BAKU HIGHER OIL SCHOOL
CHEMICAL ENGINEERING DEPARTMENT
SEPARATION PROCESSES A
LABORATORY REPORT 1
NAME
Aysu Zamanova
EXPERIMENT TITLE
Batch Distillation
GROUP NUMBER
19.1
DATE OF EXPERIMENT
07/10/2022
DATE OF SUBMISSION
23/10/2022
SUPERVISOR
Hajar Nabiyeva
Table of Contents
Synopsys: .............................................................................................................................. 2
Introduction: ......................................................................................................................... 3
Theory:.................................................................................................................................. 7
Experimental Framework: ................................................................................................... 12
Safety Precautions: ...................................................................................................................... 12
Experimental equipment: ............................................................................................................. 13
Procedure .................................................................................................................................... 16
Results: ............................................................................................................................... 17
Discussion: .......................................................................................................................... 23
Conclusion: .......................................................................................................................... 28
Bibliography ........................................................................................................................ 29
Appendix A: ......................................................................................................................... 31
1
Synopsys:
Definite, elaborate, alongside with succinct apprehension besides precise phenomena in
terms of the demonstration of speculative and academic peculiarities, paramount figures,
as well as the preponderant objective of the introductory laboratory report that is indicated
as comprehension of main aspects and working principle of batch distillation column where
especially rectification process of ethanol-water compound was carried out, will be
conscientiously addressed amidst the laboratory report. Throughout the scrutiny, certain
goals should have been attained including monitoring, determination, and controlling of
several features of mixture such as temperature alongside the distillation column device,
analysis of the generated materials as the bottom and the top product, furthermore,
carrying out material balance of the products of rectification column. Foregoing distillation
column utilized for observing rectification process of ethanol and water mixture was
produced by company named GUNT company and was specified as CE600. In the context
of measurement of profile segment of temperature, specifically 10 individual points of
temperature ranging from evaporator to the top part of the packed distillation column were
noted down, with the most pivotal one being 3rd magnitude since it is the signifying
temperature value within the evaporator also with the leading number amongst the others.
At the starting point of experiment reboiler temperature was around 72.2℃, and
temperatures of each section was repeatedly measured with the ranging timespan around
8-15 minutes until evaporator tank temperature reaching 92℃. Subsequently, once
distillate formed within the tank after passing through condenser analysis of product
sample was initiated so as to figure out certain qualities bearing density through volume
and mass computations that is for apprising ethanol quality by dint of table prepared by
GUNT company. Through calculations it was deduced that at the end of the process an
amount of 1.282 kg distillate could be collected with the ethanol mass balance being
86.67%, meanwhile initial feed to rectification column was 6kg with the mass percentage of
ethanol standing at 25%, meaning that higher quality ethanol mixture was obtained.
Nevertheless, error values for ethanol and total mass balance were acceptable as roughly
5.4 and 14%, respectively. Following results section of the report, within discussion part all
possible causes which have led to such errors were described.
2
Introduction:
The preeminent aim for conducting such laboratory scrutiny was denoted as to apprehend
most predominant understandings of rectification column alongside with the phenomena of
separation processes by means of utilizing aforementioned CE600 column which moreover
provides noteworthy opportunity of comprehending main structure and basis of separation
columns.
Taking into consideration that designing and understanding chemical/process engineering
applied devices such as pumps, reactor columns, heat exchangers, compressors and
distillation columns are of significant importance, since design characteristics and features
as quality of materials, construction method, and distillation mechanism refers to a pivotal
role within the industrial processes. Regarding to the worldwide application of industrial
processes through production approach, certain factors incorporating refining, enrichment,
purification, and concentration are important for producing and generating products with
required standards; as a consequence, various distillation and separation techniques have
been developed for meeting the preferable concentration and purification of components
such as analytical separation as chromatography which is highly utilized for discernment of
complex compounds; meanwhile, preparative separation techniques are utilized for
purification and refinery of the products that is remarked to possess almost comparable
structures with analytical separation. (Seader, n.d.) Nevertheless, methods utilized within
laboratory scale production and purification of materials may differ from that of industry
scale processes since whilst within laboratory chemists are focused on separating mixtures
with light-hydrocarbons through chromatography with gas-liquid, chemical engineers
mostly relies on distillation columns for separating exactly same compounds.
Generally, within chemical industrial processes whenever refinement of substances are
required considering that certain raw materials must be processes prior to the introduction
to the reaction section, extract gases which are incondensable as well as the undesirable
by products, cleansing the stream products, and recycling the needed compounds back to
the process, distillation columns are highly demanded so as to increase the value and
purity of the produced material. With the highly applications of separation devices, quite a
few methods within the industrial scale has been developed such as distillation, stripping,
3
extraction, and absorption; therefore, the fundamental science behind the separation
processes is noted to be phases which are banded together and are in equilibrium.
(Wankat, n.d.) The separation processes most commonly rely on either the physical or the
chemical properties of the materials especially the discrepancies between those aspects
where the main ideology behind such phenomena on all occasions depends on the
formation, dimension, and structure of material molecules, charges of the components,
solubilities within exact solvents, densities, and boiling points.
Although being highly-utilized process within high-tech era of our planet, distillation
processes are studied and discovered to date even back to 3500 before the common era
within Mesopotamia, Syria, China, and Egypt, with the predominant purpose of carrying out
operation for perfumery. So as to remove pivotal oil components from the herb materials
through application of evaporation and condensation of liquids which were architecturally
discovered with the pots and stills found in excavations within the areas of Baghdad in Iraq.
Figure 1. Extraction pot and its structure discovered in Baghdad.
(Kockmann, n.d.)
The liquid mixture poured inside the pot is vaporized through heat transfer around the
below part of the pot while some part of the vaporized substances condenses to the colder
cap as described in the figure 1. Furthermore, created droplets run through the ring and
collected there, in the exact part the organic materials such as the herbs and needed
leaves have been separated by the liquid mixture. Meanwhile, for the fermented mixtures
separation process may be carried out in order to separate alcohol substances through
vaporizing and condensing to the rings that are carried out for fragrances and perfumery
4
oils, in the meantime the exact process is applied within industry with further reflux and
extraction with the device named as Soxhlet extractor.
Several types of distillation processes are quite utilized within the industrial applications
each of them possessing certain features and structures with the predominant objective of
reaching maximum efficiency, with the types including simple, steam, short path, fractional,
vacuum, zone, and air-sensitive distillation processes. (V.R. Dhole, 1992) While simple
distillation technique introduces the method of heating the liquid compounds until they
reach the boiling point which ends up an instant condensation process of produced vapors,
fractional distillation requires a fractioning column where consequent vaporizationcondensation steps are carried out, that is called as rectification method. The other leading
dispersity between rectification and simple distillation is the differences between boiling
points of substances need to be separated since although fractional distillation was
developed to separate liquids with quite close boiling points, for the sake of purification of
separated materials boiling points for simple distillation should not be close. Moreover,
steam distillation as the other separation method is utilized for separating heat-sensitive
materials, not needing high temperature values for the whole system, slightly heated steam
line passes through the liquid mixture in order to vaporize certain part of the compound.
(McCabe, 2004)Whenever the requirement is to vaporize mixtures with high boiling
temperature points, vacuum distillation is referred since increasing temperature till higher
numbers would eventually cause undesirable energy and efficiency repercussions and
rather than foregoing process, decreasing pressure for the decrease in boiling points is denoted to be much more effective; nevertheless, other application area is separating
components which decompose at relatively high temperatures. Once the vapor pressure
reaches the pressure surrounding the system, vaporization process is initiated, following
with the condensation and collection of the top product as a distillate. With the solely
distinction from the vacuum column being the addition of inert gas when the process is fully
completed, air sensitive vacuum columns are highly utilized for compounds that will react
with the air components.
Throughout industrial chemical productions of materials, certain substances may indeed
reveal as well as display characteristics which may lead to unstable features within
surrounding at high temperature, hereinafter short path distillation is specified for
5
purification of compounds which is named as a short path since distance moves through a
compact distance prior to collection of condensate. Consequently, the zone distillation
introduces a method where melting the substance partially is necessitated preceding the
vaporization and condensation process where a zone heater is applied within a long
container. (Ouljic, 2014)
In case of complementary application of distillation and rectification processes, certain
sectors must be prenoted for comprehending the momentousness of distillation columns.
Considering that water scarcity is considered as the world-wide problem, distillation refers
to a huge solution for desalination plants which incorporates with the rectification methods
so as to further decontaminate insalubrious water sources, which moreover are applied for
fields such as lead-acid batteries, and humidifiers especially with low volume. (Bode,
1977)With the prevailing intention of reducing the vapor pressure of crude oil obtained from
the underground wells for supplemental secure stowage and conveyance, one of the
techniques of distillation so-called as oil stabilization is of utmost importance.
