Saba _ Excel _ Material Balance_ Project

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



V/LSeparato

r

SPLITTER

DC 1

DC 2

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.

Saba _ Excel _ Material Balance_ Project

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