 188, 359, 141,231,
313,285,298)
Isopropanol(l1,328,351,65,183,320,317,14,
9,272,204, 105,298,313)
13,
2-Methyl-2-propanol (14, 1 1,320,35 1,3
298)
Methyl tert-butyl ether(260,272, 10,5, 38,43,
105,255,349)
ten-Butyl ethyl ether(1 17, 124,261)
Diisopropyl ether( 184,27 1, 3 13, 1O, 1 17)
Methyl tert-pentyl ether (272,87,257)
1994
--`,,-`-`,,`,,`,`,,`---
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Not for Resale
API C H A P T E R * 5 9 2
0732290 0552781 414 W
5A1.16
PROCEDURE 5A1.16
PREDICTION OF VAPOR PRESSURE OF PURE HYDROCARBONS
Discussion
The following equation is useful for estimating the vapor pressure of pure hydrocarbons (and
narrow-boiling petroleum fractions) when the critical properties are known or can be estimated. When
the critical properties are not available or cannot be accurately estimated, Procedure 5A1.19 should
be used.
Where:
P,* = reduced vapor pressure, p"/p,.
P* = vapor pressure, in pounds per square inch absolute.
pc = critical pressure, in pounds per square inch absolute.
(In P,)(') and (ln pr)(l)= correlation terms that are given in tabular and graphical form.
o = acentric factor of hydrocarbon.
T, = reduced temperature, T / C .
T = temperature. in degrees Rankine.
T, = critical temperature, in degrees Rankine.
Procedure
Step I : Obtain the critical temperature and critical pressure from Chapter 1 or, if not available,
estimate values by the procedures of Chapter 4.
Srep 2: Calculate the reduced temperature.
Step 3: Obtain the acentric factor of the hydrocarbon from Chapter 1 or Chapter 2.
Srep 4: Obtain the correlation terms (ln P,.)(') and (In p,)(') by either interpolating linearly from
Table 5A1.17 or, at a small sacrifice in accuracy, by reading directly from Figure 5A1.18. [Alternately
use equations (5A1.16-2) and (5Al.36-33.1
Srep 5: Calculate the reduced vapor pressure by using equation (5A1.16-1). The vapor pressure is
obtained by multiplying the reduced vapor pressure by the critical pressure.
For computer calculations,the correlation terms which are equivalent to Table 5A1.17 are given by
the following equations:
(ln P,*)
(O)
= 5.92714 - 6.09648/Tr - 1.28862 In
(ln P,*) ( ' ) = 15.2518- 15.6875/q - 13.4721 In
1994
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T, + 0.169347T'
(5A l . 16-2)
T + 0.43577T,'
(5A1.16-3)
--`,,-`-`,,`,,`,`,,`---
5-39
Not for Resale
~
API CHAPTER*5 92
m
0 7 3 2 2 9 00 5 5 2 7 8 2
~~
350
m
5A1.16
COMMENTS ON PROCEDURE 5A1.16
Purpose
Procedure 5A1.16 is presented as the best method for estimating the vapor pressure of a pure
hydrocarbon which is not treated directly in Procedures 5A1. I or 5A1.3 or Figures 5A1.5 through
5A1.15. The critical conditions and acentric factormust be known or estimated. Themethod can also
be applied to narrow-boiling petroleum fractions. In the absence of critical data, use Procedure
5A1.19.
Limitations
Equation (5A1.16-1) is valid only for nonpolar substances. The method is restricted to reduced
temperatures greater than 0.30 but below the critical point. Care should be taken not to use the
equation below the freezing point.
Reliability
Equation (5A1.16-1) reproduces experimental data for pure hydrocarbons to within an average
error of 3.5 percent when the critical properties are known. The method is most reliable for reduced
temperatures between 0.5 and 0.95. When the critical properties and the acentric factor must be
estimated the errorswill be larger. The method has not been tested with petroleum fraction data.
Literature Sources
This procedure is based on the vapor pressure equations of Lee, B.I. and Kesler, M.G.,AIChE J.
21 510 (1975).
Example
Estimate the vapor pressure of 1-butene at 208.4 F.
From Chapter 1, the critical temperature is 295.6 F and the critical pressure is 583 psia. The reduced
208.4 + 459.7temperature is
0.885 .
295.6 + 459.7From Chapter 2, the acentric factor is 0.1867. By linear interpolation from Table 5A1.17
-(lnp,*)(') = 0.7232 and -(InPr*)(') = 0.6197.
Using equation (5Al.16-I):
Inp,* = -0.7232 + 0.1867 (-0.6197) = -0.8389
pr* = 0.4322
P* = 0.4322 (583) = 252 psia
The experimental value is 250 psia.
--`,,-`-`,,`,,`,`,,`---
1994
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A P L CHAPTERxS 92
m
0732290 0552783 297
m
--`,,-`-`,,`,,`,`,,`---
5A1.17
TABLE 5A1.17
CORRELATION TERMS FOR USE IN PROCEDURE 5A1.16
Tr
12.843
-(ln P,*)(')
1.o0
0.98
0.96
0.94
0.92
0.000
0.1 18
0.238
0.362
0.489
0.000
0.098
0.198
0.303
0.412
0.90
0.88
0.86
0.84
0.82
0.621
0.757
0.899
1.O46
1.200
0.528
0.650
0.78 1
0.922
1 .O73
0.80
0.78
0.76
0.74
0.72
1.362
1.237
1.531
1.415
1.708
1.896
2.093
1.608
1.819
2.050
0.70
0.68
0.66
0.64
0.62
2.303
2.525
2.761
3.012
3.280
2.303
2.579
2.883
3.21 8
3.586
0.60
0.58
0.56
0.54
0.52
3.568
3.876
4.207
4.564
4.95 1
3.992
4.440
4.937
5.487
6.098
0.50
0.48
0.46
0.44
0.42
5.370
5.826
6.324
6.869
7.470
6.778
7.537
8.386
9.338
10.410
0.40
0.38
0.36
0.34
0.32
8.133
8.869
9.691
10.613
11.656
1 1.621
12.995
14.560
16.354
18.421
0.30
20.820
1994
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-(ln P,*)(')
5-41
Not for Resale
~
A R 1 CHAPTERw5 9 2 W 0 7 3 2 2 9 00 5 5 2 7 8 4
L23 W
5A1.18
PO
--`,,-`-`,,`,,`,`,,`---
0.4
a5
0.4
a7
0.8
0.9
1.o
REDUCED TEMPERATURE, Tr
1994
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5-43
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API C H A P T E R r 5 92
m
0732290 0552785 ObT
5A1.19
PROCEDURE 5A1.19
PREDICTION OF VAPOR PRESSURE OF PURE HYDROCARBONS AND
NARROW-BOILING PETROLEUM FRACTIONS
Discussion
--`,,-`-`,,`,,`,`,,`---
Figures 5A1.20 and 5A1.21 are useful for estimating the vapor pressure of pure hydrocarbons and
narrow-boiling petroleum fractions when the critical properties or the acentric factors are not known
and cannot be estimated. When these properties are available, Procedure 5A 1.16 is recommended.
Procedure
Step I: Obtain the normal boiling point of the hydrocarbon from Chapter 1 and the WatsonK from
Chapter 2.
Step 2: Read a vapor pressure from Figure 5A1.20 using tb = r ; , where r, is the normal boiling
point and t h is the normal boiling point corrected to K = 12 (both in degrees Fahrenheit). For
naphthenes, olefins, acetylenes, and low-molecular-weight (<Cs) paraffins, it is not generally beneficial toapply the Watson K-correction, so the procedure is complete. For other hydrocarbons, proceed
to Step 3.
Step 3: Using the vapor pressure from Step 2, obtain a K-correction from Figure 5A 1.21. Subtrucr
this At (corrected withfmultiplier for superatmospheric pressures) from the true n o m ¿boiling point
to get the corrected normal boiling point, r;.
Step 4: Repeat Steps 2 and 3 until the pressure used to estimate the K-correction in Step 3 agrees
within desired limits with the value predicted in Step 2. In each repetition, the t b from Step 3 is used
in Step 2.
NOTE: To estimate a normal boiling point from a known vapor pressure, simply determine ther; from
Figure 5A1.20 and udd the K-correction fromFigure 5A1.21. No trial-and-error approach is
necessary.
This procedure may also be used with a digital computer. Figure 5A1.20 was generated from the
following equations:
(5A1.19-1)
log P* =
2663.129X - 5.994296
(5A1.19-2)
95.76X - 0.972546
for 0.0013 I X 5 0.0022 ( 2 mm Hg 4 p* 5 760 mm Hg)
log p*= 2770'085x - 6'412631 for X < 0.0013 ( P * > 760 mm Hg)
36X - 0.989679
(5A1.19-3)
Where:
p* = vapor pressure, in mm Hg.
0.0002867 ( T' )
T
748.1 - 0,2145 ( )
lb
"
X=
(5A l. 19-4)
Where:
T i = normal boiling point corrected to K = 12, in degrees Rankine.
T = absolute temperature, in degrees Rankine.
Figure 5A1.15 was generated from the following two equations:
2
AT = Tb -TL = 2.5 f ( K - 12) log
(5Al.19-5)
760
Where:
T, = normal boiling point, in degrees Rankine.
f = correction factor. For all subatmospheric vapor pressures and for all substances having normal boiling points greater than 400 F, f = 1. For substances having normal boiling points
less than 200 F, f = O. For superatmospheric vapor pressures of substances having normal
boiling points between 200 F and 400 F,f is given by:
=
Tb - 659.7
200
(5A l. 19-6)
K = Watson characterization factor.
1994
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92 W 0732290 0 5 5 2 7 8 b T T b
A PC
I HAPTER44
m
5A1.19
COMMENTS ON PROCEDURE 5A1.I9
Purpose
Procedure 5A1.19 is presented as an alternate method of estimating the vapor pressure of pure
hydrocarbons or narrow-boiling hydrocarbon mixtures. It should be used for pure hydrocarbons only
when Procedure 5Al. 16 cannot beapplied because critical properties
or acentric factors are
not available. The normal boiling point and Watson characterization factor must be known.
Limitations
This procedureis limited to pure hydrocarbons and narrow-boiling petroleum fractions, i.e., those
having less than50 F difference in a true-boiling-point (TBP) distillation. Wide-boiling fractions must
be treated by the appropriate proceduresin Chapter 8.
Reliability
Figure 5A1.20 reproduces experimental datafor pure hydrocarbons to within an average error of
eight percentforp* > 1 mm Hg and 30 percent forp* between la-6 and 1 mm Hg. Forp* < lo4 mm
Hg no experimental data are available andthe reliability of the method is unknown. The method is
most reliable for vapor pressures near atmospheric pressure. The method has not been tested with
petroleum fraction data.
Literature Sources
--`,,-`-`,,`,,`,`,,`---
Figures 5A1.20a-e and 5A1.21 andequations (5A1.19-4) and (5A1.19-5) were adapted from Maxwell and Bonnell, Vapor Pressure Charts for Petroleum Engineers,Esso Research and Engineering
Company, Linden,N.J.( 1955). Equations (5A
l. 19- 1) through (5A
l. 19-3) were obtained from Exxon
N.J., private
communication
(1977).
Research
and
Engineering
Company,
Florham
Park,
Figure 5A1.20f is from Beerbower, A. and Zudkevitch,D., “Predicting the Evaporation Behavior of
Lubricants in the Space Environment,” Preprints, Divisionof Petroleum Chemistry,American Chemical Society, Los Angeles Meeting,S(2) C-99 (April 1963).
Examples
A. Calculate the vapor pressure of 1,2,3,4-tetrahydronaphthalene(tetralin) at302 F.
From Chapter 1, the boiling point is 405.7F, and from Chapter 2,the WatsonK is 9.78.
For the first trial, assume ti, = tb = 405.7. Using this ti, and the desired temperature, 302 F, the
first estimate of the vapor pressure is read from Figure 5A1.20a as 0.20 atm. This vapor pressure
estimate the WatsonK-correction,
(152 mmHg) and a WatsonK of 9.78 are used in Figure 5A1.15 to
Ar = 4.0 F. The ti, for the second trialis tb - (tb - t i , ) = 405.7 - 4.0 = 401.7 F.
Using the new ti,, the second trial vapor pressure is 0.21 atm (160 mm Hg) from Figure SAI .20a.
From Figure 5A1.15, the new Watson K-correction is 3.9 F; thus, the third trial ri, is 405.7 - 3.9 =
401.8 F.
is read from Figure 5A1.20a as
With ti, = 401.8 F, the estimated vapor pressure for the third trial
0.21 atm. This value is identical with the second trial vapor pressure;
thus, the trial-and-error solution
is satisfied.
The estimated vapor pressure, 3.1 psia, agrees well with
an experimental valueof 3.13 psia.
B. A petroleum fraction exhibitsthe following TBP distillation curve at 10
mm Hg:
Distillation,
percent
Temperature,
deg
F
. . .. .. .
. . . . . . . ... . . . . . .
volume
by
3010
350
380
50
425
70
500
90
600
Estimate the average normal boiling point of the10- to 30-percent portion (the WatsonK is 12.5)
of the fraction.
The average boiling pointat 10 mm Hg is 365 F. From Figure 5A1.20b,tk = 628 F. From Figure
5A1.21, tb - t i = -2.4 F. Therefore, the average normal boiling point=r; + (rb - t i , ) = 628 - 2.4 =
626 F.
1994
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A PCI H A P T E R * 5
92
m
0732290 0552787 932
m
5A1.20a
1994
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--`,,-`-`,,`,,`,`,,`---
Not for Resale
5-47
A P I CHAPTERlk5 92 W 0732290 0552788 8 7 9 W
5A1.20b
--`,,-`-`,,`,,`,`,,`---
m
d
1994
5-48
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Not for Resale
A P I CHAPTERxS 9 2 M 0732270 0552789 705
m
5A1.20~
--`,,-`-`,,`,,`,`,,`---
!
1994
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5-49
Not for Resale
~~~
A PCI H A P T E R + S
92
m 0732290 0552790 427m
--`,,-`-`,,`,,`,`,,`---
O
sW
O
s
5-50
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1994
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API
C H A P T E R ~ S92
m
0 7 3 2 2 ~a552793 3 ~ m
3
--`,,-`-`,,`,,`,`,,`---
5A1.20e
1994
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5-51
Not for Resale
~~
A P I CHAPTERsS 92 M 0732290 0552792 2 T T M
--`,,-`-`,,`,,`,`,,`---
5A1.20f
994
5-52
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A P I CHAPTERx5 92
m
0732290 0552793 L36
m
5A1.21
--`,,-`-`,,`,,`,`,,`---
5-53
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Not for Resale
~~
A PC
I HAPTERr5
~
92
m
0732290 0552794 O72
m
581.1
ASTM 10% SLOPE
3
1
~
90
c
--`,,-`-`,,`,,`,`,,`---
100
8
10
12
FIGURE 5B1.1
TRUE VAPOR PRESSURE OF
GASOLINES AND FINISHED
PETROLEUM PRODUCTS
c
L
1994
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5-55
Not for Resale
A P I CHAPTERx5 92
0732249 0552775 T07
561.1
COMMENTS ON FIGURE 5B1.1
Purpose
Figure 5B 1.1 is useful for estimating the true vapor pressure
(tvp) of a gasoline or a finished
petroleum product at normal storage temperatures. The true vapor pressureof crude oils should be
determined using FigureSB 1.2.
Reliability
No estimate of the reliability of this figure is available.
Notation
Tl5 -
Ts
Slope = slope of the ASTM D 86 distillation curve at ten percentby volume distilled = 10
'
in degrees Fahrenheit per percent
distilled.
Special Comments
In the absenceof distillation data,the following approximate valuesof the ASTM ten percentslope
may be used:
Motor
gasoline
3
naphtha
Light3.5
Rvp)
psi 14(9 to
Aviation
gasoline
2
Naphtha (2 to 8 psi Rvp)
2.5
The following equation can be used instead
of Figure 5B 1.1 :
T = temperature, in degrees Rankine.
"F
S = ASTM ten percent slope
9% Distilled '
Reid = Reid vapor pressure, in pounds per square inch.
VP = exp
[(f ) ( A + B>
+ C In (Reid) + D& In (Reid)
+ P x Reid + ( E + G.& + H& In (Reid) + O x Reid) X T
+ [ZI + Z J & + Z K ln (Reid) + ZL& In (Reid)
+ ZM x Reid + ZN (Reid?]
A = 21.36512862
B = -6.7769666
C = -0.93213944
D = 1.42680425
E = -0.00568374
G = 0.00477 103
H = -0.00106045
ZI = -10177.78660360
) ].
U = 2306.00561642
ZK = 1097.68947465
ZL = -463.19014182
ZM = 65.61239475
ZN = 0.13751932
O = 0.00030246
P = -0.29459386
Literature Source
The figure is given in API Bull. 2513: Evaporation Loss in the Petroleum Industry-Causes and
Control, American Petroleum Institute, New York (1959, Reaffirmed 1973). The equations
were
Loss from External Floating Roof Tanks" Third edition,
derived in API Publication 25 17: Evaporative
1989.
Example
Estimate the tvp at 70 F of a naphtha having a ten percent ASTMslope of 3.5 and a Reid vapor
pressure (Rvp)of 11 psi.
Locate the point on the grid of Figure 5B 1.1 corresponding to a slope of 3.5 and Rvp of 11. A
straight line extended from the
70 F point on the temperature scale through this grid point intersects
the tvp scaleat 6.9 psia.
5-56
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1994
--`,,-`-`,,`,,`,`,,`---
Not for Resale
A PCI H A P T E R * 5
92
m 0732290
055279b 945
m
5B1.2
140
110
100
$I4
3
E
Q
90
5
LL
W
-4
FIGURE 5B1.2
TRUE VAPOR PRESSURE
OF
CRUDE OILS
TECHNICAL DATA BOOK
June 1993
1994
O
2
l
--`,,-`-`,,`,,`,`,,`---
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5-57
Not for Resale
A P I CHAPTERxS 92
0732290 0552797 881
561.2
COMMENTS ON FIGURE 5B1.2
Purpose
Figure 5B 1.2 is useful for estimating the true vapor pressure (tvp)
of a crude oilat normal storage
temperatures.The true vapor pressures
of gasolines and finished products should
be determined using
Figure 5B 1.1.
Reliability
No estimate of the reliability of this figure is available.
Special Comments
The following equation can be used instead
of Figure 5B 1.2.
T = temperature, in degrees Rankine.
Rvp = Reid vapor pressure, in pounds per square inch.
In vp = A + B In ( R v p ) + C ( R v p ) + DT
+
( E + F In (Rvp) + G ( R v p )
T
")
A = 7.785 11307
B = -1.08100387
C = 0.053 19502
D = 0.00451316
E = -5756.85623050
F = 1104.41248797
G = -0.00068023
Applicable Ranges:
O F < T (OF) < 140 F and 2 psic Rvp < 15 psi
Literature Source
The figure was given in API Bull. 2513: Evaporation Loss in the Petroleum industry-Causes and
Conrrol, American Petroleum Institute, New York (1959, Reaffirmed 1973). Also API Publication
25 17, Third Edition, February 1989.
Example
Estimate the tvp at
70 F of a crude oil havingan Rvp of 6 psi.
A straight line on Figure 5B 1.2 connecting the 70 F point on the temperature scaleand the 6 psi
Rvp point intersects the
tvp scale at 4.2 psia.
1994
5-58
--`,,-`-`,,`,,`,`,,`---
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5B1.3
PROCEDURE 5B1.3
BLENDING METHOD FOR REID VAPOR PRESSURE
Discussion
This procedure estimatesthe Reid vapor pressure fora blend of pure componentsand/or
petroleum fractions. The Reid vaporpressure of each stream and the molar blendingratio must be
known. The Reid vapor pressure of the blend is estimatedfrom:
--`,,-`-`,,`,,`,`,,`---
(5B1.3-1)
where:
Rvpb
a
vi
Rvp,
-
Reidvaporpressure
of the blend,psi.
1.2.
volume
fi-action of stream i.
=
Reidvaporpressure
=
-
of stream i, psi.
For a pure component, Rvpi is taken as the pure componenttrue vapor pressure at 100 F.
This procedure should not be
used for widely dissimilar componentsor streams.
Procedure
Step I: Obtain the vapor pressure of pure componentsat 100 F in Chapter 1 or the RVP of
any stream.
Step 2: Calculate the Reid vapor pressureof the blend from Equation (5B1.3-1).
5-59
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581.3
COMMENTS ON PROCEDURE 5B1.3
Purpose
This procedure is usedto estimate the Reid vaporpressure of a blend of components with
known Reid vapor pressures,as defined in ASTM Procedure 323-94.
Limitations
This method is limited to pure components and petroleum fractions.It should not be used for
widely dissimilar blends.
Reliability
This procedure has not been extensively tested. For applicable systems, the method is on
average accurate to within 1 psi. Higher errors can be expected for mixtures of unlike components.
Example
Estimate the Reid vapor pressure
of a blend that contains 7.56 gallons of tert-butyl ethyl ether
(ETBE) and 92.44 gallons of isopentane.
Step I : From Chapter 1, obtain needed d a t a .
Step 2: Calculate the Reid vapor pressureof the blend using equation(5B 1.3-1).
RVP, = (0.0756(4.1478)’-2
+
0.9244(20.4643)’-2)”’’2
RVP, = 19.2 psi
--`,,-`-`,,`,,`,`,,`---
An experimental Reid vapor pressure
for this blend is 19.0 psi.
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1999
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5B1.4
PROCEDURE 5B1.4
PREDICTION OF REID VAPOR PRESSURE
Discussion
This procedure predicts the Reid vapor pressure of a fully defined mixture by simulating ASTM
Procedure D323-94. If it is necessary to simulate a partially undefined mixture suchas a petroleum fraction
or a crude oil, please see the special comments for this procedure.
The method calculates the Reid vapor pressure ofthe liquid sample intwo steps. First, the chilled
is mixed withfour parts by volumeof air at 1 O0 F
sample is saturated witha i r . Then, onepart of the sample
and atmospheric pressure. This mixture is then flashed at 100 F and a constant total volume.The calculated
flash pressure is then corrected to obtain the Reid vapor pressure.
Procedure
Step 1: The input to this procedure is a liquid sample of known molar composition. For each
component of the input, and for oxygen and nitrogen, obtain the molecular weight,
critical
temperature, critical pressure, acentric factor,
Z, (a constant fromTable 6A2.14), and the
S , term from Table 8D 1.3.
Step 2: Saturate the sample with air using Procedure 8D1. l . The flash is conducted at 33 F and
14.696 psi. The feedto the flash is 98 mole YOsample and2% bone dry air. The liquid fiom
this flash is used for the remainder of the simulation.
Step 3: Use Procedure6A3.1 to calculate theliquid density of the liquid product
from Step 2 in units
of pound moles per cubic foot.
Step 4: One cubic foot of the sample is fédto the second flash. Multiply the liquid density by one
cubic foot to obtainthe total pound moles that will be fed to the second flash. The pound
moles of each individual component
are obtained by multiplyingthe total pound moles bythe
first flash.
liquid mole fractions from the
Step 5: Calculate the pound moles of air needed for a 4 to 1 vapor to liquid ratio at the start of the
second flash. The air is fed to the flash at 100 F and 14.696 psia. From the ideal gas law,
0.0079 pound moles of nitrogen and0.0021 pound moles of oxygen are required.
Step 6: Sum the pound moles of both the liquid sample from Step 4 and the vapor from Step 5 to
obtain the total pound molesin the mixed feed. The mole fractionof each componentin the
feed is obtained by dividing the pound moles
of the component by the total pound moles.
Step 7: Flash themixed feed at 100 F anda constant volumeof 5 f t 3 using Procedure 8D l . l . Iterate
on the pressure untilthe volumes of the two phases sums to 5 e. The volumesof the phases
are found witha material balance calculation and
appropriate density equation.For the vapor
phase, calculate the density from the gas law with a compressibility factor from the flash
calculation. The liquid density should
be determined from Procedures6A3. l .
Step 8: Subtract 14.696 psi fiom theflash pressure. The resulting valueis the predicted Reidvapor
pressure.
5-61
1999
--`,,-`-`,,`,,`,`,,`---
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Not for Resale
5B1.4
COMMENTS ON PROCEDURE 5B1.4
Purpose
This procedure is used to simulate ASTM Reid vapor pressure experimental procedures.
Limitations
The Reid vapor pressure experiments are highly sensitiveto the presence of trapped gases and light
hydrocarbons. Ifgases or parafhs with a carbon number lessthan seven are present in the mixture, the mole
fiactions of these light components must be accurately measured
to obtain a reliable prediction.
This method does not accountfor water in the atmosphere becausethe experimental procedure does
for moisture or any recordof the moisture contentof the air. Further, calculations
not require any correction
made while creatingthis method demonstratedthat the presence of water had negligible impact on
the predicted
Reid vapor pressure.
Reliability
For defined mixtures,the method reproduces experimental
data to an average deviationof 0.6 psi. For
petroleum hctions and wholecrude oils, the average deviationfiom experimental data is 0.8 psi.
Example A.
Simulate the Reid experiment
for a mixture that is 93.57 mol % isopentane and6.43% tert-butyl ethyl
ether (ETBE). The required parametersfor isopentane, ETBE, nitrogen,and oxygen are listed below.
Molecular
Weight
Acentric
Tc
(F)
P, (psia)
isopentane
72.15
369.10
0.27 0.2275
490.38
ETBE
102.18
465.53
440.92
oxygen
32.00
-181.43
nitrogen
28.01
-232.5 1
Factor
ZRA
S2
18
-0.003898
0.2957
0.2726
0.046280
73 1.44
0.0222
0.2890
0.0
493.14
0.0377
0.2893
-0.011016
Use Procedure8D1.1 to perform a flash calculation at 33 F and14.7psia of the sample saturated with
2% air.
Mole
Fraction
Mole
Feed
isopentane
0.9338
170
Fraction
Liquid
0.9
ETBE
0.0630
oxygen
0.0005
0.0042
nitrogen
0.0158
0.0648
0.0009
5-62
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--`,,-`-`,,`,,`,`,,`---
Component
1999
Not for Resale
S T D * A P I / P E T R O T D B C H A P T E R 5-ENGL L992 m 0732270 ObLSbDL 9 b 8 m
581.4
From Procedure 6A3.1, the liquid density of the saturated sample is0.5483 Ibmol/ft3.
One cubic foot, which contains 0.5483 pound moles of sample, will be fed to the second flash
calculation. To determine the pound moles
of each component, multiply bythe liquid molefractions from the
fist flash calculation.
Component
Pound Moles
isopentane
0.5 120
ETBE
0.0355
oxygen
0.0003
nitrogen
0.0005
Add 0.0077 pound moles of nitrogen and 0.0021pound moles of oxygen to the f i . Calculate the mole
fraction of each component in the feed.
--`,,-`-`,,`,,`,`,,`---
Component
Pound Moles
Mole Fraction
isopentane
0.5 120
0.9174
ETBE
0.0355
0.0636
oxygen
O.0024
0.0043
nitrogen
0.0082
0.0147
0.5581
Using Procedure 8D l . 1, perform a flash calculationon this feed at 100 F anda constant volume of 5 e. The
flash pressure is foundto be 33.8 psia by iteration. Subtracting atmospheric pressure from
the flash pressure
yelds the predxted Reid vapor pressure of 19.1 psi. The experimental value for this system from Wiltec
Research Co. is 19.0 psi.
5-63a
1999
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Not for Resale
561.4
This procedure requires afully defined mixture as a feed stream. However, for petroleum fractions
and whole crude oils, it is prohibitively expensive
to fully d e h e the mixture. Therefore,it is possibleto treat
a pseudocomponent.
the components of a complex mixtureas a blend of real pure components and
To obtain accurate predictions, the light components, trapped gases and
p a r a f i s up to a carbon
number of 6, must be treated as real components. The heavy residual
can then be treated as a single
data. Thefollowingstepsshouldbetakento
generate the
pseudocomponentcreatedfromdistillation
pseudocomponent.Thisprocedurewillrequirethespecificgravity
of the sample and the true boiling
distillation, whichcan be estimated fromD86
a distillation. It is also necessary to know the volume percentage
of the entire light end. This percentage
will be called the break volume. In other words, the break volume is
the pointat which the distillation goes from defined components
to the pseudocomponent.
Step I :
Step 2:
Step 3:
Step 4:
Calculate the volume average boiling point (VABP) using Equation2.0-3.
Use Procedure2B l.1 to calculate the mean average boiling point (MeAPB).
Calculate the sample's Watson
K from Equation2-0.8.
Determine the volume percentat which one halfof the residual is distilled.This calculation
is accomplished by taking the average
of the break volume and100%. The resultis called the
residual's midpoint volume.
Step 5: Interpolate from the true boiling point
data to find the true boiling temperature
at which the
residual's midpoint volumewill occur. This temperature is
assumed to be the residual's mean
average boiling point.
Step 6: Assume that the Watson
K is constant for the entire sample. Calculate
a specific gravity for
the residualfrom the definition of the Watson
K.
Step 7: Characterize the pseudocomponent using
Critical Temperature
Procedure 4D3.1
Critical Pressure
Procedure 4D4.1
Acentric Factor
Procedure 2B3.1
Molecular Weight
Procedure 2B2.1
The ZRAparameter can be obtained from Procedure 6A2.13 using the calculated specific
gravity. The S2parameter must be set equalto zero for pseudocomponents.
Example B.
Create aheavy residual pseudocomponentfor a crude oil given the following
data.
Volume % Distilled
True Boiling
Temperature
(F)
10
30
170.6
350.6
540.5
760.8
50
70
90
1141.3
The specific gravity is0.8445. The light end islmown to be 8.86 vol. % (the break volume)of the sample.
Calculate the volume average boiling point:
VABP = (170.6 + 350.6 + 540.5 + 760.8 + 1141.3)/5 = 592.8 F
From Procedure 2Bl.1, the mean average boihng pointis 587.4 F. The WatsonK is 12.02.
5-64a
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1999
Not for Resale
--`,,-`-`,,`,,`,`,,`---
Special Comments
-
S T D - A P I / P E T R O T D B CHAPTER 5-ENGL L972 m 0 7 3 2 2 9 0 ObL9b03 730 m
581.4
From the break volume of8.86%,the residual midpoint is calculatedas
8.86%
+
100% = 54.43%
2
Interpolating with the distillation data gives a mean average boiling point for the residual of 589.3 F. The
specific gravityof the residualis calculated as
SG
=
(589.3
459.67)'" = o.8453
12.02
+
The pseudocomponent is then characterizedas:
Critical Temperature(4D3.1)
Critical Pressure (4D4.1)
Acentric Factor (2B3.1)
Molecular Weight(2B2.1)
Z u (6A2.13)
920.0F
220.4 psia
0.6488
248 .O
0.2419
--`,,-`-`,,`,,`,`,,`---
For whole crudeoils, if the atmospheric residuumof a crude oil is not known, the physical properties
of the atmospheric residuumof another crude oil may
be substituted with little additionalloss of accuracy. It
is therefore possibleto predict the Reid vapor pressureof a crude oil from the light end compositionsand a
reference heavy residual. This approach is not recommendedfor light or NITOW boiling fractions.
5-65a
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Not for Resale
A P I C H A P T E R * 5 92
m 0732290 0552803 032 m
API TECHNICAL DATA BOOK
BIBLIOGRAPHY
1. Aldrich, “Catalog Handbook of Fine Chemicals;’ Milwaukee, W1
(1990).
2. Aldrich, Handbook of Fine Chemicals, Aldrich Chemical Co., Milwaukee, W1 (1988-89).
3. Allemand, N., Jose, J., Merlin, J.C., “Mesure des Pressions de Vapeur
d’Hydrocarbines C9 to C18n-Alcanes et n-Alkylbenzenes dansle Domain
3-1000 Pascal,” Themachim. Acta 105,79 (1986).
4.Allen. W.A., “The Maximum Pressure of Naphthalene Vapour,”
J. Chem. Soc. 77,400 (1900).
5. Alm, K., Ciprian, M., “Vapor Pressures, Refractive Index at 20 C, and
Vapor-Liquid Equilibrium at 101.325 kPa in the Methyl tert-butyl
ether-Methanol System,” J. Chem. Eng Daza 25(2), 100 (1980).
6. Ambrose,D., “Reference Values of the Vapor Pressure of Benzene and
Hexafluorobenzene,” J. Chem. Thermo. 13, 1161 (1981).
7. Ambrose, D., ‘Vapor Pressure of Some Aromatic Hydrocarbons,”
J. Chem. Thermo. 19. 1007 (1987).
8. Ambrose, D., Broderick. BE., Townsend, R., “The Vapor Pressures
above the Normal Boiling Point and the Critical Pressures of Some Aromatic Hydrocarbons,” J. Chem. Soc.: Sect.A, Inorganic Physical and
Theoretical 4, 633 (1967).
9. Ambrose, D., Counsell, J.F., Laurenson, LJ.. Lewis, G.B., “ThermodynamicProperties of Organic Oxygen Compounds. XLVII. Pressure,
Volume, Temperature Relations and Thermodynamic Properties of
Propan-2-01,”J. Chem. Thermo. 10, 1033 (1978).
10. Ambrose, D., Ellender, J.H., Sprake, H.S., Townsend, R., “Thermodynamic Properties of Organic Oxygen Compounds-XLIII. Vapour
Pressures of Some Ethers” J. Chem. Thermo. 8, 165 (1976).
1 l. Ambrose, D., Sprake, C.H.S., “Vapor Pressure of Alcohols,” J. Chem.
Thermo. 2 , 6 3 I (1970).
12. Ambrose, D., Sprake, C.H.S., Townsend, R., “Thermodynamic Properties of Organic Oxygen Compounds. XXXVII. Vapour Pressures of Methanol, Ethanol, Pentan-1-01. and Octano1 from the Normal Boiling Point
Temperature to the Critical Temperature,” J. Chem. Thermo. 7, 185 (1975).
13. Ambrose, D., Sprake, C.S., “The Vapour Pressure of Indane,”
J. Chem. Thermo. 8, 601 (1976).
14. Ambrose, D., Townsend, R., “Thermodynamic Properties of Organic
Oxygen Compounds. Part IX.The Critical Properties and Vapour Pressures
Above Five Atmospheres of Six Aliphatic Alcohols.” J. Chem. Soc. 3614
(1963).
15. Ambrose, D., Townsend, R., “Vapor Pressure of Acetylene,” Trans.
Faraday Soc. 60, 1025 (1964).
16. American Petroleum Institute “Thiophene, 2,3-and 2,SDihydrothiophene,and Tetrahydrothiophene,” API Publication 717, (November
1981).
17. American Petroleum Institute ‘Evaporation Loss in the Petroleum
Industry-Causes and Control,” API Bulletin 2513. (February 1959, Reaffirmed 1973).
18. American Petroleum Institute “Evaporation Loss from External
Floating-Roof Tanks,” API Publication 2517, Washington, D.C., Third
Edition (February 1989).
19. American Petroleum Institute Research Project 62, “Thermodynamics of Hydrocarbons from Petroleum,” Bartlesville Energy Research Center,
Bartlesville, Oklahoma, Report No. 1 (1967).
20. American Petroleum lnstitute ResearchProject 62, “Thermodynamics of Hydrocarbons from Petroleum,” Bartlesville Energy Research Center,
Bartlesville, Oklahoma, Report No. 12 (1971).
21. American Petroleum Institute Research Project 62, “Thermodynamics of Hydrocarbons from Petroleum.” Bartlesville Energy Research Center,
Bartlesville, Oklahoma, Report No. 3 (1968).
22. American Petroleum Institute Research Project 62, “Thermcdynamics of Hydrocarbons from Petroleum,” Bartlesville Energy Research Center,
Bartlesville, Oklahoma, Report No. 8 (July 1, 1970).
23. American Petroleum Institute Research Project 62, “Thermodynamics of Hydrocarbons from Petroleum,” Bartlesville Energy Research Center,
Bartlesville, Oklahoma, Report No. 7 (Jan. 1, 1970).
24. American Petroleum Institute Research Project 62, “Thermodynamics of Hydrocarbons from Petroleum,” Bartlesville Energy Research Center,
Bartlesville, OK Report No. 2 (July I , 1967).
1994
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
25. American Petroleum Institute Research Project 42. “Properties of
Hydrocarbons of High Molecular Weight,” American Petroleum Institute,
New York (1966).
26. American Petroleum Institute. API Monograph Series “Carbazole,
9-Methylcarbazole, andAcridien,” API Publication 7 16, Washington, D.C.
(1981).
27. American Petroleum Institute. APIMonograph Series “Naphthalene”
API Publication 707, Washington, D.C. (October 1978).
28. American Petroleum Institute. API Monograph Series “Tetralin,” API
Publication 705, Washington, D.C. (October 1978).
29. American Petroleum Institute. API Monograph Series ”‘Anthracene
and Phenanthrene,” API Publication 708, Washington, D.C. (January 1979).
30. American Petroleum Institute. API Monograph Series “Four Ring
Condensed Aromatic Compounds,’’API Publication 709, Washington, D.C.
(March 1979).
31. American Petroleum Institute. API Monograph Series “Indan and
Indene,” API Publication 714, Washington, D.C. (April 1980).
32. American Petroleum Institute. API Monograph Series “cis- and
fruns-Decalin”AP1 Publication 706, Washington, D.C. (October 1978).
33. American Petroleum Institute. API Monograph Series “Anthracene
and Phenanthrene,” API Publication 708, Washington, D.C. (January 1979).
34. American Petroleum Institute. API Monograph Series “Acenaphthalene, Acenaphthene, Fluorene, and Fluoranthene,” API Publication 7 15,
Washington, D.C. (January 1981).
35. American Petroleum Institute. API Monograph Series “Quinoline,”
API Publication 71 1, Washington, D.C. (December 1979).
36. American Petroleum Institute. API Monograph Series “Pyridine and
Phenylpyridine,” API Publication 710, Washington, D.C. (1979).
37. American Petroleum Institute. API Monograph Series “Isopropylbenzene and l-Methyl-2,-3. and 4-Isopropylbenzene,” API Publication 722,
Washington, D.C. (September 1984).
38. American Petroleum Institute. API Monograph Series “ren-Butyl
Methyl Ether,” API Publication 723, Washington, D.C. (November 1984).
39. American Petroleum Institute. API Monograph Series “1- and 2Methylnaphthalene and Dibenzanthracene,” API Publication 724, Washington, D.C. (February 1985).
40.American Petroleum Institute. API Monograph Series “Indole,” API
Publication 719. Washington, D.C. (April 1982).
41. American Petroleum Institute. API Monograph Series “Isoquinoline,”
API Publication 712, Washington, D.C. (December 1979).
42.Andrejew. D.N., “On theSynthesis of Alkylnaphthalenes from
Organic LithiumCompounds,” Obshch. Chem. 17, 1645 (1947).
43. Askonas, C.F., “Development of Second-Order Group Contribution
Method for the Estimation of Pure Vapor Pressure,’’ M.S. Thesis. Department of Chemical Engineering, The Pennsylvania State University (August
1986).
44. Aston, J.G., Fink, H.L., Bestful, A.B., Page, E.L., Szasz, G.J., ‘“The
Heat Capacity and Entropy, Heats of Fusion andVaporization and the Vapor
Pressure of Butene-l. TheZero Point Entropy of the Glass. The Entropy of
the Gas from Molecular Data,” J. Am. Chem. Soc. 68,52 (1946).
45. Aston, J.G., Fink, H.L., Schuman, S.C., “The Heat Capacity and Entropy, Heats of Transition ,Fusion and Vaporisation and the Vapor Pressures
of Cyclopentane. Evidence for a Non-planar Structure,” J. Amel: Chem. Soc.
65, 341 (1943).
46. Aston, J.G., Messerly, G.H., “The Heat Capacity and Entropy, Heats
of Fusion and Vaporization and the Vapor Pressure of n-Butane,” J. Ame,:
Chem. Soc. 62, 1917 (1940).
47.Aston. J.G..Messerley, G.H.,“Heat Capacities and Entropies of
Organic Compounds. II. Thermal and Vapor Pressure Data for Tetramethylmethane from 13.22 K to Boiling Point. The Entropy from its Raman Spectrum,” J. Amer. Chem. Soc. 58,2355 (1936).
48. Aston, J.G., Szasz, G.J., Fink, H.L., “The Heat Capacity and Entropy
Heats of Transition, Fusion and Vaporization and The Vapor Pressures of
Cyclohexane. The Vibrational Frequencies of Alicyclic Ring Systems,”
J. Amer: Chem. Soc. 65,1135 (1943).
49. Auwers, K., “Uber Cyclopentadien,” Chem. Ber: 45.3077 (1912).
50. Auwers, Von K., Roth, W.A., Eisenlohr, F., “Verbrennungswarmen
von Terpenen und Styrolen,” Liebigs Ann. Chem. 373,272 (1910).
5-63
--`,,-`-`,,`,,`,`,,`---
Not for Resale
~
API TECHNICAL DATA BOOK
5 l. Baghdoyan, A., Malik, J.,
Fried, Y.,“Vapor Pressures and Densities of
2,3-Dimethyl-2-Butene and 3,3-Dimethyl-l-Butene,” J. Chem. Eng. Data
130).96 (1971).
52. Bailey, AS., Pickering, GB., Smith, J.C., “Alkylnaphthalenes. Part
III.Then-Butyl-,Amyl-andHexyl-naphthalenes,”
Insf. Petrol 35, 103
( 1949).
53. Barker, J.T., “Experimentelle Bestimmung und Thermodynamische
Berechnungder Dampfdrucke von Toluol,Naphtalin, und Benzo1,”Z Phys.
Chem. (Leipzig) 71,235 (1910).
54. Beattie, J.A., Edwards, D.G., “The Vapor Pressure, Orthobaric DenJ. Amer: Chem.
sities and Critical Constants of 2,2,4-Trimethylpentanes,’’
Soc. 70,3382 ( 1948).
55. Beattie, J.A., Edwards, D.G., Marple, S . , Jr., “The Vapor Pressure,
Orthobasic Liquid Density, and Critical Constants of Isobutane,” J. Chem.
fhys. 17,576 ( 1949).
56. Beattie, J.A., Levine, S.W., Douslin, D.R., “The Vapor Pressure and
Critical Constants of Normal Pentane,” J. Am. Chem. Soc. 73.4431 (1951).
57. Beattie, J.A., Marple, S., Jr., “The Vapor Pressure, Orthobaric Liquid
Density, and Critical Constants of 1-Butene,” J. Am. Chem. Soc. 72, 1449
(1950).
58. Beerbower, A., Zudkevitch, D., “Predicting the Evaporation Behavior
of Lubricants intheSpaceEnvironment,”
Preprints, Divisionof Petrol.
Chemistry, Am. Chem.Soc., L.A. Meeting, 8(2) C-99 (April 1963).
59. Belzeck, C., Lange, J., “Reakcje Epoksyzwiakow Alifatycznych. V.
Otrzymywanietrans-Propenylbenzenu,” Rocmiki. Chem. 35, 1641 (1961).
60.Bender, P., Furukawa, G.T., Hyndman, J.R., “Vapor Pressure of Benzene above 100 C,” Ind. Eng. Chem. 44.387 (1952).
61.
Benoliel,
R.W.,
“Some Physical Constants Seven
of
Four
Carbon-Atom Hydrocarbons and Neopentane,” Masters Thesis, Pennsylvania State University (1940).
62. Bent, H.E., Cuthbertson, G.R., Dorfman, M.D., Leary, R.E., “Single
Bond Energies. I. TheC-C Bond in Hexaphenylethane,” J. Ame,: Chem
Soc. 58, 165 (1936).
63. Bergman, E., “Dipole Moment and Molecular Structure. Part XVI.
Configuration of Ethylene Compounds,”J. Chem. Soc. 402 (1936).
64. Birch, S.F., Dean, R.A. Fidler, EA., Lowry, R.A., “ThePreparation of
the C10 MonocyclicAromaticHydrocarbons,” J. Amer: Chem. Soc. 71,
1362 ( 1949).
65. Boublik, T.,Fried, V., Hala, E., “The VapourPressuresof Pure
Substances,” Elsevier,New York (1973).
66. Boublik, T., Fried, V., Hala, E., “The VaporPressures of Pure
Substances, Second Rev. Edition,” Elsevier, NewYork (1984).
67. Boundy, R.H., Boyer, R.F., “Styrene, Its Polymers, Copolymers and
Derivatives,” 55, Reinhold, New York (1952).
68. Brackman, D.S., Plesch, P.H., “Some Physical Properties of
cis-Stilbene,”J. Chem. Soc.2188 (1952).
69. Brooks, D.B., Howard, F.L., Crafton, H.C., Jr., “Physical Properties
of Purified 2,2,3-Trimethylpente,” J. Res. N d . Bur: Szd. A 23, 637
(1 939).
70.Brower.G.T.,Thodos,G.,“Vapor
Pressures of Liquid Oxygen
Between the Triple Point andCritical Point,”J. Chem. Eng. Data 13(2),262
( 1968).
71. Buckles, R., Wheeler, N.G., “cis-Stilbene,” Org. Synth. Coll. Vol. 4,
857 (1963).
72.Burchfield,J.,“Vapor
Pressures of Indene, Styreneand Dicyclopentadiene:’ J. Ame,: Chem. Soc. 64,2501 (1942).
73.Burgoyne,J.H.,“Two-Phase
Equilibrium in Binaryand Ternary
Systems. IV. The Thermodynamic Properties of Propane,” Pmc. Roy. Soc.
(hndon) 176,280 (1940).
74. Burrell, G.A., Robertson, LW., “The Vapor Pressure of Ethane and
Ethylene at Temperatures Below Their Normal Boiling Points,” J. Amer:
Chem. Soc. 37,1893 (1915).
75. Burrell, G.A., Robertson, LW., “The Vapor Pressures of Acetylene,
Ammonia andIsobutaneat Temperatures Below Their Normal Boiling
Points,”J. Amer: Chem. Soc. 37,2482 (1915).
76. Calado, J.C.G., Clancy, P., Heintz, A., Streett, W.E., “Experimental
and Theoretical Studyof the Equation of State of LiquidEthylene,”
J. Chem. Eng. Data 27,376 (1982).
77. Calingaert, G., Soroos, H., Hnizda, V., Shapiro, H., “Hexamethylethane,” J. Amer: Chem. Soc. 66, 1939 ( 1944).
78. Camin, D.L., Forziati, A.F., Rossini, ED., “Physical Properties of
n-Hexadecane, n-Decylcyclopentane,n-Decylcyclohexane, 1-Hexadecene,
n-Decylbenzene,” J. fhys. Chem. 59,440 (1954).
79. Camin, D.L., Forziati, A.F., Rossini, F.D., “Physical Properties of
n-Hexadecane, n-Decylcyclopentane, Decylcyclohexane,1-Hexadecane,
n-Decylbenzene,” J. fhys. Chem. 59,440 (1954).
