Saba _ Excel _ Material Balance_ Project
This document was uploaded by user and they confirmed that they have the permission to share it. If you are author or own the copyright of this book, please report to us by using this DMCA report form. Report DMCA
Overview
Download & View Saba _ Excel _ Material Balance_ Project as PDF for free.
More details
- Words: 1,307
- Pages: 37
P= B= I= C= D= Kmol/h : Kg /h :
26.40 22.34 41.44 1.24 0.03 91.45 4,828.59
You can change: Kmol/h : Kg /h :
P= B= I= C= D=
ANY CHANGES IN FEED STREAM MOLAR RATE, O ANY OF SYSTEM PERFORMANCE SPECIFICATION SHOULD BE APPLIED IN THIS SECTION 8
10
100.00 5,796.28 2.00 1.00 53.02 44.19 2.79
P= B= I= C= D=
Mass purity of C:
P= B= I= C= D= Kmol/h : Kg /h :
0.00 0.03 0.00 2.41 2.95 5.40 769.94
Kmol/h : 1,061.36 Kg /h : 47,725.51
P= B= I= C= D=
2.00 REACTOR
MIXER
P= B= I=
Kmol/h : 869.91 Kg /h : 37,100.63
633.50 0.71 234.84 0.84 0.03
7.00
97.31
712.91 67.24 279.07 2.08 0.06
P= B= I= C= D= Kmol/h : Kg /h :
3.00
0.26 0.90 0.41 37.72 0.16 39.46 4,651.59
6.00
7.00
10.00 P= B= I= C= D=
Fs 10 =
633.50 0.71 234.84 0.84 0.03
0.99 11.00
SPLITTER
9.00 Kmol/h : 878.70 Kg /h : 37,475.39
M MOLAR RATE, OR E SPECIFICATIONS HIS SECTION
9.00 Kmol/h : 1,015.01 Kg /h : 47,725.51 3.00
Flash C.
666.56 23.99 279.07 42.22 3.17
P= B= I= C= D=
639.89 0.72 237.21 0.84 0.03 Fr-P-9: Fr-B-9: Fr-I-9: Fr-C-9: Fr-D-9:
P= B= I= C= D= Kmol/h : Kg /h :
6.40 0.01 2.37 0.01 0.00 8.79 374.75
P= B= I= C= D= Kmol/h : Kg /h :
26.40 22.34 41.44 1.24 0.03 91.45 4,828.59
0.91 0.21 0.85 0.06 0.11
4.00
Fr-P-6: Fr-B-6: Fr-I-6: Fr-C-6: Fr-D-6:
P= 26.66 B= 23.27 I= 41.86 C= 41.37 D= 3.14 Kmol/h : 136.31 Kg /h : 10,250.12
0.09 0.11 0.77 0.99 0.07
Kmol/h : Kg /h :
44.86 5,421.52
P= B= I= C= D=
0.27 0.93 0.42 40.13 3.11
5.00
4.00 5.00
D.C. (1)
D.C. (2)
8.00
Fr-P-8: Fr-B-8: Fr-I-8: Fr-C-8: Fr-D-8:
0.02 0.86 0.87 0.09 0.04
### P = 26.40 B = 22.34 C = 1.24 D = 0.03 I = 41.44 2.26 Kg/hr Kmol/hr 5,796.28 100.00 1.00 P = 53.02 I = 2.79 B = 44.19 in p:
Please DO NOT CHANGE any number in this sheet! To chang
I = 234.84 C= 0.84 B= 0.71 P= 633.50 D= 0.0314 kmol/hr
MIXER 2,226.98 122.79 3,446.51 2,349.77
D= 0.03 C= 0.84 P = 633.50 I = 234.84 B= 0.71
1,061.36 2.00 kg/hr 47,725.51 P = 712.91 I = 279.07 B = 67.24 C= 2.08 D=
5.09 100.30 869.91 26,606.83 Frac Split "10" = 10.00 10,332.83 55.58 37,100.63 B= P= I= C= D= 3.00 1,015.01 P = 666.56 I = 279.07 B = 23.99 C = 42.22
REACTOR
0.06
D = 3.17 kg/hr
Shut Down the Process
Begin the Process
P : Propylene ( C3H6 ) I : Propane ( C3H8 ) an inert in the reactor! B : Benzene ( C6H6 ) C : Cumene (C9H12) Desired product D : diisopropylbenzene ( C12H18 ) Undesired byproduct
42.00 44.00 78.00 120.00 162.00
47,725.51
sheet! To change any number, return to the MAIN sheet.
