saba _ excel _ material balance_ project
TRANSCRIPT
P= 26.40 P= 633.50B= 22.34 B= 0.71I = 41.44 I = 234.84C= 1.24 C= 0.84D= 0.03 D= 0.03
91.454,828.59
You can change:
100.005,796.28 1,061.36
2.00 47,725.50 2.00
1.00 P= 712.91P= 53.02 B= 67.24B= 44.19 I = 279.07I = 2.79 C= 2.08
D= 0.06
P= 0.26
Mass purity of C: 97.31 B= 0.90I = 0.41C= 37.72D= 0.16
39.464,651.59
P= 0.00 7.00B= 0.03I = 0.00C= 2.41D= 2.95
5.40769.94
Kmol/h :Kg /h :
Kmol/h :Kg /h :
8 10
Kmol/h :Kg /h : Kmol/h :
Kg /h :
Kmol/h :Kg /h :
Kmol/h :Kg /h :
MIXER REACTOR
ANY CHANGES IN FEED STREAM MOLAR RATE, OR ANY OF SYSTEM PERFORMANCE SPECIFICATIONS SHOULD BE
APPLIED IN THIS SECTION
10.00 Fs 10 = 0.99869.91 P= 633.50
37,100.63 B= 0.71 11.00I = 234.84C= 0.84D= 0.03 P=
9.00 B=I =
878.70 P= 639.89 C=B= 0.72 D=
37,475.39 I = 237.21C= 0.84
P= 666.56 D= 0.03B= 23.99 9.00 Fr-P-9: 0.91I = 279.07 Fr-B-9: 0.21C= 42.22 1,015.01 Fr-I-9: 0.85D= 3.17 47,725.50 Fr-C-9: 0.06
3.00 Fr-D-9: 0.11
3.004.00
P= 26.66 P=B= 23.27 B=
Fr-P-6: 0.09 I = 41.86 I =Fr-B-6: 0.11 C= 41.37 C=Fr-I-6: 0.77 D= 3.14 D=
Fr-C-6: 0.99 136.31Fr-D-6: 0.07 10,250.12
6.00 8.00
Fr-P-8: 0.0244.86 4.00 Fr-B-8: 0.86
7.00 5,421.52 Fr-I-8: 0.875.00 5.00 Fr-C-8: 0.09
P= 0.27 Fr-D-8: 0.04B= 0.93I = 0.42C= 40.13D= 3.11
Kmol/h :
Kg /h :Kmol/h :
Kg /h :
Kmol/h :Kg /h :
Kmol/h : Kmol/h :Kg /h : Kg /h :
Kmol/h :Kg /h :
REACTOR
D.C.(2)
D.C.(1)
FlashC.
SPLITTER
ANY CHANGES IN FEED STREAM MOLAR RATE, OR ANY OF SYSTEM PERFORMANCE SPECIFICATIONS SHOULD BE
APPLIED IN THIS SECTION
6.400.012.370.010.008.79
374.75
26.4022.3441.44
1.240.03
91.454,828.59
###Please DO NOT CHANGE any number in this sheet! To change any number, return to the MAIN sheet.
D= 0.03 5.09P = 26.40 C= 0.84 100.30B = 22.34 P = 633.50 869.91 26,606.83 Frac Split "10" =C = 1.24 I = 234.84 I = 234.84 10.00 10,332.83D = 0.03 C= 0.84 B= 0.71 55.58I = 41.44 B= 0.71 37,100.63 B=
2.26 P= 633.50 P =Kg/hr Kmol/hr D= 0.0314 I =
5,796.28 100.00 kmol/hr 1,061.36 C=1.00 2.00 D=
kg/hr 47,725.50 3.00 1,015.01P = 53.02 2,226.98 P = 712.91 P = 666.56I = 2.79 122.79 I = 279.07 I = 279.07
B = 44.19 3,446.51 B = 67.24 B = 23.99C= 2.08 C = 42.22
in p: 2,349.77 D= 0.06 D = 3.17kg/hr 47,725.50
42.0044.00
B : Benzene ( C6H6 ) 78.00120.00162.00
P : Propylene ( C3H6 ) I : Propane ( C3H8 ) an inert in the reactor!
C : Cumene (C9H12) Desired productD : diisopropylbenzene ( C12H18 ) Undesired byproduct
MIXER REACTOR
Shut Down the Process Begin the Process
Please DO NOT CHANGE any number in this sheet! To change any number, return to the MAIN sheet.