80. Camin, D.L., Rossini, F.D., “Physical Properties of 15 American
Petroleum Institute Research Hydrocarbons, C9 to C15,” J. Phys. Chem. 59,
1173 (1955).
81. Camin, D.L., Rossini, F.D., “Physical Properties of the 17 Isomeric
Hexenes of the API Research Series,” J. Phys. Chem. 60, 1 4 4 6 (1956).
82. Camin, D.L., Rossini, F.D., “Physical Prpoerties of 16 Selected C7
and C8 Alkene Hydrocarbons,” J. Chem Eng. Dam 5(3), 368 (1960).
83. Campbell, K.N., Eby, L.T.,“The Preparation of Tertiary Acetylenes,”
J. Amer: Chem. Soc. 62, 1800 ( 1940).
84. Campbell, K.N., O’Connor, M.J., “The Hydrogenation of Substituted
Acetylenes with Raney Nickel,”J. Amer: Chem. Soc. 61,2897 (1939).
85. Canjar, L.N., Goldman, M., Marchman, H., ‘Thermodynamic Properties of Propylene,” Ind. Eng. Chem. 43, 1186 (1951).
86. Carmichael, L.T., Sage, B.H., “Phase Equilibria inHydrocarbon Systems: VolumetricBehavior of n-Nonane,” Ind.Eng. Chem. 45,2697 (1953).
87. Cervenkova, I., Boublik, T.,“VaporPressures, Refractive Indexes,
and Densities at 20.0 C, and Vapor-Liquid Equilibrium at 101.325 kPa, in
the terf-AmylMethyl Ether-Methanol System,”J. Chem. Eng. Data 29,425
(1984).
88. Chipman, J. Peltier, S.G., “Vapor Pressure and Heat of Vaporization
of Diphenyl,” Ind. Eng. Chem. 21, 1 106 (1929).
89. Chirico, R.D., Nguyen, A., Steele, W.V., Strube, M.M., “Vapor Pressure of n-Alkanes Revisited. New High-Precision Vapor Pressure Data on
n-Decane, n-Eicosane, and n-Octacosane,” J. Chem. Eng. Data 34, 149
(1989).
90. Clayton, J.O., Giauque, W.F.,“The Heat Capacity and Entropy of
Carbon Monoxide. Heat of Vaporization. Vapor Pressures Solid
of and Liquid. Free Energy to 5000 K from Spectrascopic Data,” J. Amer: Chem. Soc.
54,2610 (1932).
91. Clement, H.E., Wise, K.V., Johnsen, S.E., “Physical Properties of
o-, m- andp-Methylstyrene,”J. Amer: Chem Soc. 75, 1593 (1953).
92. Connolly, J.F., “Ideality of n-Butane-Isobutane Solutions,” J. Phys.
Chem. 66,1082 (1962).
93. Cook,M.W., “Vapor Pressure Apparatus,”Rev. Sci. Instr: 29,399 (1958).
94. Cope, A.C., Pike, R.A., Spencer, C.F., “Cyclic Polyolefins. XXVII.
Cis- and tmns-Cyclooctene from N,N-Dimethylcyclooctylamine,”J. Amer:
Chem. Soc. 75,3212 (1953).
95. Couch, E.J., Kobe, K.A., Hirth, L.J., “Volumetric Behavior of Nitric
Oxide,” J. Chem. Eng. Data 6(2), 229 (1961).
96. Crafts, J.M., “Pointes Fixes de Thermometrie entre 100 et 400 Tensions de Vapeur de la Napthaline, de l’eau et de la Benzophenome,” J. Chim.
fhys. 11,429 (1913).
97. Crafts, J.M., “Tensions de Vapeur de l’eau entre 40 et 100,’’J. Chim.
Phys. 13. 105 (1915).
98. Cubitt, A.G., Henderson, C., Staveley, L.A., “Some Thermodynamic
Properties of Liquid Hydrogen Sulfide and Deuterium Sulfide.” J. Chem.
Thermo. 19,703 (1987).
99. Cummings, G.M.,McLaughlin, E., “Vapor Pressures of Some Unsaturated Hydrocarbons Containing Six Carbon Atoms,” J. Chem. Soc. 1391
( 1955).
100. Dadieu, A., Pongratz, A.,Kohlrausch,K.W.F.,“Studien
zum
Ramaneffekt.XVI. Das Ramanspektrum Organischer Substanzen (cistrans-Isomeric)”Monarscht. Chem. 60,221 (1932).
101. Dana,L.I., Jenkins, A.C., Burdick, J.N., Timm, R.C.,“Thermodynamic Properties of Butane, Isobutane. and Propane,” Refrig. Eng. 12,
387 (1926).
102. Das,T.R., Reed, C.O., Jr., Eubank. P.T., “PVT Surface andThennodynamic Propertiesof n-Pentane,”J. Phys. Chem. ref: Data 22(1), 3 (1977).
103. Daubert, TE., “Vapor Pressure of 13 Pure Industrial Chemicals,” in
Experimental Results for Phase Equilibria and Pure Component Properties,
(J.R. Cunningham, D.K. Jones, eds.), DIPPR Data Series No. 1, (1991).
1 0 4 . Daubert, T.E., Danner,R.P., “Technical DataBook-PetroleumRefining, 4th Edition,’’ American Petroleum Institute, Washington, D.C. (extant
1987).
--`,,-`-`,,`,,`,`,,`---
5-64
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
1994
~
A P I CHAPTER85 9 2
0732290 0 5 5 2 8 0930 5
m
API TECHNICAL DATA BOOK
--`,,-`-`,,`,,`,`,,`---
105. Dauben, T.E., Jalowka, J.W., Goren, V., “Vapor Pressure of 22 Pure
Industrial Chemicals,“ AIChE Symposium Series 83 (256) 128 (1987).
106. Day, H.O., Nicholson, D.E., Felsing, W.A., TheVapor Pressures and
Some Related Quantities of Pentene- 1 from O to 200,” J. Amer: Chem. Soc.
70, 1784 (1948).
107. DeKruif, C.G., Krupers, T.. VanMiltenbug, J.C., Schaake, R.C.F.,
Stevens, G., “The Vapour Pressure of Solid and Liquid Naphthalene,”
J. Chem. Thermo. 13, 1081 (1981).
108. DeKruif, C.D., “Enthalpies of Sublimation and Vapor Pressures of
11 Polycyclic Hydrocarbons,” J. Chem. Thermo. 12,243 (1980).
109. Denig, F., “The Pyrolysis of Some Hydrocarbons,” Chem. Mer. Eng.
25,751 (1921).
110. Dictionary of Organic Compounds (7 Vols.), 5th ed., Chapmanand
Hall, New York, New York (1982).
111. Do&, K.W., “Copolymerization of Acetylene Derivatives with
Olefins. Retardation by Radicals from Acetylenes,” J. Ame,: Chem. 72,4681
(1950).
112. Dolliver, M.A. er al, “Heats of Organic Reactions. V. Heats of
Hydrogenation of Various Hydrocarbons,” J. Am. Chem Soc. 59, 831
(1927).
113. Dreisbach, R.R., “Physical Properties of Chemical Compounds,”
Advances in Chemistry Series, American Chemical Society, Washington,
D.C. (1955).
114. Dreisbach, R.R., Shrader, S.A., “Vapor Pressure-Temperature Data
on Some OrganicCompounds,” Ind. Eng. Chem. 41,2879 (1949).
115. Drucker, C., Jimeno, E., Kangro, W., “Dampfdrucke flussiger stoffe
bei Niedrigen Temperaturen,”Z Phys. Chem. (Leipzig) 90,513 (1915).
1 16. Ellard, J.A., Yanko, W.H., “Thermodynamic Properties of Biphenyl
andthe Isomeric Terphenyl,” Final Report, IDO-1 lo08 Monsanto Res.
Corp., US. Atomic Energy Comm. Contract AT (10-1)-1088 (1963).
117. Engineering Science Data Item, 76024, “Vapour Pressures and Critical Points of Liquids. IX. C2 to C1 1 Aliphatic Ethers and Three Aromatic
Ethers,” London (1 976).
i 18. Engineering Science Data,Item 73008, “Vapour Pressures of Pure
Substances Up to Their Critical Points II: C2 to C6 Alkenes,” London
(1973).
119. Engineering Science Data, Item 82016, “Vapour Pressures and Critical Points of Liquids XXI:Cyclic Hydrocarbons,” London (1982).
120. Engineering Sciences Data, “Validated Engineering Data Index,”
ESDU International Ltd. London (1983-84).
121. Engineering Sciences Data, Item 73029, “Vapor Pressures of Pure
Substances up to their Critical Points. III. C6 toC10 Alkylbenzenes,”
London (1973).
122. Engineering Sciences Data, Item 85008 “Vapour Pressure and Critical Points of Liquids, Part 2A: C2 toC6Alkenes:’ London (1985).
123. Engineering Sciences Data, Item 86001 “Vapour Pressures and Critical Points of Liquids Part 2c: Alkadienes and Alkynes,” London (1986).
124. Evans, T.W., Edlund, K.R., “Tertiary Alkyl Ethers. Preparation and
Properties,’’ Ind. Eng. Chem. 28, 1 186 (1936).
125. Eventova, M.S., Meilanova, D.Sh., “Oxidation of Phenylcyclohexane and Bicyclohexyl,” Vesfnik.Moscow. Uniu lO(l0) 103 (1955).
126. Farrington, P.S., Sage, B.H., “Volumetric Behavior of Propene,” Ind.
Eng. Chem. 41,1734 (1949).
127. Fawcett, F.S., “Boiling Points of Three Isomeric Heptanes,” Ind.
Eng. Chem. 38,338 (1946).
128. Felsing, W.A., Watson, G.M., “The Compressibility of Liquid
Octane,” J. Ame,: Chem. Soc. 64, 1822 ( 1 942).
129. Fernandez-Fasnacht, E., Del Rio, F., “The Vapor Pressure of C02
from 194 to 243 K,”J.Chem. Thermo. 16,469 (1984).
130. Finch, J.L., Wilhelm, R.M., “Variation with Pressure of the Boiling
Points of Napthalene, Benzophenone and Anthracene,” J. Amer: Chem. Soc.
47, 1577 (1925).
131. Finke. H.L., Scott, D.W.. Gross, M.E., Messerley, J.F., Waddington,
G., “Cycloheptane, Cyclooctane and 1,3,5-Heptatriene. Low Temperature
Thermal Properties, Vapor Pressure and Derived Chemical Thermodynamic
Properties,” J. Ame,: Chem. Soc. 78,5469 (1956).
132. Finke. H.L., Scott, D.W., Gross, M.E., Waddington, G., Huffman,
H.M., “The Entropy and Vapor Pressure of 1-Pentanethiol,” J. Ame,: Chem.
Soc. 74,2804 (1952).
133. Flanigan, D.A., Yesavage,V.F., “Enthalpy of Tetrahydronaphthalene
(Tetralin) Between 921 and 655 K and at Pressures to 10342 Wa,” J. Chem.
Thermo. 19,931 (1987).
134. Flebbe, J.L., Barclay, D.A., Manley, D.B., “Vapor Pressures of
Some C4 Hydrocarbonsand Their Mixtures,” J. Chem. Eng. Data 27,405
( 1 982).
135. Fluka “Catalog 1 6 ’ Chemika-Biochemika 1988/89, FlukaChemical
Corp. Ronkonkoma, NY (1988).
136. Forziati, A.D., Camin, D.L., Rossini, F.D.,“Vapor Pressures and
Boiling Points of Sixty API and NBS Hydrocarbons,” J. Res. Narl. Bu,:
Standards 45,406 (1950).
137. Forziati, A.F., Camin, D.L., Rossini, F.D., “Density. Refractive
Index, Boiling Point, and Vapor Pressure of Eight Monooletin (1-Alkene),
Six Pentadiene, and Two Cyclomonoolefin Hydrocarbons,”J. Res. Nur. Bur:
Srand., A 45(5), 406 (1950).
138. Forziati, A.F., Noms, W.R., Rossini, F.D.,“Vapor Pressures and
Boiling Points of Sixty API-NBS Hydrocarbons,” J. Res. Narl. Bu,: Srd.
A 43,555 (1949).
139. Fowler, L., Trump, W.N., Vogler, C.E., “Vapor Pressure of Napthalene,” J. Chem. Eng. Daru 13(2), 209 (1968).
140. Francis, A.W., Robbins, G.W., “Thevapor Pressuresof Propane and
Propylene,” J. Ame,: Chem. Soc. 55,4339 (1933).
141. Gallaugher, A.F., Hibben, H., “Studies on Reactions Relating to
Carbohydrates andPolysaccharides. LIV. The SurfaceTension Constants of
the Polyethylene Glycols and Their Derivatives,” J. Arne,: Chem. Soc. 59,
2514 (1937).
142. Galpern, G.D., Kusakov, M.M., “‘AbsorptionSpectra of Cyclohexyl
and Cyclopentylbenzenes in the Near Ultraviolet,” Trudy Insr. Nefri. A b d .
SSR 12,38 (1958).
143. Gamer, J.B., Adams, L., Stuchell, R.M., “Storage and Handling of
Butadiene, Isobutylene, Styrene and Acrylonitrile,” Perrol. Refiner 21, 321
(1942).
144. Garrick, EJ., “The Vapor Pressures of Diphenyl and of Aniline,”
Trans. Faraday Soc. 23,560 (1927).
145. Giauque, W.F., Kemp, J.D., “The Entropies of Nitrogen Tetroxide
and Nitrogen Dioxide. The Heat Capacity from 15 K to the Boiling Point.
The Heat of Vaporization and VaporPressure. The EquilibriaNz04= 2NO2
= 2N0+02,” J. Chem. Phys. 6,40 (1938).
146. Giauque, W.F., Powell, T.M., “Chlorine. The Heat Capacity, Vapor
Pressure, Heats of Fusion and Vaporization, and Entropy;’ J . Amer: Chem.
Soc. 61, 1970 (1939).
147. Gillespie, P.C., Wilding, W.V., Wilson, G.M., “Vapor-Liquid
Equilibrium Measurements on the Ammonia-Water System from 313 K to
589 K,” AIChE Symposium Series 83(256) 97 (1987).
148. Glaser, F., Ruland, H., “Untersuchungen uber Dampfdruckkurven
und kritische Daten einiger technisch wichtiger organische substanzen,”
Chem. Ingr-Tech. 29,772 (1957).
149. Good, W.D., “The Standard Enthalpies of Combustion and Formation of n-Butylbenzene, the Dimethylbenzenes, and the Tetra Methylbenzenes in the Condensed State,” J. Chem. Thermo. 7.49 (1975).
150. Goodwin, R.D.. “Hydrogen Sulfide Provisional Thermophysical
Properties from 188 to 700 K at Pressures to 75 MPa,” National Bureau of
Standards, SBSIR83-1694, Chern. Eng. Science Division, National Engineering Laboratory, Boulder, CO (October 1983).
151. Goodwin, R.D., Roder, H.M., Straty, G.C., “Thermophysical Properties of Ethane from 90 to 600 K at Pressures to 700
Bar,” National Bureau
of Standards Technical Note 684, Cryogenics Division, Boulder, Colorado
(August 1976).
152. Goodwin, R.D., Haynes, W.M., “Thermophysical Properties of
Propane from 85 to 700 K at Pressures to 70 MPa,” National Bureau of
Standards Monograph170, Boulder. Colorado (1982).
153. Haar, L., Gallagher, J.S., “Thermodynamic Properties of Ammonia,”
J. Phys. Chem. Ref: Daru 7(3), 635 (1978).
154. Haar, L., Gallagher, J.S., Kell, G.S., “NBS/NRC Steam Tables.
Thermodynamic and Transpon Properties and Computer Programs for
Vapor and Liquid States ofWater in SI Units.” Hemisphere Publishing Corporation, Washington (1984).
155. Handbook of Chemistry and Physics, 58th ed., edited by R.C. Weast,
The Chemical Rubber Co., Cleveland, Ohio (1977-1978).
1994
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
5-65
Not for Resale
A P I CHAPTER*S
92
0732290 0552804 841
API TECHNICAL DATA BOOK
--`,,-`-`,,`,,`,`,,`---
156. Handbook of Chemistryand Physics, 62nd ed., edited by R.C.
Weast, the Chemical Rubber Co., Cleveland,Ohio (1981).
157. Handbook of Data on Organic Compounds, edited by R.C. Weast,
M.J. Astle, CRC Press, Inc., BocaRaton, FL (1985).
158. Handbook of Data on OrganicCompounds, 2nd. Ed., Edited by R.C.
Weast, J.G. Grasselli, CRC Press, Boca Raton, FL (1988).
159. Harteck, P., Edse, R., “Dampfdruckmessungvon Propan,” 2, Phys.
Chem. (Leipzig) 182A, 220 (1938).
160. Haynes, W.M., Goodwin,R.D., ‘Thermophysical Properties of
Normal Butane from 135 to 700 K at Pressures to 70 MPa,” National
Bureau of Standards Monograph 169, Boulder, Colorado (1982).
161. Heisig, G.B.,“ActionofRadonon
Some UnsaturatedHydrocarbons. III. Vinylacetylene and Butadiene,” J. Am. Chem. Soc. 55, 2304,
(1933).
162. Hildebrand, J.H., Sweny, J.W.,“The Entropy of Solution of Hexane
and Hexadecane,” J. Phys. Chem. 43,297 (1939).
163.Hoffmann, F., Lang, K.F., Berlin, K., Schmidt, A.W., “Uber die
Bezlehugen Zwischen Konstibutionuna Klopffestigkeit (Konlenwasserstoffen. II.,” Bremstofch. Chem 14, 103 (1933).
164. Holloway, C., Jr., Thurber, S.H.,
“Phase Behavior in Systems of
Hydrocarbon-Furfural-Water,” Ind. Eng. Chem. 36,980 (1944).
165. Hopke, E.R., Sears, G.W., “Vapor Pressures of Trimethylbenzenes
in the Low Pressure Region,” J. Amer. Chem. Soc. 70,3801 (1948).
166. Hossenlopp, I.A., Scott. D.W., “Vapor Heat Capacities and Enthalpies of Vaporization of Four Aromaticand/or Cycloalkane Hydrocarbons,”
J. Chem. Thermo. 13,423 (1981).
167. Hossenlopp, I.A., Scott, D.W., “Vapor Heat Capacities and Enthalpies of Vaporization of Five Alkane Hydrocarbons,” J. Chem. Thermo. 13,
415 (1981).
168. Hubbard, W., Finke, H.L., Scott, D.W., McCullough, J.P., Kate, C,,
Gross, M.E., Messerly, J.F., Pennington, R.E., Waddington, G., “Thiacyclopentane: Heat Capacity, Heats of Fusion and Vaporization, Vapor Pressure,
Entropy, Heat of Formation andThermodynamic Functions,” J. Am. Chem.
Soc. 74,6025 (1952).
169. Huffman, H.M., Gross, M.E., Scott, D.W., McCullough, J.P., “Low
Temperature Thermodynamic Properties ofSix
Isomeric Heptanes,”
J. Phys. Chem. 65(3), 495 (1961).
170. Hughes, E.E., Lias, S.G., “Vapor Pressures of Organic Compounds
in the Range Below One Millimeter of Mercury:’ National Bureau of Standards Technical Note 70, Washington, D.C. (1960).
171. International Critical Tables ofNumerical Data, Physics, Chemistry,
and Technology (7 Vols. + Index), edited by E.W. Washburn, McGraw-Hill,
New York (1926-1933).
172. IUPAC, “International Thermodynamic Tables of the Fluid StateCarbon Dioxide,” edited by S. Angus, B. Armstrong and K.M. deReuck,
Pergamon Press, New York(1976).
173. IUPAC, “International Thermodynamic Tables of the Fluid StatePropylene (Propene),” edited by S. Angus, B. Armstrong, K.M. de Reuck,
Pergamon Press, Oxford (1980).
174. Jacquercd, A., Wassmer, E., “Ueber den Siedepunkt des Naphtalins,
des Diphenyls und des Benzophenons unter ver schiedenem Druckund
dessen Bestimmung mit Hilfe des Wasserstoffthermometers,” Chem. Ber:
37,2531 (1904).
175. Kassel,L.S., “Vapor Pressures ofXylenes and Mesitylene,”J. Amer.
Chem. Soc. 58,670 (1936).
176. Kay, W.B., “The Vapor Pressures and Saturated Liquid and Vapor
Densities of the Isomeric Hexanes,”J. Amer. Chem. Soc. 68, 1336 (1946).
177.Kay,W.B.,Warze],F.M.,
“2,2,4-Trirnethylpentane (Isooctane).
Vapor Pressure, Critical Constants, and Saturated Vapor and Liquid Densities,” Id.Eng. Chem. 43, 1150 (1951).
178. Kayayama, H., Harada, Y., “Vapor Pressure Measurement of Tetralin at Reduced Pressures,”J. Chem. Eng. Dura 29,373 (1984).
179. Keenan, J.H., Keyes, F.G., Hill, P.G., Moore, J.G., “Steam Tables.
Thermodynamic Properties ofWater Including Vapor, Liquid, and Solid
Phases,” John Wiley & Sons, Inc., New York, (1969).
180. Kemp, J.D., Giauque, “Carbonyl Sulfide. The Heat Capacity, Vapor
Pressure, and Heats of Fusion and Vaporization.The Third Law of Thermodynamics and Orientation Equilibrium in the Solid,” J. Amer. Chem. Soc.
59.79 (1937).
181. Kerns, W.J., Anthony, R.G., Eubank, P.T., “Volumetric Properties of
CyclohexaneVapor,” AIChESymp. Ser: 70(140). 14 (1974).
182. Kilpatrick, J.E., Pitzer, K.S., “The Thermodynamics of Dimethylbutane Including the Heat Capacity,
Heats of Transition, Fusion and Vaporization and the Entropy,” J. Am. Chem. Soc. 68, 1066 (1946).
183. Kirk-Othmer,“Encyclopediaof ChemicalTechnology,” 2nded., (22
Vols. + Suppl.), Interscience, NewYork (1966).
184. Kobe, A.K., Ravicz, A.E., Vohra,
S.P., “Critical Properties andvapor
Pressures of Some Ethers and Heterocyclic Compounds,” J. Chem Eng.
Dura 1(1), 50 (1956).
185. Kratzke,H., ‘Thermodynamic Quantities for Propane. I. The Vapour
Pressure of Liquid Propane,” J. Chem. Thermo. 12,305 (1980).
186.Kratzke,H.,Muller, S., Bohn, M., Kohler, R., “Thermodynamic
Properties of Saturated and Compressed Liquid n-Pentane,”J. Chem. Thermo. 17,283 (1985).
187. Kratzke, H.,Spillner,E., Muller, S.. “Thermodynamic Properties for
n-Butane. 1. The Vapour Pressure of Liquid +Butane,” J. Chem. Thermo.
14, 1175 (1982).
188. Kretschmer,C.B., Wiebe, R., “Liquid-Vapor Equilibriumof Ethanol
-Toluene Solutions,”J. Amer: Chem. Soc. 71, 1793 (1949).
189. Kuhn, G., “Uber die Methodik der Kondensationsgasanylse undderen Erweiterung durch Adsorption an Kieselsauregel beitiefen Temperaturen,”Angew. Chem. 44,757 (1931).
190. Kutz,W.M., Nickels, J.E., McGovern, J.J., Corson, B.B.,“Catalytic
Alkylation of Indan and Tetralin by Olefins, Alcohols and Ditehyl Ether,”
J. Ame,: Chem. Soc. 70,4026 (1948).
191. Lamb, A.B., Roper, E.E., “The VaporPressures of Certain Unsaturated Hydrocarbons,”J.Amer: Chem. Soc. 62,806 (1940).
192.Lambert,J.D., Cotton, K.J., Pailthorpe, M.W., Robinson, A.M.,
Scrivins, J., Vale, W.R.F., Young, R.M.,
“Transport Propeties of Gaseous
Hydrocarbons,” Proc. Roy. Soc. (London) A231,280 (1955).
193. Laurance,D.R., Swift, G.W., “Vapor-LiquidEquilibria in the Three
Binary and Ternary Systems Composed of n-Butane, Butene-l. and Butadiene- 1,3,” J. Chem. Eng. Dura 19(1), 6 1 ( 1974).
194. Lee, B.I., Kesler, M.G., “A Generalized Thermodynamic Correlation Based on Three-Parameter Corresponding States,” A K h E J. 21 510
(1975).
195. Leslie, E.H., Carr,A.B., “Vapor Pressure of OrganicSolutions,” hd.
Eng. Chem. 17,810 (1925).
196. Lesteva, T.M., Ogoradnikov, M.S.K., Morozova, A l , ” Zh. Prikl.
Khim. 40,891 (1967).
197. Letcher, T.M., Marsicano, F., “Vapour Pressures and Densities of
Some unsturated C6 Acyclic and Cyclic Hydrocarbons Between 300 and
320 K,” J. Chem. Thermo. 6,509 (1 974).
198. Levy, M.G.,“L-alpha-Ethylnaphthalineet ses Produits DHydrogenation,” C. R. Acud. Sci. Puris 193, 194 (1931).
199. Linder, E.G., “Vapor Pressures of Some Hydrocarbons,” J. Phys.
Chem. 35,531 (1931).
200. Linder, E.G., “Vapor Pressures of Some Hydrocarbons,” J. Phys.
Chem. 35,531 (1931).
201. Lister, M.W., “Heats of Organic Reactions.X. Heats ofBromination
of Cyclic Olefins,” J. Amer. Chem. Soc. 63, 143 (1941).
202. Lister, M.W., “Heats of Organic Reactions.X. Heats ofBromination
of Cyclic 0lefins:’L Amer. Chem. Soc. 63,143 (1941).
203. Lumbroso,H., Colse, R., Liermain,A., “Effets Inductif et Mesomere
dans les Molecules Organiques Substituees.V. Enynes Aromatiques,” Bull.
Soc. Chim. 1608 (1956).
204. Lyons, R.L., ‘The Determination of Critical Properties and Vapor
Pressure of Thermally Stable and Unstable Compounds”M.S. Thesis. Dept.
of Chem. Eng. The Pennsylvania State University (May 1985).
205. Maass, O., Wright,C.H.,“SomePhysicalPropertiesof
Hydrocarbons Containing Two and Three Carbon Atoms,” J. Am. Chem. Soc. 43,
1098 (1921).
206. Machado, J.R.S., Streett, W.B.,“Equation of State and Thermodynamic Properties of Liquid Methanol from 298 to 489 K and Pressures to
l@IOBar,”J. Chem. Eng. Dura 28,218 (1983).
207. Macknick, A.B., Prausnitz, I.M.,“Vapor
Pressures of High
Molecular-Weight Hydrocarbons,” J. Chem. Eng. Dura 24(3), 175
( 1979).
1994
5-66
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
~
A P I CHAPTER*5
92 W 0732290 0 5 5 2 8 0 57 8 8
m
API TECHNICAL DATA BOOK
208. Maess, L., Muffling, L. Von, “Uber die Dampfdruckeeiniger
Kohlenwasserstoffe und Ketone,” Angew. Chem. 50,759 (1937).
209. Marsden, C., editor, “Solvents Guide,’’ 2nd edition, Cleaver-Kume,
London (1963).
210. Matheson Company, Inc., “Matheson Gas Data Book,” 3rd ed., East
Rutherford, New Jersey (1961).
21 1. Matheson Company, Inc., “Matheson Gas Data Book,” unabridged
ed., 4 vols., East Rutherford, New Jersey (1974).
212. Matheson Company, Inc., “Matheson Gas Data Book,” 6th ed.,
Lyndhurst, New Jersey (1980).
213. Mathews, J.H., “The Accurate Measurement of Heats of Vaporization of Liquids,” J . Amer: Chem. Soc. 48,562 (1926).
2 14. Matsuda, J. Chem. Soc. Japan Ind. Chem. Sect. 60,563 (1957).
215. Maxwell, J.B., Bonnell, L.S., Vapor Pressure Charts for Petroleum
Engineers, Esso Res. and Engrg. Co., Linden, NJ (1955).
216. McCarty,R.D., Hord, J., Roder, H.M., ‘SelectedProperties of
Hydrogen (Engineering Design Data),” Center for Chemical Engineering,
National Engineering Laboratory, Nat. Bur. Stand. Monograph 168, Boulder, CO (1981).
217. McCullough, J.P., Douslin, D.R., Messerly, J.F.. Hossenlopp,
I.A., Kincheloe, T.C., Waddington, G.. “Pyridine: Experimental and
Calculated Chemical Thermodynamic Properties Between O and 1500
K; A Revised Vibrational Assignment,” J . Am. Chem. Soc. 79, 4289
(1957).
218. McCullough, J.P., Scott, D.W., Finke, H.L., Gross, M.E., Williamson, K.D., Penningon, R.E., Huffman, H.M., Waddington, G., “Ethanethiol: Thermodynamic Properties in the Solid, Liquid and Vapor States.
Thermodynamic Functionsto I O 0 0 K,” J. Ame,: Chem. Soc. 74. 2801
(1952).
219. McIntosh, D., “The Physical Properties of Liquid and Solid Acetylene,” J. Phys. Chem. 11, 306 (1907).
220. McMicking, J.H., “Vapor Pressures and Saturated Liquid and Vapor
Densities of Isomeric Heptanes and Octanes,” Ph.D. Thesis, The Ohio State
University (1961).
221. McMicking, J.H., Kay, W.B., “VaporPressures and SaturatedLiquid
and Vapor Densities of the Isomeric Heptanes
and Isomeric Octanes,” Pmc.
Am. Petrol. Ins?. 45(3) (1965).
222. Mellor, J.W., “A Comprehensive Treatise on Inorganic and Theoretical Chemistry,”Vol. 8, Longmans, London (1928).
223. Melpolder, EW., Woodbridge, J.E., Headington, C.E., “The Isolation and Physical Properties of the Diisopropyl-benzenes,” J. Amer. Chem.
Soc. 70, 935 ( 1948).
224. Mertes, T.S.. Colburn, A.P., “Binary Mixtures of n-Butanes, Isobutane, and 1-Butene with Furfural: Vapor-Liquid Equilibria and Thermodynamic Properties,” lnd. Eng. Chem. 39,787 (1947).
225. Messerly, G.H., Kennedy, R.M., “The Heat Capacity and Entropy,
Heats of Fusion and Vaporization and the Vapor Pressure of n-Pentane,”
J. Amer: Chem. Soc. 62,2988 (1 940).
226. Meyer, E.F., Holz, R.D., “High-Precision Vapor Pressure Data for
Eight Organic Compounds,” J. Chem. Eng. Datu 18(4), 359 (1973).
227. Michels, A., Lupton, J.M., Wassenaar, T., de Graaff,W., “Isotherms
of Carbon Monoxide Between O C and 150 C and at Pressures up to 3000
Atmospheres,” Physica 18, 121 (1952).
228. Michels, A., Wassenaar, T., “The Vapor Pressure of Ethylene,” Physica 16,221 (1950).
229. Michels, A., Wassenaar, T., Louwerse, P., Lunbeck, R.J.. Wolkers,
G.J., “Isotherms and Thermodynamical Functions of Propene at Temperatures between 25 and 150 C and at Densities up to 340 Amagat (Pressures
up to 2800ATM),” Physica 19, 287 (1953).
230. Michels, A., Wassenaar, T., Zwretering, T.N., “The Vapour Pressure
of Carbon Monoxide,” Physica 18, 160 (1952).
23 I . Mischenko, K.P., Subbotina, V.V., “Vapor Pressure of Ethyl Alcohol
at Temperatures from 4-460,” J. Appl. Chem. USSR, (English)40(5). 1156
(1967).
232. Moor, G. and Kanep, E.K., “Trans. Experimental Research Lab,”
Chem. COSIII. Leningrad (1936).
233. Morgan, D.L., “Extension of Pitzer Corresponding States Correlations Using New Vapor Pressure Measurements of the n-Alkanes C10 to
C28,” Ph.D. Thesis, Rice University, Houston, TX (1990).
234. Morrell, S.H., Pickering, G.B., Smith, J.C., “Alkylnaphthalenes.
Part III. The Methyl, Ethyl and N-Propyl Naphthalenes,” J. Insr. Perrol. 34,
677 (1984).
235. Mortimer, F.S., Murphy, R.V., “The Vapor Pressures of Some
Substances Found in Coal Tar,” Ind. Eng. Chem. 15(11), 1140 (1923).
236. Muthu. O., Munjal, S., Smith, B.D., “Total-Pressure Vapor Liquid
Equilibrium data forBinary Systems of Acetone with Isopropylbenzene and
Isopropenylbenzene,” J . Chem. Eng. Dura 28. 192 (1983).
237. Myers, H.S., Fenske, M.R., “Measurement andCorrelation of Vapor
Pressure Data for High Boiling Hydrocarbons,” Ind. Eng. Chem. 47, 1652
(1955).
238. Nasini, A.G., “The Molecular Dimensions of Organic Compounds.
Part III. The Viscosity of Vapours: Thiophen and Methylthiophenipyridine
and Thiazole,” Proc. Roy. Soc. (London) Vol 123A (1929).
239. Natarajan, G., Vtswanath, D.S., “Enthalpy of Vaporisation and
Vapor Pressure of Benzene, Toluene, p-Xylene, andTetralin Between 1 and
16 Bar,”J. Chem. Eng. Data 30, 137 (1985).
240. Nehzat. M.S., Hall, K.R., Eubank, P.T., “Thermophysical Properties
of Ethylene in the CriticalRegion,” J . Chem. Eng. Dara 28,205 (1983).
241. Nelson, O.A., Senseman, C.E., “Vapor Pressure Determination on
Napthalene, Anthracene, Phenanthrene and Anthraquinone Between Their
Melting Points and Boiling Points,” Ind. Eng. Chem. 14,58 (1922).
242. Nessmejanov, A.N., Petschersskaya, K.A., “Organic Mercury Compounds. XIX. Reaction of the Grignard Reagent with alpha-(Halomercuri)
Acetophenone,” Izv. Akad. SSSR, Otd. Chim. 67 (1941).
243. Nichols, W.B., Reamer, H.H., Sage, B.H., “Volumetric Behavior of
n-Heptane,” Ind. Eng. Chem. 47,2219 (1955).
244. Nicoline, E.R., “The Vaporization of Pure Organic Liquids,” Am.
Chim. 6,582 (195 I).
245. Niesen, V.G., Yesauage V.F., “Vapor-Liquid Equilibria form-Cresol/
Tetralin and TetralidQuindine at Temperatures Between 523 and 598 K,”
J. Chem. Eng. Data 33.253 (1988).
246. Nohra, S.P., Kang, T.L.,Koke, K.A., McKetta,J.J., “PressureVolume-Temperature Properties of Propyne,” J. Chem. Eng. Data 7, 150
(1962).
247. Olds, R.H.. Reamer, H.H., Sage, B.H., Lacey, W.N. “Phase Equilibria in Hydrocarbon Systems: Volumetric Behavior of n-Butane,” Ind.
Eng. Chem. 36,382 (1944).
248. Olson, A.C., “Alkylation of Aromatics,” Ind. Eng. Chem. 52, 833
( 1960).
249. Osborn, A.G., Douslin, D.R., “Vapor Pressure Relations of 36 Sulfur
Compounds Present in Petroleum,”J. Chem. Eng. Daru 11,502 (1966).
250. Osborn, A.G.. Douslin, D.R., “Vapor Pressure and Derived Enthalpies of Vaporization for Some Condensed-Ring Hydrocarbons,” J. Chem.
Eng. Daru 20(3), 229 (1975).
251. Osborn, A.G., Douslin, D.R., “Vapor Pressure Relations for the
Seven Pentadienes.” J. Chem. Eng. Datu 14,208 (1969).
252. Osborn, AG., Douslin, D.R., “Vapor-Pressure Relations for 15
Hydrocarbons,” J. Chem. Eng. Data 19, 1 14 (1974).
253. Osborn, A.C., Scott, D.W., “Vapor Pressures of 17 Miscellaneous
Organic Compounds,” J. Chem. Thermo. 12,429 (1980).
254. Osborn, G., Douslin, D.R., “Vapor Pressure Relations of 13 Nirrogen Compounds Related to Petroleum,” J. Chem.Eng. Data 13(4), 534
(1968).
255. Oscarson, J.L., Lundell, S.O., Cunningham, J.R., “Phase Equilibria for Ten BinarySystems,” AIChE Symposium Series 83(256) 1
(1987).
256. Overstreet, R., Giauque,W.F., “Heat Capacity and Vapor Pressure of
Ammonia,” J. Amer: Chem. Soc. 59.254 (1937).
257. Palczewska-Tulinska, M.,Cholinski, J., Szafranski. A., Wyrzykowska-Stankiewics, “Experimental Vapor Pressures and Maximum-Likelihood Antoine-Equation Constants for I , 1 ,I-Methoxydimethylpropane,
Thiacyclopentane and 1,4-Butanediol,” Fluid Phuse Equil. 15,295 (1984).
258. Park, W.R., Wright, C.F., “Oxymercuration of cis- and rrans- Propenylbenzene,” J. Org. Chem. 19, 1435 (1954).
259. Perry, R.E., Thodos, G., “Vapor Pressures of the Light Normal
Saturated Hydrocarbons,” Ind. Eng. Chem. 44,1649 (1952).
260. Petro-Tex Chemical Corp., “Methyl rerr-Butyl Ether,” (Material
Safety Data Sheet), Houston, Texas (1979).
1994
5-67
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A P I CHAPTERaS 9 2
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API TECHNICAL DATA BOOK
261. Philpotts, A.R., Thain, W., “Infrared Absorption Spectra of Tertiary
Peroxides,”A~l.Chem. 24,638 (1952).
262. Pittsburgh - Des Moines Steel Co. Fellowship - Mellon Institute,
“Physical and Chemical Properties of Isobutylene,” Petrol. Refiner 24(2),
99 (1 945).
263.Pitzer,K.S., Scott, D.W., “The Thermodynamics and Molecular
Structure of Benzene and Its Methyl Derivatives,” J. Am. Chem. Soc. 65,
803 ( 1943).
264. Prasad, D.H.L., “P-V-T Relations of Propane in the Range 373.15423.15 K and0.2-4.0 MPa,” AIChE J. 28,695 (1 982).
265. Prengle, H.W., Jr., Greenhaus, L.R., York, R., Jr., “Thermodynamic
Properties of n-Butane,” Chem. Eng. Pmgr. 44, 863 (1948).
266. Price, C.C., Greene, C.E., “Copolymerization of Phenylacetylene
with Vinylpyridine,” J. Polym. Sci. 6, 111 (195 1).
267. F‘rydz, R., Goodwin, R.D., “Experimental Melting and Vapor Pressures of Methane,” J. Chem. Thermo. 4, 127 (1972).
268. Reamer, H., Sage, B., “Volumetric Behavior of Nitrogen Dioxide in
the Liquid Phase,” Ind. Eng. Chem. 185 (Jan. 1952).
269.Reamer, H.H., Sage,B.H.,
“Phase Equilibria inHydrocarbon
Systems: Volumetric Behavior of Cyclohexane,” Ind. Eng. Chem., Chem.
Eng. Datu Se,: 2(1), 9 (1957).
270. Reamer, H.H., Sage,B.H.,“VolumetricandPhase
Behavior of
Propene-Propane System,” Ind.Eng. Chem. 43, 1628 (1951).
271. Riddick, J.A., Bunger, W.B., “Organic Solvents: Physical Properties
and Methodsof Purification,” 3rd ed., Wiley
Interscience, New York (1970).
272. Riedel, L.,“EineNeueUniverselleDamfdmck-formal:’
(A New
Universal Vapor Pressure Equation) Chem. h g . Tech. 26,83 (1954).
273. Robinson, D.B., Senturk, N.H., “The Vapor Pressure and Critical
Properties of Carbonyl Sulfide,”J. Chem. Thermo. 11,461 (1979).
274. Roder, H.M., McCarty, R.D.,Johnson, V.J., “Saturated Liquid Densities of Oxygen, Nitrogen, Argon and Parahydrogen,” National Bureau of
StandardsTechnical Note 361, Washington, D.C.(1968).
275. Rondeau, R.E., Harrah, L.A.,“Melting Point and VaporPressure of
3-Hexyne,” J. Chem. Eng. Datu 10,84 (1965).
276. Rotinjanz, L., Nagoinov, N., “Die Zustandsflachen des Cyclohexans:’ 2 Phys. Chem. (Leipzig) 169A, 20 (1934).
277. Sabetay, S., “Deshydration par la Potasse du Groupement Ethylol
Contigu au Noyau Benzenique. III. Deshydration des alpha,alpha-Acroylarylethanols,” Bull. Soc. Chim. Fr. 47,614 (1930).
278. Sage, B.H., Lacey, W.N., “Monograph on API Research Project 37.
Thermodynamic Properties of the Lighter ParaffinHydrocarbonsand Nitrogen,” American PetroleumInstitute, New York 20, New York(1950).
279. Sage, B.H.. Lacey, W.N., “SomeProperties of the Lighter Hydrocarbons, Hydrogen Sulfide, and Carbon Dioxide,” Monograph on API Res.
Proj. 37,American Petroleum Institute, New York 20, New York (1955).
280.Sage,B.H.,
Schaatsma, J.G.,Lacey,W.N.,
“Phase Equilibria in
Hydrocarbon Systems V. Pressure-Volume-Tempe~ture Relations and
Thermal Properties of Propane,” Ind. Eng. Chem. 26, 1218 (1934).
281. Sakoguchi, A., Iwai, Y., Takenaka, J., Arai, Y., “Measurement of
Vapor Pressures of Tetralin, 1-Naphthol. and Biphenyl Using a Flow-type
Apparatus,” Kugaku Koguku Ronbu Shu, 15(1) 11b (1989).
282. Sax, N.I., “Dangerous Properties of Industrial Materials,” 6th ed.,
Van Nostrand Reinhold Company, New York (1984).
283. Scheeline, H.W., Gilliland, E.R., “Vapor-Liquid Equilibrium in the
System Propane-Isobutylene,” Ind. Eng. Chem. 31, 1050 (1939).
284. Schiessler, R.W.Am. Doc. Inst. Doc 4597 LibraryofCongress,
Washington, D.C. (1954).
285. Schmeling, T.,Strey,R.,“EquilibriumVaporPressure
Measurements for the n-Alcohols in the Temperature Range from -30 C to 30 C,”
BerBunsenges. Phys. Chem. 87(10), 871 (1983).
286. Schuhmacher, J.P., Wibaut, J.P., “Synthesis, Defractometric Constants, and Some other PhysicalPropertiesofa
Homologous Series of
Branched Alkenes,” Rec. Trav. Chim. Pays-Bas 72, 1037 (1953).
287. Schumann, R.H., Aston, J.G., Sagenkahn, M., “The Heat Capacity
and Entropy, Heats of Fusion and Vaporisation and the Vapor Pressures of
Isopentane,” J. Arne,: Chem. Soc. 64,1039 (1942).
288. Scott. D.W., Finke, H.L., McCullough, J.P., Gross, M.E., Messerly,
J.F., Pennington, R.E., Waddington, G., “2,3-Dimethyl-2-butene:Thermodynamic Properties in the Solid, Liquid and Vapor States,” J. Ame,: Chem.
Soc. 77,4993 (1955).
5-68
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
289. Scott, D.W.,Waddington, G., “Vapor Pressure of cis-2-Pentene,
trans-2-Pentene and 2-Methyl-l-butene,” J. Am Chem. Soc. 72, 4310
( 1950).
290. Scott, D.W., Waddington, G., Smith, J.C., Hoffman, H.M., “Thermodynamic Properties of Three Isomeric Pentenes,” J. Am. Chem. Soc. 71,
2769 (1949).
291. Scott, R.B.,Ferguson,W.J., Brickwedde, F.G.,“Thermodynamic
Properties of cis-2-Butene from 15 to 1500 K,” J. Res. N d . Bur. Std.
33, 1 (1944).
292. Scott, R.B.,
Meyers,
C.H., Randis, R.D.,Brickwedde,
F.G.,
Bekkedahl, N., “Thermodynamic Properties of 1,3-Butadiene in the Solid,
Liquid and Vapor States,”J. Res. Nur. Bur. Srund.A35, 39 (1945).
293. Seglin, L., “Correlating Vapor Pressure and Latent Heat Data,” Ind.
Eng. Chem. 38,402 (1946).
294. Shen-Tu, C., Unocal, Private Communication, 1991.
295. Sidorova, N.G., “Cycloalkylation of Aromatic Compounds. (VIII)
Condensation of 2-Methylcyclohexanol and 2-MethylcyclopentanoI
with
Benzene,” Zh. Obshch. Khim. 24,94 (1954).
296. Silberbeg, I.H., McKetta, J.J., Kobe,K.A., “Compressibility of
Isopentane with the Bumett Apparatus,” J. Chem. Eng. Dura 4, 323
(1959).
297. Sivaram, A., Kobayashi, R., “Investigation of Vapor Pressures and
Heats ofVaporization of Condensed Aromatic Compoundsat Elevated
Temperatures,” J. Chem. Eng. Datu 27,264 (1982).
298. Smith, D., Srivastava, R., “Data for Pure Compounds. Part B. Halogenated Hydrocarbons and Alcohols,”Elsevier, Amsterdam (1986).
299. Smith, D., Srivastava, R., “Thermodynamic Datafor Pure Compounds. Part A. Hydrocarbons and Ketones,”Elsevier, Amsterdam (1986).
300. Smith, E.R., “Boiling Points of Benzene, 2,2,3-Trimethyl Butane,
3-Ethylpentane and 2,2,4,4-Tetramethylpntane Withinthe Range 1001500 Millimeters of Mercury,” J. Res. Nut¿. Bur. Std. A X , 129 (1941).
301. Smith, E.R.,
“Boiling
Points of +Heptane and
2,2,4-Trimethylpentane Over the Range 100 to 1500 Millimeter Pressure,” J. Res.
Nut. Bu,: Stand., A24,229 (1940).
302. Smith, H.A., Pennekamp, E.H., “The Catalytic Hydrogenation of
the Benzene Nucleus. III. The Hydrogenation of Polymethyl Benzenes,”
J. Amel: Chem. Soc. 67,279 (1945).
303. Smith, N.K.,Stewart,R.C., Osbom, AG., Scott, D.W., “Pyrene:
Vapor Pressure, Enthalpy of Combustion, and Chemical Thermodynamic
Properties,”J. Chem. Thermo. 12,919 (1980).
304. Smyth, C.P., Engel, E.W., “Molecular Orientation and the Partial
Vapor Pressure of Binary Mixtures. I. System Composed of Normal Liquids,” J. Amer Chem. Soc. 51,2646 (1929).
305. Srivastava, R., Smith, B.D., “Total-Pressure Vapor Liquid Equilibrium Data for Binary Systems ofDiethylamine with Acetone,Acetonitrile,
and Methano1,”J. Chem. Eng. Datu 30,308 (1985).