ac Split "10" =
0.99
8.79 lm/hr 11.00
SPLITTER 0.72 kg/hr 37,475.39 56.14 639.89 9.00 26,875.59 237.21 878.70 kmol/hr 10,437.20 0.84 101.32 Fr P9= 0.03 0.96 5.14 V/L kmol/hr Se Fr B9= 0.03 8.00 par Fr C9= 0.02 ato Fr D9= 0.01 r Fr I9= 0.85 136.31 10,250.12
P= B= C= D= I= kg mole
4.00 26.66 23.27 41.37 3.14 41.86 10,250.12 136.31
P= B= C= D= I=
42.00 78.00 120.00 162.00 44.00
P = 6.40 I = 2.37 B= 0.01 C= 0.01 D= 0.00 kg/hr P = 26.40 B = 22.34 C = 1.24
D = 0.03 1,119.82 I = 41.44 1,815.12 mole: 91.45 4,964.53 Fr P8= 0.99 508.80 Fr B8= 0.96 1,841.86 Fr C8= 0.03 Fr D8= 0.01 Fr I8= 0.99
268.76 104.37 0.56 1.01 0.05 MOLES KG 374.75 TOTAL I= 2.79 122.79 TOTAL B= 0.94 73.17 1,108.62 TOTAL C= 40.14 4,816.60 1,742.51 TOTAL D= 3.11 503.76 148.94 TOTAL P= 6.67 279.95 TOTAL 53.64 5,796.28 OUT 5.09 1,823.44 4,828.59 kg
DC 1
44.86 kmol/hr 5.00 0.27 42.00 0.93 78.00 40.13 120.00 3.11 162.00 0.42 44.00 kg :
11.20 72.60 4,815.59 503.71 18.42 5,421.52
D C 2
kmol/hr 39.46
6.00
P= B= C= D= I=
Fr P6= Fr B6= Fr C6= Fr D6= Fr I6=
0.99 0.97 0.94 0.05 0.99
0.26 0.90 37.72 0.16 0.41
42.00 78.00 120.00 162.00 44.00
kmol/hr 7.00 P= B= C= D= I=
0.00 0.03 2.41 2.95 0.00
42.00 78.00 120.00 162.00 44.00
5.40
REACTOR CALCULATIONS:
kg/hr
11.09 70.43 4,526.66 25.19 18.23 4,651.59
purity of cumene: 0.97
kg/hr 0.11 2.18 288.94 478.53 0.18
Purity of D 0.62
769.94
YOU CAN CHANGE THE VALUE OF "BLACK CELLS"
r
τ=
r
0.188
/ C
/ D
=K 2C P CC
Reactor Volume: Reactor T ( C ) : P_in =C_in*RT= 371,267.260 atm! Q(m3/h) = 16.000
42.000 44.000 78.000 120.000 162.000
Kmol/hr C km/m^3C kg/m^3 P= 712.915 44.557 1,871.402 I = 279.070 17.442 767.442 B= 67.238 4.202 327.787 C= 2.077 0.130 15.577 D= 0.063 0.004 0.636 total moles/h= 1,061.363 2,982.844
P (predict) 41.660
K 1 =2.8 ×10 K 2 = 2.3 ×1
= K 1C P C B
3.000 400.000
m3
K1= K2=
Prefect Mixing Continuous Reactor
KG 47,725.505
Real P 41.660
Manually Calculate Concentration of P
C_P_Out: C_B_Out: C_C_Out:
C kg/m^3 41.660 1,749.713 1.499 116.953 2.638 316.615
C_D_Out: C_I_Out:
0.198 17.442
32.121 767.442
2,982.844
The smallest
0.200
"BLACK CELLS"
K 1 =2.8 ×107 e −12,530 T K 2 = 2.3 ×10 9 e −17,650 T
f
C ,P
f
0.231 0.009 P_out = C_out * RT =
=
C ,B
0.065
=
355,051.235 atm
C km/m^3 kmol/hr C kg/m^3 P = 41.660 666.557 1,749.713 I = 17.442 279.070 767.442 B = 1.499 23.990 116.953 C = 2.638 42.215 316.615 D = 0.198 3.172 32.121 total moles/hr = 1,015.005 2,982.844
16.000 16.000 16.000 16.000 Feed and Product Price difference ($/Day16.000
alculate Concentration of P in outlet steam
41.660 17.442 1.499 2.638 0.198
31,149.628 $/day
KG 27,995.405 12,279.064 1,871.253 5,065.844 513.939 47,725.505
666.557 279.070 23.990 42.215 3.172
13.800 14.000
To analyze the finance, please enter the smallest and the largest volumetric flow rate of reactor feed stream ( m^3/h) below: The largest Flow rate: The smallest Flow rate:
0.978
8.200 8.400 8.600 8.800 9.000 9.200 9.400 9.600 9.800 10.000 10.200 10.400 10.600 10.800 11.000 11.200 11.400 11.600 11.800 12.000 12.200 12.400 12.600 12.800 13.000 13.200 13.400 13.600
14.200
8.000 16.000 8.000 0.200
Now Calculate! and Graph!