The preliminary objective of conducting the initial experiment was to apprehend the
essential aspects of separation process throughout inspecting distillation of water-ethanol
mixture: with scrutinizing temperature, volume, mass, and density values for further
obtaining quality of ethanol compound. The report then undertakes theory section amidst of
which theoretical hypothesizes, arithmetical equivalences in the context of mass, density,
and volume, as well as the equations relating mass balances referring to the most volatile
components with the equilibrium conditions. Furthermore, distillation column unit also
known as CE600 will be elucidated in a thorough fashion. Consequently, initiated with the
explanation of main parts of column, progressive methodology of experimentation will be
beheld. Figures obtained throughout laboratory scrutiny will thereupon be referred for
algebraic calculations, regarding to the results of computations remarked in the tables of
temperature profiles of distillate formations, meanwhile for later visual representations of
mass fraction of most volatile component which in this case is ethanol will be plotted.
Subsequently, probable culprits for noticeable variances between practical and
hypothetical values, expectancies for carried out investigations, analysis of plotted graphics
will be extensively explained, pursued with a summary of scrutiny with recapitulating
experimentation.
6
Theory:
Overall, distillation processes have been applied to quite a few sectors throughout
centuries ranging from household applications to industries with the preliminary intention of
separating components from a mixture with the predominant principle lying within the
boiling points, also known as the volatility differences of the substances contributing to the
mixture. Since started from the ancient times around the first century A.D., in the modernworld efficiency of the separation processes can be increased through consuming
appropriate energy sources with the increment on the equilibrium stage numbers. The
whole idea behind distillation process mostly is engaged with equilibrium stage concept
with a theoretical presence, within each stage in the distillation column the assumptions of
vapor-liquid equilibrium and movement of vapor liquid as the distillate alongside with the
liquid product to the bottom part is considered as real case concepts. Although real-case
physics features may totally accept foregoing phenomena for trayed columns, for the
packed columns this idea will
probably bear certain
misconceptions and deviations.
(Berry, 1972) With the stages
of distillation column being
adjusted with appropriate
structure, algebraic
calculations based on theoretical p resumptions
will fit the
figures
for real
distillation
Figure 2. Equilibrium
stage
concept.
(Skogestad,
2000)
columns even the ones with packed columns.
Vapor-liquid equilibrium for the ideal mixtures is figured out through the Raoult’s law stating
the fact of interrelationship between partial vapor pressure of the component with its mole
fraction in liquid phase and saturated pressure of the exact component, which is denoted
as, where the saturated pressure is given as the temperature function only:
𝑃𝑖 = 𝑥𝑖 ∗ 𝑃𝑖 𝑠𝑎𝑡𝑢𝑟𝑎𝑡𝑒𝑑 (1)
Furthermore, with Dalton’s law, which assumes partial pressure of a component is the
function between mole fraction within vapor phase and total vapor pressure of the system,
7
taken into consideration, mole fractions, as well as vapor-liquid equilibrium is figured out:
(University, 2016)
𝑃𝑖 = 𝑦𝑖 ∗ 𝑃𝑡 (2)
𝑦=
𝑖
𝑥𝑖𝑃𝑖𝑠𝑎𝑡𝑢𝑟𝑎𝑡𝑒𝑑
(3)
∑ 𝑥 ∗ 𝑃𝑠𝑎𝑡𝑢𝑟𝑎𝑡𝑒𝑑
𝑖
𝑖
𝑖
Meanwhile the relative volatility conception indicates the deviations between the boiling
points within 2 phase mixtures, that is directly connected with the equilibrium constant K
value, where K value indicates the ratio between mole fraction in vapor phase and liquid
phase, in this expression 𝑎𝑖𝑗 describes relative volatility of the components:
𝑦𝑖
(𝑥 ) 𝐾𝑖
𝑎𝑖𝑗 = 𝑦𝑖𝑗 =
(4)
𝐾
𝑗
(𝑥 )
𝑗
In order to formulate the sufficient accuracy within the system for later computations an
expression has been developed as:
𝑎𝑖𝑗 = √𝑎𝑖𝑗,𝑡𝑜𝑝 ∗ 𝑎𝑖𝑗,𝑏𝑜𝑡𝑡𝑜𝑚
(5)
Moreover, VLE (vapor-liquid equilibrium) relationship will then become an expression as,
where further expression 𝑎𝑖 describes common component:
𝑎 𝑖 𝑥𝑖
𝑦𝑖 =
(6)
∑ 𝑖 𝑎 𝑖𝑥 𝑖
Throughout batch distillation process, the mixture entering as a feed in liquid feed contains
both MVC and LVC, abbreviations standing for most volatile components and least volatile
components, with the components being ethanol and water for this experiment, furthermore
once the vaporization process is initiated within the column
process of condensation and evaporation creates a connection between liquid and vapor
phases. However, the energy required for boiling the most volatile component is acquired
through the fixed reboiler under the still pot, while the vaporized substance then passes
through a total condenser resulting in the condensed stream within the distillate section.
(Tham, 2006) Within distillation columns the reflux is forwarded to the top part of the
column since some part of condensed substance is collected; however, while reflux
provides desirable consequences for separation of substances, it also authorizes a
8
circumstance for controlling the temperature at the bottom part of the column.
Notwithstanding the fact that increment in the reflux ratio generates contact between downflowing liquid alongside with the up-flowing vapor so as to acquire an equilibrium heat,
material transfer and balance, so further purification of product, it calls for higher rate for
vaporization as well as more energy. Reflux ratio expression has been developed as the
ratio of the liquid that is removed back to the column and removed product as condensate:
𝐿𝑐
𝑅=
(7)
𝐷
Figure 3. Distillation column. (Porter, 2011)
Furthermore, several points should be taken into consideration in order to control the reflux
ratio since this can be regarded as one of the key points of bath distillation process.
Initially, the reflux ratio setpoint is persistent within the separation process, once decrement
occurs in the percentage of most volatile component within the still, the composition of the
overhead product seems to experience relative changes. As a consequence of which, a
pre-determined number for reflux ratio should be kept constant as a means to provide an
unchanging mole percentage of most volatile component. Nonetheless, reflux ratio control
may involve several complicated procedures such as cyclic procedure pattern, efficiency
based on thermodynamic laws, and optimization of residence time. Furthermore, side
stream within the whole system may also influence the reflux ratio such as further
appendage of feed can be involved to the system. (Qingli Qian, 2011)
9
Referring to the initial approach, within the laboratory experimentation reflux ratio was set
with the percentage standing at 50%.
Another predominate part for the calculations of distillation column is mass balance
throughout the system.
Figure 4. Distillation column with connected
equilibrium stages.
The initial assumption here is perfect mixing inside the stages between both of the phases,
while the material balance for the whole system can be expressed with the algebraic
equation as:
𝑑𝑁𝑖,𝑛
= (𝐿𝑛+1 ∗ 𝑥𝑖,𝑛+1 − 𝑉𝑛 ∗ 𝑦 ) − (𝐿
𝑑𝑡
𝑖,𝑛
∗𝑥
𝑛
𝑖,𝑛
−𝑉
𝑛−1
∗𝑦
𝑖,𝑛−1
)
(7)
Where,
𝐿𝑛 𝑎𝑛𝑑 𝑉𝑛 𝑎𝑟𝑒 𝑡ℎ𝑒 𝑡𝑜𝑡𝑎𝑙 𝑎𝑚𝑜𝑢𝑛𝑡𝑠 𝑜𝑓 𝑓𝑙𝑜𝑤 𝑟𝑎𝑡𝑒𝑠 𝑓𝑜𝑟 𝑙𝑖𝑞𝑢𝑖𝑑 𝑎𝑛𝑑 𝑣𝑎𝑝𝑜𝑟, 𝑟𝑒𝑠𝑝𝑒𝑐𝑡𝑖𝑣𝑒𝑙𝑦,
𝑒𝑥𝑎𝑐𝑡𝑙𝑦 𝑓𝑜𝑟 𝑡ℎ𝑒 𝑠𝑡𝑎𝑔𝑒 𝑐𝑎𝑙𝑙𝑒𝑑 𝑎𝑠 𝑛, 𝑤ℎ𝑖𝑐ℎ 𝑖𝑛 𝑡ℎ𝑖𝑠 𝑐𝑎𝑠𝑒 𝑣𝑎𝑝𝑜𝑟 𝑙𝑒𝑎𝑣𝑒𝑠 𝑠𝑡𝑎𝑔𝑒 𝑛 𝑎𝑛𝑑 𝑒𝑛𝑡𝑒𝑟𝑠
𝑠𝑡𝑎𝑔𝑒 𝑛 + 1, 𝑚𝑒𝑎𝑛𝑤ℎ𝑖𝑙𝑒 𝑡ℎ𝑖𝑠 𝑠𝑟𝑎𝑔𝑒 𝑓𝑜𝑟 𝑙𝑖𝑞𝑢𝑖𝑑 𝑖𝑠 𝑛 − 1.
