Design and Operation of a Distillation Column for the Binary Mixture
1. Design and Operation of a
Distillation Column for the
Binary Mixture:
Propane and Hydrogen Sulfide
Project Designers:
Jonathan Sherwin
Ross Starks
CHE-305-001
W. Jeffery Horne, P.E.
Bonus Design Project
April 25, 2014
2. Design and Operation of a Distillation Column for the Binary Mixture: Propane and Hydrogen Sulfide
2
Table of Contents
Abstract ........................................................................................................................................................3
Diagrams..................................................................................................................................................4-19
T-x-y Diagrams for H2S ...........................................................................................................................4-5
Activity Coefficients ...............................................................................................................................6-7
McCabe-Thiele Diagrams…………………………………………………………………………………………………………….….8-19
Process Flow Diagram for optimal Distillation Column……………………………………………………………………...20
Tables……………………………………………………………………………………………………………………………………….……..21-22
Appendix…………………………………………………………………………………………………………………………………….…..23-27
Calculations……………………………………………………………………………………………………………………………………….23
Data……………………………………………………………………………………………………………………………………..………24-26
References…………………………………………………………………………………………………………………………………………27
3. Design and Operation of a Distillation Column for the Binary Mixture: Propane and Hydrogen Sulfide
3
Abstract
We have been tasked with the job of determining the operating conditions and costs associated with the
design and operation of a distillation column, which is to be part of a 24/7/365 industrial operation. The
feed is a binary mixture of propane (C3H8) and hydrogen sulfide (H2S). The feed is a 50% by weight
mixture of propane and hydrogen sulfide. A feed mass flow rate of 2500 kg/hr is used. Both the distillate
and bottoms products are required to be at least 90% pure, which is attainable because the binary
mixture of propane and hydrogen sulfide is not azeotropic.
Equilibrium data was attained for a range of pressures: 0.1 atm, 1.0 atm, 5.0 atm, and 10.0 atm. T-x-y
data, activity coefficients, K-values, and relative volatility for the two compounds were used to construct
Equilibrium curves. This portion of our data and diagrams was calculated and is represented by
Equations 1-9 respectively.
McCabe-Thiele diagrams were constructed for each set of equilibrium data. For each set of pressure
data, feed conditions of a bubble-point liquid, a dew-point vapor, and a 50/50 by mass mixed
vapor/liquid were evaluated. Each feed scenario had an independent q-line and the values are
represented in Table 2. The minimum reflux was determined for each scenario. A ratio of reflux to
minimum reflux within the accepted range was chosen to be 1.3, so that R = 1.3Rmin. From the McCabe-
Thiele diagrams, the number of trays was determined for each scenario. The dew-point vapor feed at
0.1 atm, 5 atm, and 10 atm showed to be the most efficient, in terms of numbers of trays. R values and
the number of trays can both be seen in Table 1 for all conditions. R values were calculated using
Equation 12 and the number of trays was extrapolated from the McCabe-Thiele diagrams.
Total condenser and partial reboiler duties were calculated for all scenarios using Equations 14 and 15
with the results represented by Table 5. To use Equations 14 and 15 we found D and B, VB, and ΔH 𝑎𝑣𝑔
𝑣𝑎𝑝
by
using Equation 10, Equation 13, and the NIST Webbook respectively. Each scenario was evaluated in
terms of dollars per kilogram using equation 15 with results posted in Table 6. As seen in Table 6, the
lowest average cost is $119.98 to produce 90% pure products and this is achieved with the a bubbling
point liquid feed and an operating pressure of 10atm. Therefore, we suggest these operating conditions
to achieve profit maximization with this binary mixture: Bubbling-Point Liquid Feed, Operating Pressure
of 10atm, 10 Stages, and the feed located at Stage 5. A Process Flow Diagram for the Distillation Column
for optimal conditions can be seen in Figure 21.
4. Design and Operation of a Distillation Column for the Binary Mixture: Propane and Hydrogen Sulfide
4
Figure 1. T-x-y Diagram for H2S at 0.1 atm.
Figure 2. T-x-y Diagram for H2S at 1.0 atm.
-98
-96
-94
-92
-90
-88
-86
-84
-82
0 0.2 0.4 0.6 0.8 1
T(degreesC)
x,y
liquid H2S
vapor H2S
-65
-60
-55
-50
-45
-40
0 0.2 0.4 0.6 0.8 1
T(degreesC)
x,y
liquid H2S
vapor H2S
5. Design and Operation of a Distillation Column for the Binary Mixture: Propane and Hydrogen Sulfide
5
Figure 3. T-x-y Diagram for H2S at 5.0 atm.
Figure 4. T-x-y Diagram for H2S at 10.0 atm.
