The effect of reduced pressure on the efficiency of a packed rectification column
by Daniel O Popovac
A THESIS Submitted to the Graduate Committee in partial fulfillment of the requirements for the
degree of Master of Science in Chemical Engineering
Montana State University
© Copyright by Daniel O Popovac (1948)
Abstract:
A study is presented of the effect of reduced pressure on the efficiency of a packed rectification
column. A rectification column two feat long, one inch diameter and packed with 1/8 inch stainless
steel Fenske helices Wss employed* A test mixture of n-octane - toluene was used. Vapor-liquid
equilibrium was determined for this system at pressures of 20, 50, 100, 200, 300, 400, 640.3 and, 760
mm. Hg. absolute.
The column was then tested with the mixture at the same pressures, operating at just "below the
flooding point* Calibration was made at total reflux and at reflux ratios of 3041 and 20*1, in each case
it was found that the number, of theoretical • plates as determined' from the corresponding vapor-liquid
equilibrium diagram via the IeCabe-Ihiele method was between 11 and 14* Ihe same column calibrated
14 plates at 760 mi* Hg^ with the standard test mixture n-heptane * toluene/ IheSe results indicate that
column efficiency is independent of pressure * Design calculations may be based on vapor-liquid
equilibrium data determined at the same pressure as that at which the colum is to operate, the H.E.T.P.
of a given packing re-maining constant^ t '
I ' ■„
!BESBt 3###%' Q# BamWW 2 W M B #
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by •
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Snbmibted to th e CJtaanate' Sbamittee-.
%
U aytial fu lfillm e n t o f the requirements
■ fo r the degree Of
Master o f Sqience in Chemical Engineering
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Montana State College
ipproyedg
Sozemang Montana
Angus#*
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IA i- Ii CF COATFWIS
Page
I
SUinzaary
XI
Introduction* .
3
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4
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III
Experimental M aterials, Equipment and
Procedure . . . . . . . . . .
• • • •
IV
R esults . . . . . . . . . . . . . . .
11
V
Conclusions . . . . . . . . . . . . .
19
VI
References. .
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16
V II
Appendix. .
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18
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(Tables and Figures)
V
87103
8
3
,
-& s t * # i s ,p#ese#ted pf the. !Bdrgfeetr e f yWiicGa jpyw@%m
. W the
.#& a;2&d&ed %e^#ic&t&6& gel##,* .& SfdMdbj,*
f&o&tla& GolWa two f g # Iomg,. .one I n # &K#ietey &&a gashed
With i / 0 Iiaei-I g ta in le s g s t e e l Fenske h e lic e s Wes employe<i«
i t e s t s l » t w g o f 'a^oetase * to ia e n e was n sei^
agallfkriam was dateymlaed f or th is
#0^
fapoy*M<|UiS.
a t pressures o f
106,5 200% 3609 400$ #40$ and. /#6 MM4. I g * ahsolnth*
Ihe eoliinm was then tested, with the mixture a t th e same' pressurest Operatj1Ug'. a t ju st halew ■the flooding p oin t.^. S alih ration
TRas #&#$ a t t o t a l z a flu # ahd.8t..r#f%%%, ratl&a o f 30&I a&d$o$t<.
i& eadh a&ee. i t was
p la te s sis
# a t . tW wWW; a# tW @ r& tl#al...'
from the 4yqaf3*ews%iqd3dti&ig;
##1»
lihrium diagram v ia the IeSahe^f-Mele method ms he tween 11
and 14*
Ihe same column calibrated 14 p la t e s ,a t # 0 mi® %#
w ith the staM ar# t e s t mlBtura W%g#Wa 4 teiue&a^
fh # e '
r e s u lts in d ica te th a t column e ffic ie n c y i s independent: of pres*
sure*
Design ca lcu la tio n s may he based on w p or*liq n id e q u ili*
brlum data determined a t t h e .same pressure as that .at which
the nelw w i s t e #p@#ate% the &*#*#*#*'of e given packing re*
m&iWag eon stah tt .
X
.,y v ^ y ,,s
. .. ..
4
$6 ■$M d * e i# o f '
eolmms ■# e -# # i^aWIng $$ p la te
# # -:@apa$a%lW'"
4esire'4 and ■t&e operating eonditlana^ ■'IIany metfeads '■tax.'&$,&*>
enlating' tW nmMy
.'^ eo y etieal .'piates: 03?
-,soew*
Saary -fo? a given aeparatian. have %aen yapeg###
T hiele grapMeal method and the ^enske eqnatlon are -t# ll - ■■
known* ilQ-f-'B%- -fanthra InfineneAng Oolwnn e f^ ieaghey-'tonstth erefore ..play an Important, role 'In design caleulatioB * '
■
'-
^ ffleM noy i s not. a- funet-ion o f '.any 'single- p rep erly '# ' "r
ren d ition and -hs:S been 'in vestigated with, nany n eeu ltin g -eer# re la tio n s# • Many stu d ie s have been reported in the" litera tu re'
on th e o f f e e t - o f the p h y sical p rop erties of the m aterial being
fraotl-onated* • SrihkSw y and B ridfetd Showed th a t fo r PheS^7 •
merelai' hydroearhon fraetionatSng eolW ps and ahserhers,#7.the*
p la te e ffie ie n e y increased with th e .'deereasihg' v isc o sity # # ')
.Ji-
Thls- C orrelation was made:on commercial equipment -Wt i s ih lt *
a b le only fo r hydrocarhon. separations with low r e la tiv e v#a#t l l i t y -of- th e key components and'the average: molal liq u id '
v is c o s it y o f the column' feed.$ hoth’'at th e average tower temp**-erature and pressure*, ( I D
Brown and Soekhart- -studied the -effect o f vapor lead on
p la te e f fic ie n c y in fra ctio n a tin g columns*
(3)
They report
th a t except for Very low v e lo c itie s ^ the. overall column e ffi*
clency is re la tiv e ly independent o f mean tap er velocity^
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■BeSlmWa ■•efflusteacy being 'obtained a t the 'Basiatiam ailbwable'
v elo city Xrom ;the |ondezs:.- Brpwn Oqnatipn, (13)» ' -SBoSsp and
Blackburn Investigated and correlated th e e ffe c t of re la tiv e
amounts of the components in the s is tn r e and th e rate, OX'' dig*
t il la t io n ,upon efficiency#" .(16) ' ■' • • : 1. •
_
*:
• ,
■^ressnre has,- appeared in- t h e ' t ©chnical". lite ra ttire ' to date#Binary mixtures fo r evaluating" low' pressure d is tilla tio n col*
umns have been reported*- ‘W illiams suggested mixtures' o f
M ty l phythalate and dl^n^butyi, amolate fo r th is purpose for
pressures o f .about I mm, (17) ■Wldmak^ '%leS and -SrOhih : ■
.-V*1
studied binary m istures fo r evaluating r e c tif ic a tio n columns‘
a t pressures from 20 mm, Sg, to IGO mm, Hg* (7) ■lhey presented
-data on■two t e s t m ixtures; Ca) n*dodeeane and' cyclohexyl
cyclopentane and (b$ nitride-cane' and d icycioh exyl, *in, t h is ’
-
,rep o rt a- p lo t' of average re la tiv e v e la ti l l t y ■■versus the pres*
su re: shewed th a t for. the mixture n itrid e cane
'
dicyclqheXylg
y
the r e la tiv e v o l a t i l i t y approaches' a minimum a t ■about 1 # mm*
then r i s e s again*' For Wdodecane * ,cyolohexyl cyclopentane
the 'relative" v o l a t i l i t y :fol'l,ows'
a t 20
smooth' curve"' from a'.--Mgh
to a: low" a t #% mm* fhe- vapor liq u id equilibrium -
diagram for the: n^dodeeane
cyclohexyl' cyclopentane'' system
approaches the 4 5 -degree diagonal -from -above' as the pressure
increases' from 20 to 400 .mm* fh e diagram for n-tridecane ^
C icyclohexyl moves from below the 4-5 degree diagonal through
Ineldehoe w ith
to .above fo r InereasiB g (pressure from SD mm
to' '375: mm* '-Srissoid^ 'ihd^es hhd #& $i#.^ow ed
■■!