Whenever the steady state is considered for the operation conditions, remark indicating
altering of component moles within each stage relative to the time should be considered as
0:
𝑑𝑁𝑖,𝑛
𝑑𝑡
=0
However, to simplify the process of material balance around the system, streams in and
out of the distillation column are given as liquid feed stream (F), distillate condensed and
10
collected (D), and bottom product of column (B); in the meantime, mole fractions within
liquid phases for F, D, and B are expressed as 𝑥𝐹, 𝑥𝐷, 𝑎𝑛𝑑 𝑥𝐵.
Hence after, mass balance equation will be provided as:
𝐹 = 𝐷 + 𝐵 (8)
𝐹𝑥𝐹 = 𝐷𝑥𝐷 + 𝐵𝑥𝐵
(8.1)
With the flowrates expressed in kmoles.
Reflux ratio being kept constant throughout the process, expressions are deduced and
denoted for the short time span of the process as:
𝑑𝐷 = −𝑑𝑆
𝑥𝑑𝑑𝐷 = −𝑑(𝑆𝑥𝐵)
(8.2)
(8.3)
𝑆𝑑𝑥𝐵 = 𝑑𝑆(𝑥𝐷 − 𝑥𝐵) (8.4)
Once these balanced equations are considered an expression named Rayleigh equation
being based on differential equations and is used to study the hydrodynamic stability of the
shear flows. In this case, the equation with the integrated formula where the boundaries
are formulated as starting point from 𝑥𝐹 until it reaches the number in 𝑥𝐵 meaning from the
feed values to the bottom figures:
𝑥𝐵
𝐵
𝑑𝑥𝐵
ln = ∫
𝐹
𝑥𝐹 𝑥𝐷 − 𝑥𝐵
(8.5)
Although all the values and further calculated figures were of pivotal importance, figuring
out the value for distillate most volatile component fraction was denoted as the preliminary
objective. With the density being revealed, mass fraction could be deduced from the table
provided; henceforward, density values for ethanol must be calculated with the expression
provided below:
𝜌=
𝑚𝑚𝑖𝑥 𝑚𝑠𝑦𝑠𝑡𝑒𝑚 − 𝑚𝑣𝑒𝑠𝑠𝑒𝑙
=
𝑉𝑚𝑖𝑥
𝑉𝑚𝑖𝑥
(9)
Where,
𝜌 𝑖𝑠 𝑡ℎ𝑒 𝑑𝑒𝑛𝑠𝑖𝑡𝑦 𝑜𝑓 𝑡ℎ𝑒 𝑚𝑖𝑥𝑡𝑢𝑟𝑒, 𝑚𝑒𝑎𝑠𝑢𝑟𝑒𝑑 𝑖𝑛 𝑘𝑔 𝑝𝑒𝑟 𝑚𝑒𝑡𝑒𝑟 𝑐𝑢𝑏𝑒.
𝑚𝑚𝑖𝑥 𝑖𝑠 𝑡ℎ𝑒 𝑚𝑎𝑠𝑠 𝑜𝑓 𝑡ℎ𝑒 𝑚𝑖𝑥𝑡𝑢𝑟𝑒 , 𝑒𝑥𝑝𝑟𝑒𝑠𝑠𝑒𝑑 𝑤𝑖𝑡ℎ𝑖𝑛 𝑘𝑔.
𝑉𝑚𝑖𝑥 𝑖𝑠 𝑡ℎ𝑒 𝑣𝑜𝑙𝑢𝑚𝑒 𝑜𝑓 𝑚𝑖𝑥𝑡𝑢𝑟𝑒, 𝑚𝑒𝑎𝑠𝑢𝑟𝑒𝑑 𝑖𝑛 𝑚𝑒𝑡𝑒𝑟 𝑐𝑢𝑏𝑒.
𝑚𝑠𝑦𝑠𝑡𝑒𝑚 𝑖𝑠 𝑡ℎ𝑒 𝑚𝑎𝑠𝑠 𝑜𝑓 𝑠𝑦𝑠𝑡𝑒𝑚, 𝑎𝑙𝑠𝑜 𝑡ℎ𝑒 𝑣𝑒𝑠𝑠𝑒𝑙 𝑤𝑖𝑡ℎ 𝑡ℎ𝑒 𝑠𝑜𝑙𝑢𝑡𝑖𝑜𝑛 𝑖𝑡𝑠𝑒𝑙𝑓, 𝑚𝑒𝑎𝑠𝑢𝑟𝑒𝑑 𝑖𝑛 𝑘𝑔.
11
𝑚𝑣𝑒𝑠𝑠𝑒𝑙 𝑖𝑠 𝑡ℎ𝑒 𝑚𝑎𝑠𝑠 𝑜𝑓 𝑡ℎ𝑒 𝑒𝑚𝑝𝑡𝑦 𝑣𝑒𝑠𝑠𝑒𝑙, 𝑚𝑒𝑎𝑠𝑢𝑟𝑒𝑑 𝑖𝑛 𝑘𝑔.
With the temperature changing from the reboiler as the bottom part of distillation column to
the top, measuring and noting down the values in each part was the main procedure of
experiment. The temperature in which distillation process should stop was around 92℃,
which was pre-determined value which was chosen with the concentration of the initial
mixture boiling point as well as that of pure water within the operating pressure so as to
avoid any kind of evaporator temperature surpassing that of boiling point of least volatile
component, moreover, whenever temperature passes this limit value the efficiency of the
distillation column will drop and a permissible limit is exceeded by the amount of LVC
amount In the evaporator, with the quality of separated material being decreased. So, the
end temperature will be obtained through the equation:
𝑇𝑓𝑖𝑛𝑎𝑙 =
𝑇𝐵,𝑚𝑖𝑥𝑡𝑢𝑟𝑒 + 𝑇𝐵,𝑤𝑎𝑡𝑒𝑟
2
(10)
Experimental Framework:
Within the experimental procedure part of this laboratory experimentation, preliminary,
concise, as well as precise aspects and data in the context of the regarded unit gadgets,
devices, and apparatus for measuring needed sections will be assiduously taken into
account; in the meantime, step-by-step, and consecutive procedure for carrying out
laboratory scrutiny with predominant objective of figuring out main factors for distillation
processes will be remarked.
Safety Precautions:
Taking into account that certain safety issues may occur within the laboratory
experimentations, precautions in order to prevent any harm to human beings as well as to
the devices within the laboratories. While certain standard rules have been referred to,
additional safety preventives must indeed be contemplated. Therefore, being aware of the
dangers and hazards is of predominant significance.
Initially, notwithstanding the fact that isolation material has been utilized for covering
reboiler parts in order to both avoid any additional heat loss to the system to keep
increasing the efficiency of the system and avoiding skin contact with extremely hot parts of
12
device, some parts of the reboiler was open and any contact would cause skin burns.
Furthermore, in case of any contact of electricity grid with undistilled water would bear
undesirable repercussions such as any kind of shock with the non-designated parts. In
addition to the electricity sockets, electricity problems may as well occur within cabin of the
distillation equipment, on the grounds of this touching electrical parts of laboratory column
and confronting occurred problems are not authorized by the personnel and supervisors;
however, cabin should be kept opened whenever the device is unplugged from the
electricity socket. Consequently, since ethanol as the main substance of the
experimentation possesses features of being highly flammable, ignition within the system
would be a disastrous condition, thus presence of flame should be not allowed. One of the
most must-be-prevented occurrence within laboratory systems is explosions of the
materials once passing the temperature of ignition detonation may be initiated, so
prohibition of introducing substances with ignition temperatures being exceeded should be
taken into consideration. (Syed A. Taqvi, 2018) Meanwhile, extreme conditions of pressure
within the sealed system may lead to the implosion considering that scorches of the red
surfaces inside the burned areas results in leaking of hot stream including water and
ethanol with the concentration of former being relatively higher. Alongside with the
pressure conditions, any acquaintance with excessive heat and the humidity resulting from
the excessive usage of steam exhaustion and thermal weariness. Therefore, limit
conditions of both pressure and temperature should not be surpassed.