306. Standard Oil Company (Indiana), “Progress Report No. 2. Vapor
Pressures and Saturated Liquids and Vapor Densities of Some PureHydrocarbons in the Gasoline Boiling Range,” Whiting Lab. Report No. F46-4
( 1946).
307. Standard Oil Company (Indiana), “Progress ReportNo.1Vapor
Pressures and Saturated Liquid and Vapor Densities of Some Pure Hydrocarbons in the Gasoline Boiling Range,” Whiting Lab. Report No. F45-9
(1945).
308. Steele, W.V., Chirico, A., Nguyen, T.A., Hossenlopp, I.A., “Determination of Some Pure Compound Ideal Gas Enthalpies of Formation,”
TopicalReportNIPER-319,
National Institute for Petrol.andEnergy
Research, Bartlesville, OK 74005, January (1988).
309. Steele, W.V., Chirico, R.D., Hossenlopp, I.A., Nguyen. A., Smith,
N.K.,Gammon,B.E.,
“The Thermodynamic Properties of FiveBenzoquinolines,”J. Chem. Thermo. 21,81 (1989).
310. Steele, K., Poling, B.E., Manley,D.B.,“VaporPressures
for the
System I-Butene, Isobutane and 1,3-Butadiene,” J. Chem. Eng. Datu 21(4)
339 (1976).
31 1. Stewart, D.E., Sage, B.H., Lacey. W.N., “Volumetric Behavior of
n-Hexane in Liquid Phase,”Ind. Eng. Chem. 35,655 (1943).
312. Stucky, J.M., Saylor, J.H., “The Vapor Pressures of Some Organic
Compounds. I.,” J. Arne,: Chem. Soc. 62,2922 (1940).
3 13.Stull, D.R., “Vapor Pressure of Pure Substances,” Ind. Eng. Chem.
39,517 (1947).
1994
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339. Wackher, R.C., Linn, C.B., Grosse, A.V., “Physical Properties of
Butanes and Butenes,” lnd. Eng. Chem. 37,464 (1945).
340. Wada,T.E., Kishida, Y., Tomila, H., Suga, S., Nitta, I., Nitta, S.,
“Crystal Structure and Thermodynamical Investigations of Triethylenediamine,” Bull. Chem. Soc. Japun 33, 1317 (1960).
341. Wagner, W., Cryogenics, 13,470 (1973).
342. Walling, C., Seymour, D., Wolfstrin, K.W., ‘Copolymerization XII.
The Effect of m- and p - Substitution on the Reactivity of alpha-Methylstyrene,” J. Amer. Chem. Soc. 70, 1544 (1948).
343. Ward, S.H., Vanwinkle, M., “Vapor-Liquid Equilibria at 200 millimeters of Mercury,”Ind. Eng. Chem. 46,338 (1954).
344. Waxman, M., Gallagher, J.S., “Thermodynamic Properties of Isobutane for Temperatures from 250 to 600 K and Pressures from 0.1 to
40 MPa,” J. Chem. Eng. Dara 28,224 (1983).
345. Weissman, S., Wood, S.E., “Vapor-Liquid Equilibrium of Benzene-2,2,4-TrimethylpentaneMixture,” J. Chem. Phys. 32, 1153 (1960).
346. Whitmore, F.C., Fleming. G.H., “Preparation of Tetramethylmethane (neopentane) and Determination of its Physical Constants,” J. Ame,: Chem. Soc. 55,3803 (1933).
347. Wieczorek, S.A., Kobayashi, R., “Vapor Pressure Measurements of
Diphenylmethane, Thianapthene, and Bicyclohexyl at Elevated Temperatures.” J. Chem. Eng. Dura 25,302 (1980).
348. Wieczorek, S.A., Kobayashi, R., “Vapor-Pressure Measurements of
I-Methylnaphthalene, 2-Methylnaphthalene, and 9, 10-Di-hydrophenanthrene at Elevated Temperatures,” J. Chem. Eng. Data 26(1). 8 (1981).
349. Wilding, W.V., Wilson, L.C., Wilson, G.M.. “Vapor-Liquid Equilibrium Measurements:’ AIChE Symposium Series 83(256) 49 (1987).
350. Wilding, W.V., Wilson, L.C.. Wilson, G.M.. “Vapor-Liquid Equilibrium Measurements on Four Binary Systems of Industrial Interest,”AIChE
Symposium Series 83(256) 80 ( 1 987).
351. Wilhoit, R.C., Zwolinski, B.J., “Physical and Thermodynamic Properties of Aliphatic Alcohols,” J. Phys. Chem. Ref: Dara 2 (Suppl. No. I )
( 1973).
352. Wilke, G., Muller, H., “Dialkylaluminium-Hydride als Sterisch
Spezifische Reduktionsrnittel fur Acetylene,” Chem. Be,: 89,444 (1956).
353. Willingham, C.B., Taylor, W.J., Pignocco, J.M., Rossini, ED.,
“Vapor Pressures and Boiling Points of Some Paraffin Alkylcyclopentane,
Alkylcyclohexane, and Alkylbenzene Hydrocarbons,” J. Res. Nat. Bu,:
Sfand.,A35, 219 (1945).
354. Willingham, C.B., Taylor, W.J., Pignocco, J.M., Rossini. F.D.,
“Vapor Pressures and Boiling Points of Some Paraffin Alkylcyclopentane,
Alkylcyclohexane, and Alkylbenzene Hydrocarbons,” J. Res. Nat. Bur.
Stand.. A35,219 (1945).
355. Wilson. G.M., Johnston, R.H., Hwang, S.C., Tsonopolous, C.,
“Volatility of Coal Liquids atHigh Temperatures and Pressures,” Ind. Eng.
Process Des. Develop., 20,94 including Supplementary Material (1981).
356. Wingfoot Corp. CA: 313 (1946).
357. Wolfe, D., Kay, W., Teja, A., “Phase Equilibria in the n-Pentane +
Pent-l-ene System. 1. Critical States,” J. Chem. Eng. Data 28, 319 (1983).
358.York, P.K., Felsing, W.A., “The Vapor Pressures, Densities, and
Heats of Vaporization of 2,4,4-TrimethyI-l-Penteneand 4-Vinyl-lcyclohexene,” Texas J. Sci. 4,261 (1952).
359. Young, S., “The Vapour-Pressure. Specific Volumes, Heats of
Vaporization, and Critical Constants of Thirty Pure Substances,” Royal
Dublin Society, Scientific Proceedings, Ser. A. Vol. 12, 374 (1910).
360. Young, S., “XLVIII-On the Vapour-Pressures and Specific Volumes
of Similar Compounds of Elements in Relation to the Position of Those
Elements in the Periodic Table. Part I,” J. Chem. Soc. 55.486 (1889).
361. Younglove, B.A., “Thermophysical Properties of Fluids. I. Argon,
Ethylene, Parahydrogen, Nitrogen, Nitrogen trifluoride, and Oxygen,”
J. Phps. Chem. Rej Dara 11 (Suppl. No. I ) (1982).
362. Zander, M.,Thomas, W., “Some ThermodynamicProperties of
Liquid Ammonia: PVT Data, Vapor Pressure, and Critical Temperature,.’
J. Chem. Eng. Dara 24(1), 1 (1979).
363. Zanolini, D., Private communication, The Pennsylvania State
University (1963).
364. Zmaczynski, A., “Recherches Ebullioscopiques et Tonometriques
Comparatives de 8 Substances Organiques Etalons,”J. Chim. Phys. 27.503
(1930).
--`,,-`-`,,`,,`,`,,`---
314. Stull, D.R., “Vapor Pressure of Pure Substances-Correction,” Ind.
Eng. Chem. 39, No. 12, 1684 (1947).
315. Stull, D.R., Sinke, G.C., McDonald,R.A., Halton, W.E., Hildebrand, D.L., “Thermodynamic Properties of Indane and Indene,” Symp.
Therrnodynam., Fitzens-Wattens Tiral, No. 4 8 . 9 ~(1959).
3 16. Taylor, T.W., Murray, A.R., “Isomeric Change in Certain Stilbenes,”
J. Chem. Soc. 2078 (1938).
3 17. Tennessee Eastman Vapor Pressure Data.
3 18. Thermodynamic Research Center, “Selected Values of Properties of
Hydrocarbons and Related Compounds,’’ American Petroleum Institute
Research Project 44, Texas A & M University, College Station, Texas
(loose-leaf data sheets, extant) (1980).
3 19. Thermodynamics Research Center “TRC Thermodynamic TablesHydrocarbons,” The Texas A & M University System, College Station
(1989).
320. Thermodynamics Research Center, “Selected Values of Properties
of Chemical Compounds,” Data Project, Texas A & M University, College
Station, Texas (loose-leaf data sheets, extant,1980).
321. Thermodynamics Research Center. “Selected Values of Properties
of Hydrocarbons and Related Compounds,” Thermodynamics Research
Center Hydrocarbon Project, Texas A & M University, College Station,
Texas (1981).
322. Thermodynamics Research Center, “Selected Values of Hydrocarbons and Related Compounds,” Thermodynamic Research Center HydrocarbonProject,Texas
A & M University, CollegeStation, Texas
(1983).
323. Thermodynamics Research Center, “TRC Thermodynamic TablesHydrocarbons,” The Texas A & M University System, College Station, TX
(1986).
324. Thermodynamics Research Center, “TRC Thermodynamic TablesHydrocarbons,” The Texas A & M University System, College Station, TX
(1988).
325. Thermodynamics Research Center, “TRC Thermodynamic TablesHydrocarbons,” The Texas A & M University System, College Station, TX
( 1990).
326. Thomas, R.H.P., Harrison, R.H., “Pressure-Volume-Temperature
Relations of Propane,” J . Chem. Eng. Dara 27(1), 12 (1982).
327. Tkkner, A.W., Losing, F.D., “The Measurement of Low Vapor
Pressures by Means of a Mass Spectrometer,” J. Phys. Colloid Chem. 55,
733 (1951).
328. Thmermans. J., “Physico-Chemical Constants of Pure Organic
Substances (2 vols.),” 2nd ed., Elsevier, New York (1965).
329. Toda, H., Kosaka, Y., Fushizawki, Y., “Manufacture of Lubricating
Oil fromCrude Rubber,” J. Chem. Soc. Japan Ind. Chem. Sect. 53, 89
(1951).
330. VanHook,W.A..
“Vapor Pressures of the Methylacetylenes,
H3CCCH. H3CCCD. D3CCCH, and D3CCCD.” J. Chem. Phys. 46, 1909
(1967).
331. Vargaftik, N.B., “Tables on the Thermophysical Propertiesof
Liquids andGases,” 2nd ed., Halsted Press, New York (1975).
332. Vasserman, A.A., Rabinovich. V.A., “Therrnophysical Properties
of Liquid Air and its Components,” National Science Foundation, Special
Foreign Currency ScienceInformationProgram,Washington,D.C.
(1970).
333. Vaughan, W.E., ”The Homogenous Thermal Polymerization of
1,3-Butadiene,” J. Am. Chem. Soc. 54,3863 (1932).
334. Vaughan, W.E., Graves, N.R., “P-V-T Relations of Propylene,” Ind.
Eng. Chem. 32, 1252 ( 1940).
335. Vilcu, R., Gainab, I., Perisanu, St., Anitescu, Gh., “Vapor Pressures
of cis- and rrans-2-Butenes,” Rev. Roum. Chim. 34 (2) 697 (1989).
336. Villard, P., “Etude des Gaz Liquefies,” Ann. Chim. Phys. 10(7), 387
( 1897).
337. Vogel, A.I., “Physical Properties and Chemical Constitution. Part
III. Cyclopentane, Cyclohexane, Cycloheptane, and Some Derivatives. The
Multiplanar Structure of the Methylcyclohexane Ring.,” J. Chem. Soc. 1323
(1938).
338. Voronkow. V.G., Broun, A.S., Karpenko, G.P., “Reaction of Sulfur
with Unsaturated Compounds. III. Synthesis of 2-Phenylthiophene,” Zh.
Obshch. Khim. 19,1927 (1949).
1994
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Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
5-69
Not for Resale
A P I TDB
CHAPTERS6
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0732290 0536567 045
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CHAPTER 6
DENSITY
Revised Chapter 6 to First Edition (1966),
Second Edition (1970), Third Edition (1976), and
Fourth Edition (1983)
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A P I TDB
CHAPTER*:b
$* W
0732290 0536568 T 8 1 W
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Copyright O 1985 American Petroleum Institute
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T D B CHAPTER*b
API
**
m 0732290
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The first editionof the Technical Data Book-Petroleum Refining was published
in1966. That edition included recommendations for correlating and predicting
densities basedon the available literature through 1964. In 1972 the liquid density
portion of the chapter was revised, and the vapor density portion was revised in
1976.
Since that time a number of new correlations and considerable additionaldata
have become available. Thus, in 1983 the Data Book project staff in the Department of Chemical Engineering at The Pennsylvania State University began a revision of Chapter 6. The results of these evaluations are included in this chapter
revision. Detailed results of the evaluations and information supportingthe selection of the methods for inclusion in this chapter are presented in Documentation
Report No. 6-84, available from University Microfilms, AnnArbor, Michigan.
The evaluation work for this revision of the chapter was done by Mr. John L.
Lobo underthe direction of Drs. Ronald P. Danner and ThomasE. Daubert. The
technical work for the chapter was reviewed by the Technical Data Committee of
the American PetroleumInstitute. The advisory committeefor Chapter 6 consisted
of J. S. Lasher, Gulf OilCorporation(chapter coordinator), M. A. Albright,
Phillips Petroleum Company, and C. F. Spencer, M. W. Kellogg Company.
Ronald P. Danner
Thomas E.Daubert
Department of Chemical Engineering
The Pennsylvania State University
University Park, PA 16802
January 1984
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PREFACE
A P I TDB CHAPTER*b
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CHAPTER 6
DENSITY
PAGE
6A Density of Liquid Systems
6A1
Density Conversion Tables
Table
6A l. 1
Density Conversion .....................................
6A2
Density of Pure Liquid Hydrocarbons
Specific Gravity of Liquid Normal
Figure 6A2.1
Paraffin Hydrocarbons at Saturation
Pressures .....................................................
Specific Gravity of Liquid Isomeric
Figure 6A2.2
Heptanes at Saturation Pressures ................
Specific Gravity of Liquid Isomeric
Figure 6A2.3
Octanes at Saturation Pressures ..................
Specific Gravity of Liquid Isomeric
Figure 6A2.4
Octanes at Saturation Pressures ..................
Specific Gravity of Liquid Branched
Figure 6A2.5
Paraffin Hydrocarbons at Saturation
Pressures .....................................................
Specific Gravity of Liquid Naphthene
Figure 6A2.6
Hydrocarbons at Saturation Pressures ........
Specific Gravity of Liquid 1,3-Butadiene
Figure 6A2.7
at Saturation Pressures ................................
Specific Gravity of Liquid Olefin
Figure 6A2.8
Hydrocarbons at Saturation Pressures ........
Specific Gravity of Liquid Aromatic
Figure 6A2.9
Hydrocarbons at Saturation Pressures ........
Specific Gravity of Liquid
Figure 6A2.10
Dimethylbenzenes at Saturation
Pressures .....................................................
Specific Gravity of Liquid Aromatic
Figure 6A2.11
Hydrocarbons at Saturation Pressures ........
Figure 6A2.12
Procedure 6A2.13
Table 6A2.14
Procedure 6A2.15
Specific Gravity of Liquid Acetylenes at
Saturation Pressures ....................................
Saturated Liquid Densities of Pure
Components ................................................
Input Parameters for Equations
(6A2.13-1) and (6A2.15-1) for
Calculating Pure Saturated Liquid
Densities ......................................................
Saturated Liquid Densities of Pure
Components ................................................
6-1
6-2
6-4
6-7
6- 19
6-20
6-21
6-22
6-23
6-23
6-24
6-24
6-25
6-25
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6-0 Introduction .....................................................................................................
Liquid Density Calculation Procedures ......
Figure 6-0.1
Excess Volumes for Hydrocarbon
Table 6-0.2
Systems .......................................................
6-26
6-26
6-29
6-3 1
6-37
V
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PAGE
Figure 6A2.16
Table 6A2.17
Figure 6A2.18
Table 6A2.19
Figure 6A2.20
Table 6A2.21
--`,,-`-`,,`,,`,`,,`---
Figure 6A2.22
Procedure 6A2.23
6A3
Specific Gravities of Liquid
Hydrocarbons at One Atmosphere
(Low-Temperature Range) ..........................
Temperature Ranges for Specific
Gravity of Liquid Hydrocarbons at One
Atmosphere (Low Temperature) ................. 6-41
Specific Gravity of Liquid Paraffins and
Olefins at Atmospheric Pressure ................. 6-43
Grid Coordinates and Temperature
Ranges for Specific Gravity of Liquid
Paraffins and Olefins at Atmospheric
Pressure .......................................................
6-45
Specific Gravity of Liquid Naphthenes
and Aromatics at Atmospheric Pressure ..... 6-47
Grid Coordinates and Temperature
Ranges for Specific Gravity of Liquid
Naphthenes and Aromatics at
Atmospheric Pressure .................................
6-49
Densities of Compressed Pure Liquid
Hydrocarbons and Their Defined
Mixtures ......................................................
Analytical Method for the Densities of
Compressed Pure Liquids ...........................
Density of Liquid Mixtures
Procedure 6A3.1
Densities of Defined Liquid Mixtures at
Their Bubble Points ....................................
Procedure 6A3.2
Densities of Defined Liquid Mixtures at
Their Bubble Points ....................................
Liquid Densities of Compressed
Procedure 6A3.3
Hydrocarbon Mixtures of Defined
Composition ................................................
Procedure 6A3.4
Computer Method for the Liquid
Densities of Compressed Hydrocarbon
Mixtures of Defined Composition ..............
Figure 6A3.5
Densities of Liquid Petroleum Fractions
atLow Pressures .........................................
Procedure 6A3.6
Analytical Method for the Densities of
Liquid Petroleum Fractions at Low
Pressures .....................................................
Densities of Liquid Petroleum Fractions
Procedure 6A3.7
at High Pressures .........................................
Figure 6A3.8
Isothermal Secant Bulk Modulus at
20,000 psig for Petroleum Fractions ...........
Figure 6A3.9
Pressure Correction for Isothermal
Secant Bulk Modulus for Petroleum
Fractions ......................................................
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6-39
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6-53
6-55
6-57
6-61
6-65
6-69
6-73
6-75
6-77
6-79
6-80
A P I TDB CHAPTERrb st
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Procedure 6A3.10
Figure 6A3.11
Analytical Method for the Densities of
Liquid Petroleum Fractions at High
Pressures .....................................................
Volumetric Shrinkage Resulting from
Blending Low Molecular Weight
Hydrocarbons with Crude Oils ................... 6-83
--`,,-`-`,,`,,`,`,,`---
6B Density of Gas Systems
6B 1
Density of Pure Hydrocarbon and Nonpolar Gases
Density of Pure Hydrocarbon and
Procedure 6B l. 1
Nonpolar Gases ...........................................
Compressibility Factors, Simple Fluid
Table 6B 1.2
Term, z(O) ......................................................
Compressibility Factors, Correction
Table 6B 1.3
Tenn, 2'') ......................................................
Generalized Compressibility Factors,
Figure 6B 1.4
Simple FluidTerm ......................................
Generalized Compressibility Factors,
Figure 6B 1.5
Simple Fluid Term, Expanded Region ........
Generalized Compressibility Factors,
Figure 6B 1.6
Correction Term ..........................................
Generalized Compressibility Factors,
Figure 6B 1.7
Correction Term,Extended Region ............
Alternate (Computer) Method for the
Procedure 6B 1.S
Density of Pure Hydrocarbon and
Nonpolar Gases ...........................................
6B2
Density of Gaseous Hydrocarbon and Nonpolar Mixtures
Procedure 6B2.1
Density of Hydrocarbon and Nonpolar
Gas Mixtures ...............................................
Procedure 6B2.2
6-81
6-85
6-89
6-91
6-93
6-94
6-95
6-96
6-97
6-99
Alternate (Computer) Method for the
Density of Hydrocarbon and
Nonpolar Gas Mixtures ...............................
6-103
Bibliography ............................................................................................................
6-105
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A P I TDB
CHAPTERWb
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CHAPTER 6
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DENSITY
6-0 INTRODUCTION
Liquid Systems
per U.S. gallon at 60 F
pounds
in air, Weight
in
Density is definedas the massof a substance contained in
a unitvolumeand is frequentlyexpressedingramsper
milliliter or in pounds (weighed in vacuum) percubic foot.
Density is often indicated in terms of API gravity; specific
gravity; and pounds (weighed in air) per gallon, per cubic
foot, or per barrel. Specific gravity is the densityof a liquid
relative to that of water at stipulated conditions of temperature and pressure:
-
density of water at 60 F
= 7.481 (weight in air, in pounds per
U.S.
gallon at 60 F)
Weight in air, in poundsper barrel at60 F
gallon at 60 F)
(6-0.1)
The saturated liquid is understood to be a liquid in equilibrium with its own vapor.
ConversionTables: Conversions betweenthemore
common engineering units for liquid densities are given in
Table 6Al.l. The table covers the range of API gravity from
O to 120. All weights given are weights in ail; that is, those
that would be recorded on conventional scales or balances.
The table is to be used for engineering calculations only and
is not meant for material transfer volume computation.
The conversion table is based on constants similar to the
latest valuesof the National Bureauof Standards (1985).
Weight of water in airof 50
percent humidityat 60F and
1 atmosphere:
8.32817
gal lb per
Density of standard air at
60 F and 1 atmosphere:
0.001219 g per ml
Density of brass
at 60 F:
8.392950 g per ml
These values are very close to those used in calculating the
ASTM-IPPetroleumMeasurementTables(reference
6a)
which serve as a standard for the petroleum industry.
For conversions that are out of the range of these tables,
the followingequations may be used.
Specific gravity,60 F/60 F
141.5
API gravity + 131.5
(6-0.2)
(6-0.5)
PureLiquids: Specific gravities ofselected saturated
hydrocarbon liquids are giveninFigures 6A2.1 through
6A2.12. Valuesfor these same hydrocarbons and many other
common pure compounds can be obtained analytically
from
Procedure 6A2.13 (theRackett equation) or Procedure
6A2.15 (the COSTALD method). These two methods have
been found to be equivalent in accuracy. The input parameters for these methods are given in Table 6A2.14.
Specificgravity data for manymorehydrocarbons
at
1 atmosphere pressure are presented in three nomographs.
Low temperature data, -300 F to 100 F, are obtained from
Figure6A2.16.Thevalidtemperatureranges
for the
compounds in this figureare presented in Table 6A2.17.
The
bulk of the data, however, are in the temperature range of O
F to 400 F (the high temperature range) and are given in
Figure6A2.18(paraffinsandolefins)andFigure
6A2.20
(naphthenes and aromatics). The grid coordinates and the
temperature ranges for these hydrocarbon nomographs are
given in Tables 6A2.19 and6A2.21. Extrapolations beyond
these temperature ranges shouldnot be made.
The liquid densities of compressedpurehydrocarbons
may be estimated from the Lu chart, Figure 6A2.22, if one
density value and the critical temperature and pressure are
known. Procedure 6A2.23 provides ananalytical method of
estimating the density of compressedpure liquids. This
method canalso be used for nonhydrocarbons.
Mixtures: The densities of defined liquid mixtures at
their bubble point can be predicted by either Procedure
6A3.1 (the Rackett equation) or Procedure
6A3.2 (the
COSTALD method).Thesetwomethodshave
been
found to be equivalent in accuracy. Procedure6A3.1
requires the critical temperatures, the critical pressures,
1992
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(6-0.4)
= 42 (weight in air, in pounds per
U.S.
The conversion tables in this chapter,as well as the conversion factors in Chapter 1, are useful in interchanging the
various densityunits.
-
(6-0.3)
Weight in air, in pounds
per cubic foot at 60 F
Specific gravity,t FI60 F
- density of substance at t F
179'8874
- 0.0101578
API gravity + 131.5
6- 1
Not for Resale
A P I TDB
CHAPTERlrb
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M 0732290 O536574 285 M
API TECHNICAL DATA BOOK
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and Zu values for all components. Procedure 6A3.2
requires the critical temperatures and two characterization parameters, V* and wSRK, for all components. For
many compounds these input parameters can be obtained from Chapter 1 and Table 6A2.14. Alternate
means of estimating the parameters aresuggested in the
procedures. Both methods can be used for systems containing hydrocarbons and nonhydrocarbons.
For compressed liquid hydrocarbon mixtures, densities can be calculated using the Lu chart given in Procedure 6A3.3 or the alternate computer method (TaitCOSTALD) given in Procedure 6A3.4. The Lu chart
method requires the critical temperatures and critical
pressures of thecomponents and aknown density of the
mixture. A reasonable estimate of this last value can be
obtained by dividing the average molecular weight by
the corresponding average molar volume of the mixture; this assumes the mixture to be an ideal solution,
which is essentially true for members of a homologous
series. It is also a reasonable approximation for mix-
tures of hydrocarbons of different types, provided no
component is close to its critical point. The computer
procedure
requires
the
critical temperatures and
COSTALDparameters
for thecomponents.
It is
recommended for mixtures that do not contain polar
components.
The densities of liquid petroleum fractions at their
saturation pressures or at pressure not far above ambient can be found from the nomograph in Figure 6A3.5
if two of three characterizing parameters (Watson K ,
mean average boiling point, and API gravity at 60 F)
are known. Alternatively, the analytical method given
in Procedure 6A3.6 may be used. To obtain the density
of liquid petroleum fractions at high pressures, either
Procedure 6A3.7, which incorporates Figures 6A3.8
and 6A3.9, or Procedure 6A3.10, which is an analytical
method, is recommended.
For bothpure liquids and mixtures, Figure 6-0.1
should be helpful in selecting the proper procedure for
any particular case.
Density at 1 Atmosphere
Figure 6A2.16 or
Figure 6A2.18 or
Figure 6A2.20
h SaturatedDensity
Figures 6A2.1-6A2.12 or
Procedure 6A2.13 or
Yes
No
Procedure 6A2.15
Compressed Density
Figure 6A2.22 or
Figure 6A2.23
Bubble Point Density
Procedure 6A3.1 or
Procedure 6A2.2
Compressed Density
Procedure 6A3.3 or
Procedure 6A3.4
Petroleum Fractions
at Low Pressures
Figure 6A3.5 or
Procedure 6A3.6
Petroleum Fractions
at High Pressures
Procedure 6A3.7 or
Procedure 6A3.1O
Figure 6-0.1-Liquid
Density Calculation Procedures
1984
6-2
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API TECHNICAL DATA BOOK
n
VE= v, - cx,v,
(6-0.6)
1=1
Where:
VE = excess molar volume, cubic feet per poundmole.
V,,, = actual molar volume of the mixture at given T
and P , cubic feet per pound-mole.
xi = mole fraction of component i.
V ,= molar volume of component i at given T and p ,
cubic feet per pound-mole.
n = number of components.
This excess volume may be negative or positive depending on the components and the temperature and
pressure. Apparently no simple relation exists between
volume changes and chemical or physical properties.
When aromatic hydrocarbons are mixedwith nonaromatics or with petroleum fractions, expansion is
commonly observed; but in some instances, contraction
takes place. The expansion is greater when naphthenic
hydrocarbons are mixed with aromatics than when aromatics are mixed with paraffins. In petroleum fractions
and paraffin-paraffin systems, a contraction is generally
observed, which is greatest for mixtures of components
differing widely in molecular weight.
Excess volume usually increases with increasing temperature and decreases with increasing pressure. The
maximum value of excess volume at any given temperature does not occur at 50 mole percent concentration, but is shifted toward the component of lowest
molecular weight.
Numerous articles have appeared in the literature
concerning excess volume. At this time, however, none
of the theory involving excessvolume is sufficientlyadvanced for inclusion in this chapter. The major problems appear to be that: (1) many of the correlations
cannot predict both expansion and contraction;(2) very
few consider the effect of pressure; (3) the correlation
usually has been developed for one particular type of
mixture only: paraffin-paraffin, paraffin-aromatic, and
the like; and (4) some correlations that may be accept-
able contain parameters that are very difficult to estimate. Nevertheless, as an aid to the user in estimating
excess volume, Table 6-0.2 and Figure 6A3.11 have
been included.
Gas Systems
Gas densities are conveniently correlated using the
following modification of the perfect gas law:
1
P
P=V=xT
Where:
p = density, in pound-moles per cubic foot.
V = gas volume, in cubic feet per pound-mole.
p = pressure, in pounds per square inch absolute.
z = compressibility factor.
R = gas constant = 10.731 (cubic feet)(pounds per
square inch absolute) per (pound-mole)(degree
Rankine).
T = temperature, in degrees Rankine.
The compressibility factor, z , varies with temperature, pressure, and the nature of the substance. It
is usuallycorrelated within the framework of the simple
or extended theorem of corresponding states. In the
extended form,this theorem requires that any two substances having an identical value of a third parameter
and in identical conditions of reduced temperature and
pressure willhave the same compressibility factor.
Therefore, the compressibility factor behavior of all
gases that conform to the extended theorem can be
generalized as a function of the third parameter and
reduced temperature and pressure.
Pure Gases: Procedure 6B1.1 is presented for estimating the compressibility factors of pure hydrocarbons, and it may also be used for other nonpolar
gases. The procedure is based on the three-parameter
corresponding states correlation of Lee and Kesler (4b),
with the acentric factor, o,as the third parameter. The
Lee-Kesler correlation is a refined version of the Pitzer
corresponding states method (7b), and has been used in
Chapter 7 for a numberof thermal properties.All these
methods are internally consistent.
The compressibility factor tables for Procedure 6B1.1
are given as Tables 6B1.2 and 6B1.3. These tables have
been generated from the analytical equations of Lee
and Kesler. Double interpolations in reduced temperature and pressure are required for their use. Somewhat less reliable but more rapid predictions can be
made from theplotted forms of the tables, Figures
6B1.4 through 6B1.7.
The alternate computer method, given as Procedure
6B1.8, uses the Lee-Kesler analytical equations directly. Since the desk method is based on tables gener-
6-3
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(6-0.7)
Not for Resale
--`,,-`-`,,`,,`,`,,`---
Excess Volume of Mixing: Some of the procedures
presented in this chapter, and in other chapters,assume
that if a number of components are mixed, the resultant
density of the mixture is a simple volumetric average of
the components. In the ideal case this is correct, and for
components of quite similar molecular weights and
structures, this average is acceptable. As the molecular
weights of the components become increasingly different, however, the volume of the resultant mixture varies
somewhat from the volumetric average. This can be
represented by the concept of excess molar volume,
which is stated as follows:
A P I TDB CHAPTERlkb
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API TECHNICAL DATA BOOK
TABLE 6-0.2
EXCESS VOLUMES FOR HYDROCARBON SYSTEMS
Temperature
(F)
Description
of Mixing
Ethane-propane
n -Pentane-n -decane
n -Pentanen -hexadecane
n -Hexane-n -decane
n -Hexane-n -dodecane
80
68
68
68
59 to 95
Shrinkage
Shrinkage
Shrinkage
Shrinkage
Shrinkage
142a
81a
31a.81a
81a
31a,46a
n -Hexane+ -tetradecane
n -Hexane-n -hexadecane
n-Hexane-n-tetracosane
n -Heptane-n -dodecane
n -Heptane-n -hexadecane
77
59 to 124
124
59 to 95
68 to 104
Shrinkage
Shrinkage
Shrinkage
Shrinkage
Shrinkage
57a
31a,46a,57a,58a,81a
58a
46a
31a,81a
n -Heptane-n -tetracosane
n-Heptane-n-hexatricontane
n -0ctane-n -hexadecane
n -0ctane-n -dotricontane
n-Octane-n-hexatricontane
169
169
68 to 223
205 to 223
205 to 223
Shrinkage
Shrinkage
Shrinkage
Shrinkage
Shrinkage
58a
58a
31a,58a,81a
58a
58a
n-Nonane-n-dexadecane
n -Nonane-n -tetracosane
n -Nonane-n -dotricontane
n -Nonane-n -hexatricontane
n -Nonane-n -dohexacontane
259
124 to 259
205
205 to 259
259
Shrinkage
Shrinkage
Shrinkage
Shrinkage
Shrinkage
58a
58a
58a
58a
58a
n -Decane-n -dodecane
n-Decane-n-tetradecane
n-Decane-n -hexadecane
n -Dodecane-n -tetradecane
n -Dodecane+ -hexadecane
n -Tetradecane-n -hexadecane
77 to 95
77 to 113
68 to 113
77 to 95
77 to 113
77
Shrinkage
Shrinkage
Shrinkage
Shrinkage
Shrinkage
Ideal
'
54a
54a
31a,54a,81a
54a
54a
57a
68 to
68 to
68 to
68 to
68 to
Shrinkage
Shrinkage
Shrinkage
Shrinkage
Shrinkage
82a
82a
82a
82a
82a
System
Reference
Paraffin-Paraffin
NaphtheneNaphthene
Cyclohexane-dicyclohexyl
Cyclohexane-dicyclohexylmethane
Cyclohexane-1,2-dicyclohexylethane
Cyclohexane-l,3-dicyclohexylpropane
Cyclohexane-t-butylcyclohexane
104
104
104
104
104
Aromatic-Aromatic
Benzene-o-xylene
Benzene-m -xylene
Benzene-p -xylene
Benzene-ethylbenzene
Benzene-naphthalene
77 to 86
77 to 86
77
68
175
Expansion
Expansion
Expansion
Expansion
Variable"
110a,129a
110a,129a
129a
88a
17a
Benzene-biphenyl
Benzene-diphenylmethane
Benzene-diphenylethane
Benzene-diphenylacetylene
Benzene-diphenyloctane
158
77 to 104
140
140
77
Shrinkage
Shrinkage
Shrinkage
Shrinkage
Ideal
84a
34a,104a
84a
84a
84a
68
68
68
68
68
Ideal
Shrinkage
Shrinkage
Ideal
Shrinkage
88a
88a
88a
88a
88a
Toluene-ethylbenzene
Ethylbenzene-ethenylbenzene
Ethylbenzene-o -xylene
Ethylbenzene-p -xylene
Ethylbenzene-n -propylbenzene
6-4
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API TDB CHAPTER*b
**
m 0732290
0536577 T 9 4
API TECHNICAL DATA BOOK
TABLE 6-0.2 (Continued)
Temperature
(F)
System
Description
of Mixing
Reference
Aromatic-Aromatic
68
68
68
68
Ideal
Expansion
Expansion
Shrinkage
88a
88a
88a
88a
59 to 176
77
59
82
77
Shrinkage
Expansion
Expansion
Ideal
Expansion
24a
114a
124a
106a
116a
77
77
77
77
Variableb
Shrinkage
Shrinkage
Ideal
8a
64a
64a
64a
n-Butane-benzene
n-Hexane-benzene
n-Heptane-benzene
2,2,4-Trimethylpentane-benzene
2,2,4-Trimethylpentane-toluene
59 to 176
77 to 104
59
68 to 167
82
Shrinkage
Expansion
Expansion
Expansion
Expansion
24a
34a,57a,114a
124a
152a
106a
n -Dodecane-benzene
n-Dodecane-n-hexylbenzene
n -Dodecane-phenylcyclohexane
n -Hexadecane-benzene
77 to 104
77
77
77
Expansion
Expansion
Ideal
Expansion
34a
64a
64a
57a
Cyclopentane-benzene
Cyclopentane-toluene
Cyclohexane-benzene
Cyclohexane-toluene
17
77
59 to 104
77
Expansion
Expansion
Expansion
Expansion
149a
149a
104a,114a,124a,149a
149a
Cycloheptane-benzene
Cycloheptane-toluene
Cyclooctane-benzene
Cyclooctane-toluene
77
77
77
77
Expansion
Expansion
Expansion
Expansion
149a
149a
149a
149a
Benzene-petroleum ether
Benzene-vaseline oil
Petroleum ether-kerosine
Petroleum ether-vaseline oil
68
68
68
68
Expansion
Expansion
Shrinkage
Shrinkage
60a
60a
60a
60a
Gasoline-kerosine
Benzol-gasoline
Light naphtha-heavy naphtha
68
77
77
Shrinkage
Expansion
Shrinkage
60a
26a
137a
Ethylbenzene-isopropylbenzene
Ethylbenzene-l-methyl-4-isopropylbenzene
Ethylbenzene-r-amylbenzene
Ethylbenzene-1,2,3,4-tetrahydronaphthalene
Paraffin-Naphthene
n -Butane+yclohexane
n -Hexane+yclohexane
n-Heptanecyclohexane
2,4-Dimethylpentane-cyclohexane
n-Octane-methylcyclohexane
2,2,4-Trimethylpentane-cyclohexane
n -Dodecane-bicyclohexyl
n -Dodecane-n -hexylcyclohexane
n -Dodecane-n -heptylcyclopentane
Paraffin-Aromatic
Naphthene-Aromatic
Petroleum Fractions
~~
“Expansion at high benzene concentration and shrinkage at low benzene concentration.
Expansion at low cyclohexane concentration and expansion at high cyclohexane concentration.
1904
6-5
--`,,-`-`,,`,,`,`,,`---
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
--`,,-`-`,,`,,`,`,,`---
API TECHNICAL DATA BOOK
ated by the computer method, the
accuracies of the two
methods should be equivalent, except for small errors
introduced by the linear interpolations.
The recommended correlations have been found to
be the best available methods for general application
and internal consistency. However, equations may be
found in the literature that give superior accuracy for
specific compounds andor regions.
Gas Mixtures: For densities of gas mixtures, the
same desk method and the same computer equations
are recommended as for puregases. However, with the
possible exception of a small region in the immediate
vicinity of the critical point,thetrue
critical point
should no longer be used to calculate the reduced temperature and pressure. As outlined in Procedure 6B2.1,
the pseudocritical point is to be used to estimate thegas
density of hydrocarbon mixtures. The pseudocritical
pressure and temperature aredefined as the molar average of the critical properties of the pure components.
Methodsfor estimating the pseudocritical temperatures and pressures for mixtures of defined and undefined composition and blends of the two are given in
Chapter 4.
Many equations of varying degrees of complexity
have been proposedas substitutes forKay’s molar averages. Several of these result in improved accuracy, but
the slight improvement does not justify the increased
labor involved when calculating gas densities atthe
desk. Nevertheless, several alternates are noted in the
Special Comments for Procedure 6B2.1. The point
determined by these equations is not termed apseudocritical point, inasmuch as this book reserves that
designation for the point defined by the simple molar
averaging technique. Instead, the terms mixture correspondence temperature and mixture correspondence
pressure are used.
For computer calculations, the complexity of the
equations for the mixture correspondence point is immaterial. Therefore, as described in Procedure 6B2.2,
the somewhat more complicated “mixing rules” of Lee
and Kesler (4b) have been selected for computer calculations of the mixture correspondence points. The accuracy thus obtained is generally superior to that using
Kay’s pseudocritical point.
For both the primary desk method (Procedure6B2.1)
and the alternate computermethod (Procedure 6B2.2),
an approachis outlined for estimating the gas density of
mixtures of undefined composition. These approaches
are simple extensions of those for defined mixtures, but
no data are available to test their accuracy.
Data are notavailable to determine the reliability of
the pseudocritical or mixture correspondence approaches for mixtures exhibiting unusual (non-Type-I)
critical loci, but the accuracy of both computer and desk
methods is probably worse than quoted. Fortunately,
most systems of interest are Type I, but unusual behavior can occur even for hydrocarbon systems. The
various critical loci are described in the Introduction to
Chapter 4.
The pseudocritical temperature is lowerthan the true
critical temperature in many common systems; thus,
both liquid and vapor phases canexist at pseudoreduced temperaturesgreaterthan
unity. Under all
conditions, but particularly in this region, it isnecessary
to know the existing phase conditions. If doubt exists,
obtain the vapor-liquid equilibrium conditions for the
operating temperature and pressure from Chapter 8 to
determine whether thedesired mixture is in the vapor,
liquid, or vapor-liquid equilibrium state. In the last
case, thetwo phases must be treated separately, and the
phase compositions and amounts must first be calculated from Chapter 8.
6-6
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
1984
Not for Resale
API TDB CHAPTER*b
X*
m
0732290 0536579 8 6 7
m
6A1.1
TABLE 6A1.1
DENSITY CONVERSION
~""""""""""""""--"-""-""""""""""""""""_
APE
GRAVITY
AT 60F
SPECIFIC
WEIGHT I N A I R
G R A V I T Y LB/GAL LB/CU FT LB/BBL
AT 60F AT 60F
6 0 F / 6 0 F AT 60F
""""""""""""""""-"""""""-"~""""""""""""""""""""
API
GRAVITY
AT 60F
SPECIFIC
GRAVITY
60F/60F
WEIGHT IN A I R
LB/GAL LB/CU FT LB/BBL
AT 60F AT 60F AT 60F
"
"
"
"
~
"
"
"
"
~
"
~
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
0.0
0.1
0.2
O. 3
0.4
l . 0760
1.0752
1.0744
1 0736
1.0728
8.962
8.955
80949
8.942
8.935
67.05
67.00
66.95
66.89
66.84
376.4
376.1
375.8
375.6
375.3
5.0
5.1
5.2
5.3
5.4
1.0366
1.0359
1.0351
1.0344
1.O336
8.634
8.627
8.621
8.615
8.608
64 -59
64 -54
6 4 49
66-45
64.40
362.6
362.3
362.1
361.8
361.6
0.5
0.6
1.0720
1.0712
1.0703
l . 0695
1.0687
8.928
8.922
375.0
374.7
374.4
374.1
373.9
5 05
8.908
8.901
66.79
66.74
66.69
66. h4
66.59
5.6
5 07
5.8
5.9
1.0328
1.0321
1.0313
1.0306
1 0298
8.602
8.596
8.590
8,583
8.577
64.35
64.31
64-26
64.21
64.17
361.3
361.0
360.8
360.5
360. 2
1.3
1.4
1.0679
1.0671
l . 0663
1.0655
1.0647
8.995
8.888
8.881
8. R74
8.868
66.54
66.49
66.44
66.33
66.34
373.6
373.3
373.0
372.7
372.4
6.0
6.1
6.2
6.3
6.4
1.0291
1.0283
1.0276
1.0269
1.0261
8.571
8.565
8.558
8.552
8.546
64.12
64.07
64.03
63.98
63.93
360. O
359.7
359.5
359.2
358.9
1.5
1.6
1.7
1.8
1.9
1.0639
1.0631
1.0623
1.0615
1.0607
8.R6l
8.854
8.848
8. R41
66.29
66.24
66.19
66.14
66.09
372.2
371.9
371.6
371.3
371.1
6.5
6.6
6.7
6.8
6.9
1.0254
1.0246
1.0239
1.0231
1.0224
8.540
8.533
8.527
8.521
8.515
63 -89
63 84
63.79
63.75
63.70
358.7
358.4
358. 1
2.0
2.1
2.2
2.3
2.4
1 0599
1.0591
1.0583
1.0575
1.0568
8.828
8. R 2 1
8,815
8.808
8.801
66.04
65.99
65.94
65.89
65.84
370. B
370.5
370.2
369.9
369.7
7.0
7.1
7.2
7.3
7.4
1.0217
1.0209
1.0202
L. 0195
1.0187
8.509
8.503
8.497
8.490
8.484
63.65
63 -61
63.56
63.52
6 3 047
357.4
357.1
356.9
356.6
356.3
8.795
8.788
8,782
8.775
8.769
65.80
65.75
65.70
65.65
65.60
369.4
369.1
368.9
368.6
368.3
7.5
7.6
7.7
7.8
7.9
1.0180
1.0173
1.0165
1.0158
1.0151
8.0
8.1
8.2
8.3
8.4
0.7
0.8
0.9
1.0
1.1
1.2
2.5
2.6
2.7
2.8
2.9
1.0560
1.0552
1 0544
1.0536
1.0528
8.915
8.835
.
357.9
357.6
8.478
63 -43
8 472
63.38
8 466
8.460
8.454
63.33
63.29
63.24
356.1
355.8
355.6
355.3
355.1
1.0143
1.0136
1.0129
1 .o122
1.0114
8.448
8.442
8.436
8.430
8.424
6 3 -20
63.15
63.11
63.06
63.02
354.8
354 6
354.3
354. O
353.8
62.97
62.88
62.84
62.79
353 5
353.3
353. O
352 8
352.5
3.0
3.1
3.2
3.3
3.4
l . 0520
1.0513
1.0505
1.0697
l . 0489
8.762
8.756
8,749
8.743
a. 736
65.55
65.50
65.45
55.36
368.0
367.7
367.5
367.2
366.9
3.5
3.6
3.7
3.9
1.9481
1.0474
l . 96h6
1.0458
1.0651
8.730
8.723
8.717
8.710
8.704
65.31
65.26
65.21
65.16
65.11
366.6
366.4
366.1
365.8
365.6
8.5
8 -6
8.7
8.8
8.9
1.0107
1.0100
1.0093
1.0086
1.0078
8.418
8.412
8.406
8.400
8.394
4.0
4.1
4.2
4.3
4.4
1.0443
1.0435
1 O427
l . 0420
1.0412
8.697
8.691
8.685
8.678
8.672
65.07
65.02
64.97
64.92
64.87
365.3
365.0
364.8
364.5
364.2
9.0
9.1
9.2
1.0071
1 .O064
1.0057
1 0050
1.O043
8.388
8.382
8.376
8.370
8.364
62.75
62.70
62.66
62.61
62 -57
352 3
352.0
351.8
351.5
351.3
364.0
363.7
363.4
36301
362.9
9.5
1.0035
1 .o028
1.0021
1.0014
1o0007
8.358
8.352
8 346
8 -340
8.334
62.52
62 -48
62 -44
62.39
62-35
351.0
350 8
350.5
350.3
350.0
3.8
65.40
8.665
1. 0404
64.83
L. 0397
64.78
8.659
l . 0389
8.653
64.73
4.1
8.646
4.8
1.0382
64.68
1.0374
64.64
8.640
4.9
""""-"""""""="""""""""""""""""""""""""""""""""
NOTE
GAL = U. S. GALLON,BBL
4.5
4.6
""""""-"""""
-1984
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
9.3
9.4
9.6
9.7
9.8
9.9
.
0
62093
.
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
= 4 2 U. S- GALLONS.
6-7
--`,,-`-`,,`,,`,`,,`---
Not for Resale
A P I TDB CHAPTERS6
0732290 0536580 5 8 9
SS
6A1.1
TABLE 6A1.1 (Continued)
-
-"""_""
S
WPEEI G
C IHA
FTP
I CI
GRAVITY
AT 60F
GRAVITY
60F/60F
"_
IN A I R
LB/GAL LB/CU F T L E / B B L
A l 60F
AT 60F
"
"
"
"
"
"
"
"
"
~
"
"
"
"
"
API
GRAVITY
AT 60F
AT 60F
""-
SPECIFIC
WEIGHT I N A I R
G R A V I T Y L W G A L LB/CU F 1 L B / 8 8 L
6 0 F / 6 0 F AT 60F A l 60F
AT 6 0 f
"
"
"
"
"
"
~
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
~
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
~
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
~
"
"
"
"
"
l . 0000
9993
0.9986
0.9979
0.9972
8.328
8.322
8.316
9.311
8.335
62.30
62.26
62 22
62. 1 7
62.13
349.8
349 5
349.3
349. O
348.8
.