14.400 14.600 14.800 15.000 15.200 15.400 15.600 15.800 16.000
1,169.113 1,123.125 1,077.805 1,033.150 989.157 945.823 903.146 861.120 819.742 779.004 738.902 699.429 660.579 622.345 584.719 547.694 511.263 475.418 440.152 405.456 371.322 337.743 304.710 272.216 240.252 208.811 177.883 147.463 117.540 88.108
59.159
30.684 2.676 -24.872 -51.968 -78.620 -104.836 -130.622 -155.985 -180.934
Prices and Financial Pre-a
* Your job is just to adjust the prices for materials mentioned below according to stuck prices
Material
Purity %
Price ($/kg)
Benzene
100
0.22
Propylene
95%
0.21
Cumene
97.31
0.46
Diisopropylbenzene
62.15
0.15
d Financial Pre-analysis
Feeds' costs ($/day)
Products' prices ($/day)
Propylene
2,350
Cumene
49,974
Benzene
18,198
Diisopropylbenzene
1,723
total
20,547
total
51,697
31,150
$/day
Total Feed and Product price difference : Total Feed and Product price difference :
The Goal of this project is just to apply the principles of:
Material Balance Reaction kinetics for multiple reactions in a prefect mixing continu Stream composition specifications System Performance specifications Pre-financial analysis
in a useful programming in order to simulate a process which help t Reactor Temperature Reactor Volume Amount of Feed stream Separators’ performance specifications Splitter’s performance specifications and the Purge stream Volumetric flow rates Material Prices Can affect a process unit’s efficiency .
ect mixing continuous reactor
ocess which help to figure out how the factors:
rge stream
Designed By:
Saba Moetamed Shariati Supervisor Professor: Dr. Posarac Course : CHBE 241 " Introduction to Chemical Processes" Dept. of Chemical and Biological Engineering, The University of British Columbia, Canada , Fall 2006.
26.40 22.34 41.44 1.24 0.03 91.45 4,828.59
You can change: Kmol/h : Kg /h :
P= B= I= C= D=
ANY CHANGES IN FEED STREAM MOLAR RATE, O ANY OF SYSTEM PERFORMANCE SPECIFICATION SHOULD BE APPLIED IN THIS SECTION 8
10
100.00 5,796.28 2.00 1.00 53.02 44.19 2.79
P= B= I= C= D=
Mass purity of C:
P= B= I= C= D= Kmol/h : Kg /h :
0.00 0.03 0.00 2.41 2.95 5.40 769.94
Kmol/h : 1,061.36 Kg /h : 47,725.51
P= B= I= C= D=
2.00 REACTOR
MIXER
P= B= I=
Kmol/h : 869.91 Kg /h : 37,100.63
633.50 0.71 234.84 0.84 0.03
7.00
97.31
712.91 67.24 279.07 2.08 0.06
P= B= I= C= D= Kmol/h : Kg /h :
3.00
0.26 0.90 0.41 37.72 0.16 39.46 4,651.59
6.00
7.00
10.00 P= B= I= C= D=
Fs 10 =
633.50 0.71 234.84 0.84 0.03
0.99 11.00
SPLITTER
9.00 Kmol/h : 878.70 Kg /h : 37,475.39
M MOLAR RATE, OR E SPECIFICATIONS HIS SECTION
9.00 Kmol/h : 1,015.01 Kg /h : 47,725.51 3.00
Flash C.