Experimental equipment:
Addition to the standard equipment required within the laboratory experimentations such as
beakers, thermometers, electronic scales for measuring the mass of empty beakers as well
as with the mixture within so as to calculate sole mass of the required component, a
preliminary device for initiative scrutiny of separation processes was unit called as CE 600
fabricated by company named G.U.N.T that is the device as an exact identity of distillation
column within industrial processes with the single difference being the size of gadget. The
tools of the forgoing rectification column allowed a batch distillation process for this
experiment. Even though the whole unit consisted of 3 various classifications of distillation
columns, with the types being columns with sieve and bubble trays, and packed one, the
ultimate kind was selected which indeed allows rate of mass exchange with higher scale.
13
The feed to the system can be introduced within various heights with 3 different sections;
for the moment, preheating of the product is desirable and carried out with heat exchanger.
Furthermore, presence of additional heat exchangers authorizes temperature control for
both distillate and the bottom product considering that while the total condenser is utilized
for changing the phase of the top product from distillation column, the heat exchanger
exists with the fluid being water in order to cool down the bottom product coming from the
reboiler at the end of the procedure. In the meantime, energy transmitted to the mixture is
obtained from an evaporator with electrical powering adjusted under the distillation column.
While technical devices have already been constructed as a part of rectification column,
further electrical gadgets such as PLC touch screens for adjusting the trainer, and
integrated router for indeed operating the trainer within an alternative route through the end
device. Moreover, the whole structure of the distillation column named as CE 600 is
indicated with the picture described below:
14
Figure 5. Structure and parts of distillation
column.
1. Feed pump was constructed in order to forward the introductory feed to the system.
2. Feed tanks are used for conserving the feed whose volumes are 2x5 L.
3. Control board was mostly utilized so as to measure the temperature as well as reflux
ratio within the system.
4. Tank used to collect the distillate of the top product.
5. To create a vacuum experimentation within the system, glass filters are used.
6. Pressure gauge.
7. Valve to forward the reflux.
8. Phase separation tank which could be used in the system if more than 3
components existed in the system.
9. Total condenser.
10. Valve to forward the reflux.
11. Diaphragm-based differential pressure sensor for measuring pressure loss.
12. Solvent tank for cleaning purposes.
15
13. Column for forwarding the material.
14. Flowmeter used to measure the amount of cooling water.
15. Evaporator with electrically powered with the volume being 10 liters.
16. Heat exchanger for cooling down the temperature of the bottom product.
17. Tank for collecting the bottom product.
18. Mostly used indicator for temperature measurement within the ranges of 1 to 12.
19. Temperature measurement with the ranges being from 13 to 16.
20. Control panel for reflux ratio.
21. Pressure loss indicator panel.
22. Switch.
23. Controller.
24. USB port.
25. Preliminary switch.
26. Emergency button.
27. Measurement and indicator for level since warning occurs whenever the level is
measured to be lower than the critical moment.
28. Controlling of feed pump.
29. Controlling of heater.
Procedure:
As the initial step of the laboratory experimentation was introduction of ethanol water
mixture with the concentrations being 25% and 75%, respectively; in the meantime,
rectification column is plugged into sockets with the water network being started.
Once the ethanol water mixture was introduced into the feed tanks of the distillation
column, feed pump was activated with the valves for the pioneering flow of water inside the
evaporator.
Subsequently, the power of the evaporator was adjusted with 4000W, while that of reflux
stayed at its 100% value which was initiated succeeding transferring all the water inside the
evaporator tank, with the flowrate of water standing at 150 liters per hour that is measured
through the flowmeter.
Furthermore, temperatures throughout the system should be noted down through the
usage of control panel with the numbers for temperatures ranging from T3 to T12.
Whenever the temperature of the evaporator that is temperature denoted as T3 reaches 70
degree Celsius, heating power from the evaporator decreases.
While the operation conditions for the heating power is given as the 30% of the maximum
power, reflux ratio was adjusted with 50%. Consequently, distillate start forming within the
16
tank of collection, reflux ratio within the rectification column changes with the value staying
at 50% of its figure, meanwhile the interval for measuring the temperature of each of the
section reaches 10 to 15 minutes.
After waiting for a certain period of time, the valve connected to the distillate collector tank
is then opened in order to obtain certain amount of top product, prior to the step of
measuring empty beaker after which the total weight of beaker with the substance inside
was measured by means of an electric scale. However, for calculation of the required
aspects not only the weight of the substance but also the temperature had to be measured
with the thermometer. The process of sample taking from the top section of rectification
column kept occurring until the stages reached around 18 with the last sample being taken,
after each stage the sample taken from the tank is then poured inside the flask for not
losing any kind of product.
Once the temperature of the evaporator, as mentioned above T3, reached 92 degrees
Celsius, evaporator should be on the off position meanwhile after waiting for around 5
minutes, reflux ratio within the system was then surged to 100%. Nevertheless, since the
bottom product coming from the reboiler was extremely hot, cooling water was utilized
within the heat exchanger in order to decrease the temperature of the remnant bottom
product with it then poured inside the tank collecting for bottom product. Furthermore, the
remnant was then discharged into the flask for calculation of total volume and mass of
substance.
Afterwards, the experiment is totally concluded with finally shutting down the system
through removing it from the electricity.
Results:
In order to comprehend the carried-out experimentation with deeper understanding, graphs
should be plotted with the calculations specifically on the mass percentage numbers should
be done. As an initial step for results section of this report, temperature profiles should be
plotted.
Although temperature values were readily available through a hardware installed within the
distillation column with the values being transferred to the user interface of device, figures
17
were noted down manually so as to meet the requirements of scrutiny in terms of
temperature distributions. As a consequence, two individual profiles of temperature are
plotted differentiated from the start point of distillate formation.
Temperature profile before distillate formation
100
T3
90
T4
T5
T6
T7
T8
T9
10:19
tIME a.m.
10:26
T10
T11
T12
Temperature in celcius
80
70
60
50
40
30
20
10
0
9:50
9:57
10:04
10:12
10:33
10:40
10:48
Graph 1. Temperature values prior to distillation process
95
Temperature profile after distillate formation
T3
T4
T5
T6
T7
T8
T9
T10
T11
T12
tEMPERATURE IN CELCIUS
90
85
80
75
70
65
60
10:48
11:02
11:16
11:31
11:45
12:00
12:14
TIME a.m.
Graph 2. Temperature values after distillation process
18
12:28
Product analysis:
With mainly focusing on the produced product form the distillation column, overall mass
balance as well as material mass percentage fractions will be figured out throughout
algebraic calculations. Three individual predominant analysis of the product, mass, volume,
and as well as density, namely, will be highly regarded.
Initially for mathematical computations of mass percentage of ethanol in the system, tables
provided in the manual indicating mass percentage of ethanol referring to both temperature
and density, reference densities as well as reference mass fractions were chosen for
carrying out interpolation. Although all the calculations are denoted in Appendix A, as an
example, mass fraction of ethanol within the first sample is introduced as:
Table 1. First sample analysis.
First
Sample
Time, a.m.
Total mass, g
Net mass,
g
10:27
Beaker
mass, g
128.7
40.2
Temperature, Density,
℃
kg/m^3
50
Ethanol
mass %
88.5
25
93.507%
804
Volume, ml
Reference
density 1,
kg/m^3
802.63
Reference
density 2,
kg/m^3
805.41
Reference
MVC mass
fraction 1
94
Reference
MVC mass
fraction 2
93
Distillate formation started around 10:22 a.m., approximately 5 minutes prior to taking first
sample from the distillate. With a reference to formulae 9, density was calculated as:
𝜌=
𝑚𝑡𝑜𝑡𝑎𝑙 − 𝑚𝑏𝑒𝑎𝑘𝑒𝑟
𝑉
=
128.7 − 88.5
50
= 0.804
𝑔
𝑚𝑙
= 𝟖𝟎𝟒
𝒌𝒈
𝒎𝟑
With the temperature value standing at 25 degrees Celsius, and the reference densities
alongside with mass fractions, ethanol fraction is algebraically computed by dint of
interpolation:
𝐸𝑡% = 𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1) +
𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝐸𝑡%9𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
93 − 94
∗ (𝜌 − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)) = 94 +
∗ (804 − 802.63) = 𝟗𝟑. 𝟓𝟎𝟕
805.41 − 802.63
While all calculations are introduced in the Appendix, overall values are then introduced as
a table:
19
Table 2. Sample analysis of whole process.