■high' ^fessW es 'oh' th e "Vapor, liq u id equilibrium
=
hehsehe
to lu w e ^ (5^ ! 'f h e ir p lo ts ' showed t h a t th e vapor ’ .••-
l i q u id w rv e 'Bppro^ehed .the ';;0 degree d la g ^ h a l from "Bhove'".as ■
the" p re ssu re IB oreased from Btmespherie to' 5©0 p s i f ': •,s
fh e purpose' o f th lh 'sofk i s ' t o ' determlBe t h e -Offeet Wf re*
duced pressure on columh OffIciehef*' ■’ifowhere In' th e lite r a tu r e
i s there information conoerning' the spe'eifio e f f e o t on Veeti*- •
f lo a t ion Offioieney of-changes IB operating pressure-,i - th e •
widely diverse views enterjtaihe^ by- d f s tf lia tlo h O # 0 rt# Wh'
t h i s subIeet in d ica te a nood fo r a .berreiatloB' o f those v a fi*
a b le s -9 ! ,t e s t mixture . was sought, which- approached id e a lit y ? ■
which was easy to analyse accurately, and would'.operate oyer
■a wide range' o f pressures.,. ■f he 'system m*0#tame v toluene -prow
ed to f u l f i l l these 'requirements most readily* th e Vaporliq u id equilibrium rela tio n sh ip s were determined a t a number
of d iffe re n t pressures between -SD mm# and 760 mm.#. Sg.» absolute*
A sta n d a rd ise d
packed column was th e n c a lib ra te d a t t o t a l r e f lu x
a t 30 i l r e f lux- r a ti o and a t '#$*1 re flu x ratio- -with th e -# s t mix*
tu re a t the 'same pressures at-which the vapor liq u id 1e q u ilib ria
had' been determined-,
the number -of th e o re tic a l p la te s of the
was determined from the vapor l l q a i i e q u ilib ria by
th e McOabe^fhleid method* ' #'inee vapor a # .liquid
o u tp u t
, ' - F.
'
Map w e ll W a -faeiatriMtlngS etem inatlbns
■
i'
in .eeltimn' e f f le i e ii # g ' a l l
. made with the column operating a t ju st
below the llooaing- pd in t? and th e ,ra te of liq u id ,take: c-ff
.
determined fo r ’t he ru n s, other’ than t
o
t
a
l
■>
. • ■
mmBBiA&G*
A# m G ##®
normal heptane (.Waatyaao -Ghemiea l
was su ffic ie n tly
pure, for use without fa rth e r processing*
.
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normal octane
'
(Connecticut SarG Suther Go.) and toluene (Baker’s Analyzed)
were- subjected to r e c tific a tio n in a laboratory column haying
approximately th ir ty th e o re tic a l p la te s $ and h eart c u ts .boll*
i n | net more than ± 0*2%/ f r ^ the-normal b oiling pointer
were' separated*
:-
i
Vapor liq u id equilibrium determinations were made in a
glass Othmer s t i l l ? (12) which.was, .connected to th e vacuum
eySbeto4* -fhe. 'vaonnm system, consisted of two fiv e gallon surge
tanks.g one of which was connected to a Wegavac vacuum pump*
A B etro it lu b ricato r GO## So# 683*3# solenoid valve was
placed in the lin e between the surge tanks and the valve was
activated fey a mercury contact vacuum regulator through ;a
Fisher-SerfasS electro n ic re la y , (SMUSte*'-
Bi dlS*
connecting the vacuum pump, p ressu risin g one surge tan k with
nitrogen and reversing th e relay# th e system could be made- to
operate a t super atmospheric pressure*
operating pressure was
read from a mercury manometer connected to the system.# ■
The r e c tif ic a tio n column employed was made of pyrek-glass
two fe e t long#: one inch in., diameter# packed 23 inches high
w ith 1/8 inch ^ensM sta in le ss s te e l helicea ahd equipped w ith
a gored constant r e f i t s rubles d is ti lli n g head*
The head and
fGHasMs*
%We##L
v&aw#& syeWet sws t W t
fe&e&vwe t@ %W
*##&& W '#WWw%& a t %&& o$)@r#
daitdLagg: pewmwe*. M # » .-ata#- <0 =GwaiaKt %w tk » a%Wm w e
# # d W ##& # 8 8 th e W#% j&#gB4aN%'i8d%3Bo8B9bsM5t' swat # & t # e W W &
'Ope$&t0 8 a t $& # TaetBbGMe th e fl#@#
IPTggMKB Bkdbg&aj&dt
:
WWM&WAWwa www <AW W 6 by
th e
A ?3&3&&* 8#8#&& 4 # (M aetm e; '#3% ahe
*y 3#&#$R#&&8 o f th e m Wo s#QN& ga&B&gaw* t # th e #%&&* ;%#e e t& #
#a# @WW a # ##& TS^mAy ywo### t # #& dw #*#' ###@#%&*.
