PNGE332 WVU Saturation pressure Binary System PVT Simulator Lab Report please paraphrase these 4 lab reports into one new lab report book name:William D.

PNGE332 WVU Saturation pressure Binary System PVT Simulator Lab Report please paraphrase these 4 lab reports into one new lab report

book name:William D. McCain, Jr., The Properties of Petroleum Fluids, 2nd edition (PennWell Publishing Company, 1990). “or the third edition”

use any lab report numbers, they almost the same.

I have added a power point explaining the experiment.

I will upload the book after accepting the offer.

Thanks Saturation Pressure of a Binary
System Using PVT Simulator
Fathi PNGE 332
1
Motivation
 In this experiment we will
generate a pressure composition
diagram at constant temperature
for a mixture of CO2 and C4H10
 Observe the effect of changing
composition on a binary system
 Composition will be expressed as
the mole fraction of CO2 in the
mixture
 The pressures plotted are the
bubble point and dew point
pressures as a function of
composition
Fathi PNGE 332
2
3
1
Typical pressure composition diagram of two
component mixtures with one tie line, 123
2
Experiment 2: Pressure-Composition
Diagram
 Initially visual cell contains 10 cc n-butane at 2000 psi at
constant T
 Charging vessel #1 contains pure CO2 at 2000 psi but at room
temperature 71.6 oF
2
3
1
Typical pressure composition diagram of two
component mixtures with one tie line, 123
Fathi PNGE 332
3
Experiment 2: Pressure-Composition
Diagram (Cont.)
1.
2.
3.
4.
Find the bubble point and dew point of pure n-butane. This
corresponds to mole fraction of zero added CO2.
Restore system to its initial condition
At specific temperature the amount of added CO2 needed to
meet the required mole fractions (use Table 4)
The CO2 can be added in increments (Table 4b)or as a total
(Table 4a) which method is used depends on whether one use
the apparatus or the simulator
Fathi PNGE 332
4
Experiment 2: Using Apparatus
The only practical way is the incremental method
1. Add the amount of Co2 necessary for 0.1 mole fraction
2. let system reached the equilibrium
3. determine the saturation pressure
4. bring the cell back to 2000 psi
5. Then inject the incremental or additional amount of CO2
needed to make 0.2 mole fraction
6. Find the saturation pressures
7. Repeat from step 4
Fathi PNGE 332
5
Experiment 2: Using Apparatus
If we wanted to use the total amount method
1. add the amount of Co2 necessary for 0.1 mole fraction
2. let system reached the equilibrium
3. determine the saturation pressure
4. Purge the visual cell of the contents
5. Re-inject fresh butane
6. Allow the system to come to operating temperature (can take
several hours)
7. Add the Co2 needed for 0.2 mole fraction
8. Find the saturation pressures
9. Repeat from step 4
Fathi PNGE 332
6
Experiment 2: Using PVTLAB Simulator
Performing the Experiment using total amounts is much quicker all
you need to do is
1. Perform the experiment at 0.1 mol fraction
2. Exit then re-enter and perform, add the total amount needed
for 0.2 mole fraction
3. Collect the data exit, re-enter and continue
Performing the Experiment using incremental amounts is more
difficult since
1. After each increment you need to bring back the system to
initial pressure of 2000 psi (achieving that could be very
difficult)
2. If program crashes at any time you have to do all the steps
from begging
Fathi PNGE 332
7
Equations used to calculate Co2 volume
Fathi PNGE 332
8
Experiment 2: n-butane and Co2 Densities
Fathi PNGE 332
9