Time
10:53
10:58
11:03
11:08
11:13
11:18
11:23
11:28
11:33
11:38
11:43
11:48
11:53
11:58
12:03
12:08
12:13
12:23
Net mass,
g
Volume, ml
Temperature, Density
kg/m^3
℃
40.2
53.8
70.2
65.4
65
71.6
41.6
68.1
82.6
71
84.4
58.7
72.1
87.3
95.5
67.5
79.3
108.3
50
67.5
84
80.5
79.8
87
52
83.5
99.5
86.1
102.1
71
86.5
107
112.5
82
95
131
25
23
23.5
23
24.7
24
22.5
26
25.1
24.6
24
23.8
24.5
25
24.5
25
25
23.5
804
797.03
811.9
812.42
814.54
822.99
803.8
815.57
830.151
824.623
826.641
826.641
833.526
815.888
848
823.171
834.737
826.718
Ethanol
mass
percentage
93.507
95.729
91.098
91.934
89.717
86.717
93.621
88.897
82.563
85.878
85.706
85.323
82.393
89.107
76.527
86.309
81.732
85.434
Once mass fractions of ethanol in the top product have been calculated, a diagram
indicating the trend of mass percentage of ethanol in distillate product is plotted:
20
Mass percentage of most volatile component (ethanol)
versus time
100
Ethanol Mass Percentage %
95
90
85
80
75
10:48
11:02
11:16
11:31
11:45
12:00
12:14
12:28
Time
Graph 3. MVC mass fraction altering during distillation process
Following aforementioned phenomena, calculations on overall material balance should be
computed with the predominant intention of figuring out the deviations from the theoretical
aspects which is mainly based on as the feed is equal to the sum of bottom and top
product. Nevertheless, initially information on the each section as top, bottom, and feed
flowrates must be introduced.
Table 3. Mass balance.
Feed
Total
Ethanol/water Net Mass, g Temperature Density
Ethanol
Volume ml
% mass
mass, g
25%
kg/m^3
6000
23
Top Product
21
1500
Total
Ethanol/water Net Mass, g Temperature Density
Ethanol
Volume ml
% mass
kg/m^3
mass, g
1557
86,67
823,764
1111,629
1282,6
24,26
Bottom Prdocut
Total
Ethanol/water Net Mass, g Temperature Density
Ethanol
Volume ml
% mass
kg/m^3
mass, g
4449,76
4.033
987.356
177,1899
4393,5
28
Sum
Total mass, g
Ethanol mass, g
Initial
6000
1500
Final
5676,1
1288,819
Deviation
5.39%
14,07%
For the material balance of the experimentation, initially conditions for feed such as total
mass, mass percentage of ethanol within the mixture, and temperature should be figured
out. Considering that temperature measurement of the substance initially was not carried
out prior to the scrutiny, overall room temperature value was taken into consideration, in
the meantime mass of the feed was deduced as 6kg, while mass fraction of most volatile
component was 25%. For the top product, while total volume was figured out through
summing all the individual volumes, net mass was an empirical value and as a
consequence density value through which mass fraction of ethanol was possible to be
figured out by dint of interpolation of density values with mass percentage at 24,26℃ that is
found as average temperature value for top product. Following that, once the
experimentation was almost finalized, further bottom product was taken out of the bottom
product tank in order to measure conditions of the wastage with the water percentage
corresponding to almost 96% of the whole product; meanwhile, temperature was measured
to stay at 28℃. Furthermore, deviations from the initial feed product must be deduced
through calculations indicated below, while overall mass balance equations lead to about
5.4% error, that of ethanol was higher by roughly 8,7%.
22
𝛼𝑡𝑜𝑡𝑎𝑙 =
𝛼𝐸𝑡 =
|6000 − 5676,1|
6000
|1500 − 1288,819|
1500
∗ 100 = 5.39%
∗ 100 = 14,07%
Discussion:
Processes being related to and relied on rectification processes similar to the carried-out
experiment are considered to be of preliminary significance which indicates and provides
paramount insights into distillation processes utilized in a quite a few complexes ranging
from oil and gas industries, pharmaceuticals, analysis of complex materials, separation
pathways for mixtures, which in this laboratory experimentation was given as ethanol and
water mixture. Overall, process was conducted through separation of water and ethanol
mixture through referring to the batch distillation column with the most volatile component
being vaporized as the distillate product of the process, which indeed included controlling,
monitoring, and noting down the changes of the temperature values starting from the
temperature of evaporator and ending with the top column temperature given as the T-12,
meanwhile amongst those values total temperature values throughout the system was as
well taken into account, followed by calculations of ethanol quality within each taken
sample on a regular basis so as to figure out mass fraction of the substance. Therefore, for
further immersed understanding of the process additionally graphical methods have been
utilized such as plotting the graphs mostly dealing with temperature profiles, and material
balance over the whole process with the error being deduced. The utilized batch system
distillation column was adjusted with several gadgets and sensors enabling monitoring
system conditions. In the meantime, feed as a mixture of water and ethanol substances
with the net mass of liquid mixture being 6kg, where mass concentration of ethanol stood
at 25%, was introduced to the system at the beginning of the whole process. Alongside to
the aforementioned technological gadgets, apparatus as thermometer was also used for
deducing temperature of each sample, both distillate and bottom product.
Another preliminary factor to be considered within the discussion section is the
expectations from the experimentation even prior to beginning the process itself which
could be contemplated and discerned throughout the scrutiny. Initially, one of the
23
anticipations about the process was distillate formation temperature of evaporator since as
expected whenever temperature of evaporator reached 86.5-87 degree Celsius first
condensate distillate product started forming with the top column temperature soaring
immediately to 79,1 degree Celsius, in which first bubbles generated within the distillation
column went to the top part prior to escaping from the rectifying section and entering total
condenser to be condensed to turn into distillate product. Although in the initial conditions’
concentration of MVC was higher within the first bubbles formed, as the time goes by and
distillation process continues further quality of ethanol on both the distillate and bottom
product should decrease considering that while some part of the ethanol is transferred to
the top product, as the time goes and temperature increases, LVC also gets to the top part.
With the electric power of distillation column changing, temperature profiles should follow
an upward trend since the power kept increasing for better distillation process within the
system. Following this case, for the mass balance of the rectification column, theoretically
without a doubt the values should be the same since no amount of mass lost is taken into
consideration, meanwhile for the real case indeed some deviations from the ideal case was
deduced which was ineluctable. One of the predominant parts for distillation columns is the
fact that as temperature profiles increases quality of the most volatile component at the end
of the process will be lower in comparison with the initial conditions. Since the process
literally stopped at 92 degree Celsius, the main anticipation and reason for such an act can
be explained through as foregoing phenomena, MVC will be less as time passes thus
increasing mass percentage of LVC, which in this case was water, which would lead to
inefficient distillation process. Before starting the discussion of empirical values obtained
form results section, it should be mentioned that plotted graphs as well as obtained values
from algebraic calculations as well as equations indicated in theory section commensurate
with the expected phenomena.
Looking at the graph plotted initially in the results section, it is obvious that temperature
values indicate time-period beginning with heating process being initiated through the
evaporator and ending up with the first moment of distillation process; in the meantime,
latter sketched graph describe trend followed by temperature values until the end of the
process. Once evaporator was initiated, small increases of temperature within the
evaporator was witnessed due to heat production in the system, while other temperature
24
values except from T4 stayed almost the same, which could be caused due to T4
temperature being close enough to the evaporator section with heat being transferred. One
of the noteworthy points here is that as just mentioned within the theory part, once
evaporator is ignited so as to generate heat, all the temperatures within the system
experienced upward inclination; nonetheless, a decrease of temperature value for T6 is
discernible in the 2nd graphics with the temperature witnessing a decrease by 18℃. This
phenomenon could be exemplified through understanding that several glitches within the
sensors could occur and create undesirable consequences. Whenever time reached 10:26
a.m., temperature of distillation column sections except for T3 and T4, surged until values
reached values around 70 degree Celsius. An immediate increase in the values of other
temperatures can be related to the increasing rate of sensors picking heat from the
vaporization process. Whenever temperature of the top column reaches around 79.1℃
which commensurate with T3 temperature being 86.5℃, evaporation process commences
with the initial bubbles surging through the condenser by generation individual inaugural
liquid phases within the top tank. Furthermore, fluctuations within the system temperatures
can also be accredited to reflux ratio since temperature of the forwarded substance will be
lower compared to the top part of the system which actually is considered as one of the
preliminary purposes of refluxing products. Taken into consideration that power arranged to
the evaporator is mainly intercorrelated with temperature increase within the system,
whenever an increase in power was reviewed, from the graphs a steep growth of
temperature profile was observed leading to the apprehension that initial slope of
increment was rather lower compared to the latter one. Moreover, approximately constant
lines within the graphs are acknowledged as well cannot be ignored; nevertheless,
stabilized lines in the system do not particularly create or is mainly responsible to
abnormalities since certain amount of loss of temperature within the system is possible
through vapor temperature loss to surrounding alongside with temperature and heat
transfer with the forwarded top distillate to column itself. One of the reliable grounds for
stopping distillation process whenever temperature of evaporator reaches 92℃ is to
prevent additional pressure losses in the system through avoiding harms and damages to
distillation column.
