Control of Volatile Organic Compounds Emissions from Manufacturing

Tab1e 4-5. ADDITIONAL ENERGY REQUIREMENTS FOR CONTROL w ITH RACT IN POLYPROPYLENE PLANTS
Annual Steam Annual Natural Gas Annual Electricity Total Energy
Process Control Consumption Consumption Consumpti on Consumpti on
Control Scenario Sectiona Device 1,000 lb/yr S/Y~ 1,000 scf/yrD flyr kWhlyr $/yr bbl oillyrc $ / ~ r
Total Plant A1 1 Thermal
Incinerator - - 2.9 20 93,000 4,500 -140 4,500
Flare 4,560 28,200 700 4,300 - - 1,240 32,500
Process Section
Within Line PR Flare 170 1,050 700 4,300 - - 160 5,400
HR Flare 1,230 7,600 700 4,300 - - 420 11,900
PF Thermal - - 230 1,400 1,240 105 40 1,500
- Incinerator
f Process Section - Across Lines
--I
PR Fl are 510 3,130 700 4,300 - - 240 7,400
MR Flare 3,690 22,800 700 4,300 - - 1,030 27,100
PF Thermal - - 690 4,200 6,330 310 120 4,500
Incinerator
a PR = polymerization reaction; MR = material recovery; PF = product finishing.
b Standard cubic feet (scf) at 60°F.
C
Equivalent barrels of distil late oil required considering energy conversion efficiencies:
steam: 10001b = 1.525 GJ
natural gas: 106~tu = 1.0551 GJ and 1040 But(HHV)/scf at 60°F
electricity: 1 kwh = 9.476 x 10-3 GJ
oil: 1 GJ = 0.1628 bbl oil