15.0
15.1
15.2
15.3
15.4
0.9659
0 a9652
0.9646
O .9639
0.9632
8.044
8.038
8.033
8.027
8.022
60.09
60.05
60.01
337.8
337.6
337.4
337.1
336.9
10.5
10.6
10.7
10.8
10.9
0.9965
0.9958
0.9951
0.9944
O. 9 9 3 7
8-299
8.293
8.287
8. 2 8 1
8.276
62.08
62.04
62.00
61 -95
61.91
348.6
348.3
348.1
3474 8
347.6
15.5
15.6
15.7
15.8
15.9
0,9626
0.9619
0.9613
0.9606
0.9600
8.016
8.011
8.005
8.000
7.994
59.97
59.93
59.89
59.85
59.81
336.7
336.5
336.2
336.0
335.8
11.0
11.1
11.2
11.3
11.4
0.9930
0.9923
O. 9 9 1 6
0.9909
0.9902
8.270
8.164
8.258
8.752
8.247
61.87
61.ß2
61.78
61.74
61.69
347.3
34 7.1
346. 8
346.6
346.4
16 -0
16.1
16.2
16.3
16.4
0.9593
O ,9587
0.9580
0.9574
0.9567
7.989
7,984
7.978
7.973
7.967
59.77
59.73
59.69
59.64
59.60
335.5
335.3
335. L
334.9
334.6
11.5
11.6
11.7
11.8
11.9
c. 9 8 9 5
0.9888
O. 9 8 8 1
O. 9 8 7 4
O. 9868
8.241
8.235
8.229
8.223
8.218
61.65
61.61
61.56
61.52
61.48
346- 1
345.9
345.6
345.4
345.1
16.5
16.6
16.7
16.8
16.9
0.9561
0.9554
O 9548
0.9541
0.9535
7.962
7.957
7.951
7.946
7.941
59.56
59.52
59.48
59.44
59.40
334.4
334.2
334. O
333.7
333.5
12.0
12.1
12.2
12.3
12.4
0.9861
O. 9 8 5 4
O. 9847
0. 9 8 4 0
0.9833
8.212
8.206
8 201
8.195
8.189
61.43
6 1 39
61.35
61.31
61.26
344.9
344.7
344.4
344.2
343.9
17.0
17.1
17.2
17.3
17.4
0.9529
0.9522
O e95 16
0.9509
0.9503
7.935
7.930
7.924
7.919
7.914
59.36
59.32
59.28
59.24
59.20
333.3
333.1
332.8
332.6
332.4
12.5
12.6
12.7
12.8
12.9
0.9826
0.9820
0.9813
0.9806
0.9799
8.183
8.178
8.172
8.166
8.161
61.22
61.18
61.14
61.09
61.05
343.7
343.5
343.2
343. O
342.8
17.5
17.6
17.7
17.8
17.9
0.9497
O -9490
O 9484
O. 9 4 7 8
0.9471
7,908
7.903
7.898
7.893
7.887
59.16
59.12
59.08
59.04
59.01
332.2
331.9
331.7
331.5
331.3
13.0
13.1
13.2
13,. 3
13.4
0.9792
O. 9 7 8 6
o. 9 7 7 9
0.9772
0.9765
8.155
8.149
8.144
8.138
8.133
61.01
60.97
60.92
60-S8
60.84
342.5
342.3
342. O
341.8
341.6
18.0
18.1
18.2
18.3
18.4
0.9465
0.9459
0.9452
0.9446
O -9440
7.882
7.877
7.871
7. 866
7.861
58.97
58.93
58.89
58.85
58.81
331.0
330.8
330.6
330.4
330.2
13.5
13.6
13.7
13.8
13.9
0.9759
0.9752
o. 9 7 4 5
0.9738
0.9732
8.127
8.121
8.116
8.110
8.105
6c?. 8 0
60.76
5 0 -7 1
60.67
60.63
341.3
341.1
340.9
340.6
340.4
18.5
18.6
18.7
18.8
18.9
0.9433
0-9427
0.9421
0.9415
0.9408
7.856
7.850
7.845
7.840
7.835
58.77
58.73
58.69
58.65
58.61
329.9
329.7
329.5
329.3
329.1
14.0
14.1
14.2
14.3
14.4
0.9725
0,9718
0.9712
0.9705
O. 9 6 9 8
8.999
8.093
8.088
8.082
8.077
60.59
60.55
60.51
60.46
60.42
340.2
339.9
339.7
339.5
339.2
19.0
19.1
19 - 2
19.3
19.4
O -9402
0.9396
0.9390
0,9383
0.9377
7.830
7.824
7.819
7.814
7.809
5 8 .S7
5 8 53
58.50
58.46
58.42
328.8
328.6
328.4
328.2
328.0
14.5
14.6
14.7
14.8
14.9
0.9692
0.9685
0.9679
0.9672
O. 9 6 6 5
8.071
8 .O66
8.060
8.055
8.049
60.3P
60.34
60.30
60.26
60.22
339.0
338.8
338.5
338.3
338.1
19- 5
19.6
19.7
19.8
19.9
0.9371
0.9365
0.9358
0.9352
0-9346
7.804
56.38
58.34
58.30
58.26
58.22
327. a
327.5
327.3
327.1
326.9
--`,,-`-`,,`,,`,`,,`---
10.0
10.1
10.2
10.3
10.4
o.
~"""""""""""""""""~"""""""""~"""""""""""""""""""""_"""""""~"""""""
NOTE
-- GAL
= U.
S.
GALLUNI B E L = 4 2 U.
S.
60.13
GALLONS.
1984
6-8
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
7.798
7.793
7.788
7.783
60.17
Not for Resale
A P I TDB CHAPTERrb
J*
m
0732290 0536583 415
m
6A1.1
TABLE 6A1.1 (Continued)
API
SPECIFIC
GRAVITY
GRAVITY
"AT
_"""""""60F
""""""""
60F/60F
API
SPECIFIC
WEIGHT IN AIR
GRAVITY G R A V I T Y LB/GAl LB/CU F 1 l B / B B L
AT 60F
60F/60F
AT 60F AT 60F AT 60F
WEIGHT I N A I R
L8/6AL L 8 / C U F T L8/8BL
AT 60F AT 60F A T 60F
""_
"
"
~
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
20.0
20.1
20.2
20.3
20.4
O. 9340
0.9334
0.9328
0.9321
0.9315
7.778
7.773
7.758
7.762
7.757
58.19
58.15
58.11
56.07
58.03
326.7
326.5
326.2
326.0
325.8
25.0
25.1
25.2
25.3
20.5
20.6
20.7
20. S
20.9
O. 9309
0.9303
0.9297
0.9291
0,9285
7.752
7.747
7.742
7.737
7.732
57.99
57.96
57.92
57.88
57.84
2 1 .o
21.1
21.2
21.3
21.4
0.9279
0.9273
O 9267
0.9260
0.9254
7.727
7.722
7.717
7.712
7.707
21.5
21.6
21.7
21.8
21.9
0.9248
O 9242
0..9236
0.9230
0.9224
22.0
22.1
22.2
22.3
22 04
--`,,-`-`,,`,,`,`,,`---
25.4
0.9042
0.9036
O 9030
0.9024
0.9018
7.529
7,524
7.519
7.515
7.51 O
56.32
56 029
56.25
56 22
56.18
316.2
316.0
315.8
315.6
315.4
325.6
325.4
325.2
325.0
324.7
25.5
25.6
25.7
25.8
25.9
0.9013
0.9007
O 0900 1
O 8996
O . 8990
7.505
7.50 O
7.495
7.491
7.486
56.15
56.11
56.07
56.04
56.00
315.2
315.0
314.8
314.6
314.4
57.80
57.77
57.73
57.69
57.65
324.5
324.3
324.1
323.9
323.7
26.0
260 1
26.2
26.3
26.4
0.8984
O. 8973
0.8967
0.8961
7.481
7.476
7.472
7.467
7 462
55 097
55.93
55 090
55.86
55-82
314.2
314.0
313.8
313.6
313.4
7.701
7.676
7.491
7.685
7.6ß1
57.62
57.58
57.54
57.50
57.46
323.5
323.3
323.0
322.8
322.6
26.5
26.6
26.7
26.8
26.9
0.8956
O . 8950
0.8944
0.8939
0.8933
7.457
7.453
7.448
7.443
7.439
55.79
55.75
55 072
55 068
55.65
313.0
312.8
312.6
312.4
0.9218
0.9212
O . 9206
0.9200
0.9194
7.h76
7.671
7.666
7.561
7.656
57.43
57.39
57.35
57.32
57.28
322.4
322.2
322. O
321.8
321.6
27.0
27.1
27.2
27.3
27.4
0.8927
0.8922
0.8916
0.8911
0,8905
7.434
7.429
7.424
7.420
7.415
55.61
55.58
55.54
55.51
55.47
312.2
312.0
311.8
311.6
311.4
22.5
22.6
22.7
22.8
22.9
Ce9188
O. 9182
0.9176
0.9170
0.9165
7.651
7.646
7.641
7.636
7.63 2
57.24
57.20
57.17
57.13
57.09
321.4
321.2
320.9
320.7
320.5
27.5
27.6
27.7
27.8
27.9
0.8899
0.8894
0.8888
0.8883
0.8877
7.410
7.406
7.401
7.396
7.392
55.44
55.40
55 037
55.33
55.30
311.2
311.0
310.9
310.7
310.5
23.0
23.1
23.2
23..3
23.4
0.9259
0.9153
0.9147
0.9241
0.9135
7.627
7.622
7.617
7.612
7.607
57.05
57.02
56.98
56.94
56.91
320.3
320.1
319.9
319.7
319.5
28 e
0.8871
0.8866
0.8860
0.8855
0.8849
7. 387
7.383
7.378
7.373
7.369
55 -26
28.1
28.2
28.3
28.4
55.19
55 016
55.13
310.3
310.1
309.9
309.7
309.5
23.5
23.6
23.7
23.8
23.9
0.9129
O . 9.1 2 3
0.9117
0.9111
0.9106
7.602
7.597
7.592
7.587
7.582
56.87
56.83
56.8C
56.76
56.72
319.3
319.1
318.9
318.7
318.5
28.5
28.6
28.7
28.8
28.9
0.8844
0.8838
0.8833
0.8827
0.8822
7.364
7.359
7.355
7.350
7,346
55 -09
55 -06
55.02
54.99
54.95
309.3
309.1
308.9
308.7
308.5
24.0
24.1
24.2
24.3
24.4
O. 9100
0.9094
0.9088
0.9082
0.9076
7.577
7.573
7.558
7.563
7.558
56.69
56.65
56.61
56.58
56.54
318.3
318.1
317.8
311.6
317.4
29.0
29. 1
29.2
29.3
2 9 04
0.8816
0.8811
0.8805
0.8800
O 8794
7.34'1
7.337
7,332
7.327
7.323
54 -9
2
54.89
54.85
54.82
54.78
308.3
308.1
307.9
307.8
307.6
24.5
24 -6
24.7
24.8
24.9
O . 9071
0.9065
0.9059
0.9053
0.9047
7.5 53
7.548
7.543
7.539
7.534
56.51
56.4 7
56.43
56.40
56.36
317.2
317.0
316.8
316.6
316.4
29.5
29.6
29.7
29.8
29.9
0.8789
0.8783
O -8778
0.8772
O 8767
7.318
7.314
7.309
7.305
7.300
54.75
54.71
54.68
54.65
54.61
307.4
307.2
307.0
306.8
306.6
""""_
"""-""
0
0-8978
55 23
313.2
"
"
"
"
~
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
~
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
~
"
~
"
"
~
"
"
"
"
"
"
"
"
"
"
"
"
"
"
~
NOTE
--
GAL = U.
3.
GALLON.
B8L = 42 U.
S.
GALLONS.
6-9
1984
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
A P I TDBCHAPTERab
S*
m
0732290 0536582 351
m
6A1.1
TABLE 6A1.1 (Continued)
API
GRAVITY
AT 60F
SPECIFIC
WEIGHT I U 41R
GRAVITY
L8/GAL LB/CU F T L B / B B L
6 0 F / 5 0 F A T 60F AT 63F
A T 60F
AP I
GRAVITY
A T 60F
SW
PEC
I GI FHITC
GRAVITY
60F/60F
IN AIR
L B / G A L CB/CU FT LB/BBL
AT 60F A T 60F A T 60F
"
"
"
"
"
~
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
~
"
"
"
"
"
"
~
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
~
30.0
30.1
30.2
30.3
30.4
30.5
30.6
30.7
30.8
30.9
0.87b2
7.295
7.791
7.387
7.?R2
7.27P
54.58
54.54
54.51
54.40
54.44
306.4
306.2
306.0
305.8
305.7
35.0
35.1
35.2
35.3
35.4
O. 8735
O. 8 7 2 9
7.273
0.8724
0.8718
0.8713
7.264
7,259
7.755
54.41
54.38
54.34
54.31
54.?9
305.5
305.3
305.1
304.9
304.7
0.8708
54.24
54.21
54.18
54.14
54.11
O. 8756
0.8751
O . 8745
0 . 8740
7.?4?
0.8498
0.8478
7.076
7.072
7.068
7.063
7.059
52 -94
52.91
5 2 87
52.84
52.81
297.2
297. O
296.8
296.7
296 5
35.5
35.6
35.7
35.8
35.9
O . 8473
O. 8468
0.8463
O. 8458
O .8453
7.055
7.051
7.047
7.042
7,038
52.78
52.75
52.72
52.68
52.65
296.3
296.1
296.0
295.8
295.6
304.5
304.3
304.2
304.0
303. a
36.0
36.1
36.2
36. 3
36.4
O. 8448
O. 8 4 4 3
0,8438
0.8433
0,8428
7.034
7.030
7.025
7.021
7.017
52.62
52.59
52.56
52 53
52-50
295.4
295.2
295.1
294.9
294.7
O. 8 4 9 3
0.8488
O. 8483
0.8697
0.8692
0.8686
7.251
7.346
7.242
7.237
7.733
31.5
31.6
31.7
31.8
31.9
0. 8681
0.8676
O. 8 6 7 0
O. 8665
8560
7.228
7.724
7.719
7.215
7.711
54.08
54. c 4
54. c1
53.98
53.94
303.6
303.4
303.2
303.0
302.8
36.5
36.5
36.7
36.8
36.9
0.8423
O. 8 4 1 8
0.8413
0.8408
0.8403
7.013
7.009
7.005
7.000
6.996
52 046
5 2 043
52 040
52 e37
52.34
294. 5
294.4
294.2
294. O
293.8
32.0
32.1
32.2
32.3
32.4
O. 8 6 5 4
O 8649
O. 8 6 4 4
0.8639
O. 8633
7.206
7.202
7.197
7.193
7.199
53.91
53.88
53.84
53.81
53.78
302.7
302.5
302.3
302.1
301.9
37.0
37.1
37.2
37.3
37.4
0.8398
O 8393
0.8388
0.8383
0.8378
6.992
6.98 8
6.984
6.980
6,976
52-31
52.28
52.25
52.22
52.18
293.7
293. 5
293 3
293.1
293.0
32.5
32 e 6
32.7
32.8
32.9
O. 8628
0.8623
0.8618
0.8612
0.8607
7.184
7 . I ao
7.175
7.171
7.167
53.75
53.71
53.68
53.65
53.61
301.7
301.6
301.4
301.2
301.0
37.5
37.6
37.7
37.8
37 .9
0.8373
0.8368
O. 8 3 6 3
0.8358
0.8353
6.971
6.967
6.963
6.959
6.955
52.15
52.12
52 -09
52.06
52 -03
292. a
292.6
292.5
292 03
292 1
C.8602
0.8586
0.8581
7.162
7.158
7.154
7.149
7.145
53.58
53.55
53.52
53.48
53.45
300.8
300.6
300.5
300.3
300.1
38.0
38.1
38.2
38.3
38.4
0.8348
0.8343
0.8338
O 8333
0.8328
6.951
6.947
6.943
6.938
6.934
52.00
5 1 e97
51.94
31-91
51.88
291.9
291.8
291.6
291.4
291.2
33.5
33.6
33.7
33.8
33.9
O. 8576
0.8571
O 8565
O. 8 5 6 0
0. 8555
7.141
7.135
7.132
7.179
7.123
53.42
53.39
53.35
53.32
53.29
299.9
299.7
799.5
299.4
299.2
38.5
38.6
38.7
38.8
38.9
0.8324
0.8319
O. 8 3 1 4
018309
0.8304
6,930
6.926
6.922
6.91 8
6.914
51.85
5 1 .a2
5 1 -78
51 075
5 1 -72
291.1
290.9
290.7
290.6
290.4
34.0
34.1
34.1.
34.3
34.4
O. 8 5 5 0
O . R545
0.8540
0.8534
O. 8 5 2 9
7.119
7.115
7.110
7.136
7.192
53.26
53.23
53.19
53.16
53.13
299.0
298.8
298.6
298.5
298.3
3 9 .O
39.1
39.2
39.3
39.4
O 8299
0.8294
0.8289
0.8285
0.8280
6.910
6.906
6.902
6.898
6.894
51 e69
5 1 -66
51.63
51.60
51.57
290.2
290. o
289.9
289.7
289.5
34.5
34.6
34.7
34.8
34.9
0.8524
0.8519
0.8514
O. 8509
O. 8 5 0 4
7.098
7.Q93
7.09s
7.0R5
7.080
53. L O
53.07
53.03
53.00
52.97
298.1
297.9
297 7
297.6
297.4
39.5
39.6
39.7
39.8
39.9
O 8275
6.890
6.886
6.882
6.878
6.874
51.54
51.51
51.48
51 -45
51.42
289.4
289, 2
289.0
288.9
288.7
--`,,-`-`,,`,,`,`,,`---
3 1 .O
31.1
31.2
31.3
31 - 4
33.0
33.1
33.2
33.3
33.4
O 8702
I).
O. 8597
O. 8 5 9 1
0.8270
0.8265
0.8260
0,8256
"
"
"
"
"
"
"
"
"
"
"
"
~
"
"
"
"
~
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
~
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
~
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
NOTE
--
GAL = U.
S.
GALLON, BEL = 4 2 U.
S. GALLONS.
6-1O
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
1984
Not for Resale
API TDB CHAPTERjb
0732290 053b583 2 9 8 M
*X
6A7.7
TABLE 6A1.1 (Continued)
--`,,-`-`,,`,,`,`,,`---
40.0
49.1
40.2
40.3
40.4
O. 8 2 5 1
0.8246
0.8241
O. 8 2 3 6
O 8232
6.970
6.865
6.962
6.858
6.854
51.39
51.36
51.33
51.30
51.27
288.5
288 e 4
288.2
288.0
287.9
45.0
45.1
45.2
45.3
45.4
0.8017
0.8012
0.8008
0.8003
0.7999
6.675
6.671
6.667
6.663
6.660
49 093
49.91
49.88
49.85
49.82
280.3
280.2
280. O
279.9
279.7
40.5
40.6
40.7
40.8
40.9
0.8227
o. 8222
0.8217
0.8212
O. 8298
6.850
6 . R45
6.842
6.839
6.334
51.24
51.21
51.15
51.15
51.12
287.7
287.5
287.4
287.2
287.0
45.5
45.6
45.7
45.8
45.9
0.7994
O .7990
O. I S 8 5
O -7981
O 7976
6.656
6.652
6.648
6.645
6.641
49.79
49 7 6
49.74
49.71
49.68
279. 5
279.4
279.2
279.1
278.9
41.0
41.1
41.2
41 e 3
41 - 4
0.8203
O . 8198
0.8193
0.8189
0.8184
6.830
51.09
51.06
51.03
51.00
50.98
286.9
286.7
286.5
286.4
286.2
46.0
46.1
46.2
46.3
4 6 .4
0.7972
O e7967
0.7963
0.7958
O. 7954
6.637
6.633
6.630
6.626
6.622
49.65
49.62
49.60
49.57
49.54
278.8
278.6
278.4
278.3
278.1
41.5
41.6
41.7
41.8
41.9
O. 8 1 7 9
O. 8 1 7 4
O. 8 1 7 0
O. 8 1 6 5
0.8160
6 . R02
6.798
6.794
50.95
50.92
50.89
50.86
50.83
286.0
285.9
285.7
285.5
285.4
46.5
46.6
46.7
46.8
46.9
0.7949
O .7945
0.7941
O. 7 9 3 6
O 7932
6.618
6.615
6.61 1
6.607
6.604
49.51
49.48
49.46
49.43
49 .&O
278.0
277.8
277.7
277.5
277.3
42. O
42.1
42.2
42.3
42 - 4
0.8156
O. 8 1 5 1
0.8146
0.8142
0.8137
6.790
6.786
6.782
6.779
6.775
50.80
50.77
50.74
50.71
50.68
285.2
285.0
284.9
284.7
284.5
47. O
47.1
47.2
47.3
47.4
O. 7 9 2 7
0.7923
0.7918
0.7914
0.7909
6.600
6.596
6.592
6.589
6.585
49.37
49.35
49.32
49.29
49.26
277.2
277.0
276.9
276. 7
276.6
42.5
42.6
42.7
42.8
42 .9
O. 8132
6.771
6.767
6.763
6.759
6.755
50.65
50.62
50.59
50.57
50.54
284.4
284.2
284.0
283.9
283.7
47.5
47.6
47.7
47.8
47.9
O -7905
0.7901
0.7896
0.7892
0.7887
6.581
6.578
6.574
6.570
6.567
49.24
49.21
49.18
49.15
49.13
276.4
276.3
276.1
276. O
275.8
6.751
6.747
6.744
6.740
6.736
50.51
50.48
50.45
50.42
50.39
283.6
283.4
283.2
283.1
282.9
48. O
48.1
48.2
48.3
48.4
0.7883
0.7879
0.7874
0.7870
O . 7865
6.563
6.559
6.556
6.552
6.548
49.10
49 -07
4 9 .O4
49.02
48.99
275.6
275.5
275.3
275.2
275.0
50.36
50.33
50 30
50.28
50.25
282.7
282.6
282.4
282.3
282.1
48.5
48.6
48.7
48.8
48.9
0.7861
O .7852
0.7848
0.7844
6.545
6.541
6.537
6 534
6.530
48.96
48.93
48.91
48.88
48.85
274.9
274.7
274.6
274.4
274.3
4'3.0
43.1
43.2
43.3
43.4
0.9128
0.8123
0.8118
0.9114
0.8109
O. 8 1 0 4
0.8100
O. 8 0 9 5
O. 8 0 9 0
0.8086
6. 826
6.922
6.ßla
6.814
6.RL0
6.806
.
43.5
43.6
43.7
43.8
43.9
O. 8076
O . 8072
O. 8067
6.732
6.728
6.724
6.720
6.717
44. O
44.1
44.2
44.3
44.4
9.8063
O. 8058
O. 8 9 5 4
O. 8049
O . R044
6.713
6.709
6.705
6.701
6.698
50.22
50.19
5 0 . 16
50.13
50.10
281.9
281.8
281.6
281.5
281.3
49.0
69.1
49.2
49.3
49.4
0.7839
0.7835
O .7831
0.7826
0.7822
6.527
6.523
6.519
6.516
6.512
48.83
48.80
48.77
48.74
48.72
274.1
274.0
273.8
273.7
273.5
44.5
44.6
44.7
44. R
44.9
O. 8940
0.8035
0.8031
O. 8026
0.0022
6.694
6.690
6.686
6.682
6.678
50.08
50.05
50. 02
49.99
49.96
281.1
281.0
280.8
280.7
280.5
49.5
49.6
49.7
49.8
49.9
0.7818
0.7813
0.7809
0.7805
0.7800
6.509
6.505
6.501
6.498
6.494
48.69
48 -66
48.64
48.61
48.58
273.4
273 2
273.1
272.9
272. B
o.dos1
o ,7857
""""""""~"""""""""""""~~""""""""""~""""""""
"
"
"
"
"
"
"
"
"
~
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
~
"
"
"
"
"
"
"
"
"
"
"
~
"
"
"
"
"
"
"
"
NOTE -- GAL =
U.
S.
GALLON, BBL = 4 2 U.
S. GALLONS.
6-1 1
1984
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
API
6A1.1
TABLE 6A1.1 (Continued)
AP I
GRiVITY
AT 60F
S P E C I F I CS PWEECAI IG
PW
FH
IIECTA
I GI H
RT I N
G R A V I T Y LB/GAL L B / C U F 1 L B / B B L
60F/60F AT 6 0 F AT 60F AT 60F
GRAVITY
AT 60F
GRAVITY
60F/60F
I N AIR
LB/GAL LB/CU FT LWBBL
AT 60F AT 60F AT 60F
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
~
~
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
~
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
~
55.3
55.4
O. 7587
0.7583
0.7579
0.7575
0.7571
6.316
6.313
6.309
6.306
6,303
47.
23
47.20
47-10
47.15
265.3
265.1
265.0
264.9
264.7
271.9
271.7
271.6
271.4
271.3
55.5
55.6
55.7
55.8
55.9
0.7567
O. 7563
0.7559
O -7555
0.7551
O. 299
6.296
6.293
6.289
6.286
47.13
47.10
47.08
47.05
47.03
264.6
264.4
264.3
264.2
264.0
49.29
48.26
48 .?$
49.21
45.19
271.1
271.0
270.8
270.7
270.5
56.0
56.1
56.2
56.3
56.4
0.7547
0.7543
0,7539
0.7535
0.7531
6.283
6,279
6.276
6.272
6.269
47.00
46.97
46.95
46.92
46.90
263.9
263.7
263.6
263.4
263.3
6.437
6 -434
6.430
6.427
6.423
48. l h
48.13
49.10
48.08
48.35
270.4
270.2
270.1
269.9
269.8
56.5
56.6
56.7
56.8
56.9
O . 7527
0.7519
0.7515
0.7511
6.266
6.262
6.259
6.256
6.252
46.87
46.85
46.82
46.80
46.78
263.2
263 O
262.9
262.7
262.6
0. 7711
O. 7707
0.7703
O. 7699
0.7694
6.420
6.416
6.4 13
6.409
6.406
48.93
48. o0
47.97
47.95
47.92
269.6
269.5
269.3
269.2
269.0
57. O
57.1
57.2
57.3
57.4
0.7507
0-7503
0 .7499
O -7495
O . 749 1
6.249
6. 246
6.243
6.239
6.236
46.75
46.73
46.70
46.68
46.65
262.5
262.3
262.2
262.0
261 -9
52.6
52.7
52.8
52.9
0.7590
O. 76 86
0.7682
0.7678
0.7674
6,402
6.399
6.395
268.9
268.7
268.6
268.5
268.3
57.5
57.6
57.7
57.8
57.9
O 7487
0.7483
O 7479
0.7475
0.7471
6.233
6.229
6.226
6.223
6.219
46.63
46 -60
46.58
46.55
46 53
261.8
261.6
6.388
47.90
47.87
47.64
47.82
47.79
.
261.4
261.2
53.0
0. 7669
53.1
53.2
O. 7665
47.77
47.74
47.71
47.69
47.66
268.2
268.0
267.9
257.7
267.6
58.0
58.1
58.2
58.3
58.4
O 7467
0.7463
O 7459
0.7455
O ,745 1
6.216
6.213
6.210
6.206
6.203
46.50
46 -48
46.45
46.43
46.40
261.1
260.9
260.8
260.7
260.5
O. 7447
O. 7443
O -7440
50.0
59.1
50.2
50.3
59.4
O. 7796
O 7792
0.7788
0,7783
cl.7779
6.491
6.487
6.483
6.430
6.476
48.56
48.53
48.50
48.43
48.45
272.6
272.5
272.3
272.2
272.0
50.5
50.6
50.7
50.8
50.9
0.7775
o. 7770
0.7766
0.7762
0.7758
6.473
6.459
6.436
6.453
6.458
48.4-3
43.413
48.37
48.34
48.32
51.0
51.1
0.7753
0.7749
O. 7745
0.7741
0.7736
6.455
6.451
6.449
6.444
6.441
0.7732
0.7728
O. 7724
0.7720
0.7715
51.2
51.3
51.4
51.5
5 1 -6
--`,,-`-`,,`,,`,`,,`---
51.7
51.8
51.9
52.0
52.1
52.2
52.3
52.4
52.5
6.392
55.0
55.1
55.2
O .7523
.
47.25
261.5
5?.3
53.4
0.7661
0.7657
0.7653
6.185
6.351
6.378
6.374
6.171
53.5
53.6
53.7
53.8
53.9
C e7649
O . 1645
0,7640
0.7636
0.7637
6.368
6.364
6.361
6.357
6.754
47.64
47.61
47.58
47.56
47.53
267.4
267.3
267.2
267. O
?65.9
58.5
58.6
58.7
58.8
58.9
6.200
6.196
6.193
0
e7436 6.190
6,187
0.7432
260.4
46.38
46.36
260.3
46
-33 260.1
260. O
46.31
259.8
46.28
54. c?
54.1
54.2
6.753
6.747
6.744
6.74n
6.337
47.51
47.49
47.46
47.43
47.41
266.7
?66.6
266.4
266.3
766.1
59.0
O .7428
54.4
0.7628
0.7624
0.7620
0.7h16
0.7612
59.1
59.2
59.3
59.4
0.7424
0.7420
0.7416
0.7412
6.183
6 - 180
6.177
6.174
6.170
46.26
46.23
46.21
46.19
46.16
259.7
259.6
259.4
259.3
259.2
54.5
54.6
54.7
54.8
54.9
0.7608
9.7603
0.7599
0.7595
0.7591
6.333
47.39
47.35
47.33
47.70
47. ?Y
266.0
?h5.9
265.7
765.6
265.4
59.5
59.6
59.7
59.8
59.9
6.167
6.164
6.161
6.158
6.154
46.14
46.11
46.09
46.06
46 .O4
259.0
258.9
258.8
258.6
258.5
5+.3
"~"""_"""""""""""""""""""~
-- GAL
6.132
6.326
6.373
6.190
0
.
0.7408
O. 7405
0.7401
0.7397
0 .7393
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
~
NOTE
= U.
S.
GALL'lNr,
S R L = 42 U.
S.
GALLONS.
1984
6-12
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
API TDB C H A P T E R t b t t D 0732290 053b585 Ob0
m
6a1.1
TABLE 6A1.1 (Continued)
API
GR4VITY
AT 69F
SPECIFIC
WEIGHT I N A I R
GRAVITY
L 8 / G A L LR/CU FT L B / B 8 L
6 0 F / 6 0 F AT 6OF AT 60F
AT 60F
API
GRAVITY
AT 60F
SPECIFIC
GRAVITY
60F/60F
WEIGHT I N A I R
LRIGAL L W C U FT ~ 8 1 8 5 ~
A T 60F A T 60F AT 60F
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
~
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
~
60.0
69.1
6 0 .?
63.3
60.4
0.7399
0.7385
0.7381
0.7377
O. 7 3 7 4
6.1 51
6.148
6.145
6.141
6.138
46.02
45.99
45.97
45.94
45.92
258.3
258.2
258.1
257.9
257.8
6 5 -0
65.1
65.2
65 e 3
65.4
0.7201
0.7197
0.7194
0.7190
0.7186
5.994
5.991
5.989
5.985
5.982
44.84
44.82
44 80
44.78
44.75
251.8
251.6
251.5
251.4
251.3
69.5
69.6
60.7
60.8
60.9
0.7170
0.7366
0.7362
0.7358
0.7354
6.135
6.13?
6.129
6.125
6. L22
45.90
45.87
4 5 . 85
45.52
45.80
257.7
257. ci
257.4
257.3
257. L
65.5
6 5 -6
65.7
65 a 8
65.9
0.7183
0.7179
0.7175
0.7172
0.7168
5.979
5.976
5.973
5.970
5.967
44.73
44.71
44.68
44 - 6 6
44.64
251.1
251.0
250.9
250.7
250 6
61.0
61.1
61.7
61 e 3
61.4
0.7351
o. 7 3 4 7
o. 7 3 4 3
o. 7 3 3 9
0.7335
6.119
6.116
6.113
6.110
6.1 Ob
45.78
45.75
45.73
45.71
45.68
257.0
256.9
256.7
256.6
256.5
6 6 .O
66.1
66.2
6 6 a3
66.4
0.7165
0.7161
0.7157
0,7154
0.7150
5.964
5.961
5.958
5.955
5.952
44.62
44.59
44.57
44.55
44.53
250.5
250.4
250.2
250.1
250.0
61.5
h l .6
61.7
61.ß
61.9
0.7332
0.7328
O 7324
0.7320
0.7316
6.103
6.100
6.097
6 . (194
6. 091
45.66
45. h3
45.61
45.59
45.56
256.3
256.2
256.1
255.9
255.8
66.5
66.6
66.7
66.8
66.9
0.7146
0.7143
0,7139
0.7136
0.7132
5.949
5.946
5.943
5 940
5.937
44.50
44.48
44.46
44.44
44.41
249.9
249.7
249.6
249.5
249.3
62.0
62.1
62.2
62.3
62.4
0.7313
0.7309
0.7305
O. 7 3 0 1
0.7298
6.087
6. 084
6.081
6.078
6.075
45.54
45.52
45.49
45.47
45.45
255.7
255.5
255.4
255.3
255.1
67.0
67.1
67.2
67.3
67.4
0.7128
0.7125
0.7121
0.7118
0.7114
5.934
5.931
5.928
5.925
5.922
44.39
44.37
44.35
44.32
44.30
249.2
249.1
249. O
248.8
248.7
62.5
62.5
62.7
62.8
62.9
0.7294
0.7290
O. 7 2 8 6
0.7283
0.7279
6.072
6.069
6. F65
6.062
6.059
45.42
45.40
45.38
45.35
45.33
255.0
254.9
254.7
254.6
254.5
67.5
67.6
67.7
67.8
67.9
0.7111
0.7107
0.7103
0.7100
0.7096
5.919
5.916
5.913
5.910
5.907
44.28
44.26
44.23
44.21
44.19
248.6
248.5
248.3
248.2
248.1
63.0
63.1
67.2
63.3
63.4
0.7275
0.7271
O. 7 2 6 8
O. 7 2 6 4
0.7260
6.056
6.053
6.050
6.047
6.044
45.31
45.28
45.26
45.24
45.21
254.4
254.2
254.1
254.0
253.9
68.0
68.1
68.2
68.3
68.4
O*7093
O .7089
0.7086
0,7082
0.7079
5.904
5.901
5.898
5.895
5.892
44.17
44.15
44.12
44.10
44.08
248.0
247.8
247.7
247.6
247.5
63.5
63.6
63.7
63.8
63.9
Q.7256
0.i253
O. 7 2 4 9
0.7245
O. 7 2 4 2
6.041
6.037
6.034
6.031
6.928
45.19
45.17
45.14
45.12
45.10
253.7
253.6
253.4
253.3
253.2
68.5
68.6
68.7
68.8
68.9
0.7075
0.7071
O 7068
O 7064
0.7061
5.889
5.886
5.883
5.880
5.877
44.06
44.04
44.01
43.99
43.97
247.3
247.2
247.1
247. O
246.9
64.0
64.1
64.2
64.3
64.4
0.7238
0.7234
O. 7 2 3 0
0.7227
0.7223
6. n25
6 r 022
6.019
6.016
6.@13
45.07
45.05
45.03
45.00
44.98
253.1
252.9
252.8
252.7
252.5
69 .O
69.1
69.2
69.3
69.4
0.7057
O e7054
0.7050
0.7047
0.7043
5.875
5.872
5.869
5.866
5.863
43.95
43.93
43.90
43.88
43.86
246.7
246.6
246.5
246.4
246.2
64.5
64.6
64.7
64.8
64.9
0.7219
0.7216
0.7212
0.7208
0.7205
6.nlO
6.007
6.003
44.96
44.94
6.001)
44.89
44.87
252.4
252.3
252.1
252.0
251.9
69.5
69.6
69.7
69.8
69.9
O 7040
O .7036
0.7033
0.7029
0.7026
5.860
5.857
5. a54
5.851
5.848
43 84
43.82
43.79
43.77
43.75
246.1
246. O
245.9
245.7
245.6
.
5.997
44.91
.
6-13
--`,,-`-`,,`,,`,`,,`---
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
A P I TDB CHAPTER*b
**
m
0732290 0536586 TT7
m
6A1.1
--`,,-`-`,,`,,`,`,,`---
TABLE 6A1.1 (Continued)
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
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"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
SWPEEI C
G IH
AFTPI CI
GRAVITY
AT 60F
"_""""""""
GRAVITY
60F/60F
S P E C IAFPII C
IN A I R
L B / G A L LR/CU F T L B / B B L
AT 60F
AT 6 0 f
AT 60F
GRAVITY
AT 60F
GRAVITY
60F/60F
WEIGHT I N A I R
LB/GAL LB/CU F 1 LB/BBL
A T 60F A T 60F A T 60F
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
~
"
"
"
"
"
"
"
"
"
"
"
~
"
"
"
~
"
"
"
"
"
"
"
"
.
70.0
70.1
70.2
70.3
7') .4
0.7022
0.7'319
0.7(?15
O. 7 0 1 2
O. 7 0 0 8
5.845
5.542
5.840
5. P37
5.834
43.73
43.71
43.69
43.66
43.64
245.5
245.4
245 3
245.1
245.0
75.0
75.1
75.2
75.3
75.4
0.6852
O 6849
0.6846
0.6842
0.6839
5.704
5.701
5.698
5.695
5.692
42 -67
42.65
42.63
42.61
42 5 9
239.6
239.4
239.3
239.2
239.1
70.5
O. 7 0 0 5
70.6
70.7
70.8
70.9
0.7001
0.h998
0.6995
O. 6 9 9 1
5.831
5.828
5.825
5.822
5.819
43.62
43.60
43.58
43 S 6
43.53
244.9
244. a
244.7
244.5
244 4
75.5
75.6
75.7
75.8
75.9
O 6836
O .6832
O 6829
0.6826
0.6823
5.690
5.687
5.684
5.681
5.679
42.57
42 5 4
42.52
42 - 5 0
42.48
239.0
238.9
238.7
238.6
238.5
7 1 .O
71.1
71.2
71.3
71.4
O. h 9 8 8
0.6984
0.h981
0.6977
0.6974
5.816
5.814
5.911
5.808
5.505
43.51
43.49
43.47
43.45
43.43
244.3
244.2
244. O
243.9
243.8
76.0
76. L
76.2
76.3
76.4
0.6819
0.6816
0.6813
0.6809
0.6806
5.676
5.673
5.67 1
5.668
5 -665
42 -46
42 -44
42.42
42.40
4 2 4 38
238.4
238 3
238.2
238.0
237.9
71 .5
71.6
71.7
71.8
71.9
0.6970
0.6967
O. h 9 6 4
O. 6 9 6 0
0.6957
5.802
5.799
5.796
5.793
5.791
43.41
43.38
43.36
43.34
43.32
243.7
243.6
243.4
243.3
243.2
76.5
76.6
76.7
76.8
76.9
0.6803
0.6800
0.6796
0.6793
O 6790
5.662
5.660
5.657
5.654
5.65 L
42.36
42.34
42.32
42.30
42.28
237.8
237.7
237.6
237.5
237.4
72.0
72.1
72.2
72.3
7 2 e4
0.6953
0.6950
O. 6946
O. 6 9 4 3
0.6940
5.785
5.785
5.782
5.779
5.776
43.30
43.28
4 3 26
4 3 23
43.21
243.1
243 .O
242. 8
242.7
242 .6
77.0
77.1
77.2
77.3
77.4
0.6787
0.6783
O. 6780
0.6777
O -6774
5.649
5.646
5.643
5.641
5.638
42.26
42 2 4
42 -22
4 2 -20
42.18
237.2
237.1
237. O
236.9
236.8
72.5
72.6
72.7
72.8
72.9
0.6936
0.6933
O. 6 9 2 9
O. 6926
0.6923
5.774
5 077 1
5.768
5.765
5.762
43.19
43.17
43.15
43.13
43.11
242.5
242.4
242.3
242.1
242.0
77.5
77.6
77.7
77.8
77.9
0.6770
0.6767
0.6764
0.6761
0.6757
5.635
5.632
5.630
5.627
5 a624
42.16
42.14
42.12
42.10
42.08
236.7
236.6
236.5
236.3
236.2
7 3 .o
73.1
73.2
7? .3
73.4
0.6919
0.6916
O. 6 9 1 3
O. 6 9 0 9
0.6906
5.759
5.757
5.754
5.751
5.748
43 0 9
43.07
43.04
43.02
43 O0
241.9
241.8
241.7
241.5
241.4
78. O
78.1
78.2
78.3
78.4
0.6754
O .675 1
0.6748
O 6745
0.6741
5.622
5.619
5.616
5.614
5.611
42 06
42 -04
4 2 .O2
42.00
41 - 9 8
236.1
236.0
235.9
235.8
235.7
73.5
73.6
73.7
73.8
73.9
0.6902
0.6899
0.6896
0.6892
O. 6 8 8 9
5.745
5.743
5.740
5.737
5.734
42.98
42.96
42.94
42.92
42. 9 0
241.3
241.2
241.1
241.0
240.8
78.5
78.6
7 8 07
78.8
78.9
O -6738
0.6735
0.6732
0.6728
0.6725
5.608
5.606
5.603
5.600
5.598
41 096
41 - 9 4
41 - 9 2
41.90
41 - 8 8
235.6
235.4
235. 3
235.2
235.1
74. O
74.1
74.2
74.3
74.4
0.6886
0.6582
0.6879
0.6876
0.6872
5.731
5.729
5.726
5.723
5.720
42. 88
42.86
42.83
4 2 .'8 1
42.79
240.7
240.6
240.5
240. 4
240.2
79. O
79.1
79.2
79.3
79.4
0.6722
0.6719
0.6716
0.6713
0.6709
5.595
5.592
5.590
5.587
5.584
41 086
41 8 4
41 82
41 80
41 m78
235.0
234.9
234.8
234.7
234.5
74.5
74.6
74.7
74.8
74.9
0.6869
0.6866
O e6 862
0.6559
0.6856
5.727
5.715
5.712
5.709
5.706
42677
42.75
42.73
42.71
42.69
240.1
240.0
239.9
239.8
239.7
79.5
79.6
79.7
79.8
79.9
O .6706
O a6703
O .6700
O -6697
O -6693
5.582
5.579
5.576
5.574
5.571
41 -76
41 -74
41 a72
41.70
41 - 6 8
234.4
234.3
234.2
234. 1
234.0
6-14
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
1984
Not for Resale
A P I TDB C H A P T E R t b t f
m 0732290 0536587 733 m
6A1.1
TABLE 6A1.1 (Contlnued)
"
"
"
"
"
"
"
"
"
"
"
"
"
"
~
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
AP1
GRAVITY
AT 6OF
"_""""""""""""~"""""~"""""
SPECIFIC
GRAVITY
60F/60F
WEIGHTA PIN
I AIR
L B / G A L L B / C U FT LB/RBL
A T hOF AT h3F AT 60F
GRAVITY
AT 60F
SPECIFIC
WEIGHT I N A I R
G R A V I T Y LB/GAL L B l C U FT L B / B B î
AT 60F AT 60F
6 0 F / 6 0 F AT 60F
90.0
80.1
R0.2
80.3
63.4
O. h 6 9 0
0.6687
0.6684
0.6681
0.6678
5.568
5.566
5.563
5.561
5.554
41.66
41. h4
41.62
41. h?
41.58
233.9
233.8
273.7
233.5
233.4
85 - 0
85.1
85.2
85.3
85.4
O 6536
0.6533
0.6530
0.6527
O . 6524
5.440
5.437
5.435
5.432
5.430
40.69
r0.68
40 066
40.64
40.62
228.5
228.4
228.3
228.1
228.0
80.5
80.6
80.7
8O.R
80.9
0.6675
0.6671
0.6668
O. hb45
0.6662
5.555
5.553
5.543
5.547
5.545
41.56
41.54
41.52
41.50
41.48
333.3
233.2
233.1
213.3
232.9
85.5
85.6
85 a 7
85.8
85.9
0.6521
0.6518
0.6515
0.6512
0.6509
5.427
5.425
5.422
5.420
5.417
40.60
40.58
40.56
40.54
40.53
227.9
227.8
227.7
227.6
227.5
81.0
81.1
e l .2
81.3
81.4
0.6659
0.6656
0.6653
0.6649
0.6646
5.542
5.540
5.537
s. 5 7 4
5.532
41.46
41 e44
41.42
41.40
41.3R
232.8
232.7
232.6
232.4
232.3
86.0
86.1
86.2
86.3
86.4
0.6506
0.6503
0.6500
0.6497
O. 6 4 9 4
5.415
5.412
5.410
5.407
5.405
40.51
40.49
40.47
40.45
40 -43
227.4
227.3
227.2
227.1
227. O
91.5
0.6h43
0.6640
0.6637
O. h634
0.6631
5.529
81.6
81.7
81 . A
81.9
41.36
41.34
5.519
a6.5
86.6
86.7
86.8
86.9
0.6491
0.6488
O .6485
0.6482
0.6479
fi.
