Control of Volatile Organic Compounds Emissions from Manufacturing

Table 4-6. ADDITIONAL ENERGY REQUIRED FOR CONTROL WITHrRACT IN HIGH-DltiNSITY POLYETHYLENE PLANTS
Annual Stem Annual Natural Gas Annual Electricity Total Energy
Process Control Consua~ption Consumpti on Consumption Consuntptf on
Control Scenario Sectiona Device 1,000 lblyr flyr kbthlyr fly r bbl oillyrc fly I.
Total Plant A1 1 Thermal
Incinerator - - - - 70,520 3.50Q ' 110 3,500
Flare 3,080 19,000 700 4,300 - - 870 23,300
Process Sect ion
Within Line la Flare 1,010 6,200 700 4,300 - - 370 10,500
PF Catalytic - . - - 4,080 200 4,080 200
Incinerator
Process Section
Across Lines MR Flare 3,030 18,700 700 4,300 - - 870 23,000
a MR = material recovery; PF = product finishing.
b Standard cubic feet (scf) at 60°F.
PF Catalytic - - 210 1,310 12,040 590 52 1,900
Incinerator
C
Equivalent barrels of distil late oil required considering-energy conversion efficiencies:
steam: 10001b = 1.525 GJ
natural gas: 106~iu = 1..0551 GJ and 1040 But(HHV)/scf at 60°F
electricitv: 1 kUh = 9.476 x GJ
oi 1 : 1 GJ = 0.1628 bbl oil