$W M e t TRWtsa
t* $$#a a
r a t e * f @W#
w e # # pey e@W8&* # 8 m W a##» .w e - al&ooe# W bwt t #
&#p@ Iwot &tte3&
ItaisWBt IBRbB W a t %8s tayoed o f f ae#
th e TgSbGaaaxa; 8&Wy ^WWywWA* IRagBGBf #8# MggaM W W W . W »
SkedGaBR «hd ##& y
,d e W m # # Tw
W&#
&& & %3aet&#e #% e # # e W W ^ m o W , -WWWW t& SSkdGW
SSSSL*,
W& #yev&@Wy W w obte&Bea 0 # em%gW
mWa#na# o f W e &&#%&# e e W e t th e o##WLt&0B Of # 0 M y W #
*##%# Sb** read fy#*'*
A $ e g |# # R W
lh@#i * tm # 0 8 ltf0 8 oozmie*
W OW wW w TBw&gLiteea t o o # W % # o Wo
TpggGHBf te#pg#&t#r@ && # e #1%%* .
<»3? "% » 'W W 0 TPgte Ooae At SdBws ewW y e$ w w e#
f o r %&&#; e#l!U ^& % 8 a e t* #%ee o h te f m a t
A oW fge ^
%*
ootaBO * 1h9#88W wee M doa t o th o <edKdL&3%%H98& m d TR&#o%#B
$&#
m e f l o o d # to R esw e & tW fim ghiy we# # # $ % #
W & 'W WarB liipmt /aagmstei sa tfiat Ifee
p w ti# #
jfesl slS.gfela.3r fealow'.#o0##m# &M- 'rfefes were oo&tjWeW'W
'C
' '
'"
' '
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' fi' .
t o t a l r e f i l l fa r afeont. fiv e .fe6mra@.:. 4 vacnm receiver wap
used to obtain samples to fee analysed Wfeile Ifee eolmma re*.
imW&d a t # e
p^aemre*'
were taken'PdM I the analrsis .was eofestamt# #
Ifee re S lw
r a tio s of BOsl and 20sl$ tfee bead was properly adjusted and'
the rah eontifeued fo r a h a lf hour before, samples were taken*.
BurMg th i s time th e r a te of take o ff was determined., ffeeu
several samples were taken a t 15 minute Mterrals*. ■All ,e#ly*.
Sis Was done on the refractom eter and eompositioh determined
by the re fra c tiv e index'I- composition curve.
.Samples---Were■'
taken in th is manner u n til d i s t i l l a t e and bottoms composition
_
became a constant number- o f th eo retical, p lates apart,*:
....
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-*
..
e<mia
W
#5%# si -#$9 $;@%gB'.
aa# .#&$# 0e#faet*
I YB iMiBea' WB3?B IiffBYent' e:fioug-$i to permit accurate atiaiyslSte
- The f i r s t mixture ehosem was. eth^ibeB&B&e •■» n-octane, ' Ehese
liq u id s s a tis fie d the requirements .above hut the data obtained
on the system was .uusuita&&9* 4 ameetb equilibrium m m #
ew &' da& t W abtaiae#
' a t ' Im d' r .pm ssw #.^ %&&a &a&e #&&*#&
e a lib ra tio h with t h i s mixture impractieai^. # e system to # e a e *
,
metby&uyelo&e$&ae was the# te ste d but was found to h a # to p
lcmr $ b illin g p o in t a t 20, ami* and was therefore unsuitable
fo r th i s study*
: *.
' #*#etene * -toluene,prove# sa tisfa e to ry an# f u l f l l l s d a l l
th e requirements^ ■
the- boiling p oints of th e pure- components determined" Sn
the" equilibrium s t i l l compared favorably w ith the vapor pres*
SUre data found in the literatu re . (59 14, IS)
Ihese were
plotted' on at #ox CkBuairt and IdadLs;. MrW need to calculate- agtib*-'
v ity soeffieie& te*
u n reliab le temperature measurements a t '
20 mm. #&» made ca lib ra tio n s of vapor pressures an# a&tivl&y
co e ffic ie n ts impossible a t th is pressure, the experimental
equilibrium date and th e calculated data ,are shown In E eb les
I to V lIlf inclusive^ An example o f th e equilibrium-diagram ,
# t 480 mm* % * In 'ilia e tra te d 'In % # ra& I* B and '3# E&a&e
13
were p lo tted on graph paper.20 " . % 20 " .to give s u ffic ie n t
,.
aecwaey»'- : The eonsistance of the data is shown' to he satis^
faeto rv w m laspehfIon of th e a c tiv ity .coefficient .-dwves, -of Mgnres- 4- and 5 ah suggested by Oaaisen and Ooibnrn* (4)
Their •study shows th a t deviations- in these curves' indicate ■
inaccuracies in 'th e data* Siepes o f the lin es must always
of oppdaite s&gh'.'ht
/given v&lne o f &; i f th e _'8l$p&
one of the curves. Is equal to aero.)^fhe. other must .have a herd
slope a t the seme value e f.h # c e p t a t theytermlhhl peihts% " u " '" '
•
•
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* .
-
X» ,
.
-N
,
ry*
The approach to the value of 1#0 with a horizontal, tangent In*
d ic ates tabwali Baeult^s law applies to the opponent whose.mei
fra c tio n approaches 1 # -and Eehryt-S law demands th a t the -other
end of each curve reach a f in i te value with a f i n i t e slope*
fig u res 6 to 9:$ Inclusive^ -are p lo ts of the re la tiv e v o la tility
sis
Awam the data* ' .& p la t -of-average re la tiv e
t i l i t y versus pressure is ' shown, in Figure 10 * TM average'
re la tiv e v o la tility of th is system -Ms a maximum a t abdut- 4©0 ■
mm. Eg^ a s shown i n figure. 10*. o t# ie r reported th a t the mixture
aeetohe*water forms, eh azeotrope a t high pressures a n d :# # de*
creasing-, p re s s u re -th e 're la tiv e .M l d i i l i t y 'ihcreased* J '|B | ■ • •
Ber&* Harrison and MOhtgomery showed th a t the azeotrope cm#
p o sitio n of lsebuianol ^ethylbenzene decreases with increased
pressure* (I)
This, illu s tr a te s decreasing re la tiv e v o la tility
w ith decreasing pwegmte^
o f these reported M ta
with, th a t o f this, pgpe.^ ••.isd io ste ^ ,.-that "the e f te s t o f 'p^esstm
OA.th e r e i & t & v e " w i t h
tia#*'.