Khalid Alakeel
PNGE332
Lab#2
LAB 2
Saturation Pressure of a Binary System
Using PVT Simulator
2/26/2019
G1
Khalid Alakeel
PNGE332
Lab#2
Cover letter:
In this experiment, a mixture of two components were tested to define the bubble point
and dew point of the mixture at constant temperature. In our case, the two components were
carbon dioxide and n-butane, and the temperature was 71.6 oF.
This experiment was conducted on a PVT simulator because of the regulations of
mercury usage. Initially, the cell had 10cc of n-butane, then we started injecting CO2 gradually
from a different vessel starting from 0.1 mole until we reach 0.9 mole of CO2 and calculate the
bubble point at each time. The experiment was conducted 9 times since every time we had to
change the amount of CO2 inside the cell.
After recording the data, the graph of pressure vs mole fraction of CO2 will show the
regions of liquid, gas, and two phase are present. In addition, using table 5, we will be able to
calculate the density at the critical point which is 22oF. Finally, we will verify at least one of the
numbers in table 4.
Khalid Alakeel
PNGE332
Lab#2
Theory and objective:
This experiment will allow us to draw a saturation pressure diagram of a binary system
where we have 2 components. Using the PVT simulator, we will get accurate numbers and the
experiment will be done at a constant temperature of 71.6 F. And from the graph, we will be able
to observe the effect of changing the composition of the mixture and how it effects the bubble
and dew point.
As we know, the bubble point can be observed when the first gas bubble comes out of the
liquid. At this point, the PVT simulator allows us to record the values of liquid n-Butane, gas nButane, liquid CO2, gas CO2, as well as the pressure. Given the following data we can create the
pressure composition diagram.
By theory, as we increase the mole fraction, the bubble point and dew point increase.
However, they don’t have the same rate of change. For example, the bubble point pressure line is
linear, and the dew point pressure line in exponential (see figure 1).
Figure 1
Khalid Alakeel
PNGE332
Lab#2
Procedure:
This experiment was conducted 9 times due to the change of composition of CO2 each
time. The following procedure was done when opening the PVT simulator.
1- Withdrawing Hg from the cell by the same amount of CO2 that will be added to the cell to
make some space for it.
2- Adding the specified amount of CO2 from vessel 1 to the cell based on table 4a.
3- Checking the amounts of n-Butane and CO2 in the cell to avoid any calculation errors.
4- Withdrawing Hg from the cell until we hit the bubble point and shaking the cell each time
we withdraw to mix the two substances together.
5- Record the amounts of liquid and gas of n-Butane and CO2 when reaching the bubble
point.
6- Repeating the same process for all CO2 composition.
Khalid Alakeel
PNGE332
Lab#2
Results:
Pressure
32.5
140.9
230.7
343.3
432.63
512.32
583.02
641.21
710.41
784.31
n-C4 (liquid)
1
0.9058
0.8104
0.714
0.6164
0.517
0.4161
0.3142
0.2109
0.1072
n-C4 (gas)
1
0.2501
0.152
0.1141
0.0945
0.0824
0.0738
0.0664
0.0577
0.0488
CO2 (liquid)
0
0.0942
0.1896
0.286
0.3836
0.483
0.5839
0.6858
0.7891
0.8928
CO2 (gas)
0
0.7499
0.848
0.8859
0.9055
0.9176
0.9262
0.9336
0.9423
0.9512
liquid
two phase region
Gas
Temprature
16.9
26.9
21.9
Density @
10 Mpa 15 Mpa
878.2 920.7
802.1 866.4
840.141 893.583
Khalid Alakeel
PNGE332
Temprature = 21.9 F
Pressure
Density
10
840.141
15
893.583
13.8
880.7544
Volume of CO2 = ∗

