Control of Volatile Organic Compounds Emissions from Manufacturing

Table E-12. PROCEDURE TO CALCULATE HEAT LOAD
OF A CONDENSATION SYSTEM FOR STYRENE -- IN AIR
A-
- - .
-- -
Item Value
Heat exchanger type
Source identificati on
Source production capacity
(CAP) ,WYr
Source emission factor (E) ,
kg VOC/Mg product
Desi red emi ssi on reduction,
(%Red'n), %
Gas stream condition
Parti a1 pressure of styrene
at inlet (Pin)
Composition of gas stream
at inlet;
Styrene mass flowrate
(Ws), lb/hrd;
Gas stream vol umetri c
fl owrate (V) , acfme
Gas stream mass flowrate
(W), lb/hrf
Partial pressure of styrene
at outlet (Pout), mm Hg
Temperature required for reduction
(T1out)3 KS
Temperature required for reduction
(Tout), OF
Latent heat change of styrene (Qsty),
~tu/hrh
I
I
1
She11 and tube heat exchanger
with hot fluid in the shell
side and the cold fluid in the
tube side
Identify the polymer indusiry and
the vent from Chapters I 2 and 5
I From model plant in Chapter 2
From model plant in Chapter 2
96.1% at 3.09 kg VOC/Mg of product
40% at 0.2 kg VOC/Mg of product
I I 1 l
Assumed skturat&d styrene in
air at 80°F. latm.
0.2756 x CAP x E
I
166.:36 x W x (% Red'n)
1
I
I
1
I
I