. •’ '!Tahis- l i :hOhtsihs the; % ta..Shtmihea- ^som the eaiiM atiO h ••
rm s* ; toes© data:
'.used- tsv-meke. hMsbe.^ihieie diagrams a t
•the various ptessw es* ■(figures.. I 3. 2 and 3) . From these dla#
grams the. number: of th e o re tic a l p la tes in the. column w a s , ,
VRA'
hpm the - 2$- 44^ 0»
@# packing In t w ho&mw*' $he
4 # a , are ahaW in /
’fa h ie S# She -Bumher' o f th e o re tic a l p la tw obtained at.'the
various pressures-- were h cn sisten tiy between I i and 14*. -
-r •.i
s lig h t % -higher w lt-es obtained # t the lower pressures.; might
b e ,gusti^iad'- 'bf: the Fadt th a t operation .closer- to Flooding, was
e a sie r to obtain at- .these- pressure's'giving a higher .eFfioieney^..
Ihe F aet that, the number of th e p re tic a l p la te s are eons.istentlf
between the •lim its o f 11 and 14 shews th a t the o f fie le n e f
mains, re la tiv e ly the same with changes in operating pres sure b
I t is in te re stin g to note that, the re s u lts do n et get ste a d ily
lm rer e r higher b a t th a t th e .^ # t'# a e re p a h a ie 'S .in .tw .)W b .e r
o f p la te s obtained are scattered ,enough to in d icate ":-ne .-define- ■
i t e trend#.
■
.
In order to W r iff the r e s u lts obtained with the system
n>octane »• toluene> th e column-was c a lib ra te d . a t -th e th ree • .
WFlm'" r a tio s with .ano#em t e s t
W i# ta n e , *We3#e&e*.
^W se W w lt s 'were -p lo tte d * 6 # g . t h e . e^uiMbrium, dh#- -o f - =Brotiiilef and Quiggle0
(2)
Ihe number o f th e o r e tic a l p la te s
■oMa'ined' mas' # which' Compares
,
,
..
System ^dctaiije'
1% #&&'.%*
_
with # 1#
' '
,
t W ' ",\
I .:
tolnehe'i=. '"9-hase .kata a & *"im#3^d 6d- ’3m -SalbleS' '
.
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The fo,ITowlhg conclusions' may'he .drawn from t h i s study?
' ■!(*..
Packed column eTTicioney' i s re la tiv e ly independent,
of changes in operating pressure and/factors normally ass©*- '
elated with pressure change #
2%
The increase or decrease ■in the. degree of separation
•of a mixture- in a given column accompanying pressure, change is
due prim arily to change in the average re la tiv e v o la tility
w ith pressure.#.
■ 3*
‘Design calculations fo r re c tific a tio n should he
based upon the vapor liq u id equilibrium re la tio n a t the oper­
ating, pressure#
'
//
V,
W%5
W
Berg. &k, : Wr W%4. . 4 * ' % * » . ' & *
3%d* Bag, #hem*j%a* # # % # # )
M
Bpamiiey* is* #* ea# @a&gg%e*. #** 2&a* Bog*
3.136 (1933)
a)
Bewn# 0* S.9 aiaS loekbaet*. F»
(#
Berieea* &*, 8* eB&'gol&o&B* &-* ?&* ia6*;B#g*. #e%**3&*
(g)
B o s s , # 4 P * * & b y3l@ & l'8@ n ateB tB q f t% e P r & o c ip a l H y d ro *
( 6)
B r le k a A e * * 5 » 8 * a o d B * e d f@ e a , j * B * , i r a o s * & * !* # * $ %
(7)
63 (1943)
'"
lr e a e * ^ « $ * ^ 1 * »
981 (1942)
earMns^ 4tB Ed* ike f e?ras.Sb*-) 1943
a&* 33# ( w a }
. .
F e ia a e o * # 4 a Blsclei;* H* * BOG. O r c k lB a J * , P a p e r p r e s e o t e d
kef ore the Petroleum Division of the American Ohemzeal
Societyi5 April*., 1948
(8)
EeBshe5 M., E* % Ind# EBg» BlieMe5 p4q. 482 (1932)
( 9)
Griswold.
AtB^GhaM
(10)
(11)
Bicdake5 #* ':$,* end T h iele5 S* W*9 TraBa, A*I*dh#45 M
605 ( 1 9 2 5 ) . . . . . . . . .................. ,
Q^Qonnell5 H*, Bs.$,'IraBS» .A*l#Qh*^* *
/41 (194o)
( 12 )
Othmer5 #4 3 ,* TBd^, Eag* .dhe#. .Aoal# $4* jk ' ^ 0 (1932)
( 13 )
Othmer5 D5 E,,. and C orley, .E, H*5. Paper presented kef ore
the 108th meeting o f the ,AMerican Ohemicai SOciety5
September 5 1944 ..
(14)
Perry.
36k». 2Bd
( 15)
Souders5 S5. J r^ 5 and Brown5 0» G. 5 Xnd5 Eng6 Ihem55
98 (1934) . . .
ABdpeB9 D,, and klAlo* B, A*? ipaaB*.
223 (1943)
handbook, f O
r , EBgl neer8%
% c W ^ # ill Boeh # * * # w Tork (1941)
( 16 ) Ehodes9 E5 H* and BlackkurB5 P* O55 Ind* EB%_0 hem* 5
51 (1937)
^
W * B&e, # .# * ,
:
MljlZaas:,, K
■
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779; <-1947),,.
f 18). sHantbo^k of abem lstfy a^a. $by&&e&% ' W 6:
'' '2#h- ga# f ' $h&m$.t3&l' Bubbai1'•Bubll
,
%&$$#;■
;-f194243,);
18
Page
it
Fquillbriim Data, for, n-Oetaue ^ Toluene
a t 20 iBBie. % -# B' #- % »' f <s- o
^
-ff- ■80
Table I I .
Squilibritm Data for S fstem n^Oetane
!a b le III*
Squlllbrium Data for, Syete# n*#otena *
. ' ,
Teluene a t 100 mm^ #. .? $ > * *■ ■•» % ■»= » ■#. TB
$ab le VIf
Bquilibriim Data .for System n^Oetane •*
. Toluene a t 200, mm. , *,* * ». ^ »;»' », » »■. a. . 23,
Toluene a t
mm* . .v » •« *. * $ * # a f » T li
$abie
Equilibrium Data, fo r System n^Oetane 4 .
Ioluene a t 300 Bm^ #- •*■ » ^ •> -» *■ » @* 24
Table VI*
Equilibrium Data' fo r System n^Oetane. 4.
Table VII*
Equilibrium Bata fo r System nroqtane *
'Toluene a t 640 mm» ^ .*. .* >* 4 ■* * t 4 4 .»• 86
Teiusne a t . 48# mm* .
+ .*;&..* * » *,%,* 2#
T able V I llf Equilibrium Data for. System n^Octane $
Toluene a t 760 mm*
s # %
. * 4. # -#• ■« »• # & 2T
T a b le.%
Column C alibration Bata far System
Table %*
Column O a lib fltie n i Bata- for System
n-Oetane % Toluene » * * 4 » 4 *■ #. » *. * .29
Figure I .