25
In terms of the mass analysis of distillation process with mainly focusing on material
balance regarding 2nd table and 3rd graph, initial mass concentration of ethanol within the
system was calculated to be 93,5%, meanwhile following the same procedure second
mass concentration was deduced as 95,73%; nevertheless, the phenomena of azeotrope
should be taken into account as once an azeotrope is generated within the system as
water/ethanol mixture is prone to create such factor, the recovery of ethanol within the
system cannot be higher than 95,635%, as a consequence of which calculated values for
2nd mixture is theoretically unachievable. Nonetheless, although measurement issues may
have occurred during experiment, conditions of the system may have affected azeotrope
formation values, thus maximum quality which could be obtained through distillation must
be altered. Following, ethanol mass fractions stayed amongst the values of 85%-90%, with
the lowest value being 76,5% whenever time reached a time of 12:03, although certain
deviations within the system from a downward trend occurred, overall decreasing quality of
most volatile components indicated a similarity towards the anticipated phenomena.
Studying the graph of mass fraction of ethanol over the distillation process, although an
overall downward trend was expected and witnesses, certain time-frames such as 11:23
a.m., 11:58 a.m., and 12:23 p.m. were deduced to experience higher values for ethanol
mass fraction with the values standing at roughly 93.62, 89.11, and 85.43, namely, which
could for the last example might be exemplified through accumulation phenomena of
distillate sample within the distillate tank since with involving as well as the initial distillate
product sample with higher mass percentage of most volatile component.
Following the discussion of material balance of the products, the volume of the top product
was deduced throughout the summation of all individual values of the ethanol/water
mixture with the mass percentage of former being dominant; nevertheless, final volume of
the distillate should not have been figured out as summation since depending on the mass
fraction alongside with the temperature of the system, arrangements of ethanol and water
molecules are altered which in its turn prevents consideration of this mixture as an ideal
condition.
Another predominant section of discussion part is considering potential concepts which
could have led to errors and discernible deviations between theoretical and empirical
values. When dealing with technological devices such as gadgets and user interface
26
indicating temperature profiles of system, errors are chiefly regulated and attributed to
malfunctions of devices rather than human-based oddities since nearly no human
interaction is required for temperature measurement. Through being used for a long period
of time, some malfunctions, extremely used parts of device may require for restoration of
tech-based parts for even more precise measurements. Furthermore, as temperature
values were taken through observing appeared numbers on the interface, oscillations of
those values especially for evaporator and top column led to worrisome calculations and
measurements. However, all predominant potential culprits which could have provoked
undesirable divergences as a main source of errors, are principally generated through
calculations of material balance considering that abundant computations, as have
described within appendix A, might have caused inaccuracy. Initially, although could be
considered as frivolous, temperature measurements within the system was nearly
problematic as initial conditions for feed to the distillation column was not measured which
have ended up with the impression and assumption that this value was roughly 23℃;
meanwhile, ethanol concentration figures was indeed calculated by a reference to the
temperature of sections. As addition to the causses of faulty figures obtained, since ethanol
mass percentages have been calculated with references to both temperatures and
densities within the substances, any kind of miscalculations of aforementioned
thermodynamical properties would certainly instigated subsequent blunders and
inaccuracies of ethanol mass percentage values; for the time being, farther algebraic
computations relied on ensuing two interpolations, even three whenever temperature value
was not measured as an integer, have profoundly affected veracity of experimentation. In
terms of preventing faulty calculations and misreading on the thermometer which can be
accounted as human-being fault causes, referring to an electronic, technologically
manufactured thermometer would avoid imprecise temperature values. Even for the
density values being accurate as much as possible, utilizing a device so-called as
densitometer would avoid the necessity of measuring both volume and mass of the
samples through beaker scales and mass scale, which might carry certain error
percentages within itself, for further calculation density values. Meanwhile ethanol mass in
both distillate and wastage was deduced through acquired mass percentage values, and
thus those accumulated oversights have ended up with relative high error for ethanol mass,
27
with the number standing at 14.07%. Although aforementioned culprits are indeed also
included for overall mas balance errors within distillation column, another huge
phenomenon in this case can be indicate as losses of substance particles. Those droplets
of ethanol-water mixture which are captured as well apprehended within rectification
section with the parts mostly being heat exchangers, container tanks for both bottom and
top products, phase separation containers, and other parts, creating an accumulation even
though for an ideal case this property is taken as negligible. As the end of the
experimentation was reached, once bottom product was drained as the wastage, all
attempts and efforts were made in order to totally leak all substance in the bottom tank.
Considering that calculations were carried out based on the purity levels of both reactants
as ethanol and water being pure substances and even though distilled water was utilized in
the system, some parts of the liquid mixture alongside with the dissociated solid parts of
substances within water and ethanol solution which eventually prevented accurate
calculation of density values in the system leading to probable miscalculations and errors in
the result values. Furthermore, one of the aspects which could have affected accuracy of
the result section is the quality of ethanol since throughout the calculations solely 100%
ethanol quality was taken into account.
Conclusion:
Preliminary laboratory experimentation carried out was predominantly dedicated for
measuring quality of most volatile component within ethanol water mixture by dint of batch
distillation column which was possible to figure out with computation of substantial values,
plotted graphs indicating trend followed by ethanol mass fraction, and preponderant
essence behind distillation process. The main objective was to obtain higher ethanol
concentration substance from water ethanol mixture with 25% quality, dealing with CE600
rectification column which eventually lead to a distillate product with 86.67% ethanol mass
fraction substance with its total mass being 1282.6 grams, whereas ethanol contributed
4.033% to the bottom product. Although values had been calculated for mass balance
computations, certain deviations from the initial mixture were discernible when compared
with the initial conditions regarding both the total liquid mixture and the ethanol constituent.
28
Whereas physical properties and external conditions played a paramount role causing error
within the system, generally speaking the total downward trend for the quality, also known
as mass fraction, of ethanol with lower vaporization temperature was expected from the
system as distillation process continued occurring, with that of water increasing. Through
evaluation of temperature profiles by dint of plotting the graphs have generated almost
anticipated consequences as anticipated with the total trend for these values following an
upward style.
Another factor worth noting is the time and conditions of first distillate formation which
roughly corresponded to 10:27 a.m. with temperature value standing at 84,6 degree
Celsius, with the T-12 value standing at 24,1 degree Celsius. Distillation process continued
for overall roughly 3 hours starting with the arrangement of feed preparation and ending up
with taking the sample from the bottom product. Ultimately, though errors for ethanol mass
balance was 14.07%, that of total material balance was 5.39% which was relatively low,
potential culprits for those problems have been denoted on the discussion section. Since
distillation processes are omnipresent within industrial processes, studying and examining
rectification column is of utmost importance.
