divinylbenzene mass balance

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CHAPTER 3MASS BALANCE


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3.0 Mass balance:-

3.1 Process information:-

1. Stream (F1)Polyethybenzene (PEB) feed containing DEB (88.53 wt%), Ethylbenzene

(EB) (3.84 wt%),Benzene (3.84 wt%),Ethane (3.76wt %), is fed to flash drum.

2. Stream (F2)Ethane is completely removed from top of flash drum with some minor

other components.

3. Stream (F3)This stream is absent of inert ethane and consists of containing DEB

(92.23%), Ethylbenzene (EB) (3.974wt %),Benzene (3.84 wt%).

4. Stream (F4)Almost all of Benzene & EB is removed from top of distillation column D-1

5. Stream (F5)It only contains DEB which is fed to reactor.

6. Stream (F6)-Super heated steam at 350 C is added to reactor. Amount of steam is decided

by Steam to DEB raio (wt. basis),here it is taken 2.4.

7. Stream (F7)At conversion level of 80% of DEB,DVB product is formed along with

hydrogen,Ethyl vinylbenzene (EVB),unreacted DEB,steam,the stream is in vapour phase.

8.Stream (F8)Through the condenser all of hydrogen and water vapour is removed and

DVB present is 39.54 % which is need to be concentrated.

9. Stream (F9)-Hydrogen and water vapour of stream F7 is removed completely.

10.Stream (F10)-A major part of EVB along with some DVB is removed from top of vacuum

distillation tower D-2

11. Stream (F-11):-Its the product stream and it contains almost 55% DVB and 45% EVB

which is DVB-55,required product grade.

DVB Capacity of plant =1350 tons/year = 154.109 kg/hr


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3.2 Mass balance on individual equipment:-

PARAMETERS UNITS EMPLOYED

INDIVIDUALFLOW RATES Kg/hr

NET FLOW RATE OF STREAM

(F1,F2,F11)

Kg/hr

Flash drum:-

0.22913 DEB

0.06871 EB

0.4646 BENZENE

8.68148 ETHANE

9.44393 F2

203.294 DEB

8.81929 EB

8.81929 BENZENE

8.68148 ETHANE

229.614 F1

203.065 DEB

8.75057 EB

8.35469 BENZENE

220.17 F3


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Distillation column (D-1):-

Reactor:-

203.065 DEB

203.065 F5

8.35469 BENZENE

8.75057 EB17.1053 F4

203.065 DEB

8.75057 EB

8.35469 BENZENE

220.17 F3

203.065 DEB

203.065 F5

487.355 STEAM

487.355 F6

78.7917 DVB

80.01 EVB

3.63126 H2

487.355 STEAM

40.6129 DEB

690.401 F7


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Condenser (hydrogen separator):-

Distillation column (D-2):-

Corresponding amount of Reactant (PEB feed) required = 2006.04 tons/year

= 229.614 kg/hr

487.355 H20

3.63126 H2

0.30257 DEB

0.35819 DVB

0.43581 EVB

492.083 F9

78.7917 DVB

80.01 EVB

3.63126 H2

487.355 STEAM

40.6129 DEB

690.401 F7

78.4335 DVB

79.5741 EVB

40.3103 DEB

198.318 F8

0.76865 DVB

3.53309 EVB

39.9072 DEB

44.209 F10

78.4335 DVB

79.5741 EVB

40.3103 DEB

198.318 F8

77.6648 DVB

76.0411 EVB

0.4031 DEB

154.109 F11


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3.3 Overall material balance flowsheet:- figure 3


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divinylbenzene mass balance

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