( ) 44.01 ( ) 103

=
=
∗
= 49.97
3

( )

880.7544 ( 3 )

=
2 ∗ 4 0.6 ∗ 0.1025
=
= 0.1538
1 − 2
1 − 0.6
Vco2 = 49.97*0.1538= 7.68 cc
Lab#2
Khalid Alakeel
PNGE332
Lab#2
Results analysis:
In the PVT simulator, the Peng-Robinson’s equation was used to calculate all the data
that we have. And as we can see, the equation shows that the bubble points show a linear
relationship and the dew points show an exponential relationship. However, since we are dealing
with a computer program, there are no external interference with the environment. Therefore,
there is limited sources of errors. However, due to the assumptions of the Peng-Robinson’s
equation, which neglects the volume of gas particles and assuming that gas particles collide
perfectly elastic, we can have some sort of error.
After creating the graph of the bubble point and the dew point, we can see that the bubble
point curve is not a perfect straight line where it is supposed to be a perfect straight line.
However, it was close enough to a straight line which makes it reliable. In addition, the
relationship of pressure and temperature is not linear in real gasses, but we assumed it is linear
due to the assumptions of Peng-Robinson.
Khalid Alakeel
PNGE332
Lab#2
Conclusion:
In this experiment, the mixture of carbon dioxide and n-Butane results were reasonable
even though they were treated as an ideal gas. The graphs were close enough to the theoretical
graphs which indicates that the experiment was conducted correctly.
West Virginia University
LAB 2
Saturation Pressure of a Binary
System Using PVT Simulator
Class No. W01
February 23, 2018
Groups:
G1
Cover letter:
First of all, the experiment was held on Feb 2nd, 2018 in G11. The
goal of the experiment was to define the bubble point and the dew point
of a binary system at a specific temperature. This binary system consists
of a mixture of carbon dioxide and normal butane. The specific
temperature is 22° F
In the beginning of the experiment the pressure was 2000 psia, and
10cc of normal butane, vessel number 1 contains pure CO2 at a pressure
of 2000 psia. Therefore, the students were asked to add specific amounts
of CO2 to the n-butane, these amounts of CO2 can vary between 0.1 mole
and 0.9 mole fraction in relation to the amount of normal butane.
Inserting carbon dioxide to the visual cell was done by removing mercury
from the visual cell to the hand pump. Then, the students connected and
disconnected some valves in order to move the amount of CO2 to the
visual cell. The experiment was done nine times because each time the
student inserted a specific amount of CO2 in terms of mole fraction.
Theory, concepts and objective of the experiment:
The objective was to find the bubble and dew point pressure at
71.6° F, C. temperature is the temperature above which the gas can’t be
liquified. C. pressure is the pressure above which liquid and gas coexist.
The bubble point is the point where the first gas appears in the liquid. The
dew point is the point where the last drop of liquid converted to gas (The
Book).
The instructor showed the students how does the diagram of two
components looks like as shown in Figure1.
Figure1: Two component mixture phase
As illustrated there is a relationship between the mole fraction and
the pressure (bubble and dew points). As the mole fraction increases the
pressure increases. The simulator uses the equation PRE (Lab manual).
Experimental Procedure:
In the beginning of the experiment we opened the PVT simulator
program, then we typed:
Copylab2G1.la2 setup.par
The lab
Then press F2 in order to open two valves (8 and 9), so we can have a
communication between the visual cell and the hand pump. Then, we also
opened valves 4 and 11, there will be no change in pressure so it will
remain 2000 psia. Then, then start withdrawing mercury from the visual
cell until we have a 0.1 mole fraction using F5 bottom. Then we close
valve 8 in order to isolate the cell from the hand pump. After that, we
open valve 1 to start injecting amount of mercury to the charging vessel
as the amount of mercury withdrawn. Now we have CO2 in the cell, then
we close valves 1, 4, and 11, and open valve 8. Since we have a mixture
in this experiment we will need to use F6 in order to mix the content and