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30
Appendix A:
2nd sample:
𝑚𝑡𝑜𝑡𝑎𝑙 − 𝑚𝑏𝑒𝑎𝑘𝑒𝑟 142.3 − 88.5
𝑔 = 𝟕𝟗𝟕. 𝟎𝟑 𝒌𝒈
=
= 0.79703
𝑉
67.5
𝑚𝑙
𝒎𝟑
𝜌=
𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝐸𝑡%9𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
97 − 96
∗ (𝜌 − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)) = 96 +
∗ (797.03 − 797.82)
797.82 − 794.90
= 𝟗𝟓. 𝟕𝟐𝟗%
𝐸𝑡% = 𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1) +
3rd sample:
Since temperature was 23.5 degree Celsius, initially density values at 91% and 92%
ethanol mass fractions must be figured out through interpolation:
809.89 − 809.02
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1) = 809.02 +
∗ (23.5 − 24) = 𝟖𝟎𝟗. 𝟒𝟓𝟓 (𝟗𝟐% 𝒇𝒓𝒂𝒄𝒕𝒊𝒐𝒏)
23 − 24
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) = 811.73 +
𝜌=
812.60 − 811.73
∗ (23.5 − 24) = 𝟖𝟏𝟐. 𝟏𝟔𝟓 (𝟗𝟏% 𝒇𝒓𝒂𝒄𝒕𝒊𝒐𝒏)
23 − 24
𝑚𝑡𝑜𝑡𝑎𝑙 − 𝑚𝑏𝑒𝑎𝑘𝑒𝑟 156.70 − 88.5
𝑔 = 𝟖𝟏𝟏. 𝟗 𝒌𝒈
=
= 0.8119
𝑉
84
𝑚𝑙
𝒎𝟑
𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝐸𝑡%9𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
91 − 92
∗ (𝜌 − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)) = 92 +
∗ (811.9 − 809.455)
812.165 − 809.455
= 𝟗𝟏. 𝟎𝟗𝟖%
𝐸𝑡% = 𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1) +
4th sample:
𝜌=
𝑚𝑡𝑜𝑡𝑎𝑙 − 𝑚𝑏𝑒𝑎𝑘𝑒𝑟 153.9 − 88.5
𝑔 = 𝟖𝟏𝟐. 𝟒𝟐 𝒌𝒈
=
= 0.81242
𝑉
80.5
𝑚𝑙
𝒎𝟑
𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝐸𝑡%9𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
92 − 91
∗ (𝜌 − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)) = 91 +
∗ (812.42 − 809.89)
812.60 − 809.89
= 𝟗𝟏. 𝟗𝟑𝟒%
𝐸𝑡% = 𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1) +
5th sample:
𝑚𝑡𝑜𝑡𝑎𝑙 − 𝑚𝑏𝑒𝑎𝑘𝑒𝑟 153.5 − 88.5
𝑔 = 𝟖𝟏𝟒. 𝟓𝟒 𝒌𝒈
=
= 0.81454
𝑉
79.8
𝑚𝑙
𝒎𝟑
Since temperature was 24.7 degree Celsius, initially density values at 89% and 90%
ethanol mass fractions must be figured out through interpolation:
813.53 − 814.40
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1) = 814.40 +
∗ (24.7 − 24) = 𝟖𝟏𝟑. 𝟕𝟗𝟏 (𝟗𝟎% 𝒇𝒓𝒂𝒄𝒕𝒊𝒐𝒏)
25 − 24
𝜌=
31
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) = 817.05 +
816.17 − 817.05
∗ (24.7 − 24) = 𝟖𝟏𝟔. 𝟒𝟑𝟒 (𝟖𝟗% 𝒇𝒓𝒂𝒄𝒕𝒊𝒐𝒏)
25 − 24
𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝐸𝑡%9𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
89 − 90
∗ (𝜌 − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)) = 90 +
∗ (814.54 − 813.791)
816.434 − 813.791
= 𝟖𝟗. 𝟕𝟏𝟕%
𝐸𝑡% = 𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1) +
6th sample:
𝜌=
𝑚𝑡𝑜𝑡𝑎𝑙 − 𝑚𝑏𝑒𝑎𝑘𝑒𝑟 160.1 − 88.5
𝑔 = 𝟖𝟐𝟐. 𝟗𝟗 𝒌𝒈
=
= 0.82299
𝑉
87
𝑚𝑙
𝒎𝟑
𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝐸𝑡%9𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
87 − 86
∗ (𝜌 − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)) = 86 +
∗ (822.99 − 824.84)
822.26 − 824.84
= 𝟖𝟔. 𝟕𝟏𝟕%
𝐸𝑡% = 𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1) +
7th sample:
𝑚𝑡𝑜𝑡𝑎𝑙 − 𝑚𝑏𝑒𝑎𝑘𝑒𝑟 240.6 − 198.8
𝑔 = 𝟖𝟎𝟑. 𝟖 𝒌𝒈
=
= 0.8038
𝑉
52
𝑚𝑙
𝒎𝟑
Since temperature was 22.5 degree Celsius, initially density values at 94% and 95%
ethanol mass fractions must be figured out through interpolation:
801.55 − 802.41
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1) = 802.41 +
∗ (22.5 − 22) = 𝟖𝟎𝟏. 𝟗𝟖 (𝟗𝟓% 𝒇𝒓𝒂𝒄𝒕𝒊𝒐𝒏)
23 − 22
𝜌=
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) = 805.23 +
804.37 − 805.23
∗ (22.5 − 22) = 𝟖𝟎𝟑. 𝟑 (𝟗𝟒% 𝒇𝒓𝒂𝒄𝒕𝒊𝒐𝒏)
23 − 22
𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝐸𝑡%9𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
94 − 95
∗ (𝜌 − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)) = 95 +
∗ (803.8 − 801.98) = 𝟗𝟑. 𝟔𝟐𝟏%
803.3 − 801.98
𝐸𝑡% = 𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1) +
8th sample:
𝜌=
𝑚𝑡𝑜𝑡𝑎𝑙 − 𝑚𝑏𝑒𝑎𝑘𝑒𝑟 156.6 − 88.5
𝑔 = 𝟖𝟏𝟓. 𝟓𝟕 𝒌𝒈
=
= 0.81557
𝑉
83.5
𝑚𝑙
𝒎𝟑
𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝐸𝑡%9𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
89 − 88
∗ (𝜌 − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)) = 88 +
∗ (815.57 − 817.92)
815.30 − 817.92
= 𝟖𝟖. 𝟖𝟗𝟕%
𝐸𝑡% = 𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1) +
9th sample:
32
𝜌=
𝑚𝑡𝑜𝑡𝑎𝑙 − 𝑚𝑏𝑒𝑎𝑘𝑒𝑟
=
82.6
= 0.830151
𝑔
= 𝟖𝟑𝟎. 𝟏𝟓𝟏
𝒌𝒈
𝑉
99.5
𝑚𝑙
𝒎𝟑
Since temperature was 25.1 degree Celsius, density values for this sample can be
taken approximated as 25 degrees Celsius, thus calculations are introduced as:
𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝐸𝑡%9𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
84 − 83
∗ (𝜌 − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)) = 83 +
∗ (830.151 − 829.05)
829.05 − 831.57
= 𝟖𝟐. 𝟓𝟔𝟑%
𝐸𝑡% = 𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1) +
10th sample:
𝑚𝑡𝑜𝑡𝑎𝑙 − 𝑚𝑏𝑒𝑎𝑘𝑒𝑟
71 = 0.824623 𝑔 = 𝟖𝟐𝟒. 𝟔𝟐𝟑 𝒌𝒈
=
𝑉
86.1
𝑚𝑙
𝒎𝟑
Since temperature was 22.5 degree Celsius, initially density values at 85% and 86%
ethanol mass fractions must be figured out through interpolation:
823.96 − 824.84
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1) = 824.84 +
∗ (24.6 − 24) = 𝟖𝟐𝟒. 𝟑𝟏𝟐 (𝟖𝟔% 𝒇𝒓𝒂𝒄𝒕𝒊𝒐𝒏)
25 − 24
𝜌=
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) = 827.39 +
826.51 − 827.39
∗ (24.6 − 24) = 𝟖𝟐𝟔. 𝟖𝟔𝟐 (𝟖𝟓% 𝒇𝒓𝒂𝒄𝒕𝒊𝒐𝒏)
25 − 24
𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝐸𝑡%9𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
85 − 86
∗ (𝜌 − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)) = 86 +
∗ (824.623 − 824.312)
826.862 − 824.312
= 𝟖𝟓. 𝟖𝟕𝟖%
𝐸𝑡% = 𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1) +
11th sample:
𝜌=
𝑚𝑡𝑜𝑡𝑎𝑙 − 𝑚𝑏𝑒𝑎𝑘𝑒𝑟
84.4 = 0.826641 𝑔 = 𝟖𝟐𝟔. 𝟔𝟒𝟏 𝒌𝒈
=
𝑉
102.1
𝑚𝑙
𝒎𝟑
𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝐸𝑡%9𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
86 − 85
∗ (𝜌 − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)) = 85 +
∗ (826.641 − 824.84)