Equilibrium Curya and T heoretical P la tes
UeOotaue * Toluene .# 4 # * * ^ * 4 ? a #- 28
a t T otal Reflux a t 400 mm# Hg:# ‘ » .# <? » * 3©
fig u re a#
Equilibrium Surye -and T heoretical P lates
- a t 39#& &efTu& B stlo a t %G mm&Bg* 4.* # . 31
Figure 3»
Equilibrium Curye and Theoretical P lates
a t 2011 Reflux Ratio at, 400 mm, Hg, . » » 32
Figure 4 b
A ctiv ity C o efficien ts at Various
Figure
A c tiv ity O o effloieu ts a t Various
.
Pres-Sure-S
# .« -$- # .-# #. 4 ». « .$ $ # 4 -4 4 -.34
Pressures#, 4 * •* * .*•,# -# # ’* #. # * # # #
3.3
Rage.
IFSgWe
1 BeSeMw IhoIfatSSftieTgr. s ir # " Wk- em#
§ 0 SBQjt 'Bg-W *
-P
*: 'S' 'S :.*. -S-■.^. •«.
-p
A # 8 #
#
35 .
S1Igure fir " B e M t S v e s*: SOO sm* aW
2d0.' B#*- BgA" # #' '» #' «• % * > * •*. # # # A'' 36
SiSgtoe 8 sf R elative V o la t ilit ie s a t 300. may and
: ' 400 iffi% Bg'W-' w % # %' # # # ■&•: j#. * ¥ * #
S ig to e 9<
37'.
"R elative ■f o l a t i l i t l e .s -a t 640 mu. and
4 * * * St" 3#
76O mm# Rg4.' '# 4 * 4
SSgure :10t "Average- R elative V el& tW ty vereue
S reeeto e Sn. min* %.*
# *. « #• » w •» -* * X
t
39
TABLE I
E quilibrium Data fo r n-Octane - Toluene at 20 nsn.
Weight %
in Liquid
R e la tiv e
V o la tility
Weight #
in Vapor
n-Octane
Toluene
IOO
9 8 .1
9 4 .4
9 1 .3
8 7 .7
8 3 .0
8 2 .6
7 9 .5
7 2 .5
6 4 .5
5 6 .0
4 7 .7
3 8 .9
3 1 .8
2 6 .3
2 0 .7
1 6 .0
1 1 .3
8 .0
0
O
1 .9
5 .6
8 .7
1 2 .3
1 7 .0
1 7 .4
2 0 .5
2 7 .5
3 3 .5
4 4 .0
5 2 ,3
6 1 .1
6 8 .2
7 3 .8
7 9 .3
8 4 .0
8 8 .8
9 2 .0
1 0 0 .0
n-Octane
100
9 5 .8
8 8 .0
8 2 ,3
7 7 .1
6 9 .8
6 9 .4
6 5 .4
5 7 .3
4 7 .5
4 0 .8
3 4 .4
2 7 .6
2 2 .0
1 8 .4
1 4 .9
1 1 .9
8 .7
6 .4
0
Toluene
0
4 .2
1 2 ,0
1 7 .7
2 2 .9
3 0 .2
3 0 .6
3 4 .6
4 2 .7
5 2 .5
5 9 .2
6 3 .6
7 2 .4
7 8 .0
8 1 .6
8 5 .1
8 8 .1
9 1 .3
9 3 .6
1 0 0 .0
2 .2 6 5
2 .3 0
2 .2 6
2 .1 2
2 .1 1
2 .1 0
1 .9 9
1 .9 6 3
2 .0
1 .8 5
1 .7 4
1 .6 7
1 .6 5
1 .5 7
1 .4 9
1 .4 1
1 .3 2
1 .2 7
TABLE I I
E q u ilib r iu a D ata f o r S y stem n - O ctane - T olu en e a t $0 mm.
Weight %
in Liquid
Temp.
0C.
n -Octane
50.7
50
U9.8
lt8.8
1(8.3
1(7.5
1(6.7
L5.8
1(5.0
ltlt.2
1(5J(
1 0 0 .0
9 9 .9
1(2.8
1(1.7
1(1.2
1(0.5
1(0.2
59.3
38.9
38.5
38.2
37.9
37.6
37Jt
37.0
36.9
Toluene
0 .0
0 .1
0 .9
99.1
96.9
9L.5
92.7
88.5
85.7
3.1
lt.5
7.3
11.5
Ht.2
8 2 .8
1 7 .2
77Jt
71.9
68.7
61.0
60.0
52.0
ltlt.2
37.6
29.7
23.3
18.5
15.0
11.3
8.0
5.7
0 .0
22.6
28.1
31.3
39.0
1(0.0
1(8.0
55.8
62Jt
70.3
76.7
81.5
85.0
88.7
92.0
9U.3
100.0
Weight #
in Vapor
n -Octane
1 0 0 .0
98.9
95.5
90.0
87.0
82.1
75.5
70.7
65.5
58.2
52.8
50.0
43.2
42.5
35Jt
29.2
2b.5
20.0
16.5
13Jt
11.2
8.5
6.2
4.3
0 .0
Toluene
0 .0
l.l
4.5
1 0 .0
13.0
17.9
24.5
29.3
34.5
4i.8
47.2
50.0
56.8
57.5
64.6
70.7
75.5
80.0
83.7
86.6
08.8
91.5
93.8
95.7
100.0
Vapor Pressure
mm. Hg.
n -Octane
50.0
49.8
49.2
46.3
45.5
43.7
42.0
4o.5
38.5
37.0
36.0
35.0
33.2
33.0
31.2
30.6
29Jt
28.8
28.2
27.7
27Jt
26.7
26.5
26.0
Toluene
92.5
90.0
86.0
85.0
83.0
78.0
7 6 .0
73.0
70.5
68.0
67.0
64.0
62.0
60.5
59.6
57.0
55.8
54.8
54.0
53.2
52.5
51.8
51.0
50.0
A c tiv ity
C o e ffic ie n t
n -Octane
Toluene
R e la tiv e
V o la t i l i t y
0.981
1.003
1.012
1.012
1.016
1.019
1.028
1.013
1.021
i.o4o
1.072
1.068
1.091
1.078
1.108
1.170
1.240
1.305
1.365
I JtCB
lJt6c
1.450
2.780
1.880
1.700
lJt80
1.370
1.360
1.370
1.310
1.240
1.190
1.140
1.160
1.110
1.060
1.060
1.020
0.996
0.984
0.981
0.963
0.982
0.995
5.2
3Jt7
3.17
2.77
2Jt9
2.50
2.53
2Jt6
2.28
2.19
2.06
2.03
1.98
1.91
1.86
1.69
1.56
lJt7
1.40
1.37
1.31
1.34
TABLE I I I
E q u ilib r iu m B ata f o r S ystem n - O otane - T olu en e a t 100 mm.