41.31
41.29
232.2
232. 1
232.0
231.9
231.8
5.402
5.400
397
5.395
5.392
4 0 -4 1
40 -40
40.38
40.36
40.34
226.9
226.8
226.7
226.6
226.5
92.0
82.1
82.2
82.3
82.4
O.662ß
0.6625
O. h 6 2 1
0.6618
O. 6 6 1 5
5.516
5.514
5.511
5.508
5.506
41.27
41.25
41.23
41 2 1
41.19
231.7
231.6
231.5
231.4
231.2
87.0
87.1
87.2
87.3
87.4
O. 6476
0.6473
0.6470
0.6467
O -6464
5.390
5.387
5.385
5.382
5.380
40.32
4 0 e30
40.28
40.27
40.25
226.4
226.3
226.2
226.1
226.0
82.5
82.6
82.7
82.8
A2.9
0.6612
0.6609
O. 6676
O. 6 6 0 3
0.6600
5.503
5.501
5.438
5.496
5,493
41.17
41.15
41.13
41.11
41.09
231. 1
231.0
230.9
230.8
230.7
87.5
87.6
R7.7
87.8
87.9
0.6461
0.6458
0.6455
0.6452
O. 6 4 4 9
5.377
5.375
5.373
5.370
5.368
40.23
40.21
40.19
40.17
40.16
225.9
225.7
225.6
225.5
225.4
83.9
83.1
83.2
83.3
83.4
0.6597
0.6594
Q.6591
0.6588
O. 6 5 8 4
5.49r)
5.488
5.485
5.4R3
5.430
4 10 7
41.n6
41.04
41.02
41.00
230.6
230.5
230.4
230.3
230.2
88.0
88- 1
88.2
88.3
88.4
O. 6 4 4 6
0.6444
0.6441
0.6438
0.6435
5.365
5.363
5.360
5.358
5.355
40.14
40.12
40.10
40.08
40 0 6
225.3
225.2
225.1
225.0
224.9
83.5
83.6
83.7
83.8
83.9
O . 6581
0.6578
0.6575
0.6572
0.6569
5.478
5.475
5.473
5.470
5.467
40.98
40.96
4rl. 9 4
40.92
40.93
330.1
230.0
229.8
229.7
229.6
88.5
88.6
88.7
88.8
88.9
0.6432
O. 6 4 2 9
O. 6426
O .6423
O 6420
5.353
5.351
5.348
5.346
5.343
4 0 .O5
40.03
40.01
39.99
39.97
224.8
224.7
224.6
224.5
224.4
84.3
8%.1
84.2
84.3
84.4
O. 6566
O. h 5 6 3
O. 6 5 6 0
0.6557
O. 6 5 5 4
5.465
5.462
5.467
5.457
5.455
40.88
40.56
40. a5
40.83
40.81
229.5
229.4
229.3
229.2
229.1
89.0
89.1
89 e 2
89.3
89.4
0.6417
0.6414
0.641 1
O .6409
0.6406
5.341
5.338
5.336
5.334
5.331
39.95
39.94
39.92
39.90
39.88
224.3
224.2
224.1
224.0
223.9
84.5
84.6
84.7
84.8
84.9
0.6551
O. 6 5 4 8
O. 6 5 4 5
O. 6 5 4 %
0.6539
5.452
5.450
5.447
5.445
5.44E
40179
40.77
40.75
40.73
729.0
228.9
228.8
228.7
228.6
89.5
89.6
89.7
89.8
89.9
O. 6403
0.6400
O . 6397
0.6394
0.6391
5.329
5.326
5.326
5-32 1
5.319
39.86
39.85
39.83
39.81
39.79
223.8
223.7
223.6
223.5
223.4
"_
"-~="""""""""""""""""""""""""""""""""""""""""""
5.577
5.524
5.521
41.33
40.71
--`,,-`-`,,`,,`,`,,`---
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
~
"
"
"
"
"
"
"
"
"
"
"
"
"
~
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
~
"
"
"
"
NOTE
--
G A L = U.
S.
GALLON,
B E L = 4 2 U.
S. GALLONS.
6-15
1984
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
A P I TDB CHAPTERxb X *
m
0732290 0536588 87T
m
9 0 .O
90.1
90.2
90 - 3
90.4
0.6388
0.6385
0.6382
O. 6 3 8 0
0.6377
5.317
5.314
5.712
5.307
5.707
39.77
39.76
39.74
39.72
39.70
223.3
223.2
223.1
223.0
222.9
95.0
95.1
95.2
95.3
95.4
O 6247
O. 6244
O ,6262
0.6239
O 6236
5.199
5.197
5.196
5.192
5.190
38-69
38.88
38 86
38.84
38.83
218.4
218.3
218.2
218.1
218.0
90.5
90.6
90.7
99.8
90.9
O . 6374
0.6371
0.6368
0.6365
0.6362
5.305
s. 7 n 2
5.100
5.297
5.795
39.68
39.67
39.65
39.63
39.61
222.ß
222.7
222.6
222.5
222.4
95 - 5
9 5 -6
95.7
95.8
95.9
O -6233
0.6231
0.6228
0.6225
O -6223
5.188
5. 1 8 5
5.183
5.181
5.178
38 - 8 1
38 079
217.9
217.8
217.7
217.6
217.5
91.0
91.1
91.2
91.3
91.4
0.6360
0.6357
0.6354
0.6351
0.6348
5.293
5.799
5.288
5.286
5.287
39.59
39.58
39.56
39.54
39.52
222.3
222.2
222.1
222.0
221 9
96 .O
96.1
96.2
96.3
96 -4
0.6220
0.6217
0.6214
0.6212
0.6209
5.176
5.174
5.172
5. L 6 9
5.167
38.72
38.69
38.67
38.65
217.4
217.3
217.2
217. 1
217.0
91 e 5
91.6
91 e 7
91.8
91 -9
0. h 3 4 5
O 6342
O. 6340
0,6337
0.6334
5.781
5.278
5.276
5.274
5.771
39.51
39.49
3 9.47
39.45
39.43
221.8
221.7
221.6
221.5
221.4
96 e5
96.6
96.7
96.8
96.9
0.6206
0.6203
0.6201
O -6198
0.6195
5.165
5.163
5.160
5.158
5.156
38.64
38.62
38.60
38.59
38.57
216.9
216.8
216.7
216.6
216.5
92.0
92.1
92.2
92.3
9>.4
0.6331
0.6328
0.6325
0.6323
0.6320
5.269
5.267
5.264
5 262
5 . ?h0
39.42
39.40
39.38
3 9 36
39.35
221.3
221.2
221.1
2 2 1 .o
220.9
97.0
97.1
97. 2
97.3
97 04
0.6193
0.6190
0.6187
0.6184
0.6182
5.153
5.151
5 149
5.147
5- 144
38.55
38.54
38.52
38.49
216.4
216.4
216.3
216.2
216.1
9 2 e5
92.6
92.7
92.8
92.9
0.6317
0.6314
0.6311
O e 6309
O. 6 3 0 6
5.757
5.255
5.752
5.250
5.749
39.33
39.31
39.29
39.28
39.76
220.9
220.7
220.6
220.5
220.4
97.5
97.6
97.7
97.8
97.9
0.6179
0.6176
0.6174
0.6171
O -6 168
5.142
5.140
5.138
5.135
5.133
38 -47
3 8 -45
38.44
38.42
3 8 -40
216.0
215.9
215.8
215.7
215.6
9 3 .D
93.1
93.2
9?.3
93.4
O. 6 3 0 3
0. h300
0.6297
0.6294
0.6292
5.745
5.743
5.741
5.238
5.236
39 24
39.22
39.21
39.19
79.17
220.3
220.2
220.1
220.0
219.9
98.0
98.1
98 02
98.3
9 8 04
0.6166
0.6163
0,6160
0.6158
0.6155
5.131
5. 1 2 9
5.126
5.124
5. 1 2 2
36-38
38.37
38 a35
38.33
38.32
215.5
215.4
215.3
215.2
215.1
93.5
93.6
93.7
93.8
93.9
0.6289
0.6286
0.6283
0.6281
0.6278
5.234
5.231
5.729
5.227
5.224
39.15
39.14
39.12
39.10
39.08
219.8
219.7
219.6
219.5
219.4
98.5
98.6
98.7
98.8
98.9
0.6152
0.6150
0.6147
0.6144
0.6141
5.120
5.118
5.115
5.113
5.111
38 030
38.28
38 -27
38.25
38.23
215.0
214.9
214-8
214.8
214.7
94.0
94.1
94.2
94.3
94.4
0.6275
0.6272
O . 6269
0.6267
0.6264
5.222
5.220
5.718
5.215
5.213
39.07
39.05
39.03
39.01
39.00
219.3
219.2
219.1
219.0
218.9
99.0
99.1
99.2
99.3
99.4
0.6139
0.6136
O e6134
0.6131
0.6128
5.109
5.106
5.104
5.102
5.100
38.22
38.20
38.18
38.17
38.15
214.6
214.5
214.4
214.3
214.2
94.5
94.6
94.7
94.8
94.9
0.6261
0.6258
6256
0. 6253
0.6250
5.211
5.208
5 .?O6
5.204
5.201
38.98
38.96
38.95
38.53
38.91
218.8
218.7
218.7
218.6
218.5
99.5
99.6
99.7
99.8
99.9
0.6126
0.6123
0.6120
0.6118
0.6115
5.098
5.095
5.093
5.091
5.089
38.13
38.12
38.10
214.1
214.0
213.9
213.8
213.7
"_
r).
""""_""""""""~""""""""""~
0
38.77
38.76
38.74
38 07 1
38.50
38 -09
38.07
"
I
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
"
-
NOTE
--
GAL = U.
5.
GALLON,
BEL = 4 2 U.
S.
GALLONS.
--`,,-`-`,,`,,`,`,,`---
6-16
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
1984
A P I TDBCHAPTER*b
**
m
0 7 3 2 2 9 0 0536589 706
m
6A1. i
TABLE 6A1.1 (Continued)
SPEC
A IPFII C
GRAVITY
AT 60F
GRAVITY
60F/60F
WEIGHT AIPNI A I R
LB/GAL LB/CUFT
LWBBL
AT 60F AT 6 O F AT 60F
""""""""""""""""""""""""""""""""-"""-"---"---"-""--
S P E C I f IC
GRAVITY
AT 60F
GRAVITY
60F/60F
WEIGHT IN A I R
LB/GAL LB/CUFT
LB/BBL
AT 60F AT 6 0 f
AT 6 0 f
100.0
100.1
100.2
100.3
100.4
0.6112
0.6110
0.6107
0.6104
0.6102
5.087
5.084
5.0~32
5.080
5.078
38.05
38. 04
38- 02
38.00
37.99
213.6
213.5
213.5
213.4
213.3
105.0
105.1
105.2
105.3
105 e 4
0.5983
0.5981
O. 5978
0.5976
O 5973
4.979
4.977
4.975
4.972
4.970
37.25
37.23
37.21
37.20
37.18
209.1
209. O
208.9
208.8
208.8
100.5
100.6
100.7
100.8
100.9
0.6099
0.6097
O. h 0 9 4
O. 6 0 9 1
0.6089
5.n76
5.073
5.071
5 .O69
5.067
37.97
37.95
37.94
37.92
37.90
213.2
213.1
213.0
212.9
212.8
105.5
105.6
105.7
105.8
105.9
O. 5 9 7 0
O. 5968
0.5965
0.5963
0.5960
4.968
4.966
4.964
4.962
4.960
37.17
37.15
37 1 4
37.12
37.10
208.7
208.6
208.5
208.4
208.3
101.0
101.1
10L.2
101.3
101.4
O. 6 0 8 6
0.6083
0.6081
0.6078
0.6076
5.flh5
5 . ~ 2
5.060
5.058
5.056
37.89
37.87
37.86
37.84
37.82
212.7
212.6
212.5
212.4
212.3
1C6.0
106.1
106 2
106 e3
106.4
0.5958
O . 5955
0.5953
0.5950
O. 5948
4.958
4.956
4.954
4.952
4.949
3 7 .O9
3 7 .O7
37.06
37.04
37.03
208.2
208. L
208.1
208.0
207.9
101.5
101.6
101.7
101.8
101.9
0.6073
0.6070
O 6068
0.6065
0.6063
5.954
5.052
5.049
5.047
5.645
37.81
37.79
37.77
37.76
37.74
212.3
212.2
212.1
212.0
211.9
10605
106.6
106.7
106.8
106.9
0.5945
O. 5 9 4 3
0.5940
0-5938
0.5935
4.947
4.945
4.943
4.941
4.939
37.01
37.00
36.98
36.90
36 -95
207 8
207.7
207.6
207.5
207.4
102. o
102.1
102.2
102.3
102.4
O. 6 0 6 0
O.bD57
0.6055
C.6052
0.6050
5.043
5.041
5.039
5.036
5.034
37.73
37.71
37.69
37.68
37.66
211.8
211.7
211.6
211.5
211.4
107.0
107.1
107.2
107.3
107.4
0.5933
0.5930
0.5928
0.5925
0.5923
4.937
4.935
4.933
4.931
4.929
36.93
36.92
36 - 9 0
36.89
3 6 87
.
207.4
207.3
207.2
207.1
207.0
102.5
102.6
102.7
102.8
102.9
0.6047
0.6044
0.5042
0.6039
O. 6037
5.032
5.030
5-028
5.026
5 .P23
37.65
37.63
37.61
37.60
37.58
211.3
211.3
211.2
211.1
211.0
107.5
107.6
107.7
107.8
107.9
0.5921
0.5918
0.5916
0.5913
0.591 1
4.927
4.925
4.922
4.920
4.918
36.86
36 -84
36.83
36.81
36.79
206.9
206.8
206.7
206.7
206.6
103.0
103.1
133.2
1@!.3
103.4
0.6334
O. 6032
0.5029
0.6026
0.6024
5.021
5.019
5.017
5.015
5.n13
37.56
37.55
37.53
37.52
37.50
210.9
210.8
210.7
210.6
210.5
1 0 8 .o
108.1
108.2
108.3
108.4
0.5908
O. 5906
0.5903
O. 590 1
0.5898
4.916
4.914
4.91 2
4.91 O
4.908
36.78
206.5
36.76
206.4
3 6 ~ 7 5 206. 3
36.73
206.2
36.72
20601
0.6021
103.8
103.9
0.6019
0.5016
0.6014
0.6011
5.oii
5 .o39
5.0rJ6
5.OO4
5 .O02
37.48
37.47
37.45
37.44
37.42
210.4
210.4
210.3
210.2
210.1
108.5
108.6
108.7
108.8
108.9
0.5896
0.5893
0.5891
0.5888
0.5886
4.906
4.904
4.902
4.900
4.898
36.7C
36 .69
36 -67
36.66
36 - 6 4
206.1
206.0
205.9
205.8
205.7
104.0
104.1
1C4.2
104.3
104.4
0.6009
0.6306
0.6003
0.6001
o. 5 9 9 8
5 .o09
4.998
4.996
4.994
4.991
37.40
37.39
37.37
37.36
37.34
210.0
209.9
209.8
209.7
209.6
109.0
109.1
109 -2
109.3
109.4
O. 5 8 8 4
0.5881
0.5879
0.5876
0.5874
4.896
4.894
4.892
4.890
4.888
36.63
36 a 6 1
36.60
36.58
36.56
205.6
205.5
205.5
205 e 4
205.3
104.5
104.6
104.7
104.8
1C4.9
O. 5996
O. 5993
0.5991
0.5988
0.5986
4.98'3
4.987
4.9ß5
4.983
4.951
37.33
37.31
37.29
37.28
37.26
20S.6
209.5
209.4
209.3
209.2
109.5
109.6
109.7
109.8
109.9
0.5871
0.5869
0.5867
0.5864
0.5862
4.886
4.884
4.882
4.880
4.878
36.55
36.53
36.52
36.50
36.49
205.2
205.1
205.0
204.9
204.9
103.5
103.6
103,7
6-17
1984
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
--`,,-`-`,,`,,`,`,,`---
~~~~~~~""""~~"""~"""""""""""""""""""
A P I T D B CHAPTERtb t t
m
0732290 0536590 428
m
6A1.1
0.5852
0.5553
4.876
4. R73
4.871
4.969
4. A67
36.47
36.46
36.44
36.43
36.41
204.8
204.7
204.6
204.5
204.4
115.0
115.1
115.2
115.3
115.4
O 5740
0,5738
0.5736
O 5733
0.5731
4.776
4.774
4.773
4.771
4.769
35.7 3
35.72
35.70
35.69
35 -67
200.6
200.5
200.4
200.4
200.3
110.5
110.6
110.7
110.8
110.9
0.5847
0. 5845
O. 5942
O . 5840
O. S837
4.865
4.563
4.951
4.859
4. A57
36.40
36.38
36.37
36.35
36.34
204.3
204.3
204.2
204.1
204.0
115.5
115.6
115.7
115.8
115.9
O 5729
0.5726
O. 5724
0.5722
0.5719
4.767
4.765
4.763
4.76 1
4.759
35 -66
35.65
35 -63
35.62
35-60
200.2
200.0
200.0
199.9
111.0
111.1
111.2
111.3
111.4
O. 5835
O. 5825
4.855
4. R53
4. R51
4.949
4.847
36.32
36.31
36.29
36.28
36.26
203.9
203.8
203.8
203.7
203.6
116.0
116.1
116.2
116.3
116.4
0.5717
0.5715
0.5713
0.5710
0.5708
4.757
4.755
4.753
4.751
4.749
35.59
35.57
35 a56
35 .54
35.53
195.8
199.7
199.6
199.6
199.5
0.5523
O. 5 8 2 1
0.5818
0.5815
O. 5813
4. 845
4.543
4 841
4.839
4. R37
36.25
36.23
36. L 2
36.20
36.19
203.5
203.4
203.3
203.3
203.2
116.5
116.6
116.7
116.8
116.9
0.5706
0.5703
0.5701
O. 5 6 9 9
0.5696
4.747
4.746
4.744
4.742
4.743
35.52
35 e 5 0
35.49
35.47
35.46
199.4
199.3
199.2
199.2
199.1
o.
4.835
4.833
4.831
4.829
4.827
36.17
36.16
36.14
36.13
3 6 . L1
203.1
203 .o
202.9
202.8
202.8
117.0
117.1
117.2
117.3
117.4
O. 5 6 9 4
0.5692
O. 5 6 9 0
0.5687
O. 5 6 8 5
4.738
4.736
4.734
4.732
4.730
35 " 4 4
35 043
35.42
35 -40
35.39
199.0
19a.5
198.8
198. 8
198.7
4.925
4.923
4.SLl
4. H20
4.918
36.10
36. C R
36 07
36. c 5
3 h . C4
202.7
202.6
202.5
202.4
202.3
117.5
117.6
117.7
117.8
117.9
0.5683
0.5680
0.5678
O. 5 6 7 6
O 5674
4.728
4.726
4.725
4.723
4.721
35.37
35.36
35.34
35.33
35.32
198.6
198.5
198.4
198.4
198.3
4.816
4.91'+
4. S12
4. S10
4. soa
36 .03
202.3
202.2
202.1
202.0
201.9
118.0
36.01
36.00
35.98
35.97
118.1
118.2
118.3
118.4
0.5671
0.5669
0.5667
O. 5 6 6 5
0.5662
4.719
4.717
4.715
4.713
4.711
35.30
35.29
35 -27
35 - 2 6
35-25
198.2
198 1
198.0
198.0
197.9
35.95
35.94
35.92
35.91
35.99
20198
201.8
201.7
201.6
201.5
118.5
118.6
118.7
118.8
118.9
0.5660
0.5658
0.5655
O. 5 6 5 3
0.5651
4.709
4.708
4 706
4.704
4.702
35.23
35 e 2 2
3 5 -20
35 e 1 9
35.17
197.8
197.7
197.6
197.6
197.5
110.0
110.1
110.2
110.3
110.4
O. 5 8 5 9
O. 5 8 5 7
O. 5 8 5 4
o.
5833
0.5830
9.5828
111.5
11 1.6
111.7
111.8
111.9
112.0
112.1
112.2
112.3
112.4
S811
O. 5 8 0 9
O. 5806
0.5804
0.5802
O. 5799
O. 5797
112.5
112.6
112.7
112.8
112.9
o.
5794
O. 5792
0. 5790
1.13.0
113.1
113.2
113.3
113.4
c.5787
O. 5785
0.5783
0.5780
o. 5778
O. 5776
O. 5 7 7 3
200.1
113.5
113.6
113.7
113.8
113.9
0.5771
0.5768
O. 5 7 6 6
4.806
A04
4.872
4.800
4.793
114.0
114.1
114.2
114.3
114.4
O. 5 7 6 4
0.5761
O. 5 7 5 9
o. 5757
0.5754
4.796
4.794
4.792
4.79rj
4.788
35.88
35.86
35.85
35.83
35.92
201.4
201.3
201.3
201.2
201.1
119.0
119.1
119.2
119.3
119.4
O . 5649
0.5646
O . 5644
O. 5 6 4 2
0.5640
4.700
4.698
4.696
4.694
4,692
35.16
35.15
35 -13
35.12
35 - 1 0
197.4
197.3
197.2
197.2
197. 1
114.5
114.6
114.7
114.8
114.9
0.5752
O. 5 7 5 0
0.5747
O. 5745
0.5743
4.786
4.784
4.782
4.780
4.7 ?a
35. 81
35.79
35.78
35.76
35.75
201.0
200.9
200.9
200.8
200.7
119.5
119.6
119.7
119.8
119.9
O 5637
4.691
4.689
4.687
4.685
4.683
35 -09
35-08
35 .O6
35-05
35.03
197.0
195.9
196.8
196.8
196.7
""_"""""""""""""
"-=""""""""""""""""""""""""""-"""""""""""""""""
"QOTE
--
4.
GAL =' U.
S u
GALLON, 8ßL = 4 2 U.
S.
GALLONS.
1984
6-18
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
005635
0.5633
O 5631
0,5628
Not for Resale
--`,,-`-`,,`,,`,`,,`---
TABLE 6A1.1 (Continued)
6A2.1
--`,,-`-`,,`,,`,`,,`---
6-19
1984
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
A P I TDB CHAPTER*b
**
m
07322900536592
2TO
m
6A2.2
TEMPERATURE. F
--`,,-`-`,,`,,`,`,,`---
a
TEMPERATUREI
6-20
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
1984
Not for Resale
A P I TDB CHAPTER+b X + W 0732290 0536593 137 W
6142.3
MRANRE.F
Y
8
Y
c
1FMPERATlJRE.F
1984
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
6-21
--`,,-`-`,,`,,`,`,,`---
Not for Resale
A P I TDBCHAPTERtb
tt
m 0732290 0536594 073 m
--`,,-`-`,,`,,`,`,,`---
6A2.4
6-22
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
1984
Not for Resale
A P I TDBCHAPTER*b
** m
0732270 0536575 TOT
m
--`,,-`-`,,`,,`,`,,`---
6A2.5-6A2.6
6-23
1984
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
A P I TDB
CHAPTERfh
f t
0 7 3 2 2 9 0 053b59b 946
m
--`,,-`-`,,`,,`,`,,`---
6-24
1984
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
10
--`,,-`-`,,`,,`,`,,`---
6-25
1984
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
A P I T D BC H A P T E R t b
t t M 0732290 0536598 7 1 9 M
6A2.11-6A2.12
--`,,-`-`,,`,,`,`,,`--Y
6-26
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
1984
Not for Resale
A P I TDBCHAPTERxb
**
m
0732290 0536599 b55
m
6A2.1-6A2.12
COMMENTS ON FIGURES 6A2.1 THROUGH 6A2.12
Purpose
Specific gravity-temperature data are presented for pure hydrocarbons at saturation pressures. Additional hydrocarbons are covered in Procedures 6A2.13 and 6A2.15.
Reliability
The maximum error tobe expected from experimental data over the entire solid length of
each curve is 1.0 percent. At temperatures 100 F below the critical temperature and lower,
the estimated maximum error is 0.5 percent.
Notation
0= critical point.
Data Sources
Methane (la,3a,9a,25a,37a,47a,48a,55a,
59a,62a,71a,86a,99a,ll2a,135a,136a,
146a)
Ethane (la,7a,9a,l5a,37a,43a,49a,%a,
59a,63a,65a,66a,77a,78a,142a)
Propane (la,12a,20a,22a,28a,30a,37a,
53a,Sa,56a,63a,65a,73a,74a,79a,80a,
92a,97a,llla,113a,12la,123a,127a,138a,
144a)
n-Butane (la,16a,20a,23a,37a,43a,55a,
65a,74a,94a,105a,121a)
2-Methylpropane (isobutane) (la,lOa,l4a,
16a,20a,23a,37a,43a,%a,65a,74a,94a,
118a,121a,148a)
n-Pentane (la,20a,37a,59a,74a,lO2a,ll7a,
119a,121a,122a,140a)
2-Methylbutane (isopentane) (la,4a,
37a,59a,61a)
n-Hexane (la,35a,37a,59a,70a,107a,
134aJ50a)
2,3-Dimethylbutane (la,68a)
n-Heptane (la,37a,43a,59a,66a,83a,
107a,140a)
2-Methylhexane (83a)
3-Methylhexane (83a)
3-Ethylpentane (83a)
2,2-Dimethylpentane (83a)
2,3-Dimethylpentane (83a)
2,CDimethylpentane (83a,106a)
3,3-Dimethylpentane (83a)
2,2,3-Trimethylbutane (83a)
n-Octane (la,19a,35a,37a,41a,
59a,107a,117a)
2-Methylheptane (83a)
3-Methylheptane (83a)
4-Methylheptane (83a)
3-Ethylhexane (83a)
2,2-Dimethylhexane (83a)
2,3-Dimethylhexane (83a)
2,CDimethylhexane (83a)
2,5-Dimethylhexane (83a)
3,3-Dimethylhexane (83a)
3,CDimethylhexane (83a)
2-Methyl-3-ethylpentane (83a)
3-Methyl-3-ethylpentane (83a)
2,2,3-Trimethylpentane (83a)
2,2,4-Trimethylpentane (83a,106a)
2,3,3-Trimethylpentane (83a)
2,3,CTrimethylpentane (83,)
2,2,3,3-Tetramethylbutane(43a,83a)
n-Nonane (la,19a,37a,107a)
2,2,5-Trimethylhexane (la,37a,43a)
n-Decane (la,37a,43a,107a)
n-Dodecane (la,35a,37a,43a)
n -Hexadecane (35a)
Ethene (ethylene) (la,33a,37a,59a)
Propene (propylene) (la,20a,37a,40a,52a,
59a,74a,77a,90a,121a,145a,l5la)
l-Butene (la,13a,20a,23a,37a,74a,90a,
95a,121a,148a)
2-Methylpropene (isobutylene) (la,43a,
53a,90a,103a,148a)
cis-2-Butene (la,37a,59a,90a,148a)
trans-2-Butene (la,23a,37a,90a,148a)
1,3-Butadiene (la,29a,37a,102a,
104a,126a)
Ethyne (acetylene) (la,37a)
Propyne (methylacetylene) (la,37a,147a)
Cyclopropane (75a)
Cyclopentane (72a)
Cyclohexane (la,37a,43a,106a)
Methylcyclohexane (la,37a,43a)
Benzene (la,Ha,37a,43a,45a,50a,59a,
96a,128a)
Methylbenzene (toluene) (la,18a,37a,
43a,59a,143a)
Ethylbenzene (la,37a,101a)
1,2-Dimethylbenzene (o-xylene)
(la,37a,43a,59a,128a,l4Oa)
1,3-Dimethylbenzene (m-xylene) (la,37a,
43a,59a,128a,140a)
1,CDimethylbenzene (p-xylene) (la,37a,
43a,59a,128a)
n-Propylbenzene (la,37a,140a)
Isopropylbenzene (la,37a,101a)
Naphthalene (la,37a,89a)
Biphenyl (la,37a,87a)
6-27
1984
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No reproduction or networking permitted without license from IHS
--`,,-`-`,,`,,`,`,,`---
X = triple point.
n e broken lines indicate extrapolations beyond the limits of the available literature data.
Not for Resale
A P I TDB CHAPTERS6
SS
m 0732290
0536600 L T 7
m
6A2.13
PROCEDURE 6A2.13
SATURATED LIQUID DENSITIESOF PURE COMPONENTS
Discussion
This procedure, using the modified Rackett equation, and Procedure 6A2.15, using the COSTALD
method, are both recommended methods for the calculation of the saturated densities of pure liquids.
Equation (6A2.13-1) is applicable from the triple point to the critical point.
Where:
ps = saturated liquid density at temperature T, in pound-moles per cubic foot.
R = gas constant = 10.731 (pounds per square inch absolute) (cubic feet) per (pound-rnole)
(degree Rankine).
= reduced temperature, T/T,.
T = temperature, in degrees Rankine.
T, = critical temperature, in degrees Rankine.
pc = critical pressure, in pounds per square inch absolute.
ZRA= an empirically derived constant (see Table 6A2.11).
Procedure
--`,,-`-`,,`,,`,`,,`---
(6A2.13-1)
Step 1: Obtain the critical temperature and critical pressure from Chapter l .
Step 2: Obtain a ZRAvaluefrom Table 6A2.14. If the compound is not listed in Table 6A2.14 and
one or more experimental saturated liquid density values are available, calculate a Z ~ ~ v a l from
ue
equation (6A2.13-1). If the compound is not listed in Table 6A2.14 and no experimental saturated
liquid density data are available, the critical compressibility value in Chapter 2 may be used as an
estimate for ZRA.
Step 3: Calculate the reduced temperature and then calculate the desired density using equation
(6A2.13-1).
6-29
1992
Copyright American Petroleum Institute
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No reproduction or networking permitted without license from IHS
Not for Resale
A P I TDB CHAPTER*b
*X
m
0732290 0536601 033
m
6A2.13
COMMENTS ON PROCEDURE6A2.13
Purpose
An equation is given for calculating the saturated liquid densities of pure liquids. This equation has
an accuracy comparable to the COSTALD method given in Procedure 6A2.15. Many hydrocarbons
are also covered in Figures 6A2.1 through 6A2.12, which may be more convenient to use.
Limitations
The equation is generally applicable between the triple point and thecritical point. When the value
of ZRAis not available, a Z u should be calculated from any available density data using Step 2 of
the procedure. If no such data areavailable, Z, may be substituted for ZRA.
Reliability
Theaverage absolute deviations from experimental data with equation (6A2.13-1) were 0.7
percent for hydrocarbons and 1.2 percent for nonhydrocarbons (32a). The equation is very sensitive
to the value of ZRA, particularly in the region near the critical point. If Z, is used in place of Z,, the
average absolute deviations increased to 3 percent for both the hydrocarbons and the nonhydrocarbons.
Literature Source
Adapted from Rackett, J. Chem Eng. Data 15 514 (1970) as described by Spencer and Danner,
J. Chem. Eng. Data 17 236 (1972). ZR* values in Table 6A2.14 have been calculated by the
Technical Datu Book staff from experimental saturated density data or taken from Spencer and
Adler, J. Chem. Eng. Datu 23 82 (1978).
Example
The density of saturated liquid propane at 30 F is desired.
From Chapter 1,
T, = 206.06 F
p, = 616.00 pounds per square inch absolute
molecular weight = 44.10
From Table 6A2.14, 2,
= 0.2763.
T, = 206.06 + 459.7 = 665.8 R
T,=
30.0 + 459.7
= 0.736
665.8
From equation (6A2.13-1),
1 - (10.731) (665.8)
0.2763 [ 1.0 + ( I .O - 0.736) 2'7
PS
613.0
-
= (11.599)(0.2763)
]
["0+0'68351
= 1.3304 cubic feet per pound-mole
ps = 0.7517 pound-mole per cubic foot
= 0.7517 X -x44.10
62.43
= 0.5310 gram per millimeter
The experimental value (30a) is 0.5315 gram per milliliter.
6-30
Copyright American Petroleum Institute
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1992
--`,,-`-`,,`,,`,`,,`---
Not for Resale
A P I T D BC H A P T E R r b
**
m
0732270 0 5 3 b b 0 2 T 7 T
m
6A2.14
TABLE 6A2.14
INPUT PARAMETERS FOR EQUATIONS (6A2.13-1) AND (6A2.15-1)
FOR CALCULATING PURE SATURATED LIQUID DENSITIES
Liquid
ZRA
%RK
(CU
V*
ft / lb-mole)
Hydrocarbons
Paraffins
Methane
Ethane
Propane
n-Butane
2-Methylpropane(isobutane)
--`,,-`-`,,`,,`,`,,`---
0.2880
0.2819
0.2763
0.2730
0.2760
0.0108
0.0990
0.1517
0.1931
O. 1770
1.592
2.335
3.205
4.075
4.1 14
n-Pentane
2-Methylbutane(isopentane)
2,2-Dimethylpropane (neopentane)
n-Hexane
2-Methylpentane
0.2685
0.27 18
0.2763
0.2637
0.2673
0.2486
0.2275
O. 1964
0.3047
0.2781
4.987
4.959
5 .O07
5.898
5.890
3-Methylpentane
2,ZDimethylbutane
2,3-Dimethylbutane
n-Heptane
2-Methylhexane
0.2690
0.2733
0.2704
0.2610
0.2637
0.2773
0.2339
0.2476
0.3494
0.3282
5.820
5.821
5.783
6.895
6.846
3-Methylhexane
3-Ethylpentane
2,2-Dimethylpentane
2,3-Dimethylpentane
2,CDimethylpentane
0.2632
0.2664
0.2673
0.2636
0.2661
0.3216
0.3094
0.2879
0.2923
0.3018
6.778
6.669
6.768
6.611
6.810
3,3-Dimethylpentane
2,2,3-Trimethylbutane
n-Octane
2-Methylheptane
3-Methylheptane
0.2735
0.2728
0.2569
0.2581
0.2576
0.2672
0.2503
0.3962
0.3769
0.37 16
6.627
6.608
7.856
7.832
7.748
4-Methylheptane
3-Ethylhexane
2,2-Dimethylhexane
2,3-Dimethylhexane
2.2-Dimethylhexane
0.2588
0.2585
0.2639
0.2622
0.2658
0.3711
0.3678
0.3378
0.3472
0.3436
7.755
7.289
7.735
7.633
7.707
2,5-Dimethylhexane
3,3-Dimethylhexane
3,4-Dimethylhexane
2-Methyl-3-ethylpentane
3-Methyl-3-ethylpentane
0.2614
0.2601
0.2632
0.2612
0.2666
0.3576
0.3196
0.3381
0.3308
0.3047
7.782
7.095
7.564
7.095
7.289
2,2,3-Trimethylpentane
2,2,4-Trimethylpentane
2,3,3-Trimethylpentane
2,3,4-Trimethylpentane
2,2,3,3-Tetramethylbutane
0.2673
0.2682
0.2686
0.2656
0.2745
0.2970
0.303 1
0.2903
0.3161
0.2171
7.495
7.672
7.420
7.51 1
7.319
n-Nonane
2,2,5-Trimethylhexane
n-Decane
n-Undecane
n-Dodecane
0.2555
0.2637
0.2527
0.2500
0.247 1
0.4368
0.3567
0.4842
0.5362
0.5452
8.857
8.663
9.919
10.997
12.107
n-Tridecane
n-Tetradecane
n-Pentadecane
n-Hexadecane
0.2468
0.2270
0.2420
0.2386
0.6 186
0.5701
0.7083
0.747 1
13.323
14.452
15.654
16.882
1992
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No reproduction or networking permitted without license from IHS
6-31
Not for Resale
API T D B CHAPTER+b
+X
m 0732290 0536603 906 m
6A2.14
TABLE 6A2.14 (Continued)
Liquid
V*
(CUft / lb-mole)
ZUA
WSRK
Paraffins
n-Heptadecane
n-Octadecane
n-Nonadecane
n-Eicosane
0.2343
0.2292
0.7645
0.7946
0.8196
0.9119
17.954
19.205
20.368
22.032
Naphthenes
Cyclopropane
Cyclobutane
Cyclopentane
Methylcyclopentane
1,l-Dimethylcyclopentane
0.2743
0.2761
0.2709
0.27 12
O. 1348
O. 1866
O. 1943
0.2302
0.2721
2.579
4.165
5.096
6.013
5.937
6.062
6.127
6.081
4.950
Hydrocarbons
-
-
-
1-cis-2-Dimethylcyclopentane
1-trans-2-Dimethylcyclopentane
1-cis-3-Dimethylcyclopentane
1-trans-3-Dimethylcyclopentane
Cyclohexane
0.2729
0.2662
0.2698
0.2737
0.2678
0.2149
Methylcyclohexane
Cycloheptane
Cyclooctane
0.2702
0.2696
0.2667
0.2350
0.2430
0.2537
5.941
Olefins
Ethene (ethylene)
Propene (propylene)
1-Butene
cis-2-Butene
trans-2-Butene
0.28 13
0.2783
0.2735
0.2705
0.2722
0.0852
O. 1424
O. 1867
0.2030
0.2 182
2.098
2.930
3.808
3.702
3.792
2-Methylpropene (isobutylene)
1-Pentene
cis-2-Pentene
trans-2-Pentene
2-Methyl-1-butene
0.2727
0.2692
0.2687
0.2705
0.2607
O. 1893
0.2330
0.2406
0.2373
0.2287
3.795
4.727
4.605
4.692
4.625
3-Methyl-1-butene
2-Methyl-2-butene
1-Hexene
1-Heptene
0.2739
0.2571
0.2654
0.2614
0.2286
0.2767
0.2800
0.3310
4.710
4.6 18
5.621
6.589
1-Octene
1-Nonene
1-Decene
0.2565
0.2533
0.25 19
0.3747
0.4171
0.4645
7.545
8.543
9.632
0.2707
0.2686
0.2713
0.2677
O. 1594
0.2509
O. 1932
0.2235
O. 1470
2.355
3.497
3.527
4.312
4.311
0.2680
0.2707
0.2703
0.2709
0.2691
0.1162
O. 1583
O. 1873
0.2161
0.2469
O. 1305
4.392
4.31 1
1.807
2.577
3.450
3.374
0.2696
0.2645
0.2619
0.2108
0.264 1
0.3036
4.107
5.025
5.930
Diolefins and Acetylenes
F’ropadiene
1,2-Butadiene
1,3-Butadiene
1,2-Pentadiene
1-cis-3-Pentadiene
1-trans-3-Pentadiene
2-MethyLL3-butadiene
Ethyne (acetylene)
F’ropyne (methylacetylene)
1-Butyne
2-Butyne
Aromatics
Benzene
Methylbenzene (toluene)
Ethylbenzene
6-32
-
0.2281
-
1992
--`,,-`-`,,`,,`,`,,`---
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-
Not for Resale
A P I TDB
CHAPTERS6
SS
0732290 053bbO4 842
6A2.14
TABLE 6A2.14 (Continued)
V*
Liquid
(CU
fi / lb-mole)
ZRA
WSRK
0.2626
0.2594
0.2590
0.2599
0.3127
0.3260
0.3259
0.3462
5.884
5.977
5.991
6.885
0.2616
0.2578
0.2746
0.261 1
0.3377
0.3917
0.3659
0.30 19
6.842
7.883
7.833
6.142
Acids
Formic acid
Acetic acid
Propionic acid
Butyric acid
Isobutyric acid
0.2049
0.2242
0.2486
0.2482
0.2403
0.4730
0.4624
0.5 13 1
0.6041
0.6181
1.874
2.789
Valeric acid
Adipic acid
Stearic acid
0.2475
0.2295
0.2352
0.6269
0.6701
1.2312
7.759
21.513
0.2340
0.2523
0.2537
0.2508
0.5656
0.637 1
0.6279
0.6689
1.919
2.807
3.692
3.705
1-Butanol
2-Butanol
1-Pentanol
3-Pentanol
1 -Hexanol
0.2570
0.2568
0.2588
0.2666
0.2612
0.5945
0.5885
0.5938
0.7094
4.551
4.373
5.506
5.500
1-Decano1
Dodecanol
Ethylene glycol
Diethylene glycol
Glycerol
Phenol
0.2627
-
0.2477
0.2494
0.1918
0.2767
1.1256
1.2280
1.2006
1.9845
0.4259
13.268
3.396
5.642
6.598
4.500
0.28 16
0.3167
0.4442
0.0967
0.3064
1.603
2.433
4.200
2.323
3.332
0.3241
0.3502
0.3456
0.3967
4.042
4.860
5.056
6.020
0.4730
0.3965
0.3672
0.4624
0.5131
2.090
3.032
3.843
2.93 1
3.854
Hydrocarbons
Aromatics
1,2- Dimethylbenzene(o-xylene)
1,3-Dimethylbenzene (m-xylene)
1,4-Dimethylbenzene(p-xylene)
n-Propylbenzene
lsopropylbenzene (cumene)
n-Butylbenzene
Biphenyl
Naphthalene
Organics
Aldehydes and Ketones
Formaldehyde
Acetaldehyde
Furfural
Ketene
Acetone
Methyl ethyl ketone
Diethyl ketone
Methyl isopropylketone
Methyl isobutyl ketone
Amides
Formamide
n-Methylformamide
n, n-Dimethylformamide
Acetamide
Propionamide
-
0.223 1
0.2387
0.2448
-
0.2448
0.2524
0.2557
-
0.2589
O. 1983
0.2110
0.2242
0.2243
-
-
-
6-33
1992
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-
-
--`,,-`-`,,`,,`,`,,`---
Alcohols andGlycols
Methanol
Ethanol
1-Propanol
2-Propanol
-
Not for Resale
API
T D B CHAPTER86
88
m 0732290 0536605
789
m
6A2.14
TABLE 6A2.14 (Continued)
V*
Liquid
ZRA
WSRK
(CUft / lb-mole)
Organics
Amines and Anilines
Methylamine
Ethylamine
Propylamine
Isopropylamine
Butylamine
0.2597
0.2640
0.2644
0.2685
0.2666
0.28 13
0.285 1
0.2957
0.2785
0.3295
Isobutylamine
Dimethylamine
Diethylamine
Dipropylamine
Trimethylamine
0.2735
0.2642
0.2568
0.2691
0.2788
0.3627
0.3044
0.3045
Triethylamine
Aniline
n-Methylaniline
n, n-Dimethylaniline
0.2693
0.2607
0.2849
0.2558
0.3196
0.4041
0.2581
0.2587
0.2593
0.2553
0.2538
0.2537
0.2849
0.3 180
0.3254
0.361 1
Vinyl acetate
n-Propyl acetate
Methyl propionate
Ethyl propionate
Methyl n-butyrate
0.2608
0.2544
0.2568
0.2546
0.2564
0.3384
0.3941
Methyl isobutyrate
Methyl acrylate
Ethyl acrylate
0.2585
0.2560
0.2583
Esters
Methyl formate
Ethyl formate
n-Propyl formate
Methyl acetate
Ethyl acetate
Ethers
Dimethyl ether
Methyl ethyl ether
Methyl-n-butyl ether
Methyl isobutyl ether
Methyl vinyl ether
Diethyl ether
Ethyl vinyl ether
Diisopropyl ether
-
-
-
0.3807
0.2738
0.2683
0.2655
-
0.2643
-
0.2699
1.959
2.839
-
-
2.903
4.655
-
6.449
4.647
-
-
3.623
4.570
4.275
-
-
-
0.3373
0.3908
4.229
5.198
0.2036
0.2189
0.3137
0.3049
0.2489
2.710
3.550
5.402
5.413
3.221
0.2846
0.2673
0.3300
4.505
3.968
6.399
0.2125
1.688
Halogen Compounds
6-34
Methyl fluoride
Difluoromethane
Trifluoromethane
Carbon tetrafluoride
1,l-Difluoroethane
0.2491
0.2465
0.2587
0.2801
0.2534
1,1,1-Trifluoroethane
Perfluorocyclobutane
Peduoro-n-butane
Fluorobenzene
Hexafluorobenzene
0.25 18
0.2705
0.2699
0.2662
0.2567
Hexafluoroacetone
Trifluoroacetonitrile
Methyl chloride
Dichioromethane
0.2664
0.2664
0.2679
0.26 19
-
0.2672
0.1855
-
-
0.2434
-
0.1529
0.1916
-
4.328
-
-
2.183
2.830
1992
--`,,-`-`,,`,,`,`,,`---
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0.2529
-
Not for Resale
A P I TDB CHAPTER*b
**
0732290 053bbOb
615
m
6A2.14
TABLE 6A2.14 (Continued)
Liquid
ZRA
%RK
V*
(CU ft
/ lb-mole)
Halogen Compounds
Chloroform
Tetrachloromethane
Chloroethane
Chlorobenzene
Chlorodifluoromethane
ChIorotrifluoromethane
0.275 1
0.2721
0.2640
0.2650
0.2680
0.2797
0.2129
O. 1926
0.2876
0.2461
0.2192
o. 1800
3.596
4.41 1
2.976
4.895
2.622
2.894
Trichlorofluoromethane
Dichlorodifluoromethane
Ethyl bromide
Brornobenzene
Iodobenzene
0.2757
0.2779
0.2896
0.2637
0.2646
O. 1837
0.1796
0.2266
0.2481
3.941
3.439
3.306
5.132
-
-
Nitrogen compounds
Acetonitrile
Propionitrile
Butyronitrile
Benzonitrile
Nitromethane
Nitrobenzene
0.2010
0.2156
0.2286
0.2466
0.23 13
0.2473
0.3382
2.573
0.3566
0.3295
0.4348
5.217
2.605
5.349
Oxides
Ethylene oxide
Propylene oxide
0.2593
0.2622
0.21 14
2.154
-
-
Sulfides
Dimethyl sulfide
Methyl ethyl sulfide
Methyl n-propyl sulfide
Diethyl sulfide
Methyl isopropyl sulfide
0.27 13
0.2689
0.2653
0.267 1
0.2728
O. 1893
0.2435
0.2770
0.2938
0.2494
3.220
4.115
5.012
5.025
5.019
Methyl n-butyl sulfide
Ethyl n-propyl sulfide
Methyl sec-butyl sulfide
Methyl isobutyl sulfide
Ethyl isopropyl sulfide
0.2620
0.2643
0.2688
0.2683
0.27 13
0.3220
0.3250
0.2946
0.2933
0.2940
5.953
5.972
5.95 1
5.935
5.975
Methyl terr-butyl sulfide
Ethyl n-butyl sulfide
Di-n-propyl sulfide
n-Propyl isopropyl sulfide
Ethyl sec-butyl sulfide
0.2720
0.261 1
0.2615
0.2677
0.2658
0.2387
0.3730
0.3741
0.3428
0.3398
5.872
6.944
6.939
6.933
6.869
Ethyl isobutyl sulfide
Ethyl tuf-butyl sulfide
Diisopropyl sulfide
Di-n-butyl sulfide
Diisoamyl sulfide
Diallyl sulfide
0.2665
0.2704
0.2747
0.2561
0.2589
0.2525
0.3421
0.2848
0.3098
0.4824
0.6181
O. 1031
6.914
6.850
6.93 1
8.996
11.234
5.978
Ammonia
Argon
Carbon dioxide
Carbon disulfide
Carbon monoxide
0.2466
0.2933
0.2729
0.2850
0.2898
0.2520
1.123
1.208
1S03
2.707
1.476
Chlorine
Flourine
Hydrogen
Hydrogen bromide
0.2781
0.2886
0.3218
0.2855
0.0690
0.0588
-
-
lnorganics
-
0.0693
1.959
1.O72
1.O29
1.589
--`,,-`-`,,`,,`,`,,`---
0.2276
O. 1921
0.0663
6-35
1992
Copyright American Petroleum Institute
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No reproduction or networking permitted without license from IHS
-
Not for Resale
A P I T D B CHAPTERS6
S t
m
0732290053bb07
551
m
6A2.14
TABLE 6A2.14 (Continued)
V*
Liquid
ZRA
%RK
(CUft / lb-mole)
Hydrogen chloride
Hydrogen flouride
Hydrogen sulfide
Kzypton
Neon
0.2673
O. 1473
0.28 18
0.2901
0.3005
0.1322
0.3826
0.0827
0.0013
-
1.343
0.939
1.592
1.469
0.68 1
Nitric oxide
Nitrogen
Nitrogen dioxide
Nitrous oxide
Oxygen
0.2652
0.2893
0.2419
0.2748
0.2890
0.5846
0.0403
0.8486
0.1418
0.02 18
1.O65
1.444
1.460
1.570
1.182
lnorganics
Phosgene
Sulfur dioxide
Sulfur trioxide
Xenon
-
0.2792
0.2450.2667
0.4215 13
0.25
0.0115
0.2829
-
1
1.929
1.958
1.818
--`,,-`-`,,`,,`,`,,`---
6-36
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No reproduction or networking permitted without license from IHS
1992
Not for Resale
API
TDB CHAPTERvb
**
0732290 053bb08 498
m
6A2.15
PROCEDURE 6A2.15
SATURATED LIQUID DENSITIES OF PURE COMPONENTS
Discusslon
This method, using the COSTALD equation, and Procedure 6A2.13, using the modified
Rackett equation, are bothrecommendedmethodsfor
the calculation of the saturated
densities of pure liquids.