827.39 − 824.84
= 𝟖𝟓. 𝟕𝟎𝟔%
𝐸𝑡% = 𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1) +
12th sample:
𝜌=
𝑚𝑡𝑜𝑡𝑎𝑙 − 𝑚𝑏𝑒𝑎𝑘𝑒𝑟
=
58.7
= 0.826761
𝑔
=. 𝟖𝟐𝟔. 𝟕𝟔𝟏
𝒌𝒈
𝑉
71
𝑚𝑙
𝒎𝟑
Since temperature was 23.8 degree Celsius, initially density values at 85% and 86%
ethanol mass fractions must be figured out through interpolation:
824.84 − 825.71
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1) = 825.71 +
∗ (23.8 − 23) = 𝟖𝟐𝟓. 𝟎𝟏𝟒 (𝟖𝟔% 𝒇𝒓𝒂𝒄𝒕𝒊𝒐𝒏)
24 − 23
33
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) = 828.26 +
827.39 − 828.26
∗ (23.8 − 23) = 𝟖𝟐𝟕. 𝟓𝟗𝟒 (𝟖𝟓% 𝒇𝒓𝒂𝒄𝒕𝒊𝒐𝒏)
24 − 23
𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝐸𝑡%9𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
85 − 86
∗ (𝜌 − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)) = 86 +
∗ (826.761 − 825.014)
827.594 − 825.014
= 𝟖𝟓. 𝟑𝟐𝟑%
𝐸𝑡% = 𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1) +
13th sample:
𝑚𝑡𝑜𝑡𝑎𝑙 − 𝑚𝑏𝑒𝑎𝑘𝑒𝑟 161 − 88.9
𝑔 =. 𝟖𝟑𝟑. 𝟓𝟐𝟔 𝒌𝒈
=
= 0.833526
𝑉
86.5
𝑚𝑙
𝒎𝟑
Since temperature was 24.5 degree Celsius, initially density values at 82% and 83%
ethanol mass fractions must be figured out through interpolation:
834.07 − 834.95
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1) = 834.95 +
∗ (24.5 − 24) = 𝟖𝟑𝟒. 𝟓𝟏(𝟖𝟐% 𝒇𝒓𝒂𝒄𝒕𝒊𝒐𝒏)
25 − 24
𝜌=
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) = 832.44 +
831.57 − 832.44
∗ (24.5 − 24) = 𝟖𝟑𝟐. 𝟎𝟎𝟓 (𝟖𝟑% 𝒇𝒓𝒂𝒄𝒕𝒊𝒐𝒏)
25 − 24
𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝐸𝑡%9𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
83 − 82
∗ (𝜌 − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)) = 82 +
∗ (833.526 − 834.51)
832.005 − 834.51
= 𝟖𝟐. 𝟑𝟗𝟑%
𝐸𝑡% = 𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1) +
14th sample:
𝜌=
𝑚𝑡𝑜𝑡𝑎𝑙 − 𝑚𝑏𝑒𝑎𝑘𝑒𝑟
𝑉
=
87.3
= 0.815888
107
𝑔
𝑚𝑙
= 𝟖𝟏𝟓. 𝟖𝟖𝟖
𝒌𝒈
𝒎𝟑
𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝐸𝑡%9𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
90 − 89
∗ (𝜌 − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)) = 89 +
∗ (815.888 − 816.17)
813.53 − 816.17
= 𝟖𝟗. 𝟏𝟎𝟕%
𝐸𝑡% = 𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1) +
15th sample:
𝑚𝑡𝑜𝑡𝑎𝑙 − 𝑚𝑏𝑒𝑎𝑘𝑒𝑟
95.5 = 0.848 𝑔 = 𝟖𝟒𝟖 𝒌𝒈
=
𝑉
112.5
𝑚𝑙
𝒎𝟑
Since temperature was 24.5 degree Celsius, initially density values at 76% and 77%
ethanol mass fractions must be figured out through interpolation:
848.85 − 849.72
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1) = 849.72 +
∗ (24.5 − 24) = 𝟖𝟒𝟗. 𝟐𝟖𝟓(𝟕𝟔% 𝒇𝒓𝒂𝒄𝒕𝒊𝒐𝒏)
25 − 24
𝜌=
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) = 847.28 +
846.41 − 847.28
∗ (24.5 − 24) = 𝟖𝟒𝟔. 𝟖𝟒𝟓 (𝟕𝟕% 𝒇𝒓𝒂𝒄𝒕𝒊𝒐𝒏)
25 − 24
34
𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝐸𝑡%9𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
77 − 76
∗ (𝜌 − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)) = 76 +
∗ (848 − 849.285)
846.845 − 849.285
= 𝟕𝟔. 𝟓𝟐𝟕%
𝐸𝑡% = 𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1) +
16th sample:
𝜌=
𝑚𝑡𝑜𝑡𝑎𝑙 − 𝑚𝑏𝑒𝑎𝑘𝑒𝑟
=
𝑉
67.5
= 0.823171
82
𝑔
𝑚𝑙
𝒌𝒈
= 𝟖𝟐𝟑. 𝟏𝟕𝟏
𝒎𝟑
𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝐸𝑡%9𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
86 − 85
∗ (𝜌 − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)) = 85 +
∗ (823.171 − 826.51)
823.96 − 826.51
= 𝟖𝟔. 𝟑𝟎𝟗%
𝐸𝑡% = 𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1) +
17th sample:
𝜌=
𝑚𝑡𝑜𝑡𝑎𝑙 − 𝑚𝑏𝑒𝑎𝑘𝑒𝑟
=
𝑉
79.3
= 0.834737
95
𝑔
𝑚𝑙
𝒌𝒈
= 𝟖𝟑𝟒. 𝟕𝟑𝟕
𝒎𝟑
𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝐸𝑡%9𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
82 − 81
∗ (𝜌 − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)) = 81 +
∗ (834.737 − 836.56)
834.07 − 836.56
= 𝟖𝟏. 𝟕𝟑𝟐%
𝐸𝑡% = 𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1) +
18th sample:
𝜌=
𝑚𝑡𝑜𝑡𝑎𝑙 − 𝑚𝑏𝑒𝑎𝑘𝑒𝑟
=
108.3
= 0.826718
𝑔
= 𝟖𝟐𝟔. 𝟕𝟏𝟖
𝒌𝒈
𝑉
131
𝑚𝑙
𝒎𝟑
Since temperature was 23.5 degree Celsius, initially density values at 85% and 86%
ethanol mass fractions must be figured out through interpolation:
824.84 − 825.71
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1) = 825.71 +
∗ (23.5 − 23) = 𝟖𝟐𝟓. 𝟐𝟕𝟓 (𝟖𝟔% 𝒇𝒓𝒂𝒄𝒕𝒊𝒐𝒏)
24 − 23
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) = 828.26 +
827.39 − 828.26
∗ (23.5 − 23) = 𝟖𝟐𝟕. 𝟖𝟐𝟓 (𝟖𝟓% 𝒇𝒓𝒂𝒄𝒕𝒊𝒐𝒏)
24 − 23
𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝐸𝑡%9𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
85 − 86
∗ (𝜌 − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)) = 86 +
∗ (826.718 − 825.275)
827.825 − 825.275
= 𝟖𝟓. 𝟒𝟑𝟒%
Bottom Product Sample:
𝐸𝑡% = 𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1) +
𝜌=
𝑚𝑡𝑜𝑡𝑎𝑙 − 𝑚𝑏𝑒𝑎𝑘𝑒𝑟
𝑉
=
171.8
= 0.987356
174
𝑔
𝑚𝑙
35
= 𝟗𝟖𝟕. 𝟑𝟓𝟔
𝒌𝒈
𝒎𝟑
𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝐸𝑡%9𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
5−4
∗ (𝜌 − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)) = 4 +
∗ (987,356 − 987,30)
988,99 − 987.30
= 𝟒, 𝟎𝟑𝟑%
𝐸𝑡% = 𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1) +
Top Product Total Sample:
𝜌=
𝑚𝑡𝑜𝑡𝑎𝑙 − 𝑚𝑏𝑒𝑎𝑘𝑒𝑟
=
1282,6
= 0.823764
𝑔
= 𝟖𝟐𝟑. 𝟕𝟔𝟒
𝒌𝒈
𝑉
1557
𝑚𝑙
𝒎𝟑
Since temperature was 24.26 degree Celsius, initially density values at 85% and 86%
ethanol mass fractions must be figured out through interpolation:
821.39 − 822.26
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1) = 822.26 +
∗ (24,26 − 24) = 𝟖𝟐𝟐, 𝟎𝟑𝟒 (𝟖𝟔% 𝒇𝒓𝒂𝒄𝒕𝒊𝒐𝒏)
25 − 24
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) = 824.84 +
823.96 − 824.84
∗ (24,26 − 24) = 𝟖𝟐𝟒, 𝟔𝟏𝟏 (𝟖𝟕% 𝒇𝒓𝒂𝒄𝒕𝒊𝒐𝒏)
25 − 24
𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝐸𝑡%9𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 2) − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)
87 − 86
∗ (𝜌 − 𝜌(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1)) = 86 +
∗ (823,764 − 822.034)
824,611 − 822,034
= 𝟖𝟔, 𝟔𝟕%
𝐸𝑡% = 𝐸𝑡%(𝑟𝑒𝑓𝑒𝑟𝑒𝑛𝑐𝑒 1) +
36