666.56 23.99 279.07 42.22 3.17
P= B= I= C= D=
639.89 0.72 237.21 0.84 0.03 Fr-P-9: Fr-B-9: Fr-I-9: Fr-C-9: Fr-D-9:
P= B= I= C= D= Kmol/h : Kg /h :
6.40 0.01 2.37 0.01 0.00 8.79 374.75
P= B= I= C= D= Kmol/h : Kg /h :
26.40 22.34 41.44 1.24 0.03 91.45 4,828.59
0.91 0.21 0.85 0.06 0.11
4.00
Fr-P-6: Fr-B-6: Fr-I-6: Fr-C-6: Fr-D-6:
P= 26.66 B= 23.27 I= 41.86 C= 41.37 D= 3.14 Kmol/h : 136.31 Kg /h : 10,250.12
0.09 0.11 0.77 0.99 0.07
Kmol/h : Kg /h :
44.86 5,421.52
P= B= I= C= D=
0.27 0.93 0.42 40.13 3.11
5.00
4.00 5.00
D.C. (1)
D.C. (2)
8.00
Fr-P-8: Fr-B-8: Fr-I-8: Fr-C-8: Fr-D-8:
0.02 0.86 0.87 0.09 0.04
### P = 26.40 B = 22.34 C = 1.24 D = 0.03 I = 41.44 2.26 Kg/hr Kmol/hr 5,796.28 100.00 1.00 P = 53.02 I = 2.79 B = 44.19 in p:
Please DO NOT CHANGE any number in this sheet! To chang
I = 234.84 C= 0.84 B= 0.71 P= 633.50 D= 0.0314 kmol/hr
MIXER 2,226.98 122.79 3,446.51 2,349.77
D= 0.03 C= 0.84 P = 633.50 I = 234.84 B= 0.71
1,061.36 2.00 kg/hr 47,725.51 P = 712.91 I = 279.07 B = 67.24 C= 2.08 D=
5.09 100.30 869.91 26,606.83 Frac Split "10" = 10.00 10,332.83 55.58 37,100.63 B= P= I= C= D= 3.00 1,015.01 P = 666.56 I = 279.07 B = 23.99 C = 42.22
REACTOR
0.06
D = 3.17 kg/hr
Shut Down the Process
Begin the Process
P : Propylene ( C3H6 ) I : Propane ( C3H8 ) an inert in the reactor! B : Benzene ( C6H6 ) C : Cumene (C9H12) Desired product D : diisopropylbenzene ( C12H18 ) Undesired byproduct
42.00 44.00 78.00 120.00 162.00
47,725.51
sheet! To change any number, return to the MAIN sheet.
ac Split "10" =
0.99
8.79 lm/hr 11.00
SPLITTER 0.72 kg/hr 37,475.39 56.14 639.89 9.00 26,875.59 237.21 878.70 kmol/hr 10,437.20 0.84 101.32 Fr P9= 0.03 0.96 5.14 V/L kmol/hr Se Fr B9= 0.03 8.00 par Fr C9= 0.02 ato Fr D9= 0.01 r Fr I9= 0.85 136.31 10,250.12
P= B= C= D= I= kg mole
4.00 26.66 23.27 41.37 3.14 41.86 10,250.12 136.31
P= B= C= D= I=
42.00 78.00 120.00 162.00 44.00
P = 6.40 I = 2.37 B= 0.01 C= 0.01 D= 0.00 kg/hr P = 26.40 B = 22.34 C = 1.24
D = 0.03 1,119.82 I = 41.44 1,815.12 mole: 91.45 4,964.53 Fr P8= 0.99 508.80 Fr B8= 0.96 1,841.86 Fr C8= 0.03 Fr D8= 0.01 Fr I8= 0.99
268.76 104.37 0.56 1.01 0.05 MOLES KG 374.75 TOTAL I= 2.79 122.79 TOTAL B= 0.94 73.17 1,108.62 TOTAL C= 40.14 4,816.60 1,742.51 TOTAL D= 3.11 503.76 148.94 TOTAL P= 6.67 279.95 TOTAL 53.64 5,796.28 OUT 5.09 1,823.44 4,828.59 kg
DC 1
44.86 kmol/hr 5.00 0.27 42.00 0.93 78.00 40.13 120.00 3.11 162.00 0.42 44.00 kg :
11.20 72.60 4,815.59 503.71 18.42 5,421.52
D C 2
kmol/hr 39.46
6.00
P= B= C= D= I=
Fr P6= Fr B6= Fr C6= Fr D6= Fr I6=
0.99 0.97 0.94 0.05 0.99
0.26 0.90 37.72 0.16 0.41
42.00 78.00 120.00 162.00 44.00
kmol/hr 7.00 P= B= C= D= I=
0.00 0.03 2.41 2.95 0.00
42.00 78.00 120.00 162.00 44.00
5.40
REACTOR CALCULATIONS:
kg/hr
11.09 70.43 4,526.66 25.19 18.23 4,651.59
purity of cumene: 0.97
kg/hr 0.11 2.18 288.94 478.53 0.18
Purity of D 0.62
769.94
YOU CAN CHANGE THE VALUE OF "BLACK CELLS"
r
τ=
r
0.188
/ C
/ D
=K 2C P CC
Reactor Volume: Reactor T ( C ) : P_in =C_in*RT= 371,267.260 atm! Q(m3/h) = 16.000
42.000 44.000 78.000 120.000 162.000
Kmol/hr C km/m^3C kg/m^3 P= 712.915 44.557 1,871.402 I = 279.070 17.442 767.442 B= 67.238 4.202 327.787 C= 2.077 0.130 15.577 D= 0.063 0.004 0.636 total moles/h= 1,061.363 2,982.844
P (predict) 41.660
K 1 =2.8 ×10 K 2 = 2.3 ×1