Equations (6A2.15-1) through (6A2.15-3) are applicable in the reduced temperature range
from 0.25 to 1.0.
1
-=
V'i)(l - OSRKV(i))
(6A2.15-1)
P.
v*
~2 = 1 + a(1 - Tc)"3+ b ( l -
+~
( -lT,) + d(1 - Tr)'"3
(6A2.15-2)
(6A2.15-3)
Where:
ps= saturated liquid density at temperature T , in pound-moles per cubic foot.
= characteristic volume, in cubic feet per pound-mole (see Table 6A2.14).
V
wSRK= acentric factor optimized for vapor pressure data in the Soave-Redlich-Kwong
equation of state (see Table 6A2.14).
T, = reduced temperature, TIT,.
T = temperature, in degrees Rankine.
T, = critical temperature, in degrees Rankine.
U = -S2816
1
C = -0.81446
e = -0.296123
g = -0.0427258
b = 1.43907
d = 0.190454
f = 0.386914
h = -0.0480645
Procedure
Step I: Obtain the critical temperature from Chapter 1.
Step 2: Obtain V* and wSRKvalues from Table 6A2.14. If the compound is not listed in
Table 6A2.14, the acentric factorW given in Chapter 2 may be used in place of wSRK,and the
critical volume given in Chapter 1 may be used in place of V * .
Step 3: Calculate the reduced temperature and then calculate the desired density using
equations (6A2.15-1) through (6A2.15-3).
1984
Copyright American Petroleum Institute
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No reproduction or networking permitted without license from IHS
--`,,-`-`,,`,,`,`,,`---
Not for Resale
6-37
A P I TDBCHAPTERtb
tf
m
0732290 O536609 324
m
6A2.15
COMMENTS ON PROCEDURE 6A2.15
Purpose
Equations are given for calculating the saturated liquid densities of pure liquids. This
method has an accuracy comparable to the Rackett equation given in Procedure 6A2.13.
Many hydrocarbons are also covered in Figures 6A2.1 through 6A2.12, which may be more
convenient to use.
Limitations
The equation is applicable in the reduced temperature range between 0.25 and 1.0. When
the values of wSRKand V * are not available, the acentric factor and the critical volume may
be used in their place.
Reliability
The average absolute deviations from experimental datawith this method were 0.8 percent
for hydrocarbons and 2.1 percent for nonhydrocarbons (32a). Somewhat larger errors are
obtained if the acentric factor and the critical volume are used in place of oSRK and V * .
Literature Source
The COSTALD method was developed by Hankinson and Thomson, AZChE Journal, 25
653 (1979). The values listed in Table 6A2.14 for OSRK and V * have been taken from the
above paper or from tabulated values obtained through personal communication with the
authors.
Example
--`,,-`-`,,`,,`,`,,`---
The density of saturated liquid propane at 30 F is desired.
From Chapter 1,
T, = 206.01 F
molecular weight = 44.097
From Table 6A2.14,
oSRK
= 0.1532,
and V * = 3.205 cubic feet per pound-mole.
T, = 206.01 + 459.7 = 665.7 R
30.0 + 459.7 = o.736
T, =
665.7
Using equations (6A2.15-2) and (6A2.15-3),
1+ (-1.52816)(1-
v':)=
+ (-0.81446)(1=
0.736)'" + (1.43907)(1- 0.736)2/3
0.736) + (0.190454)(1- 0.736)4"
0.4291
v;)= -0.296123 + (0.386914)(0.736) + (-0.0427258)(0.736)'+
(0.736 - 1.00001)
=
(-0.0480645)(0.736)3
0.2033
From equation (6A2.15-1),
1
- = (3.205)(0.4291)[1- (0.1532)(0.2033)]
PS
= 1.3325 cubic
feet per pound-mole
ps= 0.7505 pound-mole per cubic foot
= 0.7505 x 62:43 x
= 0.5301 gram
44.097
per milliliter
The experimental value (30a) is 0.5315 gram per milliliter.
6-38
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No reproduction or networking permitted without license from IHS
1984
Not for Resale
API
T D B CHAPTER*b
*X
m 0732290 0536630 O46 m
6A2.16
1O 0
50
F
M 6A2.16
SPECIFK GRAVITIES
OF
LIQUID HYDROCARBONS
AT ONE AThKWHERE
COW-TEMPERATURE RANGE
~
Y
O
[
9
\
IL
t
-50
i
c
Y
a
c
c
4
*c
o
RopLIf
>
4
0:
(3
--`,,-`-`,,`,,`,`,,`---
Note:
SeeBackOfFigureforCarments
See Table 6A2.17 fw Temperoture
METIUN
o
Ranges
00 NOT EXTRAPOLATE
O. 4 0
6-39
1984
Copyright American Petroleum Institute
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No reproduction or networking permitted without license from IHS
J
Not for Resale
A P I TDB CHAPTERS6
SS
m 0732290 053663l1 T82 m
6A2.16
COMMENTS ON FIGURE 6A2.16
Purpose
Specific gravity-temperature data are presented for pure liquid hydrocarbons at 1 atmosphere pressure.
Limitations
The nomograph is valid only for liquids within the temperature ranges specified for each
hydrocarbon in Table 6A2.17.
Reliability
Within the specified temperature limits, the nomograph will reproduce the experimental
data with less than 1 percent error.
Literature Source
The data used in constructing the nomograph were obtained from API Research Project
44, Selected Values of Physical and Thermodynamic Properties of Hydrocarbons and Related
Compounds, Thermodynamics Research Center, Texas A&M University, A&M Press, College Station, Texas (loose-leaf data sheets, extant 1971).
Example
1984
6-40
Copyright American Petroleum Institute
Provided by IHS under license with API
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Not for Resale
--`,,-`-`,,`,,`,`,,`---
Estimate the liquid Wensity of n-butane at -100 F and 1 atmosphere.
From Table 6A2.17, this temperature is determined to be within the valid range of the
nomograph. The pivot point labeled n-butane is located on the nomograph. A straight line
from -100 F on the temperature scale drawn through the pivot point intersects the specific
gravity scale at 0.673.
The experimental value (la) is 0.674.
A P I TDB CHAPTERmb
**
m
0732290 053bbL2 919
m
6A2.I 7
TABLE 6A2.17
TEMPERATURE RANGES FOR SPECIFIC GRAVITY OF LIQUID HYDROCARBONS
AT ONE ATMOSPHERE (LOW TEMPERATURE)
Temperature Range
(F)
Hydrocarbon
Paraffins
Methane
Ethane
Propane
n -Butane
2-Methylpropane (isobutane)
-292
-202
-166
-112
-130
to -274
to -130
to -58
to -4
to+14
n-pentane
2-Methylbutane (isopentane)
2,2-Dimethylpropane (neopentane)
n -Hexane
n -Heptane
-130
-58
+32
-130
-130
to
to
to
to
to
+32
+50
+50
+32
+32
3-Ethylpentane
2,2-Dimethylpentane
n -Octane
2,2,4-Trimethylpentane (isooctane)
n -Nonane
-166
-112
-58
-148
-58
to
to
to
to
to
+32
+32
+32
+32
+32
Naphthene
-184 to+32
Methylcyclohexane
Oleflns
-256
-292
-166
-130
-76
Ethene (ethylene)
Propene (propylene)
l-Butene
l-Pentene
l-Hexene
to
to
to
to
to
-166
-58
+14
+32
+32
--`,,-`-`,,`,,`,`,,`---
6-41
1984
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
**
A P I TDBCHAPTER*b
m
0732290 0536633 855
m
6A2.18
SPECIFICGRAVITY
OF LIQUID PARAFFINS
A N D OLEFINS
L
J
1
Q
z
ir
Y
X
L
1984
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
6-43
--`,,-`-`,,`,,`,`,,`---
Not for Resale
A P I TDB
CHAPTERS6
ff
H 0732290 053bblV 791
m
6A2.19
TABLE 6A2.19
GRID COORDINATES AND TEMPERATURE RANGES FOR SPECIFIC GRAVITY
OF LIQUID PARAFFINS AND OLEFWS AT ATMOSPHERIC PRESSURE
Hydrocarbon
Temperature
Range
(F)
Grid Coordinates for
Figure 6A2.18
X
Y
1.20
0.85
1.35
0.73
1.18
Paraffins
--`,,-`-`,,`,,`,`,,`---
n -Hexane
2-Methylpentane
3-Methylpentane
2,2-Dimethylbutane
2,3-Dimethylbutane
14 to
14 to
14 to
32 to
14 to
140
140
140
86
122
n -Heptane
2-Methylhexane
3-Methylhexane
3-Ethylpentane
2,2-Dimethylpentane
14 to
32 to
50 to
14 to
14 to
194
140
104
194
158
0.08
1.10
1.00
1.25
1.00
1.40
1.22
1.30
1.13
1.25
2,3-Dimethylpentane
2,4-Dimethylpentane
3,3-Dimethylpentane
2,2,3-Trimethylbutane
n-Octane
32 to
32 to
32 to
14 to
14 to
122
122
122
122
248
1.30
1.15
1.25
1.13
1.25
2.80
1.75
2.70
1.75
3.20
2-Methylheptane
3-Methylheptane
4-Methylheptane
3-Ethylhexane
2,ZDimethylhexane
32 to
32 to
14 to
32 to
32 to
140
140
140
140
122
1.51
1.35
1.50
1.40
1.43
3.00
3.30
3.31
3.68
2.84
2,3-Dimethylhexane
2,CDimethylhexane
2,s-Dimethylhexane
3,3-Dimethylhexane
3,CDimethylhexane
32 to
32 to
14 to
32 to
32 to
122
122
212
122
140
1.35
1.20
1.33
1.42
1.10
3.58
3.00
2.73
3.55
3.85
2-Methyl-3-ethylpentane
3-Methyl-3-ethylpentane
2,2,3-Trimethylpentane
2,2,4-Trimethylpentane
2,3,3-Trimethylpentane
14 to
32 to
32 to
14 to
32 to
122
122
122
194
122
1.10
1.31
1.45
1.30
1.51
3.85
4.40
3.81
2.65
4.33
2,3,4-Trimethylpentane
n -Nonane
n -Decane
4-n -Propylheptane
n -Undecane
2-Methyldecane
n -Dodecane
n -Tridecane
5-n-Butylnonane
n -Tetradecane
32 to 122
14 to 248
14 to 284
32 to 210
14 to 266
32 to 210
32 to 284
32 to 284
32 to 210
50 to 302
1.45
1.45
1.63
1.56
1.68
1.72
1.78
1.80
1.75
1.82
3.95
3.90
4.45
4.80
5.08
4.95
5.54
5.92
6.10
6.28
7-Methyltridecane
2,2,3,3,5,6,6-Heptamethylheptane
n -Pentadecane
n -Hexadecane
2"ethylpentadecane
32 to
32 to
50 to
68 to
32 to
1.90
2.01
1.80
1.88
1.95
6.32
8.28
6.58
6.87
6.75
210
210
302
302
210
6-45
1984
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
2.35
2.00
2.40
2.88
1.80
Not for Resale
API TDB CHAPTERtb t t W 0732290 0536615 b2B W
6A2.19
TABLE 6A2.19 (Continued)
Temperature
Range
(F)
Grid Coordinates for
Figure 6A2.18
X
Y
86 to 356
86 to 248
104 to 212
104 to 338
104 to 338
1.90
1.95
2.05
2.35
2.23
7.10
7.35
32 to
32 to
32 to
212 to
302 to
210
210
210
572
572
2.15
2.17
2.20
2.30
2.40
8.18
8.33
8.63
8.98
9.70
Olefins
1-Pentene
1-Hexene
1-Heptene
1-Octene
1-Nonene
14 to
14 to
32 to
32 to
32 to
50
140
194
248
248
0.71
0.90
1.13
1.39
1S 8
0.31
1.69
2.83
3.73
4.50
1-Decene
1-Undecene
1-Dodecene
1-Tridecene
1-Tetradecene
32 to 248
32 to 248
32 to 248
32 to 248
32 to 248
1.57
1.60
1.80
1.80
1.85
5.04
5.51
6.00
6.37
6.70
1-Pentadecene
1-Hexadecene
1-Heptadecene
1-Octadecene
1-Nonadecene
1-Eicosene
32 to 104
50 to 248
68 to 248
68 to 248
86 to 248
86 to 248
1.88
1.93
1.90
1.92
1.97
1.95
6.98
7.23
7.42
7.61
7.80
7.95
Hydrocarbon
ParaffIns
n-Heptadecane
n -0ctadecane
n -Nonadecane
n -Eicosane
n-Heneicosane
n -TriCosane
n -Tetracosane
n -Hexamsane
n-Triacontane
n-Tetracontane
6-46
7.85
7.98
1984
--`,,-`-`,,`,,`,`,,`---
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
7.55
Not for Resale
A P I TDB
CHAPTER+h
**
m
0 3 3 2 2 9 0 0536616 5 6 4
m
6A2.20
1.16
FIGURE 6A2 20
SPECIFIC
GRAVITY
OF LIQUID NAPHTHENES
1.10
AND AROMATICS
AT ATMOSPHERIC PRESSURE
1.O5
12
11
-
10
-
1.o0
9 -
0.95
u.
8 -
O
t
2
u.
c
7 -
f4
0.90
c
6 -
t
U
>
Ir
’
6 .
2u
4
0.86
--`,,-`-`,,`,,`,`,,`---
Y
Y
M
CL
v)
3.
0.80
2i
t
1
0.76
O
O
Note
See
Bock
of Flgure for Comments
S e e Table 6 A 2 2 for Temperature
Ranges and Grld Coordlnoter
DO NOT EXTRAPOLATE
1
2
X
3
4
0.70
0.66
6-47
1984
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No reproduction or networking permitted without license from IHS
Not for Resale
A P I TDB CHAPTERbb t b
m
0732290 0536637 Y T O
m
6A2.18-6A2.20
COMMENTS ON FIGURES 6A2.18 and 6A2.20
Purpose
Specific gravity-temperature data are presented for pure hydrocarbons at 1 atmosphere
pressure.
Limitations
The nomograph is valid only within the temperature ranges specified for each compound
in Tables 6A2.19 and 6A2.21.
Reliability
Within the specified temperature limits, the nomograph will reproduce the experimental
data with less than 1 percent error.
Literature Sources
The data used in constructing the nomograph were obtained from API Research Project
44, Selected Values of Physical and Thermodynamic Properties of Hydrocarbons and Related
Compounds, Thermodynamics Research Center, Texas A&M University, A&M Press, College Station, Texas (loose-leaf data sheets, extant 1971). Data were also obtained from API
Research Project 42, Properties of Hydrocarbons of High Molecular Weight Synthesized by
Research Project 42 of the American Petroleum Institute, 1 9 4 M 6 , American Petroleum
Institute, New York (1967). A small amount of data were takenfrom Egloff, Physical
Constants of Hydrocarbons, Vols. I-IV, Reinhold Publishing Corp., New York (193S53).
Example
--`,,-`-`,,`,,`,`,,`---
Estimate the density of liquid benzene at 122 F and 1 atmosphere pressure.
From Table 6A2.21, 122 F is determined to be within the temperature range for this
compound on thenomograph. The X and Y grid coordinates of 0.82 and 4.29 are first located
on the nomograph grid (Figure 6A2.20) to locate the pivot point for benzene.
A straight line from 122 F on the temperature scale drawn through the pivot point intersects the specific gravity scale at 0.846. The experimental value is 0.8469.
6-48
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1984
Not for Resale
A P I TDBCHAPTER86
X 8
m
0732290 053bb18 337
m
6A2.21
TABLE 6A2.21
GRID COORDINATES AND TEMPERATURE RANGESFOR SPECIFIC GRAVITY
OF LIQUID NAPHTHENES AND AROMATICS AT ATMOSPHERIC PRESSURE
Hydrocarbon
Temperature
Range
(F)
Grid Coordinates for
Figure 6A2.20
x
Y
Naphthenes
Cyclopentane
Methylcyclopentane
Ethylcyclopentane
n -Propylcyclopentane
n-Butylcyclopentane
14 to 104
14 to 158
14 to 212
14 to 230
14 to 230
2.65
2.80
2.95
3.13
3.10
n-Pentylcyclopentane
n -Hexylcyclopentane
n -Heptylcyclopentane
n -0ctylcyclopentane
n-Nonylcyclopentane
14 to
14 to
14 to
14 to
14 to
n -Decylcyclopentane
n-Undecylcyclopentane
n-Dodecylcyclopentane
n -Tridecylcyclopentane
n-Tetradecylcyclopentane
14 to 230
14 to 230
32 to 230
50 to 230
50 to 230
3.10
3.25
3.31
3.28
3.27
3.35
3.30
3.43
3.35
3.30
1.55
1.60
2.18
2.50
2.78
3.00
3.15
3.30
3.44
3.50
3.63
3.75
3.77
3.87
3.92
n-Pentadecylcyclopentane
n -Hexadecylcyclopentane
Cyclohexane
Methylcyclohexane
Ethylcyclohexane
68 to 230
86 to 230
50 to 176
14 to 212
14 to 230
3.40
3.43
2.86
3.00
3.12
3.99
4.02
2.60
2.30
2.89
n -Propylcyclohexane
n -Butylcyclohexane
n -Pentylcyclohexane
n -Hexylcyclohexane
n-Heptylcyclohexane
n-Octylcyclohexane
2-Cyclohexyloctane
n -Nonylcyclohexane
n -Decylcyclohexane
n 4Jndecylcyclohexane
14 to 230
14 to 212
14 to 230
14 to 230
14 to 230
3.18
3.23
3.41
3.40
3.42
3.05
3.23
3.40
3.51
3.61
14 to 230
32 to 210
68 to 230
32 to 230
50 to 230
3.50
2.05
3.42
3.40
3.45
3.70
3.10
3.80
3.90
3.95
n -Dodecylcyclohexane
n -Tridecyclohexane
n -Tetradecyclohexane
n -Pentadecyclohexane
n -Hexadecyclohexane
68 to 230
68 to 230
86 to 230
86 to 230
104 to 230
3.58
3.43
3.46
3.44
3.38
4.00
4.08
4.11
4.17
4.22
l-Cyclohexyleicosane
Spiro(4S)decane
Spiro(5,6)dodecane
Bicyclopentyl
32 to 210
32 to 150
32 to 210
32 to 210
32 to 210
2.34
1.57
1.81
2.01
1.85
3.43
4.31
4.65
5.50
4.25
Spiro(5,5)undecane
Bicyclohexyl
cis-Decahydronaphthalene
trans -Decahydronaphthalene
2-n-Butyldecahydronaphthalene
2-Decyldecahydronaphthalene
32 to
68 to
32 to
32 to
32 to
32 to
2.06
2.12
1.92
1.88
2.08
2.26
5.09
5.00
5.13
4.42
4.70
4.53
cis -0,3,3-Bicyclooctane
210
210
210
210
210
210
6-49
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230
230
230
230
230
Not for Resale
6A2.21
TABLE 6A2.21 (Continued)
Hydrocarbon
Temperature
Range
(F)
Grid Coordinates for
Figure 6A2.20
X
Y
Naphthenes
--`,,-`-`,,`,,`,`,,`---
1,2,3,4,5,6,7,8-0ctahydroanthracene
Perhydroanthracene
Perhydrophenanthrene
9-n -Dodecylperhydroanthracene
2-n-Dodecylperhydrophenanthrene
9-n -Dodecylperhydrophenanthrene
32 to
32 to
32 to
32 to
68 to
32 to
210
210
210
210
210
210
2.20
2.04
2.20
2.28
2.60
2.31
9.30
6.37
6.80
5.74
5.70
5.57
Benzene
Methylbenzene (toluene)
Ethylbenzene
1,2-Dimethylbenzene (o-xylene)
1,3-Dimethylbenzene (m-xylene)
50 to
14 to
14 to
14 to
14 to
176
230
230
494
158
O. 82
1.37
1.41
1.so
1.so
1,4-Dimethylbenzene (p-xylene)
n -Propylbenzene
Isopropylbenzene
1-Methyl-2-ethylbenzene
1-Methyl-3-ethylbenzene
68 to 158
14 to 248
14 to 194
50 to 104
50 to 104
1S 4
1.52
1.54
1.71
1.60
4.29
4.11
4.18
4.60
4.11
4.04
4.09
4.09
4.70
4.20
l-Methyl-4-ethylbenzene
1,2,3-Trimethylbenzene
1,2,4-Trimethylbenzene
1,3,5-Trimethylbenzene
n-Butylbenzene
32 to 176
32 to 104
32 to 158
32 to 212
14 to 210
1.64
1.70
1.61
1.60
1.68
4.09
5.10
4.52
4.19
4.08
n -Pentylbenzene
n -Hexylbenzene
n-Heptylbenzene
n-Octylbenzene
n-Nonylbenzene
n-Decylbenzene
n-Undecylbenzene
n -Dodecylbenzene
n-Tridecylbenzene
n-Tetradecylbenzene
14 to 356
14 to 356
14 to 356
14 to 356
14 to 356
14 to 356
14 to 356
50 to 230
40 to 356
68 to 356
2.80
1.84
1.89
1.93
2.01
2.03
2.07
2.07
2.10
2.10
86 to 356
86 to 356
32 to 210
32 to 210
100 to 210
2.10
2.11
2.30
2.31
1.77
32 to 210
32 to 210
32 to 210
68 to 210
32 to 210
1.82
1.81
2.01
2.24
1.95
32 to 210
32 to 210
140 to 392
32 to 302
32 to 210
1.73
1.69
1.69
2.30
1.79
4.05
4.06
4.05
4.05
4.05
4.05
4.05
4.06
4.07
4.07
4.07
4.08
4.02
4.02
8.45
7.98
8.27
6.91
6.08
7.27
10.60
11.10
9.00
8.99
8.49
Aromatics
n -Pentadecylbenzene
n-Hexadecylbenzene
1,3-Di-n-decylbenzene
1,4-Di-n-decylbenzene
Diphenylmethane
1,2-Diphenylethane
1,l-Diphenylethane
1,l-Diphenylheptane
1,l-Diphenyltetradecane
1,l-Diphenyl-l-heptene
1,2-Diphenylbenzene
1,3-Diphenylbenzene
Naphthalene
l-Methylnaphthalene
2"ethylnaphthalene
6-50
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A P I TDB CHAPTERxb x *
m
0732290 0536620 T95
m
6142.21
TABLE 6A2.21 (Continued)
Hydrocarbon
Temperature
Range
(F)
Grid Coordinates for
Figure 6A2.20
X
Y
--`,,-`-`,,`,,`,`,,`---
Aromatics
l-Ethylnaphthalene
2-Ethylnaphthalene
1,2-Dimethylnaphthalene
1,6-Dimethylnaphthalene
l-n -Propylnaphthalene
32 to
32 to
32 to
32 to
32 to
284
284
284
284
284
2.08
2.31
2.11
2.10
2.18
8.72
8.28
9.07
8.59
8.25
l-n -Butylnaphthalene
2-n-Butylnaphthalene
l-t-Butylnaphthalene
2-t -Butylnaphthalene
l-n-Pentylnaphthalene
32 to 284
32 to 210
32 to 210
32 to 210
32 to 284
2.01
1.96
1.99
1.92
2.13
7.74
7.37
8.20
7.43
7.51
l-n-Hexylnaphthalene
l-n-Octylnaphthalene
l-n -Nonylnaphthalene
l-n -Decylnaphthalene
2-n -Butyl-2-n-hexylnaphthalene
32 to 284
32 to 284
32 to 176
32 to 176
32 to 210
2.10
2.00
2.13
2.19
2.05
7.20
6.71
6.59
6.46
6.41
9-n -Butyl-l-n -hexylnaphthalene
l-n 4Jndecylnaphthalene
l-n -Dodecylnaphthalene
l-alpha-Naphthylpentadecane
32 to 210
68 to 176
68 to 176
32 to 210
2.20
2.09
2.10
2.27
6.38
6.29
6.12
5.98
32 to 210
32 to 210
213 to 338
32 to 210
2.18
2.29
-2.25
2.03
10.20
7.91
-12.22
11.59
9-n -Butylanthracene
9-n -Dodecylanthracene
Phenanthrene
4,5-Dimethylphenanthrene
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API TDB CHAPTERab
*X
m
0 7 3 2 2 9 0 0536623 921
m
6A2.22
0.3
0.4
0.5
0.6
1.25
FIGURE 6A2.22
DENSITIES
1.20
,20
OF COMPRESSED
'URE L IQUI D.HYDROCARBONS
1.15
J5
N D THEIR DEFINED MIXTURES
TECHNICAL DATA BOOK
1.lo
,lo
1.05
1.O5
4 1.00
1.00
V
8
Cr'
9
6F
Lu
oi
8V
0.95
Ji 0.95
Z
:
--`,,-`-`,,`,,`,`,,`---
0.90
0.90
0.85
0.85
0.80
0.80
0.3
0.4
0.5
O.7
0.6
0.8
0.9
1 .o
REDUCEDTEMPERATURE , T,
6-53
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API TDB CHAPTERvb
**
m 0732290 0536622 B b B m
6A2.22
COMMENTS ON FIGURE 6A2.22
Purpose
The effect of temperature and pressure on the densities of pure liquid hydrocarbons and
their defined mixtures is estimated from this figure. One input density is required. In using
this figure for mixtures, follow Procedure 6A3.3
Discussion
The correlation is based on the relationship CJp1 = Cdp2 = constant, where pl and pz
represent two densities and C, and C, represent the corresponding density correlation
factors.
Where this relation holds, any density maybe expressed as a function of one known
density:
P2
=
c
2
PlG
(6A2.22-1)
Where p is the density in units of weight per volume.
Reliability
The average error in estimating the density of a pure hydrocarbon is 1percent. However,
errors up to 10 percent can be expected at reduced temperatures greater than 0.95.
Notation
C = an empirical density correlation factor (explained above).
T, = reduced temperature, TIT,.
T = temperature, in degrees Rankine.
T, = critical temperature, in degrees Rankine.
pr= reduced pressure, p/pc.
p = pressure, in pounds per square inch.
p c = critical pressure, in pounds per square inch.
Special Comment
In Figure 6A2.22, the saturation line can be considered pl.= O for interpolation. An
average error of 1 percent can be expected in this case.
Literature Source
Figure adapted from Lu, Chem. Eng. 66 [9] 137 (1959).
Example
Estimate the liquid density of n -nonane at 220 F and 1000 pounds per square inch absolute.
From Chapter 1, T, = 610.7 F; p c = 332 pounds per square inch absolute; pm = 44.94
pounds per cubic foot. The reference condition, denoted by subscript 1, is 60 F and 1
atmosphere. Therefore,
60 + 459.7 - o.486
+ 459.7 -
= 610.7
p
=-=(J
l4
332
.O443
Tr2
200 + 459.7 - o.635
+ 459.7 -
= 610.7
1000
pr2= 332 = 3.01
From Figure 6A2.22, C, = 1.077 and C2= 0.998. Using equation (6A2.22-1),
pz = 44.94 -= 41.64
pounds per cubic foot
The experimental value (19a) is 41.11 pounds per cubic foot.
6-54
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A P I TDB CHAPTER*b t*
0732290 053bb23 7 T 4
6A2.23
PROCEDURE 6A2.23
ANALYTICAL METHOD FOR THE DENSITIES OF COMPRESSED PURE LIQUIDS
Discussion
The following equation is to be used to calculate densities of compressed pure liquids. It
is applicable in the pressure range from the saturation pressure to 10,000 pounds per square
inch absolute.
(6A2.23-1)
B
PC
-=
-1
+ ü(1-
TJ”’
+ 6(1 - T,)” + d(1-
T,) + é ( l -
(6A2.23-2)
(6A2.23-3)
(6A2.23-4)
Where:
p = liquid density at temperature T and pressure P , in pound-moles per cubic foot.
ps= saturated liquid density at temperature T , in pound-moles per cubic foot.
p = pressure, in pounds per square inch absolute.
p s = vapor pressure at temperature T , in pounds per square inch absolute.
p c = critical pressure, in pounds per square inch absolute.
T, = reduced temperature, TIT,.
T =temperature, in degrees Rankine.
T, = critical temperature, in degrees Rankine.
wSRK= acentric factor optimized for vapor pressure data in the Soave-Redlich-Kwong
equation of state Gee Table 6A2.14).
4 = -9.070217
d_= -135.1102
g = 0.250047
= 0.0861488
b = 62.45326
f=
4.79594
h = 1.14188
k = 0.0344483
i
Procedure
Step 1: Obtain the critical pressure and critical temperature from Chapter 1.
Step 2: Obtain wSRK from Table 6A2.14. If the compound is not included in this table, the
acentric factor from Chapter 2 may be substituted for wSRK.
Step 3: Calculate the reduced temperature.
Step 4: Obtain the saturated liquid density using experimental data, or calculate it using
figures or procedures given in this chapter.
Step 5: Obtain the saturation vapor pressure using experimental vapor pressure data, or
calculate it using figures or procedures given in Chapter 5.
Step 6: Substitute the saturated density, reduced temperature, vapor pressure, critical
pressure, and wSRKin equations (6A2.23-1) through (6A2.23-4) to obtain the liquid density
at the desired temperature and pressure.
6-55
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A P I TDB CHAPTERxb
X*
m 0732290
053bb2V 630 W
6A2.23
COMMENTS ON PROCEDURE 6A2.23
Purpose
The procedure is presentedas an alternate analyticalmethod to calculate the effectof temperature
and pressure on the densities of pure liquids.
Limitations
This equation was found to work well for reduced temperatures below 0.95.
proven satisfactory when tested against a few nonhydrocarbons.
This method has
Reliability
The average absolute deviationsfrom experimental data were 1.2 percent for pure hydrocarbons
and 2.1 percent for a setof 13 nonhydrocarbon liquids (32a).
Literature Source
AIChE J o u m l 2 8 671 (1982).
The equation was developed by Thomson, Brobst, and Hankinson,
Example
From Table 6A2.14,OSRK= 0.3962, and Z,
T = -T=
r
T,
= 0.2569.
212 + 459.7 = o.656
564.22 +459.7
Using equation (6A2.13-1) the saturated liquid density is calculated:
1 - (10.731)
(564.22
360.6
PS
"
--`,,-`-`,,`,,`,`,,`---
Estimate the liquid density of n-octane at 212
F and 4410 pounds per square inch absolute.
From Chapter 1,
T, = 564.22 F
pc = 360.6 pounds per square inch absolute
molecular weight = 114.232
+ 459.7)
exp0.2569
[ +(
1
1-
212 + 459.7
564.22 +459.7
T'']
= 2.8742 cubic feet per pound-mole
From Chapter2, the acentric factor W = 0.3962.
Using the procedure given in Chapter5, the saturation vapor pressure is calculated:
ln P;" = (-2.81 12) + (0.3962) (-2.95)
P;" =
PS
-
=0.01869
PC
p s = 6.74 pounds per square inch absolute
Substituting into equations (6A2.23-2) through (6A2.23-4) gives
C = 0.086148 + (0.034483) (0.3998) = 0.099934
e" = exp[4.79594+ 0.250047(0.3998) + 1.14188(0.3998)2] = 160.5
B = 360.6[-1- 9.070217(0.344)" + 62.45326(0.344)u3 -135.1102(0.344)
= 5594.5 poundsper square inch absolute
+ 160.5(0.344)4"]
(5594.5 + 4410)
(5594.5 + 6.74)
P
= 2.708 cubic feet per pound-mole
p = 0.3693 pound-mole per cubic foot
= 0.3693 X
~
62.43
x 114.232
= 0.6758 gram per milliliter
The experimental value (41a) is 0.6769 gram
per milliliter.
6-56
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A P I TDB CHAPTERtb
**
m
0732290 053bb25 5 7 7
m
6A3.1
PROCEDURE 6A3.1
DENSITIES OF DEFINED LIQUID MIXTURES
AT THEIR BUBBLE POINTS
Discussion
This procedure, using the modified Rackett equation, and Procedure 6A3.2, using the COSTALD
method, are both recommended methods for the calculation of the densities of defined liquid mixtures
at their bubble points.
Equation (6A3.1-1) is applicable up to a reduced temperature of 0.95.
(6A3.1-1)
n
=
,AR'
c
(6A3.1-2)
%'%Ai
i= 1
T, = TIT,,
n
n
(6A3.1-3)
(6A3.1-4)
(6A3.1-5)
C
j =1
(6A3.1-6)
(6A3.1-7)
Where:
p = liquid density at the bubble point, in pound-moles per cubic foot.
bp
R = gas constant, 10.731 (pounds per square inch absolute) (cubic feet) per (pound-mole)
(degree Rankine).
xi = mole fraction of component i.
T = critical temperature of component i, in degrees Rankine.
ci
p = critical pressure of Component i, in pounds per square inch.
'i
V = critical volume of component i, in cubic feet per pound-mole.
"i
ZRAi
= an empirically derived constant for component i (see Table 6A2.14).
T = temperature, in degrees Rankine.
Step I: Obtain the critical temperatures, critical pressures, critical volumes, and molecular weights
from Chapter 1. For each component of the defined mixture obtain ZRAifrom Table 6A2.14. If ZRA,
is not available, calculate a value from equation (6A2.13-1) using any experimental density value
value in Chapter 2 may be used as an
available for component i. If no such data are available, the Zci
estimate for ZRA, .
Step 2: Compute the molar average ZRA,using equation (6A3.1-2).
Step 3: The mixture correspondence temperature, T,, , is computed using equations (6A3.1-4)
through (6A3.1-7). For desk calculation purposes, a molar average critical temperature may be used.
Step 4: Compute thereduced temperature.
Step 5: Compute the bubble point density from equation (6A3.1-1).
6-57
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--`,,-`-`,,`,,`,`,,`---
Procedure
Not for Resale
**
A P I TDBCHAPTERxb
m 0732290
0 5 3 b b 2 b 403
m
6A3.1
COMMENTS ON PROCEDURE6A3.1
Purpose
Procedure 6A3.1 is to be used to predict the density of a liquid mixture at its bubble point. This
procedure has an accuracy comparable to the COSTALD method given inProcedure 6A3.2.
Special Comments
This procedure may be used to predict the density of defined mixturescontaining inorganic gases
such as hydrogen, hydrogen sulfide, carbondioxide, and nitrogen. Values of ZRAfor inorganics are
given in Table 6A2.14.
Limitations
The procedure should not beapplied at reduced temperaturesgreater than 0.95.
The procedure should not be used for mixtures containing more than 0.5 mole fraction carbon
dioxide or nitrogen, or for mixtures containing more than 0.45 molefraction hydrogen.
Reliability
This method has beenevaluated only with binarydata. Errors in the calculated densities are about
2.5 percent using this method. Errors may be as high as 20 percent as the critical temperature is
reached. For mixtures containing inorganics, the error is about 4 percent. As the critical region is
approached, errors as high as 30 percent can beobtained. For mixtures containing more than50 mole
percent carbon dioxide or hydrogen, errors in the rangeof 15 to 30 percent should be expected. For
systems with more thantwo components, no estimate of the errors is available.
If the molar average pseudocritical temperature is used for desk calculation purposes, an average
error of 7 percent should be expected.
Literature Source
The equation was developed by Spencer and Danner,J. C'hem. Eng. Data 18 230 (1973).
Example
Estimate the bubble point density of an ethane-n-heptane mixture at 91 F, The mixture contains
58.71 percent ethane.
Chapter 1 gives the following data for the two components:
Property
Critical temperature, F
Critical pressure, psia
Critical volume, CU ft per lb
Molecular weight
100.205
89.92
706.50
0.0788
5 12.70
396.8
0.0691
--`,,-`-`,,`,,`,`,,`---
Ethane
30.070
From Table 6A2.14, Z R , (ethane) = 0.2819, and ZR, (n-heptane) = 0.2610.
2
1
89.92 + 459.7 = 549.62 R
TI =
Tc2 =
512.70 + 459.7 = 972.4 R
ZRA, = (0.5871) (0.2819) + (0.4129) (0.2610) = 0.2733
By equation (6A3.1-5),
(0.587 1) (0.0788) (30.070)
+ (0.4129) (0.0691) (100.205)]
= [ (0.5871) (0.0788) (30.070)
= 0.3273
92= 1 - Q
(for binary systems)
= 1 - 0.3273
= 0.6727
1992
6-58
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API TDB CHAPTER*b
*X
m
0732290 05366217 34T
m
6A3.1
Using equation (6A3.1-7) and critical volume per mole,
kll
= k22 = o
From equation (6A3. 1-6),
T,I I = 549.62R
= 972.4 R
= J(549.62)(972.4) (1 -0.0465) = 697.1 R
T,12 =
Using equation (6A3.1-4), the mixture correspondence temperatureis calculated.
T,, = (0.3273)2 (549.62) + (0.6727)2 (972.4) + (2.0) (0.3273) (0.6727) (697.2)
= 806R
The reduced temperatureof the mixture is
The bubble point densityis now calculatedfrom equation(6A3.1-1).
1
- = ( 10.731)
(972.4)
(0.4129)
(549.62)
(0.5871)
706.50
-+
396.8
1
(0.2733)
1 + ( 1 - 0.6833?’7
1
= 1.6914 cubic feet per pound-mole
p
= 0.5912 pound-moles per cubic foot
bp
--`,,-`-`,,`,,`,`,,`---
= (0.5912)
( 1]
62.43
[ (0.5871) (30.070)
+ (0.4129) (100.205) 1
= 0.5600 gram per milliliter
The experimental value(664 is 0.5720 gram per milliliter.
6-59
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A P I T D B C H A P T E R w b * t W 0732290 053bb28 286 W
6A3.2
PROCEDURE 6A3.2
DENSITIES OF DEFINED LIQUID MIXTURESAT THEIR BUBBLE POINTS
Discussion
This procedure, using the COSTALD method, and Procedure 6A3.1, using the modified
Rackett equation, are both recommended methods for calculating the density of defined
liquid mixtures at their bubble points.
The following equations are applicable up to a reduced temperature of 0.95.
1 = v;vp(l
-
(6A3.2-1)
- wsRK,vp)
Pbp
--`,,-`-`,,`,,`,`,,`---
(6A3.2-2)
(6A3.2-3)
(6A3.2-4)
(6A3.2-5)
V,TT., = ( VTc,V.Tc,)’n
(6A3.2-6)
V g ’ = 1+ ~ ( - lTr)”’ + b(1- Tr),’
+ ~ ( 1 -T,) + d(1 -
(6A3.2-7)
(6A3.2-8)
\
-
Where:
pbp = liquid density at the bubble point, in pound-moles per cubic foot.
uSRK,
= acentric factor of component i optimized for vapor pressure data in the SoaveRedlich-Kwong equation of state (see Table 6A2.14).
x , = mole fraction of component i.
V: = characteristic volume, in cubic feet per pound-mole (see Table 6A2.14).
T =temperature, in degrees Rankine.
T,, = critical temperature of component i, in degrees Rankine.
U = -1.52816
C = -0.81446
e = -0.296123
g = -0.0427258
h = -0.0480645
b = 1.43907
d = 0.190454
f = 0.386914
Procedure
Step 1: Obtain critical temperature from Chapter 1and V* and oSRK from Table 6A2.14.
If any component of the defined mixtureis not listed in Table 6A2.14, use its critical volume
from Chapter 1 for V* and the acentric factor from Chapter 2 for osRK.
Step 2: Compute the molar average characteristic volume, V:, using equation (6A3.2-2)
and omusing equation (6A3.2-3).
Step 3: Calculate the mixture correspondence temperature of the mixture using the mixing
rules given by equations (6A3.2-5) and (6A3.2-6).
Step 4: Compute the reduced temperature and substitute it into equations (6A3.2-7) and
(6A3.2-8) to obtain V$’) and V?).
Step 5: Compute the bubble point density from equation (6A3.2-1).
6-61
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T D B CHAPTERrb
API
X*
W 0732290 0536629 LI2 W
6A3.2
COMMENTS ON PROCEDURE6A3.2
Purpose
Procedure 6A3.2 is to be used to predict the density of a liquid mixture at the bubble point. This
procedure has an accuracy comparable to the modified Rackett method given in Procedure 6A3.l .
Special Comments
This procedure may be used to predict density of defined mixtures containing inorganics. Values
of WSRK and V* for inorganics are included inTable 6A2.14.
Limitations
The procedure should not be applied at reduced temperatures greater than 0.95. The procedure has
a higher average error formixtures containing hydrogen or carbon dioxide.
Reliability
This method has been evaluated only with binary data where the average error was about 2.4
percent. Higher errors are reported as the critical region is approached. For mixtures containing
inorganics, an average error of 4 percent is reported (32a). For systems with more than two components, no estimate of the errors is available.
Literature Source
This equationwas developed by Hankinson and Thomson, AIChE Journal 25 653 (1979).
Example
Estimate the bubble point density of a methane-n-decane mixture at 160 F. The mixture contains
20 mole percent methane.
From Chapter 1, the molecular weights of the components are 16.04 for methane and 142.28 for
n-decane, and the critical temperatures are -I 16.67 F for methane and 652.00 F for n-decane.
From Table 6A2.14, vi*, in cubic feet per pound-mole, is 1.592 for methane and 9.919 for
n-decane, and % R K ~ is 0.0074 for methane and 0.4916 for n-decane.
Compute the molar average characteristic volume using equation (6A3.2-2).
V i = (1/4) I(0.2) (1.592) + (0.8) (9.919) + 3[ (0.2) (1.592)2n + (0.8) (9.919)2/3]
x [(0.2) (1.592)'"
+ (0.8) (9.919)''3]
]
= (1/4) (8.254+ 3[0.2727 + 3.69321 [0.2335 + 1.718911
= 7.871 cubic feet per pound-mole
Compute osRhusing equation (6A3.2-3).
CO~RG
= (0.2) (0.0074) + (0.8) (0.4916)
= 0.3948
Calculate T,, using equations (6A3.2-5) and (6A3.2-6).
TI = -1 16.67 + 459.7 = 343.11 R
q2= 652.00 + 459.7 = 1,111.7R
y;Tl2 = GT,,[
(1.592) (343.11) (9.919) (1,111.7)]1'2
= 2454.2 (cubic feet) (degrees Rankine) per (pound-mole)
T,, = [ (0.2)2(1.592) (343.11) + (2) (0.2) (0.8) (2454.2)
+ (0.8)2(9.919) (1,111.8)]/7.871
= 999.2 R
Compute the reduced temperature from equation (6A3.2-4).
T, = (160 + 459.7)/999.2= 0.620
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A P TI D BC H A P T E R x b
*X
m
0732290 053bb30 934
m
6A3.2
Calculate V$" and VAE)using equations (6A3.2-7) and (6A3.2-8).
V$) = 1 - 1.52816(1- 0.620)'"
- 0.81446(1- 0.620)
=
+ 1.43907(1-
+ 0.190454(1-
0.620)2/3
0.620)"3
0.391
v p = - 0.296123 + (0.386914)(0.620) - (0.0427258)(0.620)*- (0.0480645)(0.620)3
(0.620 - 1.00001)
= 0.221
Calculate the bubble point density using equation (6A3.2-1)
- (7.871)(0.391)[1 - (0.3948)(0.221)]
"
pbp
= 2.809
Pbp
cubic feet per pound-mole
= 0.3560 pound-mole per cubic foot
= 0.3560(&)[(0.2)(16.043)
+ (0.8)(142.286)]
= 0.667 gram per milliliter
The experimental value (120a) is 0.670 gram per milliliter.
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6-63
A P I TDB CHAPTERsb
**
m
0732290 0536633 8 7 0
m
6A3.3
PROCEDURE 6A3.3
LIQUID DENSITIES OF COMPRESSED
HYDROCARBON MIXTURES OF DEFINED COMPOSITION
Discussion
The correlation is based on the relationship Cl/pl = CJp, = constant, where pl and pz
represent two densities of the mixture and Cl and C, represent the corresponding density
correlation factors. These factors are obtained from Figure 6A2.22.
Where this relation holds, any density, pz, may be expressed as a function of one known
density, pl, as shown in equation (6A2.22-1).
Procedure
Step 1: From Chapter 1, obtain the critical temperature, T,, and the critical pressure, pc,
for each compoundin the mixture. If a referencedensity for the mixture is not known,obtain
the density at 60 F and 1 atmosphere for each component also from Chapter 1.
Step 2: Calculate the pseudocritical (molar average) temperature and pressure for the
mixture. Compute the pseudoreduced temperature and pressure for the known reference
point, if available, and for the desired conditions. If individual compound reference points
are being used, compute the average density for themixture at 60 F and 1 atmosphere using
equation (6A3.3-1) or equation (6A3.3-2).
In terms of mole fractions,
"
(6A3.3-1)
pl=%
C" PP
t=1
In terms of weight fractions,
P1 =
1.0
7
(6A3.3-2)
x%
I=1
P,
Where:
pl = reference density of the mixture, in units of weight per volume.
pp = density of pure component i at 60 F and 1 atmosphere except for lighter hydrocarbons
(see note), in units of weight per volume.
n = number of components in the mixture.
x, = mole fraction of component i.
M , = molecular weight of component i.
x,, = weight fraction of component i .
NOTE: For mixtures containing the lighter hydrocarbons, such as n-butane and thoseof lower
molecular weight, a slightly different procedure is required. Since these hydrocarbons exist
as gases at 60 F and 1 atmosphere, Chapter 1 lists the liquid density at 60 F and the
equilibrium vapor pressure. Each reference density must, therefore, be converted to the
same pressure (the vapor pressure of the lightest component) before computing the average
density of the mixture. For methane mixtures, use Procedure 6A3.1 to calculate a reference
density for the mixture. If the vapor pressure is not available, use the Procedures in Chapter
5 to approximate a vapor pressure for the mixture. (This value serves as the reference
pressure.) For ethane and ethenea referencepoint of -30 F at saturatedconditions has been
selected. The following properties are valid for ethane and ethene at these conditions:
Component
Ethane
Ethene (ethylene)
Density
Vapor Pressure
(Pounds per Square
Inch Absolute)
Gram per
Milliliter
Pounds per
Cubic Foot
135
240
0.4741
0.4510
29.60
28.16
Examples B and C in the comments on this procedure deal with mixtures containing light
hydrocarbons when reference densities for the mixtures are not available.