Frac Split "10" = 0.99 8.79 lm/hr11.00
0.72 kg/hr 37,475.39 56.14 P = 6.40 268.76639.89 9.00 26,875.59 I = 2.37 104.37237.21 878.70 kmol/hr 10,437.20 B= 0.01 0.560.84 101.32 C= 0.01 1.010.03 0.96 5.14 D= 0.00 0.05 MOLESkmol/hr 0.03 8.00 kg/hr 374.75 TOTAL I= 2.79
0.02 TOTAL B= 0.940.01 P = 26.40 1,108.62 TOTAL C= 40.140.85 B = 22.34 1,742.51 TOTAL D= 3.11
136.31 10,250.12 C = 1.24 148.94 TOTAL P= 6.67
4.00 D = 0.03 5.09 53.64
P = 26.66 42.00 1,119.82 I = 41.44 1,823.44B = 23.27 78.00 1,815.12 mole: 91.45 4,828.59 kgC = 41.37 120.00 4,964.53 0.99D = 3.14 162.00 508.80 0.96I = 41.86 44.00 1,841.86 0.03
kg 10,250.12 0.01mole 136.31 0.99 kmol/hr
39.46
P = 0.26B = 0.90C = 37.72D = 0.16
44.86 kmol/hr 6.00 I = 0.415.00
P = 0.27 42.00 11.20B = 0.93 78.00 72.60C = 40.13 120.00 4,815.59 0.99D = 3.11 162.00 503.71 0.97I = 0.42 44.00 18.42 0.94
kg : 5,421.52 0.050.99
kmol/hr7.00
P = 0.00B = 0.03C = 2.41D = 2.95I = 0.00
Fr P9=Fr B9=Fr C9=Fr D9=Fr I9=
TOTAL OUT
Fr P8=Fr B8=Fr C8=Fr D8=Fr I8=
Fr P6=Fr B6=Fr C6=Fr D6=Fr I6=
V/LSeparato
r
SPLITTER
DC 1
DC 2
5.40
REACTOR CALCULATIONS:
KG122.79
73.174,816.60
503.76279.95
5,796.28
kg/hr
42.00 11.0978.00 70.43 purity of cumene:
120.00 4,526.66162.00 25.19 0.97
44.00 18.234,651.59
kg/hr
42.00 0.11 Purity of D78.00 2.18
120.00 288.94 0.62162.00 478.53
44.00 0.18
769.94
= 0.188
Reactor Volume: 3.000 K1= Reactor T ( C ) : 400.000 K2=
P_in =C_in*RT= 371,267.254 atm!Q(m3/h) = 16.000
Kmol/hr C km/m^3C kg/m^342.000 P = 712.915 44.557 1,871.40244.000 I = 279.070 17.442 767.44278.000 B = 67.238 4.202 327.787
120.000 C = 2.077 0.130 15.577162.000 D = 0.063 0.004 0.636 KG
total moles/h= 1,061.363 2,982.844 47,725.504
P (predict) Real P41.660 41.660
C kg/m^3C_P_Out: 41.660 1,749.713C_B_Out: 1.499 116.953C_C_Out: 2.638 316.615
C_D_Out: 0.198 32.121C_I_Out: 17.442 767.442
2,982.844
The smallest Flow rate:
Prefect Mixing Continuous Reactor
r C¿
=K 1C PC B
r D¿
=K 2C PC C
K1=2 .8×107 e−12 ,530 /T
K2=2 .3×109 e−17 ,650 /T
m3τ
Manually Calculate Concentration of P in outlet steam
YOU CAN CHANGE THE VALUE OF "BLACK CELLS"
0.200 8.2008.4008.6008.800
0.065 9.0009.2009.400
0.978 9.6000.231 9.8000.009 10.000
P_out = C_out * RT = 355,051.230 atm 10.20010.40010.600
C km/m^3 kmol/hr C kg/m^3 KG 10.800P = 41.660 666.557 1,749.713 27,995.404 11.000I = 17.442 279.070 767.442 12,279.064 11.200B = 1.499 23.990 116.953 1,871.253 11.400C = 2.638 42.215 316.615 5,065.844 11.600D = 0.198 3.172 32.121 513.939 11.800
total moles/hr = 1,015.005 2,982.844 47,725.505 12.00012.20012.400
16.000 41.660 666.557 12.60016.000 17.442 279.070 12.80016.000 1.499 23.990 13.00016.000 2.638 42.215 13.20016.000 0.198 3.172 13.400
13.600
31,149.628 $/day 13.80014.000
14.200
14.400
stream ( m^3/h) below: 14.60014.800
The largest Flow rate: 8.000 15.000
The smallest Flow rate: 16.000 15.20015.400
8.000 15.6000.200 15.800
16.000
Feed and Product Price difference ($/Day
To analyze the finance, please enter the smallest
and the largest volumetric flow rate of reactor feed
K1=2 .8×107 e−12 ,530 /T
K2=2 .3×109 e−17 ,650 /T
Manually Calculate Concentration of P in outlet steam
f C, P=
f C, B=
Now Calculate! and Graph!
YOU CAN CHANGE THE VALUE OF "BLACK CELLS"
1,169.1131,123.1251,077.8051,033.150
989.157945.823903.146861.120819.742779.004738.902699.429660.579622.345584.719547.694511.263475.418440.152405.456371.322337.743304.710272.216240.252208.811177.883147.463
117.54088.108
59.159
30.684
2.676-24.872
-51.968
-78.620-104.836-130.622-155.985-180.934
Prices and Financial Pre-analysis
Material Purity % Price ($/kg)
Benzene 100 0.22
Propylene 95% 0.209
Cumene 97.31 0.46
Diisopropylbenzene 62.15 0.15
* Your job is just to adjust the prices for materials mentioned below according to stuck
prices
Prices and Financial Pre-analysis
Propylene 2,350 Cumene 49,974
Benzene 18,198 Diisopropylbenzene 1,723
total 20,547 total 51,697
31,150 $/day
Feeds' costs ($/day)
Products' prices ($/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 BalanceReaction kinetics for multiple reactions in a prefect mixing continuous reactorStream composition specificationsSystem Performance specificationsPre-financial analysis
in a useful programming in order to simulate a process which help to figure out how the factors:
Reactor TemperatureReactor VolumeAmount of Feed streamSeparators’ performance specificationsSplitter’s performance specifications and the Purge streamVolumetric flow ratesMaterial Prices
Can affect a process unit’s efficiency .
The Goal of this project is just to apply the principles of:
Reaction kinetics for multiple reactions in a prefect mixing continuous reactor
in a useful programming in order to simulate a process which help to figure out how the factors:
Splitter’s performance specifications and the Purge 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.