= K 1C P C B
3.000 400.000
m3
K1= K2=
Prefect Mixing Continuous Reactor
KG 47,725.505
Real P 41.660
Manually Calculate Concentration of P
C_P_Out: C_B_Out: C_C_Out:
C kg/m^3 41.660 1,749.713 1.499 116.953 2.638 316.615
C_D_Out: C_I_Out:
0.198 17.442
32.121 767.442
2,982.844
The smallest
0.200
"BLACK CELLS"
K 1 =2.8 ×107 e −12,530 T K 2 = 2.3 ×10 9 e −17,650 T
f
C ,P
f
0.231 0.009 P_out = C_out * RT =
=
C ,B
0.065
=
355,051.235 atm
C km/m^3 kmol/hr C kg/m^3 P = 41.660 666.557 1,749.713 I = 17.442 279.070 767.442 B = 1.499 23.990 116.953 C = 2.638 42.215 316.615 D = 0.198 3.172 32.121 total moles/hr = 1,015.005 2,982.844
16.000 16.000 16.000 16.000 Feed and Product Price difference ($/Day16.000
alculate Concentration of P in outlet steam
41.660 17.442 1.499 2.638 0.198
31,149.628 $/day
KG 27,995.405 12,279.064 1,871.253 5,065.844 513.939 47,725.505
666.557 279.070 23.990 42.215 3.172
13.800 14.000
To analyze the finance, please enter the smallest and the largest volumetric flow rate of reactor feed stream ( m^3/h) below: The largest Flow rate: The smallest Flow rate:
0.978
8.200 8.400 8.600 8.800 9.000 9.200 9.400 9.600 9.800 10.000 10.200 10.400 10.600 10.800 11.000 11.200 11.400 11.600 11.800 12.000 12.200 12.400 12.600 12.800 13.000 13.200 13.400 13.600
14.200
8.000 16.000 8.000 0.200
Now Calculate! and Graph!
14.400 14.600 14.800 15.000 15.200 15.400 15.600 15.800 16.000
1,169.113 1,123.125 1,077.805 1,033.150 989.157 945.823 903.146 861.120 819.742 779.004 738.902 699.429 660.579 622.345 584.719 547.694 511.263 475.418 440.152 405.456 371.322 337.743 304.710 272.216 240.252 208.811 177.883 147.463 117.540 88.108
59.159
30.684 2.676 -24.872 -51.968 -78.620 -104.836 -130.622 -155.985 -180.934
Prices and Financial Pre-a
* Your job is just to adjust the prices for materials mentioned below according to stuck prices
Material
Purity %
Price ($/kg)
Benzene
100
0.22
Propylene
95%
0.21
Cumene
97.31
0.46
Diisopropylbenzene
62.15
0.15
d Financial Pre-analysis
Feeds' costs ($/day)
Products' prices ($/day)
Propylene
2,350
Cumene
49,974
Benzene
18,198
Diisopropylbenzene
1,723
total
20,547
total
51,697
31,150
$/day
Total Feed and Product price difference : Total Feed and Product price difference :
The Goal of this project is just to apply the principles of:
Material Balance Reaction kinetics for multiple reactions in a prefect mixing continu Stream composition specifications System Performance specifications Pre-financial analysis
in a useful programming in order to simulate a process which help t Reactor Temperature Reactor Volume Amount of Feed stream Separators’ performance specifications Splitter’s performance specifications and the Purge stream Volumetric flow rates Material Prices Can affect a process unit’s efficiency .
ect mixing continuous reactor
ocess which help to figure out how the factors:
rge stream
Designed By:
Saba Moetamed Shariati Supervisor Professor: Dr. Posarac Course : CHBE 241 " Introduction to Chemical Processes" Dept. of Chemical and Biological Engineering, The University of British Columbia, Canada , Fall 2006.
Related Documents
Saba _ Excel _ Material Balance_ Project
November 2019 2
Material Balance
December 2019 16
Material Balance
May 2020 9
Excel Material
July 2020 3
Saba
May 2020 7