Control of Volatile Organic Compounds Emissions from Manufacturing

.ble 5-4. POLYPROPYLENE MODEL PLANT PARAMETERS AND EMISSION CONTROL COSTS
process ~ectionb
Parameter Total Planta PR MR PF
Production Capacity (Gg/yr) 141
47c
VOC Concentration, wt. %
Gas Flowrate, acfm
Gas Temperature, OF
Flow Time, hr/yr
Uncontrolled Emission
Factor, kg VOC/Mg Product
Total Uncontroll ed VOC
Emissions, Mglyr
Total Existing VOC
Emissions, Mg/yre 847
Projected Control ~evicef TI, F
Assumed VOC Reduction
Efficiency, %
Control 1 ed VOC
Emissions, Mg/yr 103 12 85 7
Installed Capital Cost, $ 635,900 (TI)
90,600 (F)
Annual ized Cost, $/yr 186,700 (TI)
65,70O'(F) .
a Excludes emissions from raw material preparation.
C
27,200
21,500
25,000
21,400
(F)g
(~)h
(F)g
(~)h
64,200
31,100
53,800
30,400
(F)g
(~)h
(F)9
(~)h
414,1009
377,500h
130,8009
118,500h
b Parameters are provided on a process section across lines basis and represent initial stream
conditions from the sources.
Assumed plant has 3 process lines, each at 47 Gg/yr production capacity.
d Including stream G, dryer vent, at 0.6 kg VOC/Mg product.
e Based on assumed 90 percent control of selected streams (given in Table 4-4, footnote a).
f TI thermal incinerator; F = flare; CI = catalytic incinerator.
g~osts
for emission control across lines (i .e., at 141 Gg capacity).
h 1
Costs for emission control within a single 1 ine (i .e., at 47 Gg capacity).