Step 3: In Figure 6A2.22, locate the values of Cl at thereduced conditions of the reference
point and C, at the reduced conditions of the desired density.
Step 4: Compute the unknown density, p2, from equation (6A2.22-1).
--`,,-`-`,,`,,`,`,,`---
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6-65
API T D B CHAPTERt6
*X
E 0732290 0536632 707 W
6A3.3
COMMENTS ON PROCEDURE6A3.3
Purpose
The procedure is given for estimating the liquid densities of defined hydrocarbon mixtures. For
pure compounds, see Figure6A2.22.
Limitations
Pseudocritical pressures and temperatures of a mixture are used in the correlation. However, near
the critical point this may lead to large errors; it is desirable to use the actual critical values in this
area, if available. Also, for methane systems, the pseudocritical values differ greatly from the actual
critical values, and rather high errors may result for these systems.
The recommended volumetric average technique for computingthe reference density does not take
into account the excess volume of mixing. This procedure, if used instead of an experimental
reference density, can result in larger errors in the computed density.
Reliability
Using a volumetric average density for a reference condition, an average error of slightly more than
2 percent can be expected. As the reduced temperature approaches 0.95, errors approaching 15
percent may occur.
Llterature Source
Figure 6A2.22 is adapted from Lu, Chem. Eng. 66 [9] 137 (1959).
Examples
--`,,-`-`,,`,,`,`,,`---
A. Estimate the liquid density of a mixture containing 60.52 mole percent ethylene and 39.48 mole
percent n-heptane at 900 pounds per square inch absolute and 162.7 F. For this mixture, the density
at 49 F and 400 pounds per square inch absolute is known to be 37.55 pounds per cubic foot.
From Chapter 1,
T, (ethylene) = 48.58
pc (ethylene) = 729.8
T, (n-heptane) = 5 12.70
pc (n-heptane) = 396.8
Where:
T, = critical temperature, in degrees Fahrenheit.
pc = critical pressure, in pounds per square inch absolute.
The pseudocritical properties are calculated as follows:
TF = (0.6052) (48.58)+ (0.3948) (512.70) = 231.81 F
pw = (0.6052) (729.8)= (0.3948) (396.8) = 598.33 pounds per square inch absolute
Where:
Tpc,pw = pseudocritical properties of the mixture, defined as the sum of the products of each
individual T, or pc and the corresponding mole fraction.
Then
49 + 459.7
I'
= 231.81 +459.7
-
400
598.33
= 0.736
= 0.668
T
'2
=
162.7 + 459.7
= 0.900
231.81 + 459.7
-
598.33
900
- 1.50
-
Where:
T, = reduced temperature, T/T,.
T = temperature, in degrees Rankine.
pr = reduced pressure, p/pc.
p = pressure, in pounds per square inch absolute,
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A P I TDB CHAPTER*b
**
m
0732290 053hb33b43
m
6A3.3
From Figure 6A2.22, C, = 0.900 and C2= 0.756, and using equation (6A2.22-1),
pz = 3 7 . 5 5 H = 31.54 pounds per cubic foot
The experimental value is 32.15 pounds per cubic foot.
B. Estimate the liquid density of a mixture containing 20 mole percent ethane and80 mole
percent n-decane at 160 F and 3000 pounds per square inch absolute. No known density for
the mixture is available.
Chapter 1 gives the following data for the two components:
Property
Ethane
652.1F
Critical temperature,
Critical pressure, psia
Density at 60 F, lb per CU ft
Molecular weight
90.09
707.8
-
30.07
n -Decane
304
45.72
142.3
Use values of saturated ethane liquid density and vapor pressure at -30 F as listed in the
note under Step 2 of this procedure.
The density of n-decane must be corrected to the same vapor pressure and temperature
as ethane.
60 + 459.7
= 652.1
+ 459.7
-30 + 459.7 = o.386
652.1 + 459.7
= 0.467
14.7
prl= -= 0.048
304
From Figure 6A2.22, Cl = 1.092 and C2 = 1.142. By equation (6A2.22-1), the calculated
density of n-decane at -30 F and 135 pounds per square inch absolute is
1 142
1.O92 = 47.81 pounds per cubic foot
p2 = 45.72-
The density of the mixture at -30 F and 135 pounds per square inch absolute is computed
using equation (6A3.3-1).
Finally, estimate the desired mixture density. The pseudocritical conditions are
TF = (0.2)(90.09) + (0.8)(652.1) = 539.7 F
ppc= (0.2)(707.8)+ (0.8)(304) = 384.76 pounds per square inch absolute
and the pseudoreduced conditions are
=
459.7 + (-30)
459.7 + 539.7
459.7 + 160 = o,62o
+ 539.7
= 0.430
= 497.7
From Figure 6A2.22, Cl = 1.115 and Cz= 1.028, and by equation (6A2.22-1),
= 42.78
pounds per cubic foot
--`,,-`-`,,`,,`,`,,`---
p2 = 46.40%
The literature value is 43.07 pounds per cubic foot.
For mixtures containing light components other than ethane, ethene, or methane,
a similar
procedure is followed. However, the densities of the heavier components are corrected to the
vapor pressure of the light component at 60 F.
C . Estimate the liquid density of a mixture containing 20 mole percent methane and 80
mole percent n-decane at 160 F and 3000 pounds per square inch absolute. The vapor
pressure of the mixture is 795 pounds per square inch absolute. No known density for the
mixture is available.
6-67
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A P I TDB CHAPTERtb X *
W 0732290053663458T
m
6A3.3
Chapter 1 gives the following data for the components:
Property
Methane
Critical temperature, F652.1
Critical pressure, psia
304
Molecular weight
142.3
n -Decane
-116.63
667.8
16.043
The calculation of the bubble point volume of the mixture at 160 F and 795 pounds per
square inch absolute is shown in the example in Procedure 6A3.2 to be 2.809 cubic feet per
pound-mole.
The average molecular weight of the mixture is
MW, = (0.2)(16.043) + (0.8)(142.3) = 3.21 + 113.8
= 117.0 pounds
per pound-mole
The density can then be expressed as
1.0
p, = pbp= 2 . 8 ( ~X
117.0 - 41.65 pounds per cubic foot
The pseudocritical and pseudoreduced conditions are
TPe= (0.2)(-116.63)
+ (0.8)(652.1) = 498.4 F
ppc= (0.2)(667.8) + (0.8)(304) = 376.8 pounds per square inch absolute
459.7 + 160
=459.7 + 498.4 =
T, = T,, = 0.647
Pr1
795 -2.11
=-376.8
From Figure 6A2.22, CI = 0.983 and C2 = 1.014, and by equation (6A2.22-1),
1 014
p2 = 41.65-= 42.96 pounds per cubic foot
0.983
--`,,-`-`,,`,,`,`,,`---
The literature value is 43.23 pounds per cubic foot.
6-68
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A P I TDB C H A P T E R f b f f
m 0732290
053bb35 4Lb
m
6A3.4
PROCEDURE 6A3.4
COMPUTER METHOD FOR THE LIQUID DENSITIES OF
COMPRESSED HYDROCARBON MIXTURES OF DEFINED COMPOSITION
Discussion
The Tait-COSTALD equation, (6A2.23-1), may be used to calculate liquid densities of
compressed hydrocarbon mixtures. A set of mixing rules is used to define the mixture
properties.
(6A3.4-1)
B = -1
-
Pm,
+ ü(l - Tr)"' + 6(1 -
+ d(l-
T,)
+ i ( 1 - T,)'"'
(6A3.4-2)
(6A3.4-3)
(6A3.4-4)
T, =- T
Tm,
(6A3.4-5)
(6A3.4-8)
(6A3.4-9)
(6A3.4-10)
(6A3.4-11)
(6A3.4-12)
(6A3.4-13)
(6A3.4-14)
--`,,-`-`,,`,,`,`,,`---
(6A3.4-15)
(6A3.4-16)
Where:
pm = density of liquid mixture at temperature T and pressure P , in pound-moles per
cubic foot.
pbp = bubble point density of liquid mixture at temperature T, in pound-moles per cubic
foot.
p = pressure, in pounds per square inch.
pbp= bubble point pressure of mixture at temperature T , in pounds per square inch.
T =temperature, in degrees Rankine.
xi = mole fraction of component i.
V,* = characteristic volume of component i , in cubic feet per pound-mole (see Table
6A2.14).
T,, = critical temperature of component i , in degrees Rankine.
wSRK,= acentric factor for component i optimized for vapor pressure data in the SoaveRedlich-Kwong equation of state (see Table 6A2.14).
R = gas constant, 10.731 (pounds per square inch absolute) (cubic feet) per (poundmole)(degree Rankice).
ã = -9.070217
4 = -135.1102
g = 0.250047
= 0.0861488
b = 62.45326
f=
4.79594
h = 1.14188
k = 0.0344483
i
6-69
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A P I TDB CHAPTERtb t t
m
0732290 053bb3b 352
m
6A3.4
Procedure
Step 1: Obtain the critical temperature from Chapter 1 and Vi* and OSRK~for each component from
Table 6A2.14. If any compound is not listed inTable 6A2.14, use its critical volume from Chapter 1
for Vi*and the acentric factor from Chapter2 for osRKi.
Step 2: Calculate the mixture properties using equations (6A3.4-6) through (6A3.4-9). The saturation vapor pressure is obtained using equations (6A3.4-10) through (6A3.4-16).
Step 3: Calculate the bubble point density of the mixture using either Procedure 6A3.1 or 6A3.2.
Step 4: Substitutethe values calculated in Steps 1, 2, and 3 in equations (6A3.4-1) through
(6A3.4-4) to obtain the liquid density of the mixture at thedesired temperature and pressure.
COMMENTS ON PROCEDURE6A3.4
Purpose
--`,,-`-`,,`,,`,`,,`---
The procedure is an alternate computermethod to estimate compressed liquid densities of defined
hydrocarbon mixtures.
Limitations
This equation is applicable in the reduced temperature range below 0.95. The method has been
found to give erroneous corrections when used with organic (polar) mixtures. In these cases, it is
recommended that the saturated density be used rather than correcting it with equation (6A3.4-1).
Reliability
The average error in estimating the density of defined hydrocarbon mixtures is reported at
1 percent. Unsatisfactory results were obtained for nonhydrocarbon (polar) mixtures (32a).
Literature Source
The equation was developed by Thomson, Brobst, and Hankinson, AIChE Journal 28 67 1 (1982).
Example
Estimate the liquid density of a mixture containing 20 mole percent ethane and 80 mole percent
n-decane at 160 F and 3000 pounds per square inch absolute.
Chapter 1 gives the following data for the components:
Property
Molecular weight
Critical temperature, F
Critical pressure, psia
Ethane
n-Decane
30.07
89.92
706.80
142.286
652.00
305.20
From Table 6A2.14,
is 0.0983 for ethane and 0.4916 for a-decane, and Vi*,in cubic feet per
pound-mole, is 2.335 for ethane and9.919 for n-decane.
T , = 89.92 + 459.7 = 549.62 R
Tc2 = 652.00+459.7= 1,111.7R
Calculate the mixture properties using equations (6A3.4-6) through (6A3.4-9). From equation
(6A3.4-8).
V: = (1/4) ((0.2) (2.335)
+ (0.8) (9.919) + 3[ (0.2) (2.335)2/3 + (0.8) (9.919)2/3]
x [ (0.2) (2.335)’”
= (1/4) (8.402 + 3[0.3520
+ (0.8) (9.919)’” 1 )
+ 3.69321 [0.2653 + 1.71891)
= 8.1204 cubic feet per pound-mole
6-70
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m
T D B CHAPTER*b
API
0732290 0 5 3 b b 3 7 299 D
6A3.4
--`,,-`-`,,`,,`,`,,`---
Using equations (6A3.4-7)
and (6A3.4-6),
e;742=
k$17&1 = [ (2.335)(549.62)
(9.919)
(llll.7)]''2
= 3761.9(cubic feet) (degrees Rankine) per (lb-mole)
Tmc = [ (0.2); (2.335) (+54
29
(.
06
.2)(0.8) (3761.9)
+ (0.8); (9.919)
(1111.7)]/(8.1204)
= 1023.8R
and fromequation (6A3.4-9),
(0.09
+8(0.8)
3) (0.4916)= 0.4129
= (0.2)
wSRK,
Determine the bubble point pressure using equations (6A3.4-10)
through (6A3.4-16).
,z = 0.291- (0.080) (0.4129)= 0.258
pmc= (0.258) (10.731) (1023.6)/(8.1204)
= 349.0pounds per square inch absolute
T, = (160+ 459.7)/(1023.6)= 0.6054
a = 35.0- (36.010.6054)
- 96.73log (0.6054)+ (0.6054)6
= -3.4297
ß = log (0.6054)+ 0.372154 (-3.4297)
= -.3457
= (5.8031817)log (0.6054)+ (0.70608141)
(-3.4297)
Rm
=
=
-1.5258
(4.86601)
(-0.3457)
Rm
= -1.6822
( o$ )
log
p
bp
= -1.5258+ (0.4129)
(-1.6822)
= -2.2204
= 2.171pounds per square inch absolute
The bubble point density is calculated using Procedure 6A3.2.
+ 1.43907( 1 - 0.6054)2/3
-0.81446(1 - 0.6054)+ 0.190454(1 - 0.6054)4/3
= 0.3871
Vio)= 1 - 1.52816(1 - 0.6054)'"
Vi') = (-0.296123)+
(0.386914) (
-0(
.0
6.
00
542
)7258)
(0.6054- 1.00001)
(0.60-54
(0
).
20480645)
(0.6054)3
= 0.2235
i= (8.1204)
(0.3[8I70)(0.4129)
(0.2235)]
= 2.8532cubic feet per pound-mole
Calculate the liquid density at 160 F and 3000 pounds per square inch absolute using equations
(6A3.4-1)
through (6A3.4-4).
C = 0.086148+ 0.034483
(0.4129)
= 0.1004
ë = exp [4.79594+ (0.250047)
= 163.02
B
= -1
349.0
- (9.070217)(1
-
(0.4+12(9
1)
.14188)
0.6053)'"
(0.4129);]
+ (62.45326)( I - 0.6053)u3
-(135.1102)(1-0.6053)+(163.02)(l-0.6053)4'3
= 19.822
6-71
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A P I TDB
CHAPTER*b
S*
W 0732290 0536638 125 W
6A3.4
B = (19.822)(349.0) = 6917.9 pounds per square inch absolute
(6917.9 + 3000.0)
1
= (2.8525)[ 1 - (0.1004) ln
Pm
(6917.9 + 2.171)
= 2.749 cubic feet per pound-mole
pm = 0.3638 pound-mole per cubic foot
1
= (0.3637)(m)[(0.2)(30.07)
1
+ (0.8)(142.286)]
--`,,-`-`,,`,,`,`,,`---
= 0.6982 gram per milliliter
The literature value is 0.6925 gram per milliliter.
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API T D B CHAPTER*b
X*
m 0732290 0536637 Ob1 m
6A3.5
FIGURE 6A3.5
1000
DENSITIES
-
900
800
OF LIQUID
-
PETROLEUM FRACTIONS
AT LOW
-
PRESSURES
-
1.05
-
U0
-
0.95
-
0.90
-
700
-..
I
600
-
-
u.
-ass
UJ
a!
2
2
500
ge
-
-
Qao
-
a75
-
0.70
-
0.65
-
W O
-
o55
-
0.50
MEAN-AVERAGE
-
BOILINGPOINT,
F
300
D E GA P I
-
200
O
100
-
&?
WATSON K
d
0-
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8%
--`,,-`-`,,`,,`,`,,`---
400
API
TDB CHAPTERvb
X*
0732290 0536640 8 8 3
6A3.5
COMMENTS ON FIGURE 6A3.5
Purpose
This figure provides a graphical method of obtaining the density of liquid petroleum fractions at
their saturation pressures or at pressures not far above 1 atmosphere. For high pressures, a pressure
correction should be applied as given in Procedures 6A3.1 and 6A3.10.
Limitations
Two of three characterizing parameters (the API gravity at 60 F, the mean average boiling point,
and theWatson K factor) must be known or calculated from known data touse this figure. The mean
average boiling point and K can be obtained from procedures in Chapter 2 if the API gravity and
average molecular weight of the fraction are known.
The characterization factor is alsogiven by the following equation:
(6A3.5-1)
Where:
MeABP = mean average boiling point, in degrees Rankine.
sp gr = specific gravity.
Reliability
Errors in the calculated densities are about 0.3 percent at 1 atmosphere. This amounts to about
0.0024 grams per milliliter.
Special Comment
The following can be used instead of Figure 6A3.5:
T
MeABP
SG
Denl
= Temperature, in degrees Rankine.
= Mean Average Boiling Point, in degrees Rankine.
= Specific Gravity
= Liquid Density (Ib,/ft3)
Denl = A
A
B
C
D
E
[
SC2-
(B x S G - C + D x M e A B P ) ( T - E )
MeABP
1”*
= 62.3636
= 1.2655
= 0.5098
= 8.011 X
= 519.67
Literature Source
Adapted from Ritter, Lenoir, Schweppe, Petrol. Rejner 37 [ll]225 (1958).
Example
Estimate the liquid density, at 160 F and atmospheric pressure, of a petroleum blend with a mean
average boiling point of 538 F and A P I gravity of 30.6.
Using the mean average boiling point and theAPI gravity, the pivot point is located, and then a line
is constructed through this point and the 160 F point on the left hand scale.The resulting density value
is 0.835 gram per milliliter.
The experimental value (20a) is0.8343 gram per milliliter.
6-74
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--`,,-`-`,,`,,`,`,,`---
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A P I TDB CHAPTERS6
SS
m
0732290 053bbYL ? I T
m
6A3.6
PROCEDURE 6A3.6
ANALYTICAL METHODFOR THE DENSITIES OF LIQUID PETROLEUM
FRACTIONS AT LOW PRESSURES
Discussion
The modified Rackett equation may be used to calculate the density of petroleum fractions at their
saturation pressures or at pressures not far above 1 atmosphere if an API gravity or a specific gravity
at some temperature is known.
(6A3.6-1)
Where:
p = density of liquid petroleum fraction, in pound-moles per cubic foot.
R = gas constant, 10.731 (pounds per square inch absolute) (cubic feet) per (pound-mole)
(degree Rankine).
T, = reduced temperature, TIT’,.
T = temperature, in degrees Rankine.
T’, = pseudocritical temperature, in degrees Rankine.
pp. = pseudocritical pressure, in pounds per square inch absolute.
ZR, = an empirically derived constant.
Procedure
Step 1: From the available characterizing parameters, obtain the mean average boiling point
(MeABP) and specific gravity at 60 F using procedures given in Chapter 2.
Step 2: Use procedures in Chapters 2 and 4 to calculate the pseudocritical temperature, pseudocritical pressure, and molecular weight.
Step 3: Calculate Z ~ ~ f r oequation
m
(6A3.6-1), using the specific gravity or density at a known
temperature.
Step 4: Equation (6A3.6-1) may now be used to predict the density of the petroleum traction at
different temperatures.
1992
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6-75
Not for Resale
A P I TDB CHAPTERvb X *
0732290 053bbLl2
656
6A3.6
--`,,-`-`,,`,,`,`,,`---
COMMENTS ON PROCEDURE6A3.6
Purpose
The procedure isan analytical method to predict the density of petroleum fractions at their saturation pressuresor at pressures not far above 1 atmosphere. At least two characterizing parameters for
For high pressures, a pressure
the petroleum fraction should be known
for this method to be applied.
correction shouldbe applied as given in Procedures6A3.7 and 6A3.10.
Reliability
The method hadan average error of 0.75 percent when tested against a data set consisting
of highmolecular-weight hydrocarbons and petroleum fractions.
Literature Source
Private communication, Spencer, C.F., M. W. Kellogg Co., Houston, Texas (1983).
Example
Estimate the liquid density, at160 F and atmospheric pressure, of a petroleum blend with a mean
average boiling point of538 F and API gravity of 30.6.
MeABP = 538 + 459.7 = 997.7 R
sp gr, 60 FI60 F = 141.5/(30.6 + 131.5) = 0.87292
p. 60 F = 0.87292 X 0.99904 = 0.87208 gram per milliliter
The molecular weight is determined using the procedure given in Chapter
2.
M = 20.486 exp [1.165 x l e ( 9 9 7 . 7 ) -7.78712 (0.873)
+ 1.1582 x
(997.7)(0.873)](997.7)’.26007(0.873)4.98308
= 215.1
The pseudocritical temperature,
TF, and the pseudocritical pressure,h,
are calculated.
TF = 10.6443 exp [-5.1747 x lo4 (997.7) - 0.54444 (0.873)
+ 3.5995 x lo4 (997.7) (0.873)] (997.7)0.81067 (0.873)0.53691
= 1355.6R.
pF = 6.162 x lo6 expr-4.725 x lo3 (997.7) - 4.8014 (0.873)
+ 3.1939 x
(997.7)(0.873)](997.7)-0.4844(0.873)4.0846
= 273.2 pounds per square inch absolute
60 F and the other quantities computed above,ZMis calculated from
Using the known density at
equation (6A3.6-1).
T,=
60 + 459.7
= 0.3833
1355.6
= 0.24894
At 160 F,
V = (82.053)
[ T] [ 2]
1355.6
(0.24894)
= 257.6 cubic centimeters per gram-mole
[
1
1 + (1 - 0.3833) 2/7
1
215.1
p = __ = 0.8350 gram per milliliter
257.6
The experimental value(20a) is 0.8343 gram per milliliter.
1992
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~~
Not for Resale
A P I T D BC H A P T E R t b
*S W
0732290 05366113 5 7 2 W
6A3.7
PROCEDURE 6A3.7
DENSITIES OF LIQUID PETROLEUM FRACTIONSAT HIGH PRESSURES
Discusslon
Figures 6A3.8 and 6A3.9 correlate densities of petroleum fractions at high pressures.
When the density at ambient pressures is found from Figure 6A3.5 or Procedure 6A3.6, the
following equation may be used in conjunction with Figures 6A3.8 and 6A3.9 to determine
the density at any pressure:
(6A3.7-1)
Where:
--`,,-`-`,,`,,`,`,,`---
po= density of sample at temperature of interest and ambient pressures.
p = density of sample at temperature and pressure of interest.
p = pressure, in pounds per square inch gage.
B T = isothermal secant bulk modulus = -(l/po)(Ap/AV)T
Bm = isothermal secant bulk modulus at 20,000 pounds per square inch gage, the tem-
perature of interest, and density
pa.
Procedure
Step 1: Use Figure 6A3.5 or Procedure 6A3.6 to obtain the density of the fraction at the
specified temperature and ambient pressures.
Step 2: Obtain theisothermal secantbulk modulus at 20,000 pounds per square inch gage,
BZO,from Figure 6A3.8 using the density computed in Step 1.
Step 3: Obtain the isothermal secant bulk modulus, Br, at the desired pressure from
Figure 6A3.9. Enter the chart with the modulus Bm found in Step 2 and draw a horizontal
line to its intersection with the line representing 20,000 pounds per square inch gage. A
vertical line drawn through the intersection gives the modulus at any other pressure at the
specified temperature.
Step 4: Calculate the density at the selected temperature and pressure from equation
(6A3.7-1).
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A P I TDB CHAPTER%
**
0732290 0 5 3 6 6 4 4 429
m
6A3.7
COMMENTS ON PROCEDURE 6A3.7
Purpose
The procedure is given for estimating pressure corrections for the liquid densities of petroleum
fractions at high pressures. Figures 6A3.8 and 6A3.9 are parts of this procedure.
Limitations
The liquid density at or near atmospheric pressure must be known or estimated from Figure 6A3.5
or Procedure 6A3.6 for thisprocedure to beused.
Reliability
At high pressures, the error is about 1.5 percent.
Literature Source
Figures 6A3.8 and 6A3.9 were adapted from Wright, ASLE Trans. 10 349 (1967).
Example
--`,,-`-`,,`,,`,`,,`---
Estimate the liquid density, at 68 F and 5400 pounds per square inch gage, of a petroleum fraction
with a Watson characterization factor of 12.28 and API gravity of 3 1.4.
From Figure 6A3.9, the density at 68 F and atmospheric pressure is found to be 0.865 grams per
milliliter.
at the specified temperature is 339,000 pounds per square inch gage.
Using Figure 6A3.8,
From Figure 6A3.9, BT at 5400 pounds per square inch gage and68 F is 272,000 pounds per square
inch gage.
The density is determined fromequation (6A3.7-1).
p=
0.865
= 0.8826 grams per milliliter
0.9801
~
The experimental value (5a) is 0.8838 grams per milliliter.
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A P I TDB CHAPTER+b + t
07322’30 053661.15 365
6A3.8
--`,,-`-`,,`,,`,`,,`---
O
100
200
300
400
500
600
TEMPERATURE, F
6-79
1984
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A P I TDBCHAPTER*b
*f
m 0732270
053bb4b 2TL
m
6A3.9
2.5 X
2x
1
I
ISOTHERMAL
FOR
SECANT BULK MODULUS
lw
FOR
PETROLEUM
FRACTION
O.
--`,,-`-`,,`,,`,`,,`---
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A P I TDB CHAPTER*b t*
0732290
0536647
L38
--`,,-`-`,,`,,`,`,,`---
6A3.1O
PROCEDURE 6A3.10
ANALYTICAL METHOD FOR THE DENSITIES OF LIQUID
PETROLEUM FRACTIONS AT HIGH PRESSURES
Discussion
For the generation of a large amount of data, an analytical version of Procedure 6A3.7
provides a more convenient method. From a reference density (value at ambient pressures),
the densities at higher pressures can easily be calculated using the analytical forms of Figures
6A3.8 and 6A3.9 given below. The reference density for each specified temperature must be
obtained from Figure 6A3.5 or calculated from equation 6A3.6-1.
Figure 6143.8 is represented by the following equation:
log B20 = -6.1(10-4)T
+ 4.9547 + 0.7133~
(6A3.10-1)
Where:
Bu, = secant bulk modulus at 20,000 pounds per squareinch gage and given temperature.
T = temperature, in degrees Fahrenheit.
p = density at ambient pressures and given T, in grams per milliliter.
The constant pressure lines in Figure 6A3.9 are correlated by the following equation:
B7=mX
+ BI
(6A3.10-2)
Where:
BT = secant bulk modulus at the specified pressure.
m = slope of the line.
BI = secant bulk modulus at the Y-intercept.
X , the unmarked abcissa of Figure 6A3.9, is calculated from the following equation:
(6A3.10-3)
Where:
BI.^ = secant bulk modulus at the intercept of the line representing 20,000 pounds per
square inch gage in Figure 6A3.9 (100,000 pounds per square gage).
m m = slope of the line representing 20,000 pounds per square inch gage (23,170).
The intercept, B I , and the slope, m , at the desired pressure are given by the following
equations:
BI= 1.52(104)+ 4.704~-2.58O7(lO-’)p2 + 1.0611(10-’~p3
m = 21,646 + 0.0734~+ 1.4463(10-7)p2
(6A3.10-4)
(6A3.10-5)
Where:
p = pressure, in pounds per square inch gage.
Procedure
Step 1: Calculate the density of the fraction at the specified temperature and ambient
pressures from Figure 6A3.5 or Procedure 6A3.6.
Step 2: Determine the isothermal secant bulk modulus at 20,000 pounds per square inch
gage and the specified temperature from equation (6A3.10-1).
Step 3: Using equation (6A3.10-3) and the value obtained in Step 2, calculate X .
Step 4: Calculate the modulus intercept and slope at the desired pressure from equations
(6A3.10-4) and (6A3.10-5).
Step 5: Using the values obtained in Steps 3 and 4, calculate the isothermal secant bulk
modulus at the desired pressure from equation (6A3.10-2).
Step 6: Obtain the desired density from equation (6A3.7-1).
6-81
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API T D B CHAPTER*b
X*
m
0732290 0536648 074
m
6A3.1O
COMMENTS ON PROCEDURE 6A3.10
Purpose
The procedure is given as an alternate analytical method for estimating the pressure
correction for the liquid density of a petroleum fraction at any temperature.
Limitations
The liquid density at or near atmospheric pressure must be known or estimated from
Figure 6A3.5 or Procedure 6A3.6 for this procedure to be used.
Reliability
The average error for calculated densities is approximately 1.7 percent. As the critical
point is approached, the error may be as high as 5 percent.
Literature Source
Private communication, Spencer, C . F., M. W. Kellogg C o . , Houston, Texas (June 1982).
Example
Estimate theliquid density, at 68 F and 5400 pounds per squareinch gage, of a petroleum
fraction with a Watson K of 12.28 and an API gravity of 31.4.
From Figure 6A3.5, the density at 68 F and ambient pressures is found to be 0.865.
The isothermal secant bulk modulus at 20,000 pounds per square inch gage is determined
from equation (6A3.10-1).
--`,,-`-`,,`,,`,`,,`---
log B20 = ( ~ 6 . 1 ) ( 1 0 - ~ ) ( 6 +
8 )4.9547 + (0.7133)(0.865) = 5.53
Bzo = 339,000 pounds per square inch gage
The X reference is now claculated from equation (6A3.10-3).
X = (339,000 - 1 0 0 , ~=)
23,170
The intercept and slope at the desired pressure are now calculated.
BI = 1.52
+ 4.704 (5400) - 2.5807 (lo-')
(5400)'
+ 1.0611 (10"D)
= 39,860 pounds per square inch gage
m = 21,646
+ 0.0734 (5400) + 1.4463(10") (5400)'
= 22,046
The isothermal secant bulk modulus at desired pressure is:
BT = mX
+ Br = (22,046) (10.31) + 39,862
= 267,160 pounds per square inch gage
The density is now determined from equation (6A3.7-1).
0.865
P=-=o.9798
0.8828 gram
per
milliliter
The experimental value (5a) is 0.8838 gram per milliliter.
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(5400)3
~~
A P I TDB C H A P T E R t b t t
m
0732290 0 5 3 b b 4 9 TOD
m
6A3.1 i
--`,,-`-`,,`,,`,`,,`---
E)
'33N383441a AIlAV13 IdV
6-83
1984
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A P I TDB CHAPTERvb
Y*
W 0732290 053bb50 7 2 2
m
6A3.11
COMMENTS ON FIGURE 6A3.11
Purpose
The volumetric shrinkage resulting from blending low-molecular-weight hydrocarbons
with crude oils is estimated from this figure. This shrinkage occurs when light products such
as propane, butane, natural gasoline, and high-gravity produced distillates are mixed with
crude oil streams.
The curves shown in Figure 6A3.11 for various concentrations of lighter components were
calculated with the aid of the following formula:
S =2.14(10-5)C-0.'"04G'.76
(6A3.11-1)
Where:
S = shrinkage factor, as percent of lighter component volume.
C = concentration, in liquid volume percent, of lighter component in mixture.
G = gravity difference, in degrees API.
Reliability
This equationwas not evaluated in the presentwork. The literature source has determined
that it can be used with a high degree of confidence to calculate shrinkage at concentrations
up to21 percent of the lighter component. The equation is not valid at concentrationsabove
50 percent of the lighter component.
Literature Source
Adapted from API Bull. 2509C, Volumetric Shrinkage Resulting from Blending Volatile
Hydrocarbons with Crude Oils, 2nd ed., Am. Petrol. Inst., Washington, D.C. (1967).
Determine the volume of a mixture of 95,000 barrels of crude oil having a gravity of
30.TAPI at 60 F and 5000 barrels of natural gasoline having a gravity of 86.5"API at 60 F.
The gravity difference is
86.5 - 30.7 = 55.8"API
In Figure 6A3.11, at the intersection of the gravity difference and 5 percent of the lighter
component, S = 2.3 percent.
The volume of the mixture is calculated as follows:
2.3 (5000)
= 115 barrels shrinkage
5000 - 115 = 4885 barrels natural gasoline
4885 + 95,000 = 99,885 barrels mixture
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--`,,-`-`,,`,,`,`,,`---
Example
A P I TDB CHAPTERxb
**
0732290 0536653 b b 9
6A3.11
PROCEDURE 681.1
DENSITYOFPUREHYDROCARBONANDNONPOLARGASES
Discussion
The following equation is to be used to predict the compressibility factor of pure hydrocarbon gases:
z = z ( o ) + 0 z(')
(6Bl.l-1)
Where:
z = compressibility factor, dimensionless.
z(O) = compressibility factor for thesimple fluid, which is tabulated as a function of T, and
pr in Table 6B1.2 and plotted in Figures 6B1.4 and 6B1.5.
z(') = correction term for molecular acentricity, which is tabulated as a function of T, and
pr in Table 6B1.3 and plotted in Figures 6B1.6 and 6B1.7.
T, = reduced temperature, TI T,.
T =temperature, in degrees Rankine.
= critical temperature, in degrees Rankine.
p . = reduced pressure, p l p , .
p = pressure, in pounds per square inch absolute.
p E= critical pressure, in pounds per square inch absolute.
W = acentric factor.
If the vapor is saturated (in equilibrium with the liquid phase), the z(O)and z") terms
should be interpolated in pr from the following tabulation rather than Tables 6B1.2 and
6B1.3.
(0)
(1)
(0)
z(')
Pr
1.00
0.99
0.98
0.97
0.291
0.35
0.38
0.40
-0.080
-0.083
-0.085
-0.087
0.65
0.60
0.55
0.50
0.615
0.64
0.665
0.688
-0.069
-0.063
-0.056
-0.049
0.96
0.95
0.94
0.92
0.41
0.42
0.43
0.45
-0.088
-0.089
-0.089
-0.090
0.45
0.40
0.35
0.30
0.711
0.734
0.758
0.783
-0.041
-0.033
-0.025
-0.018
0.90
0.85
0.80
0.75
0.70
0.47
0.50
0.53
0.56
0.59
-0.091
-0.090
-0.087
-0.081
-0.075
0.25
0.20
0.15
0.10
0.05
0.809
0.835
0.864
0.896
0.935
-0.012
-0.008
-0.005
-0.002
Pr
0.000
The compressibility factor obtained fromequation (6Bl.l-1) determines the vapor volume
(or density) in the following equation of state:
(6B1.1-2)
Where:
V = molar volume, in cubic feet per pound-mole.
p = molar density, in pound-moles per cubic foot.
R = gas constant, 10.731 (pounds per square inch absolute)(cubic feet) per (pound-mole)
(degree Rankine).
Procedure
Step I : Obtain the critical temperature and pressure of the hydrocarbon from Chapter 1
and the acentric factor from Chapter 2.
Step 2: Calculate the reduced temperature and ressure at which a gas density is required.
Step 3: Obtain the correlation terms z(O)and z8). If the most accurate values are desired,
use Tables 6B1.2 and 6B1.3 with linear doubleinterpolationp, and T,. When near saturation,
the interpolation procedure may not be satisfactory (see Special Comments). If slightly less
accurate values are acceptable, they may be obtained rapidly from Figures 6B1.4 through
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6-85
--`,,-`-`,,`,,`,`,,`---
Not for Resale
A P I TDB CHAPTERrb
**
m
0732270 053bb525T5
m
6B1.1
6B1.7. When the vapor is saturated, use the tabulation presented above with a vapor pressure
from Chapter 5 if only temperature is known.
Step 4: Calculate the compressibility factor using equation (6Bl.l-l), and the volume or
density using equation (6Bl.1-2).
This procedure should befollowed when T and p are known and V is unknown. A suitable
modification (trial-and-error) should be used when V is known and T or p is desired.
COMMENTS ON PROCEDURE 6B1.1
Purpose
--`,,-`-`,,`,,`,`,,`---
This procedure is to be used to predict gas densities of pure hydrocarbons and nonpolar
gases. Tables 6B1.2 and 6B1.3 or Figures 6B1.4 through 6B1.7 are required in this procedure.
The method is best suited to desk calculations, and Procedure 6B1.8 should be used with
digital computers. Methods for hydrocarbon mixtures are given in 6B2.
Limitations
In general, this procedure is not accurate for polar substances.
Reliability
Errors between calculated and experimental compressibility factors are usually less than 1
percent except in the critical region, where errors of 30 percent can occur. This region of
maximum uncertainty is indicated in Figure 6B1.4.
The reliability decreases with uncertainties in the critical properties of the compounds.
Notation
The notation used in Tables 6B1.2 and 6B1.3 and Figures 6B1.4 through 6B1.7 was defined
for equations (6Bl.l-1) and (6B1.1-2).
Special Comments
The broken line in Table 6B1.2 indicates the discontinuity between compressibility factors
for liquid (to theright and above) and vapor (to theleft and below). Interpolations must not
be made across this line. Always use table values that apply to the desired phase only. Near
the brokenline,any necessary extrapolations should be made with respect to reduced
pressure at constant reduced temperature.
For hydrogen, do not use the critical constants listed in Chapter 1to calculate the reduced
properties; use the following values (lb, 6b):
X=75 R
p c = 305 pounds per square inch absolute
In regions of very rapid change of the simple fluid and correction terms with reduced
pressure andor temperature, a linear interpolation from the tables may not be satisfactory
even though the tablevalues are spaced more closely. Here, thefigures should be used either
directly or as a guide for correcting interpolations made using values from the tables.
The figures may be extrapolated to lower reduced pressuresby noting that z(O) approaches
unity and z ( ' )approaches zero as the pressure approaches zero. In many engineering applications, these limiting values may be used for all reduced pressuresbetween O and 0.2. If even
more precise results are desired than the extrapolated values (rarely), use the following
equation:
+
z = 1 +&[(0.1445 0.073~)- (0.330 - 0.46o)T;' - (0.1385 + 0 . 5 0 ~ ) T ; ~
T,
- (0.0121 + 0.097~)T,-~
-0.0073~T~-~]
(6B1.1-3)
Literature Sources
Tables 6B1.2 and 6B1.3 were generated from the generalized correlation of Lee and
Kesler, AZChE Journal 21 510 (1975). Equation (6B1.1-3) and the table for saturated vapor
compressibility factors were taken from Pitzer et al., J . Am. Chem. Soc. 77 3433 (1955).
1984
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**
A P I TDBCHAPTER*b
m
0 7 3 2 2 7 0 0536653 431
m
6B1.1
Example
Estimate the molar volume of 2-methylpropane (isobutane) at 310 F and 1250 pounds per square
inch absolute.
From Chapter 1, Tc = 274.98 F and p c = 529.1 pounds per square inch absolute, and from Chapter
2, O = 0.1770.
T,=
310.0+459.7 =
274.98 + 459.7
P, = 12'0 = 2.363.
~
529.1
To determine from
Table 6B1.2, interpolate first in reduced temperature. Figure 6B1.4 shows
that both interpolations can be safely performed linearly.
At T,= 1.04,
At
z(O) = 0.362 + (0.386 - 0.362)
2.363 - 2.2
= 0.382
2.4 - 2.2
= 0.367 + (0.390 - 0.367)
2.363 - 2.2 = o,386
2.4 - 2.2
= 0.382 + (0.386 - 0.382)
1.O48 - 1.04
= 0.385
1.05 - 1.04
T,= 1.05,
Combining these,
Similarly, using Table 6B1.3,8) = -0.061. The compressibility factor iscalculated from equation
(6Bl.l-l), and the volume from equation (6B1.1-2).
z = 0.385 + (0.1770) (-0.061) = 0.374
V=
(0.374) ( 10.731) (3 10.0 + 459.7)
= 2.47 cubic feet per pound-mole
1250
--`,,-`-`,,`,,`,`,,`---
An experimental value for the compressibility factor is0.377.
6-87
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C
Reduced
"
Temperature
0.600.400.20
0.80
0.90
1.00
1.10
1.20
1.30
1.40
1S O
1.60 1.801.70
0.174
0.156
0.143
0.132
0.124
0.231
0.208
0,190
0.176
0.165
0.260
0.234
0.214
0.198
0.185
0.289
0.260
0.238
0.220
0.206
0.318
0.286
O. 262
O. 242
O. 226
0.347
0.312
0.285
0.264
0.246
0.376
0.338
0.309
O. 286
O. 267
0.405
0.364
0.333
0.308
0.287
0.433
0.390
0.356
O. 329
0.308
0.462
0.416
0.380
0.351
0.328
0.491
0.442
0.041
0.116
0.104
0.095
0.088
0.082
0.373
0.348
0.520
0.468
0.421
0.395
0.369
0.55
0.60
0.65
0.70
0.75
0.039
0.037
0.036
0.034
0.034
0.078
0.074
0.071
0.069
0.067
0.117
0.111
0.106
0.103
0.100
0.155
0.148
0.141
0.137
0.133
0.175
0.166
0.159
0.153
0.149
0.194
0.184
0.176
0.170
0.166
0.213
0.203
0.194
0.187
0.182
0.232
0.221
0.211
0.204
O. 198
0.252
0.239
0.229
0.221
0.214
0.271
0.257
0.246
O. 237
0.230
0.290
O.275
0.263
O. 254
0.246
0.309
0.293
0.281
0.270
0.262
0.328
0.312
0.298
0.287
0.278
0.341
0.330
0.315
0.303
0.294
0.80
0.85
0.90
0.95
0.98
0.854 0.066
0.881 L 0.066
0.901
0.780
0.917
0.821
0.840
0.925
0.099
0.098
0.101
0.697 7
0.736
0.131
0.130
0.132
0.141
0.589
0.147
0.146
0.148
0.156
0.175
0.163
0.161
0.163
0.171
0.184
O. 178
0.177
0.178
O. 185
O. 197
O. 194
o. 192
0.193
0.200
0.210
0.210
0.208
0.209
0.214
0.223
0.226
0.223
0.223
0.229
0.237
0.241
0.238
0.238
0.243
0.250
0.257
0.253
0.253
0.257
0.264
0.272
0.268
0.268
0.272
0.278
0.288
0.283
0.282
0.286
0.291
0.99
1.o0
1.01
1.o2
1.O3
0.928
0.930
0.932
0.934
0.936
0.845
0.851
0.856
0.861
0.866
0.747
0.757
0.767
0.776
0.785
0.614
0.635
0.654
0.671
0.686
0.507
0.548
0.578
0.604
0.626
0.196
0.289
0.465
0.515
0.550
0.204
0.217
O. 249
0.360
0.215
0.224
0.237
0.263
0.317
O. 228
0.234
O. 243
0.257
0.279
0.241
0.246
0.253
O. 262
0.276
O. 254
0.258
0.264
0.271
0.281
O. 267
0.271
0.276
0.282
0.290
0.280
0.284
0.288
0.293
0.300
0.294
0.291
0.301
0.305
0.311
1.o4
1.O5
1.O6
1.O7
1.O8
0.938
0.940
0.942
0.944
0.945
0.870
0.874
0.878
0.882
0.886
0.793
0.800
0.807
0.814
0.820
0.700
0.713
0.725
0.736
0.746
0.645
0.662
0.677
0.691
0.705
0.579
0.603
0.624
0.642
0.659
O. 494
0.531
0.561
0.586
0.608
0.386
O. 488
0.522
0.552
0.316
0.363
0.411
O. 454
0.491
0.296
0.325
0.360
0.398
0.435
0.295
0.313
0.337
O. 365
0.3%
0.300
0.313
0.330
0.351
0.375
0.308
0.318
0.331
0.347
0.365
0.318
0.326
0.336
0.348
0.363
1.09
1.10
1.11
1.12
1.13
0,947
0.948
0.950
0.951
0.953
0.890
0.893
0.896
0.899
0.902
0.827
0.832
0.838
0.843
0.848
0.756
0.765
0.773
0.781
0.789
0.717
0.728
0.738
0.748
0.757
0.674
0.688
0.701
0.713
0.724
O. 627
O. 645
0.661
0.675
O. 689
0.577
0.598
0.618
0.636
0.652
0.522
O. 549
0.573
0.594
0.613
0.469
0.500
0.528
0.552
0.575
0.428
0.458
0.487
0.513
0.537
0.401
0.427
0.454
0.480
0.505
0.386
0.409
0.432
0.456
0.479
0.380
0.399
0.419
0.439
0.460
0.680
0.736
O. 778
0.811
O. 859
0.647
0.711
0.758
0.795
0.848
0.613
O. 686
0.738
0.778
0.837
0.580
0.661
0.718
O. 762
O. 826
0.549
0.636
0.699
0.747
0.815
0.523
0.613
0.681
0.732
0.804
0.502
0.593
0.663
0.717
0.794
0.058
0.052
0.048
0.044
""-
1
1
7
L"""
0.404
1
!
!