-25
-20
-15
-10
-5
0
5
0 0.2 0.4 0.6 0.8 1
T(degreesC)
x,y
liquid H2S
vapor H2S
-5
0
5
10
15
20
25
30
0 0.2 0.4 0.6 0.8 1
T(degreesC)
x,y
liquid H2S
vapor H2S
6. Design and Operation of a Distillation Column for the Binary Mixture: Propane and Hydrogen Sulfide
6
Figure 5. Activity Coefficients of H2S & C3H8 vs. liquid mole fractions at 0.1 atm.
Figure 6. Activity Coefficients of H2S & C3H8 vs. liquid mole fractions at 1.0 atm.
0.000
0.200
0.400
0.600
0.800
1.000
1.200
1.400
0 0.2 0.4 0.6 0.8 1
ActivityCoefficient
Liquid Mole Fraction
H2S
C3H8
0.000
0.200
0.400
0.600
0.800
1.000
1.200
1.400
0 0.1 0.2 0.3 0.4 0.5 0.6 0.7 0.8 0.9 1
ActivityCoefficient
Liquid Mole Fraction
H2S
C3H8
7. Design and Operation of a Distillation Column for the Binary Mixture: Propane and Hydrogen Sulfide
7
Figure 7. Activity Coefficients of H2S & C3H8 vs. liquid mole fractions at 5.0 atm.
Figure 8. Activity Coefficients of H2S & C3H8 vs. liquid mole fractions at 10.0 atm.
0
0.2
0.4
0.6
0.8
1
1.2
1.4
0 0.1 0.2 0.3 0.4 0.5 0.6 0.7 0.8 0.9 1
ActivityCoefficient
Liquid Mole Fraction
H2S
C3H8
0.000
0.200
0.400
0.600
0.800
1.000
1.200
1.400
0 0.2 0.4 0.6 0.8 1
ActivityCoefficient
Liquid Mole Fraction
C3H8
H2S
8. Design and Operation of a Distillation Column for the Binary Mixture: Propane and Hydrogen Sulfide
8
Figure 9. McCabe-Thiele Diagram for a Bubble Point Vapor Feed at 0.1 atm.
The McCabe-Thiele Diagram was created from the equilibrium curve and a 45⁰ line on a
squared chart. The dotted bottoms liquid mole fraction line, xB, was drawn at 0.1. The dotted
feed liquid mole fraction line, zF, was drawn at 0.5. The dotted distillate liquid mole fraction
line, xD, was drawn at 0.9. The q-line was drawn from zF, using equation 11 and Table 2. The
Operating Line for the Minimum Rectifying Section was drawn from the intersection of the q-
line with the equilibrium curve to the intersection of xD with the 45⁰ line. The slope of the
Minimum Rectifying Section was determined and an Rmin value was calculated. An R value was
then calculated from equation 12, and the Operating Line for the Rectifying section was then
adjusted. The Operating Line for the Stripping Section was then draw from the intersection of
the Operating Line for the Rectifying Section and the q-line to the intersection of xB with the
45⁰ line. The stage lines were then stepped off from xD to xB. The number of equilibrium stages
was then counted from the number of stage lines. This method was used in all McCabe-Thiele
Diagrams, referenced in Figures 10-20.
9. Design and Operation of a Distillation Column for the Binary Mixture: Propane and Hydrogen Sulfide
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Figure 10. McCabe-Thiele Diagram for a Dew Point Vapor Feed at .1 atm.
10. Design and Operation of a Distillation Column for the Binary Mixture: Propane and Hydrogen Sulfide
10
Figure 11. McCabe-Thiele Diagram for a 50/50 by mass Vapor/Liquid Feed at .1 atm.
11. Design and Operation of a Distillation Column for the Binary Mixture: Propane and Hydrogen Sulfide
11
Figure 12. McCabe-Thiele Diagram for a Bubble Point Liquid Feed at 1 atm.
12. Design and Operation of a Distillation Column for the Binary Mixture: Propane and Hydrogen Sulfide
12
Figure 13. McCabe-Thiele Diagram for a Dew Point Vapor Feed at 1 atm.
13. Design and Operation of a Distillation Column for the Binary Mixture: Propane and Hydrogen Sulfide
13
Figure 14. McCabe-Thiele Diagram for a 50/50 by mass Vapor/Liquid Feed at 1 atm.
14. Design and Operation of a Distillation Column for the Binary Mixture: Propane and Hydrogen Sulfide
14
Figure 15. McCabe-Thiele Diagram for a Bubble-Point Liquid Feed at 5.0 atm.
15. Design and Operation of a Distillation Column for the Binary Mixture: Propane and Hydrogen Sulfide
15
Figure 16. McCabe-Thiele Diagram for a Dew-Point Vapor Feed at 5.0 atm.
16. Design and Operation of a Distillation Column for the Binary Mixture: Propane and Hydrogen Sulfide
16
Figure 17. McCabe-Thiele Diagram for a 50/50 by mass vapor/liquid feed at 5.0 atm.
17. Design and Operation of a Distillation Column for the Binary Mixture: Propane and Hydrogen Sulfide
17
Figure 18. McCabe-Thiele Diagram for a Bubble-Point Liquid Feed at 10.0 atm.