Weight %
in Liquid
Temp.
°C*
65.5
6^.6
6U.2
63
6U.o
62.5
61.2
59.6
58Ji
57.0
55.6
55.2
5UJi
53.8
53.3
53.0
52.6
52.2
52.0
n-Octane
100.0
99.9
97.8
97.6
91.9
96.9
99.0
65.5
78.6
70.8
62.8
5U.2
12.3
32.1
25.6
17.5
13.3
9.0
6.9
0.0
Toluene
0.0
0.1
2.2
2J|
8.1
3.1
i i .0
H1.5
21Ji
29.2
37.2
Ii5.8
57.7
67.9
7l|Ji
82.5
86.7
91.0
93.1
100.0
Weight <
in Vapor
Vapor Pressure
mm. Hg.
n -Octane
Toluene
n -Octane
100.0
98.9
9(|.0
93.5
8IJ1
90.7
76.2
70.2
60.5
50.2
ii3.1
37Ji
28.5
22.2
18.2
13.1
10.5
7.0
5.5
0.0
0.0
1.1
6.0
6.5
18.6
9.3
23.8
29.8
39.5
ii9.8
56.9
62.6
71.5
77.8
81.8
86.9
89.5
93.0
9ti.5
100.0
100.0
96Ji
91.8
91.5
98.5
90.5
85.5
8I.5
76.0
71.0
67.5
63.O
62.0
60.0
58.0
57.0
56.5
55.0
51.5
Toluene
168
165
162
157
161
152
Hi5
137
130
123
116
IlIi
HO
107
105
103
102
100.5
100
A c tiv ity
C o e ffic ie n t
n -Octane
Toluene
1.030
1.052
1.042
1.000
6.55
1.65
1*67
lJ|6
1.86
1J|2
I J|2
1.35
1.31
1.25
I . 0l|0
1.002
1.008
1.013
1.000
1.018
1.095
1.088
1.150
1.225
1.310
I JlOO
I JllO
IJ46C
1.18
1.09
I .Oil
1.025
1.003
1.002
1.002
1.010
R e la tiv e
V o la t il it y
Uel
2.78
2.79
2.59
3.21
2.53
2.50
2J|0
2.k)
2.23
1.9ll
1.ali
1.66
1.55
IeUl
1.31
1.31
1.27
TABLE IV
E q u ilib r iu m D ata f o r S ystem n - O ctane - T olu en e a t 200 mm*
Weight %
in Liquid
Weight %
in Vapor
Vapor Pressure
ran. Hg.
Temp.
°C.
n-Octane
Toluene
n -Octane
Toluene
n-Octane
83 J+
8 2 .0
8 1 .0
79
7 8 .0
7 6 .2
TM
7 3 .8
7 2 .8
7 1 .0
7 0 .0
6 9 .7
69*6
6 9 .5
69 Jt
100.0
9 9 .0
9 5 .0
9 0 .7
8lt.6
7 6 .0
67.3
5 7 .0
lt9.5
3 7 .3
2 7 .8
2 0 .3
1 3 .6
0 .0
1 .0
5 .0
9 .3
15 Jt
2Lt.0
3 2 .7
1+3-0
5 0 .5
6 2 .7
7 2 .2
7 9 .7
86 J ;
9 2 .8
100.0
100.0
9 3 .0
8 7 .1
7 8 .8
6 8 .7
5 7 .9
ItS .3
3 9 .7
33-5
2k Jt
1 8 .9
lit .9
0 .0
7 .0
12 .9
2 1 .2
31 .3
1+2 .1
5 1 .7
6 0 .3
6 6 .5
7 5 .6
8 1 .1
8 5 .1
9 0 .0
9k .6
100.0
200
190
183
173
162
152
lk3
138
132
123
119
117
116.2
116
7.2
0 .0
IO rO
5Jt
0 .0
Toluene
"306
298
285
268
252
239
230
223
210
20k
202
201
200.2
200
A c tiv ity
C o e ffic ie n t
n-Octane
0.990
1.002
1.003
1.005
1.003
1 . 00k
1.010
1.025
1.063
1 . 11+2
1.255
1.263
1.293
Toluene
k .560
1.730
1.600
1.515
1.390
1.320
1.220
1.180
1.155
1.110
1.060
I .
oko
1.022
R ela tiv e
V o la t il it y
7.53
2.81
2 .5 9
2 .5 0
2 .3 0
2 .2 0
2 .01
1.89
1 . 8k
1.6 6
lJ+5
l J +2
1 .3 6
TABLE V
E q u ilib r iu m D ate f o r S ystem n - Ootane - T o lu en e a t 30 0 mm*
Weight %
in Liquid
Temp.
°C.
n -Octane
9U4
93.1
92*3
91.it
90.7
88*8
87.3
85.7
83.1
82.0
81.3
80.8
80.6
80Jt
80.2
80.1
100.0
Toluene
96.7
92.3
88.6
82.5
73.8
6U.7
52.0
2*3.7
3W
29.0
18.9
0.0
1.6
3.3
7.7
IlJt
17.5
26.2
35.3
2*8.0
56.3
65.2
71.0
81.1
11.8
8 8 .2
0 .0
100.0
98 J j
8.2
91.8
Weight %
in Vapor
n -Octane
100.0
93.6
68.3
83.0
76.7
66.1
56.2
2*6J*
36.8
30J*
23.8
19.7
13.2
8.5
6.5
0.0
Toluene
0.0
6Jt
11.7
17.0
23.3
33.9
2*3.8
53.6
63.2
69.6
76.2
80.3
8 6 .8
91.5
93.5
1 00.0
Vapor Pressure
mm. Hg*
n -Octane
500
280
273
265
236
239
230
215
198
190
185
182
179
178
177
A c tiv ity
C o e ffic ie n t
Toluene
n -Octane
2*2*2
2*32*
1*20
2*12
390
368
350
321
310
307
302*
302
301
300.2
300.0
1.020
1.005
1.020
1.015
1.005
1.008
1.002
1.072
1.100
1.110
1.115
1.165
1.215
1.32*5
Toluene
2.720
2J*50
1.580
1J*85
1J*90
1.365
1.300
1.230
1.200
1.150
1.120
1.067
1.01*0
1.020
R e la tiv e
V o la t il it y
i*.20
3.89
2j*6
2.36
2J*2
2.20
2.12
1.86
1.78
1.71
1.67
1.53
I J*2*
1.29
TABLE VI
E q u ilib r iu m D ata f o r P ystw a n - Octane - T olu en e a t JiOO am .