to let the system in equilibrium. Now, using F5 we will start withdrawing
mercury until the bubble point which is 0.002 cc (you must use F6 after
each withdrawing). Then record the analysis in an excel sheet. Also, press
F10 to record a chromatographic analysis. Then repeat this experiment
with the same temperature, but different mole fractions, each time record
the data.
Results and calculations:
P
Xco2
32.569
140.9
342.66
433.11
512.54
581.13
641.19
700.11
773.31
0
0.0942
0.2855
0.3842
0.4833
0.5839
0.6858
0.7891
0.8938
yco2
xc4
0
0.7699
0.8857
0.9056
0.9177
0.9262
0.9336
0.9423
0.9585
yc4
1
0.9058
0.7145
0.6158
0.5167
0.4161
0.3142
0.2109
0.11062
1
0.2501
0.1143
0.0944
0.0823
0.0738
0.0664
0.0577
0.0415
Volume
Mole
of CO2
Fraction Added
0.1
0.57
0.2
1.282
0.3
2.197
0.4
3.418
0.5
5.126
0.6
7.69
0.7
11.962
0.8
20.505
0.9
46.137
900
800
700
Liquid
600
500
400
two phase region
300
200
100
Gas
0
0
0.2
0.4
0.6
0.8
Bubble Point
1
1.2
Dew Point
Figure 2: Pressure, mole fraction of CO2
Since the temperature of 22° C is not found in table 5 in the lab manual,
we have to use an average between 16.9and 26.9 same thing for the
density.
D
T
10 Mpa
15 Mpa
16.9
878.2
920.7
26.9
802.1
866.4
21.9
840.15
893.55
940
920.7
920
Density
900
878.2
880
866.4
860
840
820
802.1
800
780
0
5
10
15
20
25
30
Temperature C
Figure 3: Temp. Vs. Density
So, the density at a 13.8 Mpa is 880.169 Kg/M3.
Pressure Vs. Density
900
890
Density
880
870
860
850
840
830
0
2
4
6
8
10
12
14
16
Pressure MPa
The volume of carbon dioxide is not calculated yet so, the equation given
has to be used in order to find the volume.
Molecular weight of carbon dioxide = 44.010 kg/kmole
Density of carbon dioxide = 880.169 kg/m3
Volume of carbon dioxide = (44.010/880.169)*103 = 50.002cc/mole =
50.002*(0.6*0.1025/0.4) = 7.69 cc
Analysis and Discussion:
PVT simulator uses PR equation (lab manual) this simulator is an old
program and it is not well updated (the book), so there might be some
minor errors.
P = (RT)/(V-b) – a/(V2+2Vb-b2)
This equation is not correct because of some reasons (the book):
1- the tubing in the system which is the lines leading between the
valves, has no volume.
2- Pressure changes happen isothermally
3- Joule-Thomson impacts are ignored.
4- Mercury is considered as non-compressible substance.
5- Equilibrium in thermodynamic is instantaneous
Conclusion:
A mixture of carbon dioxide and normal butane was examined for
the bubble point and dew point at a specific temperature using PVT
simulator. There is a relationship between the pressure and the mole
fraction “as the pressure increases the mole fraction increases”. The
interpolations (table 5 in the lab) was used to determine the density at a
given temperature. On the graph the highest point indicates the critical
point.
References:
1- McCain, William D. The Properties of Petroleum Fluids. PennWell Books, 1990.
2- Lab manual, EXP 2: Saturation Pressure of a Binary System Using PVT
Simulator
Lab #2:
Saturation Pressure of a Binary System Using PVT
Simulator
1/12/2016
Table of Contents
Pages
Cover Letter……………………………………………………………3-4
1
Theory, concepts, and objective……………………………..5-6
Experimental Procedure………………………………………….7-9
Results and calculations………………………………………….10-11
Analysis and discussion…………………………………………..12-14
Conclusions……………………………………………………………….15
References…………………………………………………..……………16
Cover Letter
Dear Dr. Fathi,
In Experiment # 2, the main objective was to generate a pressure composition diagram
at a constant temperature for a mixture of CO2 and C4H10. This diagram is used to display how
2
changing the composition of a binary system effects the system as a whole. Once this diagram
was constructed, a tie-line could be created from the data points. The pressures plotted in the
diagram are bubble point (PB) and the dew point (PD) pressures of the binary system as a
function of composition, expressed as the mole fraction of CO2.
The procedure to generate this pressure composition diagram was carried out using the
PVT simulator. The initial conditions for this lab were that the visual cell contained 10 cc. of
normal butane at 2000 psia at room temperature, 71.6°F. A charging vessel containing pure
CO2, initially at 2000 psia and room temperature, was used to add specific volumes of CO2 to