0.444
0.444
--`,,-`-`,,`,,`,`,,`---
0.30
0.35
0.40
0.45
0.50
1.15
0.955
1.200.786
0.810
0.833
0.878
0.920
0.961
0.966
1.25
0.970
1.30
0.977
1.40
0.931
0.940
0.953
0.894
0.908
0.930
0.857
0.876
0.906
0.838
0.860
0.894
0.818
0.844
0.883
0.713
0.761
O. 798
0.827
0.871
1s o
1.60
1.70
1.80
2.00
0.982
0.986
0.989
0.991
0.994
0.964
0.971
0.977
0.982
0.989
0.946
0.958
0.967
0.974
0.984
0.928
0.944
0.956
0.966
0.980
0.919
0.937
0.951
0.962
0.977
0.910
0.931
0.946
0.958
0.975
0.902
O. 924
0.941
0.955
0.973
0.893
0.918
0.937
0.951
0.971
0.885
0.912
0.932
0.948
O. 970
0.877
0.906
O. 928
0.944
0.968
0.869
0.900
0.923
0.941
0.966
0.861
0.894
0.919
0.938
0.965
0.854
0.889
0.915
0.935
0.963
0.846
0.884
0.911
0.933
0.962
2.50
3.00
3.50
4.00
0.999
1.001
1.002
1.002
0.998
1.002
1.004
1.004
0.997
1.003
1.005
1.007
0.997
1.004
1.008
1.009
0.997
1.005
1.009
1.010
0.997
1.006
1.010
1.011
0.997
1.007
1.011
1.013
0.997
1.007
1.012
1.014
0.997
1.O08
1.013
1.015
0.997
1.009
1.014
1.017
O. 998
1.010
1.016
1.018
0.998
1.011
1.017
1.019
0.998
1.012
1.018
1.021
0.999
1.013
1.019
0.908
0.744
0.774
0.803
0.858
1984
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
1.022
A P I TDB CHAPTER*b
**
m
0732290 0536655 204
m
TABLE 081.2
COMPRESSIBILITY FACTORS, SIMPLE FLUID TERM, zt0)
(PART OF PROCEDURE OBl.l)
Reduced Pressure
0
80
.60
2.40
2.20
2.00
1.80
1.70
11.491
3.442
0.578
0.520
0.474
0.438
1.328
1.312
'1.298
g1.287
1.278
0.347
0.330
0.315
0.303
0.294
'1.272
'1.268
.1.268
3.272
3.278
0.288
0.283
0.282
0.286
0.291
3.280
3.284
3.288
3.293
3.300
1.437
1.290
1.176
1.084
1.009
1.721
1.545
1.407
1.297
1.206
2.005
1.799
1.637
1.508
1.402
2
2
1
1
1
0.855
0.948
0.809
0.8%
0.853
0.816
0.785
1.131
1.069
1.016
0.971
0.933
1.314
1.240
1.177
1.124
1.079
1
1
1
1
1
0.616
0.601
0.589
0.582
0.579
0.688 0.760
O 670 0.739
0.656 0.722
0.646
0.709
0.642 0.703
0.901
0.874
0.852
0.834
0.825
1.040
1.W
0.979
0.956
0.944
1
1
1
1
1
0.553
0.553
0.553
0.553
0.554
0.578
0.578
0.578
0.578
0.578
0.640
0.640
0.639
0.638
0.638
0.702
0.700
0.699
0.698
0.697
0.822
0.820
0.818
0.816
0.814
0.941
0.937
0.934
0.931
0.928
1
1
1
1
1
0.531
0.532
0.533
0.535
0.537
0.555
0.555
0.556
0.558
0.559
0.578
0.579
0.580
0.581
0.582
0.638
0.638
0.638
0.638
0.639
0.696
0.696
0.695
0.695
0.695
0.812
0.810
0.808
0.807
0.806
0.925
0.922
0.920
0.917
0.915
1
1
1
1
0.517
0.520
0.523
0.526
0.530
0.539
0.541
0.544
0.547
0.550
0.561
0.563
0.565
0.568
0.571
0.583
0.585
0.587
0.589
0.592
0.639
0.695
0.695
0.695
0.6%
0.697
0.805
0.804
0.803
0.802
0.802
0.913
0.911
0.909
0.907
0.521
0.554
0.594
0.636
0.718
0.539
0.567
0.603
0.641
0.718
0.558
0.582
0.613
0.648
0.720
0.577
0.599
0.626
0.657
0.724
0.597
0.616
0.640
0.648
0.699
0.707
0.719
0.736
0.776
0.801
0.803
0.807
0.816
0.840
0.903
0.899
0.898
0.900
0.911
0.789
0.841
0.881
0.912
0.955
0.785
0.838
0.879
0.911
0.955
0.784
0.836
0.878
0.910
0.956
0.784
0.836
0.878
0.910
0.957
0.785
0.837
0.878
0.911
0.959
0.788
0.839
0.880
0.913
0.961
0.801
0.848
0.887
0.920
0.968
0.820
0.862
0.898
0.930
0.977
0.870
0.902
0.932
0.959
1.002
0.930
0.952
0.975
0.996
1.033
1.008
1.028
1.037
1.040
1.010
1.031
1.040
1.043
1.013
1.035
1.043
1.047
1.015
1.038
1.047
1.050
1.018
1.041
1.050
1.053
1.021
1.045
1.054
1.057
1.030
1.054
1.063
1.066
1.039
1.063
1.072
1.075
1.061
1.085
1.092
1.094
1.087
1.108
1.114
1.114
0.409
0.635
0.571
0.522
0.482
0.450
0.693
0.623
0,569
0.525
0.490
0.750
0.674
0.616
0.569
0.530
0.807
0.726
0.663
0.612
0.571
0.865
0.778
0.709
0.655
0.611
0.922
0.829
0.756
0.698
0.651
0.979
0.880
0.803
0.741
0.691
1.037
0.932
0.850
0.784
0.731
1.094
0.983
0.897
0.827
0.771
1.151
1.034
0,943
0.870
0.811
0.385
0.366
0.350
0.336
0.326
0.423
0.402
0.384
0.369
0.358
0.461
0.438
0.418
0.537
0.509
0.486
0.467
0.451
0.575
0.545
0.520
0.499
0.482
0.612
0.580
0.553
0.531
0.513
0.650
0.616
0.587
0.563
0.544
0.687
0.651
0.620
0.595
0.574
0.725
0.389
0.499
0.473
0.452
0.434
0.420
0.654
0.627
0.605
0.762
0.721
0.687
0.659
0.635
0.318
0.313
0.311
0.314
0.318
0.349
0.343
0.340
0.342
0.345
0.379
0.372
0.369
0.369
0.372
0.409
0.401
0.397
0.3%
0.398
0.439
0.430
0.425
0.423
0.425
0.469
0.459
0.453
0.450
0.451
0.499
0.488
0.480
0.477
0.477
0.528
0.516
0.508
0.503
0.503
0.558
0.544
0.535
0.529
0.528
0.587
0.573
0.562
0.556
0.554
0.294
0.297
0.301
0.305
0.311
0.320
0.323
0.326
0.330
0.334
0.347
0.349
0.352
0.355
0.358
0.373
0.375
0.377
0.380
0.382
0.399
0.401
0.403
0.405
0.407
0.426
0.427
0.428
0.430
0.432
0.451
0.452
0.453
0.455
0.456
0.477
0.478
0.479
0.480
0.481
0.503
0.503
0.504
0.504
0.505
0.528
0.528
0.528
0.529
0.530
3.308
3.318
3.331
3.347
3.365
0.318
0.326
0.336
0.348
0.363
0.339
0.345
0.352
0.361
0.371
0.362
0.367
0.372
0.379
0.386
0.386
0.390
0.394
0.399
0.405
0.410
0.413
0.417
0.421
0.426
0.434
0.437
0.482
0.443
0.447
0.458
0.460
0.463
0.466
0.469
0.486
0.489
0.492
0.507
0.508
0.510
0.512
0.514
3.386
3.409
9.432
3.456
3.479
0.380
0.399
0.419
0.439
0.460
0.382
0.395
0.410
0.425
0.442
0.395
0.404
0.415
0.427
0.439
0.412
0.419
0.427
0.436
0.446
0.431
0.437
0.444
0.451
0.459
0.452
0.456
0.462
0.468
0.474
0.473
0.477
0.481
0.486
0.492
0.495
0.498
C.502
0.506
0.511
3.523
:X613
3.681
:3.732
0.804
0.502
0.593
0.663
0.717
0.794
0.476
0.561
0.633
0.691
0.775
0.467
0.540
0.610
0.669
0.759
0.468
0.531
0.595
0.653
0.745
0.477
0.530
0.587
0.642
0.734
0.489
0.534
0.585
0.636
0.725
0.504
0.542
0.588
0.634
0.720
0.854
0.889
0.915
0.935
0.963
0.846
0.884
0.911
0.933
0.962
0.833
0.874
0.928
0.960
0.821
0.865
0.898
0.923
0.958
0.810
0.857
0.892
0.919
0.957
0.801
0.851
0.888
0.916
0.956
0.794
0.845
0.884
0.914
0.955
3.998
1.012
1.018
1.021
0.999
1.013
1.019
1.022
1.OOO
1.015
1.022
1.025
1.001
1.018
1.025
1.028
1.002
1.020
1.028
1.031
1.004
1.023
1.031
1.034
1.006
1.026
1.034
1.037
1.404
--`,,-`-`,,`,,`,`,,`---
3.373
0.348
0.520
0.468
0.427
0.395
0.369
0.904
0.402
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
0.440
0.484
Not for Resale
0.686
0.668
0.730
1.294
1.162
1.060
0.977
0.910
0.770
0.738
0.711
0.640
0.641
0.643
0.644
0.660
0.678
0.700
0.750
0.906
1
1
1
1
1
1
1
1
1
(
6B1.2
1.437
1.290
1.176
1.084
1.009
1.721
1.545
1.407
1.297
1.206
2.005
1.799
1.637
1.508
1.402
2.288
2.051
1.866
1.718
1.5%
2.851
2.554
2.321
2.134
1.980
3.131
2.804
2.547
2.340
2.171
3.411
3.053
2.772
2.546
2.360
3.967
3.548
3.219
2.954
2.735
0.30
O. 35
0.40
O. 45
0.50
0.948
0.8%
0.853
0.816
0.785
1.131
1.069
1.016
0.971
0.933
1.314
1.240
1.177
1.124
1.079
1.494
1.409
1.337
1.275
1.222
1.852
1.744
1.652
1.573
1.505
2.029
1.909
1.807
1.720
1.644
2.205
2.073
1.961
1.865
1.781
2.553
2.398
2.266
2.152
2.053
0.55
0.60
0.65
0.70
0.75
0.760
0.739
0.722
0.709
0.703
0.901
0.874
0.852
0.834
0.825
1.040
1.007
0.979
0.956
0.944
1.177
1.138
1.105
1.076
1.061
1.446
1.394
1.350
1.311
1.290
1.578
1.520
1.470
1.426
1.402
1.708
1.645
1.589
1.540
1.513
1.966
1.890
1.823
1.763
1.731
0.80
0.85
0.90
0.95
0.98
0.702
0.700
0.699
0.698
0.697
0.822
0.820
1.057
1.052
1.048
0.816
0.814
0.941
0.937
0.934
0.931
0.928
1.040
1.284
1.277
1.271
1.265
1.259
1.395
1.387
1.380
1.373
1.367
1.504
1.496
1.488
1.480
1.473
1.721
1.710
1.701
1.691
1.682
0.99
1.00
1.01
1.o2
1.O3
0.6%
0.6%
0.695
0.695
0.695
0.812
0.810
0.808
0.807
0.806
0.925
0.922
0.920
0.917
0.915
1.036
1.032
1.029
1.026
1.022
1.254
1.248
1.243
1.238
1.233
1.360
1.354
1.348
1.342
1.336
1.465
1.458
1.451
1.444
1.438
1.672
1.664
1.655
1.646
1.638
1.04
1.O5
1.O6
1.O7
1.O8
0.695
0.695
0.695
0.696
0.697
0.805
0.804
0.803
0.802
0.802
0.913
0.911
0.909
0.907
0.906
1.019
1.017
1.014
1.011
1.009
1.228
1.223
1.219
1.214
1.210
1.330
1.325
1.319
1.314
1.309
1.431
1.425
1.419
1.413
1.407
1.630
1.622
1.614
1.606
1.599
1.O9
1.10
1.11
1.12
1.13
0.699
0.707
0.719
0.736
0.776
0.801
0.803
0.807
0.816
0.840
0.903
0.899
0.898
0.900
0.911
1.004
0.995
0.989
0.986
0.987
1.202
1.184
1.170
1.158
1.142
1.299
1.278
1.259
1.244
1.220
1.395
1.370
1.348
1.328
1.298
1.585
1.552
1.522
1.496
1.453
1.15
1.20
1.25
1.30
1.40
0.820
0.862
0.898
0.930
0.977
0.870
0.902
0.932
0.959
1.002
0.930
0.952
0.975
0.996
1.033
0.995
1.008
1.024
1.040
1.069
1.134
1.132
1.134
1.139
1.152
1.205
1.197
1.193
1.192
1.1%
1.276
1.262
1.253
1.247
1.243
1.419
1.394
1.374
1.359
1.339
1S O
1.60
1.70
1.80
2.00
1.039
1.063
1.072
1.075
1.061
1.085
1.092
1.094
1.087
1.108
1.114
1.114
1.114
1.132
1.136
1.134
1.176
1.185
1.183
1.177
1.210
1.213
1.208
1.200
1.244
1.241
1.233
1.222
1.316
1.300
1.284
1.268
2.50
3.00
3.50
4.00
0.818
1.044
6-89
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
--`,,-`-`,,`,,`,`,,`---
Reduced
Temperature
.00
6.00
5.00
A P I TDB CHAPTER*b X *
m
0 7 3 2 2 9 00 5 3 6 6 5 70 8 7
m
CO
~
(
Reduced
Temperature
0.20
0.40
0.60
0.30
0.35
0.40
0.45
0.50
-0.016
-0.018
-0.019
-0.019
-0.018
-0.032
-0.037
-0.038
-0.037
-0.036
-0.048
-0.055
-0.057
-0.056
-0.054
-0.074
-0.076
-0.074
-0.072
-0.073
-0.083
-0.085
-0.084
-0.080
-0.081
-0.092
-0.095
-0.093
-0.089
-0.089
-0.101
-0.104
-0.102
-0.098
-0.097
-0.110
-0.113
-0.111
-0.107
-0.105
-0.120
-0.123
-0.120
-0.116
-0.113
-0.129
-0.132
-0.130
-0.124
-0.121
-0.138
-0.141
-0.139
-0.133
-0.129
-0.147
-0.151
-0.148
-0.142
-0.137
-0.156
-0.160
-0.157
-0.150
0.55
0.60
0.65
0.70
0.75
-0.017
-0.016
-0.016
-0.015
-0.014
-0.034
-0.033
-0.031
-0.029
-0.028
-0.051
-0.049
-0.046
-0.044
-0.042
-0.068
-0.065
-0.061
-0.058
-0.055
-0.077
-0.072
-0.069
-0.065
-0.062
-0.085
-0.080
-0.076
-0.072
-0.068
-0.093
-0.088
-0.083
-0.079
-0.074
-0.102
-0.096
-0.091
-0.085
-0.081
-0.110
-0.104
-0.098
-0.092
-0.087
-0.118
-0.111
-0.105
-0.099
-0.093
-0.126
-0.119
-0.112
-0.106
-0.100
-0.134
-0.127
-0.119
-0.112
-0.106
-0.143 -0.151
-0.134 -0.142
-0.127 -0.134
-0.119 -0.125
-0.112 -0.118
0.80
0.85
0.90
0.95
0.98
-0.116
-0.072
-0.044
-0.026
-0.018
-0.027
-0.027
-0.112
-0.059
-0.039
-0.040
-0.039
-0.040
-0.111
-0.064
-0.053
-0.051
-0.050
-0.054
-0.110
-0.059
-0.057
-0.055
-0.057
-0.069
-0.065
-0.062
-0.060
-0.061
-0.064
-0.071
-0.068
-0.065
-0.064
-0.064
-0.077
-0.073
-0.070
-0.068
-0.066
-0.083
-0.078
-0.075
-0.071
-0.068
-0.088
-0.084
-0.079
-0.075
-0.071
-0.094
-0.089
-0.084
-0.079
-0.074
-0.100
-0.094
-0.088
-0.082
-0.077
-0.105
-0.099
-0.093
-0.086
-0.080
-0.111
-0.104
-0.097
-0.090
-0.083
0.99
-0.016
-0.034
-0.053
-0.080
-0.114
-0.068
-0.014 -0.029
1.00
-0.012 -0.024
1.01
-0.010 -0.020
1.o2
-0.009 -0.016
1.O3
-0.044
-0.035
-0.028
-0.021
-0.059
-0.043
-0.030
-0.020
-0.067
-0.042
-0.026
-0.013
-0.064 -0.065
-0.066
-0.069
-0.088 -0.061 -0.061 -0.063
0.008 -0.047 -0.054
-0.022
0.089 0.023 -0.031
-0.006
0.116 0.032
0.005 0.059
-0.065
-0.059
-0.045
-0.015
-0.071
-0.068
-0.062
-0.052
-0.034
-0.074
-0.077
-0.080
-0.071 -0.074
-0.065 -0.069
-0.057 -0.062
-0.044 -0.051
-0.076
-0.072
-0.065
-0.056
1.o4
1.O5
1.06
1.O7
1.O8
-0.007
-0.005
-0.004
-0.003
-0.002
1.09
1.10
O.Oo0
-0.012
-0.009
-0.006
-0.003
-0.001
0.801.401.30
0.90
1.201.101.00
-0.064
-0.011 -0.003
0.006
-0.003
-0.005 0.003 0.013
0.009
0.019
O.Oo0
0.004
0.015 0.025
-0.015
-0.010
1.50
1.801.701.60
0.014
0.022
0.028
0.034
0.039
0.053
0.053
0.055
0.057
0.044
0.048
-0.145
-0.165
-0.169
-0.166
-0.159
0.121
0.106
0.097
0.092
0.090
0.103
0.136
0.139
0.133
0.126
0.039 -0.002 -0.023 -0.035 -0.044
0.095 0.045 0.010 -0.012 -0.026
0.132
0.091 0.051 0.020 -0.001
0.056 0.029
0.090
0.148 0.126
0.090 0.061
0.152
0.148 0.122
0.063
0.066
0.068
0.071
0.073
0.090
0.090
0.091
0.092
0.122
0.118
0.116
0.115
0.114
0.150
0.147
0.143
0.140
0.138
0.159
0.163
0.163
0.161
0.159
0.145
0.160
0.168
0.172
0.173
0.119
0.142
0.158
0.169
0.176
0.091
0.118
0.139
0.156
0.169
0.060
0.002
0.004
0.006
0.008
0.010
0.007
0.011
0.014
0.016
0.019
0.019
0.024
0.027
0.031
0.034
0.029
0.034
0.038
0.041
1.13
0.001
0.002
0.003
0.004
0.044
0.051
0.054
0.057
1.15
1.20
1.25
1.30
1.40
0.005
0.008
0.011
0.013
0.015
0.013
0.019
0.024
0.027
0.031
0.024
0.033
0.039
0.043
0.048
0.040
0.050
0.060
0.067
0.071
0.076
0.062
0.072
0.078
0.082
0.086
0.077
0.085
0.090
0.093
0.096
0.094
0.099
0.103
0.105
0.106
0.114
0.115
0.116
0.117
0.117
0.134
0.131
0.130
0.129
0.128
0.155
0.148
0,144
0.142
0.138
0.171
0.164
0.158
0.155
0.149
0.182
0.178
0.172
0.167
0.160
0.183
0.189
0.184
0.179
0.170
1S O
1.60
1.70
1.80
2.00
0.016
0.016
0.016
0.016
0.016
0.032
0.033
0.033
0.032
0.031
0.050
0.050
0.050
0.049
0.077
0.077
0.075
0.073
0.069
0.086
0.096
0.094
0.084
0.082
0.077
0.092
0.106
0.103
0.101
0.098
0.115
0.112
0.109
0.106
0.099
0.125
0.121
0.118
0.114
0.106
0.134
0.130
0.126
0.122
0.113
0.144
0.139
0.134
0.129
0.120
0.153
0.148
0.142
0.137
0.127
0.163
0.156
0.150
0.145
0.134
2.50
3.00
3.50
4.00
0.013
0.012
0.010
0.009
0.027
0.023
0.020
0.018
0.072
0.062
0.054
0.049
0.084
0.072
0.090
0.078
0.068
0.061
0.0%
0.083
0.073
0.065
0.1M
0.088
0.077
0.069
0.108
0.093
0.082
0.073
0.113
0.098
1.11
1.12
0.050
0.057
0.061
0.066
0.068
0.086
0.046
0.068
0.067
0.065
0.062
0.040
0.053
0.035
0.030
0.027
0.046
0.040
0.059
0.051
0.045
0.065
0.057
0.050
0.036
0.040
0.044
0.090
0.084
0.090
0.092
0.078
0.067
0.059
0.053
0.064
0.057
1984
--`,,-`-`,,`,,`,`,,`---
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
0.086
0.077
API TDB CHAPTERU6
**
m 0732290 0536658
TL3
m
TABLE 661.3
COMPRESSIBILITY FACTORS, CORRECTIONTERM, z(')
(PART OF PROCEDURE 6Bl.l)
Reduced Pressure
.602.40
2.202.001.80
1.70
-0.145
-0.165
-0.169
-0.166
-0.159
-0.161
-0.183
-0.188
-0.184
-0.176
-0.177
-0.202
-0.206
-0.202
-0.193
-0.193
-0.220
-0.225
-0.220
-0.210
-0.209
-0.238
-0.243
-0.238
-0.227
-0.225
-0.256
-0.262
-0.256
-0.244
-0.241
-0.274
-0.280
-0.273
-0.261
-0.257
-0.292
-0.298
-0.291
-0.278
-0.273
-0.310
-0.316
-0.309
-0.294
-0.289
-0.328
-0.335
-0.326
-0.311
-0.304
-0.346
-0.353
-0.344
-0.328
-0.320
-0.363
-0.371
-0.361
-0.344
-0.360
-0.408
-0.416
-0.405
-0.385
-0.400
-0.452
-0.460
-0.448
-0.425
-0.479
-0.540
-0.549
-0.533
-0.505
-0.557
-0.628
-0.636
-0.616
-0.583
0.143
-0.134
-0.127
-0.119
-0.112
-0.151
-0.142
-0.134
-0.125
-0.118
-0.167
-0.157
-0.148
-0.138
-0.130
-0.183
-0.172
-0.162
-0.151
-0.142
-0.199
-0.187
-0.175
-0.164
-0.153
-0.215
-0.202
-0.189
-0.177
-0.165
-0.231
-0.217
-0.203
-0.189
-0.176
-0.246
-0.231
-0.216
-0.201
-0.187
-0.262
-0.246
-0.229
-0.214
-0.198
-0.278
-0.260
-0.243
-0.226
-0.209
-0.293
-0.274
-0.256
-0.238
-0.220
-0.308
-0.288
-0.269
-0.249
-0.231
-0.324
-0.303
-0.282
-0.261
-0.241
-0.362
-0.337
-0.313
-0.290
-0.267
-0.399
-0.372
-0.345
-0.318
-0.293
-0.473
-0.439
-0.406
-0.374
-0.342
-0.545
-0.505
-0.465
-0.427
-0.390
-
-0.105
0.099
0.093
-0.086
-0.080
-0.111
-0.104
-0.097
-0.090
-0.083
-0.122
-0.114
-0.106
-0.097
-0.089
-0.132
-0.123
-0.114
-0.104
-0.096
-0.143
-0.133
-0.122
-0.111
-0.102
-0.153
-0.142
-0.131
-0.118
-0.108
-0.164
-0.151
-0.139
-0.124
-0.114
-0.174
-0.160
-0.146
-0.131
-0.120
-0.184
-0.169
-0.154
-0.138
-0.126
-0.193
-0.178
-0.162
-0.144
-0.132
-0.203
-0.186
-0.169
-0.151
-0.138
-0.213
-0.195
-0.177
-0.157
-0.144
-0.222
-0.203
-0.184
-0.163
-0.150
-0.245
-0.224
-0.202
-0.179
-0.164
-0.268
-0.244
-0.219
-0.194
-0.178
-0.312
-0.283
-0.253
-0.224
-0.206
-0.355
-0.320
-0.286
-0.253
-0.232
-
.0.077
-0.074
-0.069
-0.062
-0.051
-0.080
-0.076
-0.072
-0.065
-0.056
-0.086
-0.082
-0.078
-0.072
-0.065
-0.092
-0.088
-0.084
-0.079
-0.072
-0.098
-0.094
-0.090
-0.085
-0.079
-0.104
-0.100
-0.096
-0.091
-0.085
-0.110
-0.106
-0.101
-0.096
-0.091
-0.116
-0.112
-0.107
-0.102
-0.097
-0.122
-0.118
-0.113
-0.108
-0.102
-0.128
-0.123
-0.118
-0.113
-0.108
-0.134
-0.129
-0.124
-0.119
-0.113
-0.139
-0.135
-0.129
-0.124
-0.119
-0.145
-0.140
-0.135
-0.130
-0.124
-0.159
-0.154
-0.148
-0.143
-0.137
-0.173
-0.167
-0.161
-0.156
-0.150
-0.200
-0.193
-0.187
-0.181
-0.174
-0.225
-0.219
-0.212
-0.205
-0.198
-
-0.056
-0.043
-0.027
-0.007
0.017
-0.064
-0.054
-0.042
-0.028
-0.010
-0.072
-0.063
-0.053
-0.041
-0.027
-0.078
-0.071
-0.062
-0.052
-0.040
-0.085
-0.077
-0.070
-0.061
-0.050
-0.090
-0.084
-0.076
-0.068
-0.059
-0.096
-0.090
-0.083
-0.075
-0.066
-0.102
-0.095
-0.089
-0.081
-0.073
-0.107
-0.101
-0.094
-0.087
-0.079
-0.113
-0.106
-0.100
-0.093
-0.118
-0.112
-0.105
-0.098
-0.091
-0.131
-0.125
-0.118
-0.111
-0.104
-0.143
-0.137
-0.130
-0.124
-0.117
-0.167
-0.161
-0.154
-0.147
-0.140
-0.191
-0.184
-0.176
-0.169
-0.162
-
-0.047
-0.036
-0.024
-0.011
-0.064
-0.055
-0.045
-0.034
-0.022
-0.071
-0.062
-0.053
-0.042
-0.032
-0.077
-0.083
-0.097
-0.109
-0.133
-0.154
-0.069 -0.075 -0.089
-0.060 -0.066 -0.081
-0.050 -0.057 -0.073
-0.040 -0.048 -0.064
-0.102
-0.094
-0.086
-0.078
-0.125
-0.118
-0.110
-0.103
-0.147
-0.139
-0.132
-0.124
-0.035 -0.044
-0.012 -0.026
0.020 -0.001
O. 056
0.029
0.090
0.061
-0.085
--`,,-`-`,,`,,`,`,,`---
0.137
0.156
-0.160
-0.157
0.150
-
-
-
-
-
-
-
0.119
0.142
0.158
0.169
0.176
0.091
0.043
0.118
0.139
0.156
0.169
0.070
0.095
0.117
0.137
0.011 -0.011
-0.027
-0.039
-0.049
-0.057
0.033
0.007 -0.012 -0.026 -0.037
0.004 -0.012 -0.025
0.026
0.056
0.047
0.022
0.003 -0.012
0.078
0.040
0.019
0.067
0.003
0.100
0.182
O. 178
O. 172
O. 167
o. 160
0.183
0.189
0.184
0.179
0.170
0.167
0.199
0.203
0.199
0.189
0.137
0.193
0.211
0.214
0.206
0.105
0.176
0.209
0.221
0.220
0.077
0.154
0.200
0.222
0.231
0.053
0.131
0.186
0.217
0.237
0.033
0.109
0.169
0.208
0.240
0.017
0.090
0.152
0.196
0.239
0.003 -0.008 -0.018 -0.027 -0.046 -0.061 -0.087 -0.108 0.030
0.072
0.056
0.005 -0.014 -0.044 -0.068 0.043
0.135
0.119
0.090
0.061
0.037
0.001 -0.025 0.104
0.144
0.087
0.047
0.018 0.170
0.113
0.184
0.157
0.236
0.231 0.225
0.174
0.134
0.101
0.217
0.196
O. 153
o. 148
O. 142
0.137
0.127
0.163
0.156
0.150
0.145
0.134
0.181
0.173
0.166
0.159
0.148
0.197
0.189
0.181
0.173
0.160
0.212
0.203
0.195
0.187
0.173
0.225
0.216
0.208
0.199
0.185
0.235
0.228
0.220
0.211
0.1%
0.243
0.238
0.230
0.222
0.207
0.249
0.247
0.240
0.232
0.217
0.253
0.254
0.249
0.242
0.227
0.254
0.259
0.256
0.250
0.236
0,254
0.263
0.262
0.257
0.244
0.252
0.265
0.267
0.264
0.252
0.244
0.267
0.276
0.277
0.268
0.231
0.263
0.279
0.285
0.282
0.201
0.247
0.275
0.290
0.300
0.172
0.225
0.263
0.287
0.310
O. 108
0.093
0.082
0.073
0.113
0.098
0.086
0.077
0.124
0.108
0.095
0.085
0.135
0.117
0.103
0.093
0.146
0.126
0.112
0.100
0.156
0.135
0.120
0.108
0.166
0.144
0.128
0.115
0.176
0.153
0.136
0.122
0.185
0.161
0.143
0.129
0.194
0.169
0.151
0.136
0.203
0.177
0.158
0.142
0.211
0.185
0.165
0.149
0.219
0.193
0.172
0.155
0.237
0,210
0.189
0.171
0.254
0.227
0.204
0.186
0.283
0.256
0.233
0.213
0.305
0.282
0.258
0.238
Copyright American Petroleum Institute
Provided by IHS under license with API
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-
-
661.3
04.504.00
6.00
Reduced
Temperature
7.00
14.00
12.00
11.00
10.00
8.00
-0.360
-0.408
-0.416
-0.405
-0.385
-0.400
-0.452
-0.460
-0.448
-0.425
-0.479
-0.540
-0.549
-0.533
-0.505
-0.557
-0.628
-0.636
-0.616
-0.583
-0.636
-0.715
-0.723
-0.699
-0.660
-0.792
-0.886
-0.894
-0.861
-0.810
-0.869
-0.791
-0.978
-0.940
-0.883
-0.946
-1.056
-1.061
-1.019
-0.955
-1.100
-1.223
-1.225
-1.173
-1.097
0.30
0.35
0.40
0.45
0.50
0.324
0.303
0.282
0.261
0.241
-0.362
-0.337
-0.313
-0.290
-0.267
-0.399
-0.372
-0.345
-0.318
-0.293
-0.473
-0.439
-0.374
-0.342
-0.545
-0.505
-0.465
-0.427
-0.390
-0.615
-0.569
-0.523
-0.479
-0.436
-0.752
-0.693
-0.635
-0.579
-0.525
-0.819
-0.753
-0.689
-0.627
-0.568
-0.885
-0.812
-0.742
-0.674
-0.610
-1.013
-0.928
-0.845
-0.766
-0.691
0.55
0.60
O. 65
0.70
0.75
0.222
0.203
0.184
0.163
0.150
-0.245
-0.224
-0.202
-0.179
-0.164
-0.268
-0.244
-0.219
-0.194
-0.178
-0.312
-0.283
-0.253
-0.224
-0.206
-0.355
-0.320
-0.286
-0.253
-0.232
-0.396
-0.356
-0.318
-0.280
-0.258
-0.474
-0.425
-0.379
-0.334
-0.308
-0.512
-0.459
-0.408
-0.360
-0.331
-0.549
-0.491
-0.437
-0.385
-0.355
-0.621
-0.555
-0.493
-0.434
-0.401
0.80
0.85
0.90
0.95
0.98
0.145
0.140
0.135
0.130
0.124
-0,159
-0.154
-0.148
-0.143
-0.137
-0.173
-0.167
-0.161
-0.156
-0.150
-0.200
-0.193
-0.187
-0.181
-0.174
-0.225
-0.219
-0.212
-0.205
-0.198
-0.251
-0.243
-0.236
-0.228
-0.221
-0.299
-0.290
-0.282
-0.273
-0.265
-0.322
-0.313
-0.304
-0.295
-0.286
-0.345
-0.335
-0.326
-0.316
-0.307
-0.390
-0.379
-0.368
-0.357
-0.347
0.99
1.o0
1.01
1.o2
1.O3
0.118
0.112
0,105
0.098
0.091
-0.131
-0.125
-0.118
-0,111
-0.104
-0.143
-0.137
-0.130
-0.124
-0.117
-0.167
-0.161
-0.154
-0.147
-0.140
-0.191
-0.184
-0.176
-0.169
-0.162
-0.213
-0.205
-0.198
-0.190
-0.183
-0.256
-0.248
-0.239
-0.231
-0.222
-0.277
-0.268
-0.259
-0.250
-0.241
-0.297
-0.288
-0.278
-0.269
-0.260
-0.337
-0.326
-0.316
-0.306
-0.296
1.04
1.O5
1.06
1.O7
1.O8
0.083
0.075
0.066
0.057
0.048
-0.097
-0.089
-0.081
-0.073
-0.064
-0.109
-0.102
-0.094
-0.086
-0.078
-0.133
-0.125
-0.118
-0.110
-0.103
-0.154
-0.147
-0.139
-0.132
-0.124
-0.175
-0.167
-0.160
-0.152
-0.144
-0.214
-0.206
-0.197
-0.189
-0.181
-0.233
-0.224
-0.215
-0.207
-0.198
-0.251
-0.242
-0.233
-0.224
-0.215
-0.286
-0.276
-0.267
-0.257
-0.247
1.09
1.10
1.11
1.12
1.13
-0.128
-0.088
-0.047
-0.006
0.075
-0.164
-0.123
-0.082
-0.042
0.035
-0.181
-0.139
-0.098
-0.058
0.019
-0.197
-0.154
-0.112
-0.072
0.005
-0.228
-0.133
-0.139
-0.097
-0.019
1.15
1.20
1.25
1.30
1.40
--`,,-`-`,,`,,`,`,,`---
0.320
0.363
0.371
0.361
0.344
-0.406
0.027 -0.046 -0.061 -0.087 -0.108
0.030 0.005 -0.014 -0.044 -0.068
0.090 0.061 0.037
0.001 -0.025
0.047
0.018
0.144
0.087
0.113
0.134
0.101
0.217
0.174
0.196
0.252
0.265
0.267
0.264
0.252
0.244
0.267
0.276
0.277
0.268
0.231
0.263
0.279
0.285
0.282
0.201
0.247
0.275
0.290
0.300
0.172
0.225
0.263
0.287
0.310
0.146
0.204
0.248
0.279
0.313
0.106
0.167
0.218
0.258
0.310
0.090
0.152
0.204
0.247
0.305
0.076
0.138
0.192
0.237
0.300
0.052
0.116
0.171
0.218
0.290
1S O
1.60
1.70
1.80
2.00
0.219
O. 193
0.172
0.155
0.237
0.210
0.189
0.171
0.254
0.227
0.204
0.186
0.283
0.256
0.233
0.213
0.305
0.282
0.258
0.238
0.323
0.304
0.281
0.260
0.348
0.338
0.319
0.299
0.356
0.353
0.336
0.316
0.362
0.365
0.350
0.332
0.371
0.385
0.376
0.360
2.50
3.00
3.50
4.00
6-91
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
A P I TDB CHAPTERxb s f
m
0732270053bbb0b7L
m
--`,,-`-`,,`,,`,`,,`---
661.4
6-93
1984
Copyright American Petroleum Institute
Provided by IHS under license with API
No reproduction or networking permitted without license from IHS
Not for Resale
A P I TDB CHAPTER*b
*X
m 0732290 0536663
508
m
6B1.5
2.5
3.0
4.0
5.0
6.0
8 .O
10.0
14.0
REDUCED PRESSURE , Pr
6-94
1984
--`,,-`-`,,`,,`,`,,`---
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Not for Resale
A P I TDB CHAPTERtb * X
m
0732290 0 5 3 b b b 2 4 4 4
m
681.6
--`,,-`-`,,`,,`,`,,`---
6-95
1984
Copyright American Petroleum Institute
Provided by IHS under license with API
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Not for Resale
API TDB CHAPTERtb t t W 0732270 053bbb3 380 W
661.7
0.36
0-39
o .3 5
0.35
0.3 C
0.3 O
CI
.-
Y
N 0.25
0.25
I
K
W
0.20
o -20
i, 0 . 1 5
W
U
0.15
z
o
-
c
Pt
O
*
0.10
0.10
0.05
0.05
0.00
0.0
I
U
o
Io
iE
>
E
-I
c
a
o
E
m
-0.05
- 0.05
-0.10
-0-1
-0.15
-0.1 5
-0 -2 o
-20.0
a
I
O
o
3 .O
4 .O
5.0
REDUC E D
6-96
6.0
8.0
P R ESSURE,
10.0
o
20.0
pr
--`,,-`-`,,`,,`,`,,`---
Copyright American Petroleum Institute
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1984
Not for Resale
API
TDB CHAPTERxb
**
0732290 0536661) 217
6B1.8
PROCEDURE 681.8
ALTERNATE (COMPUTER) METHOD FOR THE DENSITY OF PURE
HYDROCARBONANDNONPOLARGASES
Discussion
The following method, whichwas used to generate the tables in Procedure 6Bl.1, is
recommended for estimatingthe density of pure hydrocarbon and nonpolargases by a digital
computer.
Where:
z = compressibility factor, dimensionless.
compressibility factor forthe simple fluid, whichis obtained from equation
(6B1.8-2).
Z ( h ) = compressibility factor for the heavy reference fluid (n-octane), which is obtained
from equation (6B1.8-2).
W = acentric factor of the compound for which the density is sought.
= acentric factor for the heavy reference fluid (n-octane) = 0.3978.
(0) =
The compressibility factors for the simple fluid z(O)and the heavy reference fluid z ( ~are
)
obtained from the following equation.
Where:
z(')= z(O) when the constants are those listed below for the simple fluid.
z(') = z ( ~when
)
the constants are those listed below for the heavy reference fluid.
p . = reduced pressure, p i p . .
p = pressure, in pounds per square inch absolute.
pc = critical pressure of the compound whose density is sought, in pounds persquare inch
absolute.
V ,=p,V/RT,.
V = molar volume of the simple fluid or of the heavy reference fluid, asthe case may be,
in cubic feet per pound-mole.
R = gas constant, 10.731 (pounds per squareinch absolute)(cubic feet) per (pound-mole)
(degree Rankine).
T, = critical temperature of the compound whose density is sought, in degrees Rankine.
T, = reduced temperature, T/ T,.
T = temperature, in degrees Rankine.
B=bl-bz/T,-b3JT:-bqITr3
C=C~-C~/T,+C)/T,?
D=dl+dZlI;
Two sets of constants are given below, one setfor the simple fluid and the other setfor the
heavy reference fluid.
Constant
bz
b,
b,
c1
c2
c3
c4
d l x 10"
d2 x lo4
ß
Y
1984
Copyright American Petroleum Institute
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No reproduction or networking permitted without license from IHS
Simple Fluid
Heavy Reference Fluid
0.1181193
0.265728
0.154790
0.030323
0.0236744
0.0186984
0.0
0.042724
0.155488
0.623689
0.65392
0.060167
0.2026579
0.331511
0.027655
0.203488
0.0313385
0.0503618
0.016901
0.041577
O. 48736
0.0740336
1.226
0.03754
--`,,-`-`,,`,,`,`,,`---
Not for Resale
6-97
A P I TDB CHAPTERtb t t
m
0732290 0536665 L53
6B1.8
Procedure
Step I: Obtain the critical temperature and pressure from Chapter 1 and the acentric
factor from Chapter 2.
Step 2: Calculate the reduced temperature and reduced pressure at which the density is
desired.
Step 3: Solve equation 6B1.8-2 for V,, using the constants for the simple fluid. Since the
equation is not explicit in V,, an iterative procedure will be required. Having obtained V, for
the simple fluid, use the reduced conditions obtained in Step 2 to calculate z(")=p,V,l T,.
Step 4: Repeat Step 3 for the heavy reference fluid using the same reduced temperature
and pressure. Hence, obtain z@).
Step 5: Use equation 6B1.8-1 to obtain the compressibility factor z for the gas under
consideration.
Step 6: Evaluate the volume from the relation V = z R T / p .
COMMENTS ON PROCEDURE 681.8
Purpose
This procedure is presented for calculating gas densities of pure hydrocarbons and nonpolar gases using a digital computer. Methods for mixtures are given in 6B2.
Limitations
In this work, the procedure has not been tested with data for nonhydrocarbons. The
literature source, however, indicates general agreement for nonpolar or slightly polar nonhydrocarbons so that reasonable results may be expected.
Reliability
Errors between calculated and experimental compressibility factors are usually less than 1
percent except in the immediate vicinity of the critical region, where errors as high as 30
percent can occur. The original literature source gives the range of applicability of the
equation as a reduced temperature of 0.3 to 4.0 and a reduced pressure of O to 10.0. Based
on a limited amount of testing, it was determined that the equation may be used up to
reduced pressures of 20 with little additional error. The reliability decreases with uncertainties in the critical properties of the compounds.
Speclal Comments
The following special considerations must be taken into account when solving the equations.
The equation has several volume roots, and the solution can converge on thewrong value.
These incorrect values are easily identified because they differ substantially from the expected value. Suitable checks must be built into the solution to guard against possible
convergence to the wrong root.
For saturated vapors, both temperature and pressure must be used as input parameters
(with vapor pressure predictions from Chapter 5 when necessary) and the calculations performed as if the point were in the homogeneous region.
For hydrogen, do not use the critical constants listed in Chapter 1 to calculate the reduced
properties; use the following values (lb, 6b):
T,=75 R
p . = 305 pounds per square inch absolute
Literature Source
The equations in this procedure were developed by Lee and Kesler, AIChE Journal 21 510
(1975).
1984
6-98
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.~
A P I T D B CHAPTER*b
X*
m
0732290 053bbbb 09T
m
PROCEDURE 662.1
DENSITY OF HYDROCARBON AND NONPOLAR GAS MIXTURES
Discussion
The tables and figures of Procedure 6B1.1 are to be applied to hydrocarbon mixtures by
using the pseudocritical temperature and pressure insteadof the truecritical temperature and
pressure to calculate reduced conditions. The pseudocritical properties, which are defined as
the molar averages of the component true critical properties, are given in Chapter 4 for
mixtures of defined and undefined composition and blends of the two. The mixture acentric
factor, which is defined as the molar average of the component acentric factors, may be
estimated for undefined mixtures from Chapter 2. The following are summaries of these
definitions:
n
Tpc
=
c
x, T,,
(6B2.1-1)
r=1
Where:
G,= pseudocritical temperature, in degrees Rankine.
T,, = critical temperature of component i, in degrees Rankine.
n = number of components in the mixture.
x , = mole fraction of component i.
ppc=
c x,
PEI
(6B2.1-2)
,=I
Where:
ppc= pseudocritical pressure, in pounds per square inch absolute.
p a = critical pressure of component i, in pounds per square inch absolute.
c
n
O
=
X I WI
(6B2.1-3)
r= 1
Where:
O = mixture acentric factor.
W, = acentric factor of component i.
Procedure
Step I: For mixtures of known composition, obtainthe critical pressures and temperatures
for all of the components from Chapter 1 and the acentric factors from Chapter 2.
Step 2: Calculate the pseudocritical temperature and pressure using equations (6B2.1-1)
and (6B2.1-2) and the mixture acentric factor using equation (6B2.1-3). (For petroleum
fractions and blends of petroleum fractions with mixtures of known composition, obtain the
pseudocritical conditions from Chapter 4 and the mixture acentric factor from Chapter 2.)
Calculate the reduced temperature and pressure.
Step 3: Calculate the gas density using Steps 3 and 4 of Procedure 6Bl.l with the reduced
conditions calculated previously.
1984
6-99
--`,,-`-`,,`,,`,`,,`---
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A P I T D BC H A P T E R x b
t*
m
0732290 053bbb7 T 2 6 D
682.1
COMMENTS ON PROCEDURE682.1
Purpose
--`,,-`-`,,`,,`,`,,`---
This procedure is to beused with Procedure 6B1.1to estimate the gas densities of mixtures
of hydrocarbons with other hydrocarbons andor with nonpolar nonhydrocarbon substances.
Limitations
In general, the method is not applicable to mixtures containing polar components.
Reliability
Errors in calculated compressibility factors rarely exceed 2 percent except in the critical
region, where 15-percenterrors should be expected and errorsof 50 percent can occur. This
region of maximum uncertainty is the same as that indicated in Figure 6B1.4.
When compared with approximately 6500 data points for a wide variety of hydrocarbon
mixtures of known composition, the overall average error was 4 percent, with well over 90
percent of the errors less than 2 percent.
The reliability of the modification for mixtures of undefined composition was not evaluated.
Special Comments
For hydrocarbon-hydrocarbon mixtures that donot containmethane, slightly better results
are obtained in the immediate critical region using true rather than pseudocritical temperatures and pressures. This region is defined approximately by the following pseudoreduced condition boundaries: 1.0 < T,< 1.2, and 1.0 <pr < 3.0. True critical conditions are
correlated in Chapter 4. Notice that theliquid phase can exist in this region even though the
pseudoreduced temperature is greater than unity (see Introduction to Chapter 4).
For supercritical temperatures (T, > 1) and high pressures ( p r > S), the error can be reduced to approximately 1percent by using the following mixture correspondence pressure
instead of the pseudocritical pressure which is defined by equation (6B2.1-2):
n
RTF
pmc
=
c x,zer
,=I
2 s&M,
(6B2.1-4)
,=1
Where:
pmc= mixture correspondence pressure, in pounds per square inch absolute.
R = gas constant,10.731 (pounds persquare inch absolute)(cubic feet) per(pound-mole)
(degree Rankine).
z, = critical compressibility factor of component i (from Chapter 2).
V, = critical volume of component i (from Chapter l ) , in cubic feet per pound.
M,= molecular weight of component i (from Chapter 1).
More reliable gas densities can be obtained under most temperature-pressure conditions
using the mixture correspondence rulesof Lee and Kesler (4b), Joffe (2b), Stewart et al. (9b),
or Leland and Mueller (5b). However, the small advantage in accuracy does not justify the
added labor involved in using these methods.
For mixtures containing hydrogen, do not use the hydrogen critical constants listed in
Chapter 1to calculate the pseudocritical properties. For hydrogen, use the following values
(lb, 6b): T, = 75 R and p c = 305 pounds per square inch absolute.
Literature Sources
Equations (6B2.1-1) and (6B2.1-2) were given by Kay, Znd. Eng. Chem., 28 1014 (1936).
Equation (6B2.1-4) was developed by Rausnitz and Gunn, AZChE Journal, 4 430 (1958).
Examples
A. Estimate the molar volume of a gaseous mixture of 90 mole percent propane and
10 mole percent benzene at 460 F and 4000 pounds per square inch absolute.
1984
6-1O0
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Not for Resale
~~
A P I TDB CHAPTERxb
*X
m
0732290 053bbbB962
m
6B2.1
Critical Temperature
Mole
Fraction
Component
Propane
Benzene
206.0
R
F
0.90
55
o.2.120
Molar average0.1576
665.7
1011.9
700.3
625.7
T, =
460 +459.7
=
700.3
Pr=
4o00 = 6.393
625.7
critical
Pressure
@ia)
Acentric
Factor
616.3
710.4
0.1517
0.2108
--`,,-`-`,,`,,`,`,,`---
The critical properties tabulated below were obtained from Chapter 1 and the acentricfactors from
Chapter 2.
FromTable6B1.2,z~0~=0.851,andfromTable6B1.3,z~'~=0.047.Usingequations(6B1.1-1)and
(6Bl . 1-2)from Procedure 6Bl.1,
z = 0.851 + (0.1576) (0.=04
0.85
7)
V=
(0.859)( 10.731) (460+ 459.7)
= 2.12cubic feet per pound-mole
4000
An experimental compressibility factor is 0.857.
B. Estimate the specific volume of a completely vaporized petroleum fraction at 560 F and
180pounds per square inch absolute having an API gravity of 53.9and the following ASTM D 86
distillation properties:
10
Distillation, percent by volume30
Temperature, F
230150
50 90 70
295
351
450
The volumetric average boiling point is thus 295 F, and the slopeis 3.75F/ percent distilled.
From Chapter 2,the molal and mean average boiling points are. 248.6F and 266.5F, respectively.
From Chapter 4,TF = 1062.8R and + = 408.9pounds per square inch absolute. From Chapter 2,
W = 0.333and the averagemolecular weight is 116.5.
T,=
p =
r
560 + 459.7
1062.8
180
-
419
=
= 0.9594
0.430
From Table 6B1.2, = 0.826,and from Table 6B1.3,z(l) = -0.041.Using equations (6Bl.l-1)
and (6Bl. 1-2)from Procedure 6Bl. 1,
z = 0.826+ (0.36)(-0.041) = 0.811
(10.731) (560+459.7)
= 49.3cubic feet per pound-mole
180
= 49.311 =10
6.427cubic feet per pound
V=
(0.811)
1992
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