18. Design and Operation of a Distillation Column for the Binary Mixture: Propane and Hydrogen Sulfide
18
Figure 19. McCabe-Thiele Diagram for a Dew-Point Vapor Feed at 10.0 atm.
19. Design and Operation of a Distillation Column for the Binary Mixture: Propane and Hydrogen Sulfide
19
Figure 20. McCabe-Thiele Diagram for a 50/50 by mass vapor/liquid feed at 10.0 atm.
20. Design and Operation of a Distillation Column for the Binary Mixture: Propane and Hydrogen Sulfide
20
Reflux Drum
Reflux
TotalCondenser
Boilup
Partial Reboiler
999912 kW/h
Bottoms
Distillate
Feed
2500 kg/h
50% wt. H2S
50% wt. C3H8
Pi: 10.0 atm
Feed Conditions: Bubble Point Liquid
1
10
5
6
1250 kg/h
xD = 0.90 H2S
1250 kg/h
xB = 0.10 H2S
999831 kW/h
Figure 21. Process Flow Diagram for optimal Distillation Column for Bubble Point Liquid Feed Condition
at 10.0 atm.
21. Design and Operation of a Distillation Column for the Binary Mixture: Propane and Hydrogen Sulfide
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Tables
Pressure
Feed Conditions Rmin R Number of Trays
0.1 atm
Bubble-Point Liquid 0.7699 1.0008 10
Dew-Point Vapor 1.7777 2.3110 8
50/50 by mass vapor/liquid 1.6666 2.1666 10
1.0 atm
Bubble-Point Liquid 0.9613 1.2496 12
Dew-Point Vapor 2.0000 2.6000 10
50/50 by mass vapor/liquid 1.3182 1.7136 11
5.0 atm
Bubble-Point Liquid 0.7778 1.0111 11
Dew-Point Vapor 1.8182 2.3637 8
50/50 by mass vapor/liquid 1.1807 1.5349 10
10.0 atm
Bubble-Point Liquid 0.7778 1.0111 10
Dew-Point Vapor 1.8182 2.3637 8
50/50 by mass vapor/liquid 1.1807 1.5349 10
Table 1. Rmin values, R values, and Number of Trays for respective Feed Conditions and Pressures.
Feed Condition q slope of q-line
Bubble Point Liquid 1 vertical
Dew Point Vapor 0 horizontal
50/50 by mass vapor/liquid 0.5 -1
Table 2. q values and slope of q-line, given by equation 11, for respective Feed Conditions.
P=.1atm BP DP 50-50
m of strip 1.500 1.763 1.662
Vb 2.001 1.311 1.510
P=1atm BP DP 50-50
m of strip 1.445 1.625 1.582
Vb 2.250 1.600 1.717
P=5atm BP DP 50-50
m of strip 1.497 1.737 1.667
Vb 2.011 1.357 1.500
P=10atm BP DP 50-50
m of strip 1.497 1.737 1.667
Vb 2.011 1.357 1.500
Table 3. Representation of equation 13 for respective Pressures.
P (atm) ΔH (kJ/kg)
0.1 466.03
1 486.16
5 434.67
10 397.73
Table 4. Average Heat of Vaporization for the Binary Mixture at the respective Pressure from Nist
Webbook.
22. Design and Operation of a Distillation Column for the Binary Mixture: Propane and Hydrogen Sulfide
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BP
(kW/h)
DP
(kW/h)
50/50
(kW/h) BP ($/kg)
DP
($/kg)
50/50
($/kg)
P=.1atm Qc 1165534 1928826 1466037 139.86 231.46 175.92
Qr 1165534 763763 879622 139.86 91.65 105.55
139.86 161.56 140.74 AVG
P=1atm Qc 1367107 2187720 1649077 164.05 262.53 197.89
Qr 1367107 972320 1043293 164.05 116.68 125.20
164.05 189.60 161.54 AVG
P=5atm Qc 1092715 1827585 1377317 131.13 219.31 165.28
Qr 1092803 737435 815013 131.14 88.49 97.80
131.13 153.90 131.54 AVG
P=10atm Qc 999831 1672235 1260241 119.98 200.67 151.23
Qr 999912 674751 745734 119.99 80.97 89.49
119.98 140.82 120.36 AVG
Table 5. Cost analysis representative of equations 14-16.
27. Design and Operation of a Distillation Column for the Binary Mixture: Propane and Hydrogen Sulfide
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References
Seader, J. D., Ernest J. Henley, and D. Keith Roper. Separation Process Principles. Third ed. N.p.:Courier
Westford, 2011. Print.
NIST Chemistry Webbook. N.p., n.d. Web. 24 Apr. 2014. <http://webbook.nist.gov/chemistry/>.
Thermophysical Properties of Fluid Systemsby E.W. Lemmon, M.O. McLinden, D.G.
Friend