the mixture in order to make 10 different mole fractions of CO2. Each individual mole amount
of CO2 added to the butane generated different bubble point pressures due to the variation of
the composition of the binary mixture. The PVT simulator allowed the user to pump the
amount of mercury needed to make 0 – 0.9 mole fraction of CO2 into the charging cell which in
turn transferred that exact amount of CO2 to the visual cell. The components then reached
chemical equilibrium and the bubble points were found by removing arbitrary amounts of
mercury from the visual cell until 0.002 cc or less of gas was displayed. This process was
repeated for 0 to 0.9 mole fraction of CO2. To find the dew point pressure, one of the 9 mole
fractions of CO2 was used but with 1 cc of butane instead of 10 cc in order to allow for more
room in the visual cell to expand the liquid to the gas phase. Since one-tenth of the original
volume of butane was used, one-tenth the amount of CO2 added to find the bubble points was
used to find the dew point.
Using this procedure for each of the mole fractions of CO2, several different bubble
point pressures were found that were used to generate the pressure composition diagram. The
liquid and gas compositions, Xi and Yi respectively, for both the CO2 and C4H10 were displayed by
the chromatograph once each bubble point was found. The experiment was started by first
finding the bubble point of the system with 0 mole fraction of CO2 which was found to have a
bubble point of 32.569 psia. For 0.1, 0.2, 0.3, 0.4, 0.5, 0.6, 0.7, 0.8, and 0.9 mole fraction of CO 2
initially in the visual cell, the bubble point pressures were 140.9 psia, 245.18 psia, 343.30 psia,
433.11 psia, 512.54 psia, 581.14 psia, 640.58 psia, 700.38 psia, and 773.25 psia, respectively. It
is a clear trend that as the mole fraction of CO2 was increased, the bubble point pressures
3
increased as well. The dew point was found using one-tenth the amount of CO2 added for 0.4
mole fraction of CO2. After repeating the procedure for finding the bubble point, the dew point
pressure was found to be 68.323 psia. It is necessary to understand that the accuracy of the
simulator regarding the pressure was (+ or – 0.001 psia). The accuracy of the composition of the
liquid and gas of CO2 and C4H10 was (+ or – 0.0001 %).
The theory behind this experiment involves two-component mixtures and the pressurecomposition diagrams that are generated using the data found in the experiment. It is
necessary to notice that in a pressure- volume diagram for a two-component mixture, the line
from the bubble point to the dew point isn’t straight like it was in the diagram for the pure
component. This is due to the changes in composition of the liquid and gas in the two-phase
region (McCain). Regarding the attributes of the pressure-composition diagram, a bubble point
line and dew point line are created using the data from the experiment which together form
the saturation envelope of the two-component mixture. If the pressure and composition
combinations occur above the envelope, the mixture is completely liquid. Likewise, if the
combination occurs below the envelope, the mixture is completely liquid (McCain). If the
composition and pressure occur within the envelope, the mixture is in two-phases. The bubble
point line is the center of the compositions of liquid when two-phases are present and the dew
point line is the center of the compositions of gas when the mixture is in two phases. A tie line
is the line that connects the bubble point line to the dew point line. Ratios of moles of gas and
liquid to the total moles of the mixture can be calculated by using these tie lines. Establishing
the bubble point line, dew point line, and tie line is the premise of this experiment. Finding this
criteria allows for easy computation of percent gas and percent liquid at specific pressures and
compositions.
Sincerely, Cole Bertol
Theory, concepts, and objective
4
The objective of this experiment was to create a pressure-composition diagram using
the bubble point pressures of a mixture of CO2 (carbon dioxide) and C4H10 (butane) as a function
of composition of CO2 in mole fraction. Ten different increments of mole fraction of CO2 were
used (0-0…
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