feed ratio benzene to propylene 2:1

=200 mol/h

105 mol/h

305 mol/h

propylene =100mol/h

propane =5 mol/h

305 mol/h

xb=0.65

xp1=0.33

xp2=0.02

2 reaction are taking place:

material blance around the reactor:

C3H6+C6H6 C9H12

C3H6+C9H12 C12H18

2 information about the process inside the reactor:

propylene conversion in the reactor = 0.99

Cumene selectivity over the DIPB =31

X1+X2=99 mole/hr

(X1-X2)/X2=31

Using the general material balance equation effluent stream can be specified:

Reactor Effluent:

X1= 96 and X2=3

Input – output + generation – consumption=0

Benzene =104 mol/h

Propylene = 1mol/h

Propane = 5 mol/h

Cumene= 93 mol/h

DIBP= 3 mol/h

6 mol/hr

Propylene = 1mol/h

Propane = 5 mol/h

Benzene =104 mol/h

Cumene= 93 mol/h

DIBP= 3 mol/h

Top stream 98.1% benzene an the balance cumene.

Bottom stream is free of benzene.

Material Balance around T-201

benzene material balance and overall material balance around the column will help to find

(xb)F=(xb)D+(xb)B 104= (0.981)D+0

D=106.1 mol/h

F=D+B B=93.1 mol/h

Benzene =104 mol/h

Cumene = 2.1 mol/h

Cumene=90.1 mol/h

DIBP= 3 mol/h

Top stream 99.9% Cumene an the balance DIPB(0.001).

Bottom stream is free of Cumene.

material Balance around T-202

benzene material balance and overall material balance around the column will help to find

(xb)F=(xb)D+(xb)B 90.9= (0.999)D+0

D=90.99 mol/h

F=D+B B=2.91 mol/h

DIPB= 2.91 mol/h

cumene= 90.9 mol/h

DIPB= 0.09 mol/h

Cumene from T-202 =90.9 mol/h * 120= 10908 g/h = 10908*10^-6 ton/year

the plant operate 8000 h/year 87.26 ton/year

scaling up factor= 100,000/87.26 = 1146

Scale up factor:

Needed Raw Material:

Benzene = 143020.8 ton/year

Propylene = 38505.6 ton/year

Energy Balance

25 ⁰C 1 atm

350 ⁰C and 25 atm

Heating Duty

350 ⁰C and 25 atm

Exothermic Reaction

Cooling Duty

40 ⁰C and 1 atm

Cooling Duty

From

To

Flash Calculation

Cooling for Condenser

Cooling for Condenser

Heating Duty Before the Reactor

Benzene, Propylene and propane are heated from (25⁰C,1atm) to (350⁰C,25atm)

phase change

Reference point

collect vapor and liquid Cp

minor effect of (V∆P)

∆H= 4.17×10^9 Kj/ year

V∆P=12.78×10^3 Kj/year

Heat of formation method.

isothermal and isobaric operation.

Reference point for elements at 25 C

Cooling Duty to keep isothermal operation:

∆H =( H_formation +∫cp.dt〗).∆n

∆H=2.616×10^11 kj/year

Cooling Duty After the Reactor:

Benzene, Propylene, Propane, Cumene and DIPB are heated from (350⁰C,25 atm) to (40⁰C,1atm)

phase change

Reference point

collect vapor and liquid Cp

minor effect of (V∆P)

∆H= 2.49×10^13 Kj/ year

V∆P=971 Kj/year

H=∫cp.dt〗

H=∫cp.dt〗

Flash Calculation for Vapor Fraction:

benzene, cumene, propylene, propane

and DIPB at 40 ⁰C and 1 atm

V=0.0142

All distillate is benzene

column operate at 1 atm

Construct Process path to calculate ∆H

Cooling Duty for Distillate condenser

∆H= -3.9*10^10 kj/year

All distillate is Cumene

column operate at 1 atm

Construct Process path to calculate ∆H

Cooling Duty for Distillate condenser

∆H= -3.26*10^10 kj/year

**Thank you**

**Done by:**

Lahaq Al-Nashri 200640640

Lahaq Al-Nashri 200640640