Weight %
in Liquid
Temp.
0C.
n -Octane
103.0
101.6
100.0
98.5
97.0
95J+
94.5
93.5
94J:
93.7
92.5
92.0
91.5
91.2
90.7
90.3
89.6
89.2
88.9
88.8
88.7
100.0
98.5
95.5
91.9
86.0
BO.9
73.5
56.9
71.9
64.0
53.8
50.5
46.3
36.6
27.7
22.7
18Jj
13Ji
8.5
4.2
0.0
Toluene
0.0
1 .5
4.5
8.1
14.0
19.1
26.5
43.1
28.1
36.0
46.2
49.5
53.7
63Ji
72.3
77.3
81.6
86.6
91.5
95.8
100.0
Weight %
in Vapor
Vapor Pressure
am. Hg.
n -Optane
Toluene
n -Octane
100.0
94.3
87.7
78.3
67.5
61.0
53.5
4i.o
52.1
46.1
36Ji
34.3
32.0
24.9
19.8
16.1
12.8
9.7
6.5
5.7
0.0
0.0
5.7
12.3
21.7
32.5
39.0
46.5
59.0
47.9
53.9
63.6
65.7
68.0
75.1
80.2
83.9
87.2
90.3
93.5
96.3
100.0
400
370
350
334
314
302
290
281
288
282
270
268
264
261
258
255
248
246
240
239
Toluene
575
560
530
512
480
470
450
467
454
437
432
424
420
415
4n
4o4
402
4oi
400.5
4oo
A c tiv ity
C o e ffic ie n t
n -Optane
1.035
1.050
1.020
1.000
1.010
1.005
1.025
1.005
1.020
1.005
1.015
1.045
1.040
1.110
1.115
1.125
1.185
1.275
lJi75
Toluene
2.650
1.950
2.030
1.840
1.700
lJi90
1.220
IJ4.6O
1.320
1.265
1.240
1.200
1.130
1.075
1.058
1.0$2
1.042
1.020
1.010
P e la tiv e
V o la t i l i t y
3.97
2.97
3.14
2.96
2.71
2Jil
1.90
2.35
2.08
2.04
1.95
1.83
1.74
1.55
1.53
1.53
1Jt4
1.34
1.14
TABLE V II
E q u ilib r iu m D ate f o r S ystem n -O c te n e - T o lu en e a t 6 J4.O mm*
Weight %
in Liquid
Temp*
n -Octane
Toluene
w eigh t %
in Vepor
n~Octane
Toluene
n -Octane
100.0
95.5
91.8
89.0
8?fO
76.9
70.6
63.2
5lt.0
50.0
a .3
39.1
3l*.8
30.8
26.8
22.2
19.8
17.1
0.0
lt.5
8.2
11.0
16.0
23.1
29Jt
36.8
lt6.0
50.C
55.7
60.9
65.2
69.2
73.2
77.8
80.2
82.9
85Jt
87.3
89.2
91.2
93.7
100.0
6lt0
°c.
118J t
116.6
115.8
115.3
l l i t .8
lllt.O
112.8
111*5
109Jt
108.8
107.8
107.2
106.5
105.8
105.6
105.0
ICit.6
lC it.2
IQLfO
10%.8
103.6
1(9 Jt
103.3
103.2
100.0
99.0
97.6
96Jt
93.8
90Jt
86.1
79.3
72.5
68.7
62.3
56.7
lt9.9
a .7
38.1
32.7
26.3
23.8
20.0
17.1
IltJt
I lJ t
8.1
0.0
0 .0
1.0
2Jt
3.6
6.2
9.6
13.9
20.7
27.5
31.3
37.7
W.3
50.1
55.3
61.9
67.3
71.7
76.2
80.0
82.9
85.6
88.6
91.9
100.0
Vapor Pressure
mm. Hg*
llt .6
12.7
10.8
8.8
6.3
0.0
595
580
568
557
5lt0
520
510
1*75
1*61*
Ut8
Wt2
1*35
i»2lt
lt20
ItlO
lt07
'tOlt
lt03
1x02
ltd
ItOO
ItOO
Toluene
920
875
870
865
8lt5
820
780
7h0
720
705
697
677
668
660
655
6ft9
646
6U,
6Lt3
61*2
61tl
61*0
titO
A c tiv ity
C o e ffic ie n t
n -Octane
I . OttO
I . OttO
I . OttO
1.030
1.010
1.010
1.000
1.005
1.005
1.015
1.000
1.025
I . OttO
1.070
1.060
1.100
1.HtO
1.160
1.190
1.230
1.21x0
1.260
Toluene
3.130
2Jt90
2.21*0
1.910
1.820
1.650
lJ*6o
Ut50
I Jt20
1.31*0
1.29c
1.230
1.200
1.150
1.130
1.10$
1.082
1.065
1.050
I . OttO
1.030
1.022
R e la tiv e
V o la t i l i t y
lt.66
3.6t*
3.27
2.88
2.85
2.58
2 .2 3
2.25
2.19
2.08
2.d*
1.87
1.81
1.68
1.70
1.60
1.51
IJ46
1 J tP
I.39
1.5U
1.31
TABLE VIII
E q u ilib r iu m D ata f o r System n - O ctane - T o lu en e a t 760 mm*
W eight %
i n L iq u id
W eight %
in Vapor
Temp.
0C
n -Octane
Toluene
n -Octane
Toluene
125.2
12U.0
125.0
122.2
120.7
119.0
117
116.2
115.0
115.8
115.0
112.5
111.6
100.0
9 9 .3
9 7 .7
9L .9
9 0 .7
8 5 .6
0 .0
0 .7
2 .3
5 .1
9 .3
16 J i
2 2 .6
3 0 .2
3 5 .5
ii5 .5
5 3 .8
6 3 .8
7 3 .2
8 0 .8
8 9 .5
9U-8
100.0
100.0
9 7 .1
9 3 .5
8 7 .7
80 Ji
6 9 .3
6 1 .8
5 5 .6
1(6.9
3 8 .1
3 2 .7
2 5 .2
19.3
111.2
8 .2
it.l
0 .0
0 .0
2 .9
6 .5
12.3
IS .6
3 0 .7
3 8 .2
111.0
110.5
110.2
110.1
rrJx
6 9 .8
6U.5
5h.5
U&,2
3b .2
2 6 .8
19.2
10.5
5 .2
0 .0
UhJx
5 3 .1
6 1 .9
6 7 .3
7*1.6
8 0 .7
8 5 .8
9 1 .8
9 5 .9
100.0
Vapor P ressu re
nun. Hg.
n -Octane
760
720
700
660
660
6L5
598
579
558
527
522
518
511
1*98
I186
ii78
Toluene
1200
1150
1060
1050
975
930
900
866
titiO
822
810
790
775
766
762
760
A c t iv it y
C o e f f ic ie n t
n~Ge tane
1.035
l.d iO
1.035
1.020
0 .9 9 0
1.015
I . 0L5
0.990
1.010
1.025
1.020
1.075
1.130
1.220
1.250
Toluene
2.630
1.870
1.700
1.560
1J*60
1.580
1.21*0
1.310
1.230
1.160
1.100
1.060
l.OtlO
1.020
I . UlO
R e la tiv e
V o la tility
h»2h
2 .9 5
2^1
2.3 8
2 .2 6
2 .1 2
I .85
2 .0 6
1.95
1.7 7
1.61*
I .53
1.1*3
1.32
1.28
28
TABLK IX
Column C a lib r a tio n Data f o r System n-Ootane - Toluene
■Veiyht $ Toluene
In S t i l l p o t
P re ssu re
h e ig h t % Toluene
in D i s t i l l a t e
Kim. Hg.
T o ta l
R eflu x
3 0 :1
R e flu x
R a tio
2 0 :1
R e flu x
R a tio
T o ta l
R eflu x
30 :1
R eflu x
R a tio
2 0 :1
R e flu x
R a tio
Through­
put
m l./ia in .
20
1 7 .6
1 1 .0
8 .1
9 6 .6
9 6 .5
9 6 .2
1 .8 0
50
5 .5
7 .3
1 6 .0
9 6 .9
9 6 .9
9 6 .2
9 .3
100
4 .4
7 .3
8 .4
9 6 .7
9 6 .2
9 6 .5
1 2 .7
200
3 .9
8 .0
1 0 .5
9 6 .7
9 6 .5
9 6 .5
1 8 .7
300
9 .9
1 2 .0
9 .9
9 7 .0
9 6 .6
9 6 .1
2 0 .8
400
1 0 .6
1 3 .0
1 5 .8
9 6 .4
9 6 .1
9 5 .9
2 5 .8
640
8 .1
1 4 .0
1 7 .4
9 6 .0
9 5 .5
9 4 .4
2 6 .9
760
7 .6
1 2 .8
1 8 .1
9 5 .4
9 5 .6
9 5 .3
'
.-■/♦
Column S ta n d a r d iz a tio n w ith System n-Heptana - Toluene
2 8 .6
2 0 .5
1 8 .0
2 8 .0
9 2 .5
760
8 8 .9
9 0 .0
2 8 .0
29
TABLS X
C olu m C a lib r a t Ioh Data f o r System n-O ctane - T oluene
Nuidber o f
T h e o r e t ic a l P la t e s
•ea sure
i* Hg.
T o ta l
H eflu x
30 s i
R e flu x
R a tio
H .S .T .P .
20 Si
R eflu x
R a tio
T o ta l
R eflu x
30 s i
R eflu x
R a tio
2 0 :1
R eflu x
R a tio
20
13
14
15
1 .7 7
1 .6 4
1 .5 3
50
13
14
12
1 .7 7
1 .6 4
1 .9 2
100
1 3 .5
1 3 .5
1 3 .7 5
1 .7 0
1 .7 0
1 .6 7
200
1 2 .5
1 2 .5
1 2 .5
1 .8 4
1 .8 4
1 .8 4
300
1 1 .5
1 1 .7 5
1 1 .5
2 .0
1 .9 6
2 .0
400
11
11
11
2 .0 9
2 .0 9
2 .0 9
640
1 1 .5
1 1 .5
1 1 .5
2 .0
2 .0
2 .0
760
1 1 .7 5
12
1 1 .7 5
1 .9 6
1 .9 2
1 .9 6
1 .6 4
1 .6 4
Column S ta n d a r d iz a tio n w ith System n-IIeptane - T oluene
760
14
14 '
14
1 .6 4
WEIGHT PER CENT
TOLUENE IN VAPOR
30
20
WEIGHT
40
PER CENT
60
TOLUENE
80
IN LIQUID
Figure I
Equilibrium Curve and Theoretical Plates at Total Reflux
at 400 mm. Hg.
31
20
WEIGHT
40
PER CENT
60
TOLUENE
80
IN LIQUID
Figure 2
Equilibrium Curve and Theoretical Plates at 30:1 Reflux
Ratio at 400 mm. Hg.
32
WEIGHT PER CENT
TOLUENE
IN LIQUID
Figure 3
Equilibrium Curve and Theoretical Plates at 20:1 Reflux
Ratio at 400 mm. Hg.
33
O TOLUENE
• N-OCTANE
50 MM
ACTIVITY COEFFICIENT
* • #-+-
*o
IOO MM
200 MM
WEIGHT PER CENT TOLUENE IN LIQ.UID
Figure 4
A ctiv ity C o efficien ts at Various Pressures
v~ o
34
O
•
MM
400
MM
A CTIV ITY
COEFFICI
300
TOLUENE
N O C T A NE
20
W EIGHT
PER
640
MM
760
MM
40
CENT
60
TOLUENE
IN
80
LIQUID
Figure 5
A ctiv ity C o efficien ts at Various Pressures
MM
RELATIVE
50
)
20
WEIGHT
30
PER
40
50
CENT TOLUENE
Figure 6
60
IN
70
LI OkUI D
RELATIVE
VOLATILITY
36
WEIGHT
PER
CENT
Figure
TOLUENE
IN
L KXUID
7
R elative V o la t ilit ie s at 100 mm. and 200 mm. Hg
t
37
3 .0 -
MM
RELATIVE
VOLATILITY
400
W EIGHT
PER
CENT
TOLUENE
IN
LIClUID
Figure 8
R elative V o la t ilit ie s at 300 mm. and 400 mm. Eg
38
W EIGHT
PER
760
MM
640
MM
CENT
TOLUENE
IN
Lt CXUI D
R elative V o la t ilit ie s at 640 mm. and 760 mm. Hg.
"
2.1
v
K
O
(3
3
5
C)
d'a
>
W
>
P
3'«
U
OC
UI
O
W
S
200
ABSOLUTE
300
400
PRESSURE
500
IN
600
700
*00
MM.
Figure 10
Average R elative V o la tility versus Pressure in
mm. Hg.
MONTANA STATE UNIVERSITY LIBRARIES
762 100 5208 9
N3 7 S
I uuJ l g y io a
_______ nnp. g__________________ _
Popovac, D. 0.
----Ihe—e ffe c t—o f reduced pressure on the e ffic ie n c y of a
packed recti f i r a t i o n r»r>1nmn
—------------—
nUTF
K3?8
I
ISSUED TD
87108
cap. 2
Z