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1 , a.a. <br /> - <br /> K-A <br /> A <br />_ y <br /> k: <br /> t <br /> 116 <br /> �q <br /> Some form of vapor omission <br /> emissions,and these levels are too high for direct atmospheric discharge. <br /> r control is required. Among the choices of activated carbon,thermal oxidation,and catalytic <br /> ss onlon,the <br /> cont of <br /> chnologY for <br /> nteca Bean <br /> latter is the favored 1 schematic drawinlg ofache proposed Site. <br /> ail vapor extraction a, emission control system <br /> options follows. A <br /> is shown in Figure 9. <br /> 3.3.3.11 Emission Control system Evaluation <br /> Treatment by granular activated carbon is not recommended for the Manteca site at this time. <br /> Conservatively,carbon can be loaded by 10 percent before saturation, but the exact value depends on <br /> s <br /> temperature, pressure, humidity and flow rate, Based on the expected extraction rate of 233 Ibs/day, <br /> ivated carbon was eliminate <br /> approximately 2,330 lbs of carbon will be saturated each day. Granular act <br /> as an air treatment technology for this site due to economic considerations. <br /> to warrant use of oxidation <br /> a <br /> At the Manteca site, the hydrocarbon .,,;.ding is high <br /> technologies. As Opposed to carbon systems where the hydrocarbon saturated cdrocarbvnsarbon ireb� <br /> additional treatment or disposal, oxidation treatment technologies destroy the by <br /> air to <br /> combustion. Hydrocarbon-laden vapors extracted from the subsu�U�ef? with <br /> ambient <br /> drocarbons are converted to <br /> increase the oxygen content prior to treatment. The complex petro } <br /> carbon and hydrogen oxides (such as water and carbon dioxide). and can handle a <br /> Thermal oxidation operates at higher temperatures than catalytic oxidation, <br /> higher influent concentration of hydrocarbons. The thermal oxidizer is fueled both by the process stream <br /> approximately 1400°F. At 20,000 11911,the expected <br /> and by propane or natural gas;combustion occurs at app Y <br /> process <br /> r <br /> ely <br /> hydrocarbon concentration to be treated,the heat contribution from the add tions the Iprocessxlst etam <br /> 30%, and fuel requirements would be high to maintain 1400°F. In <br /> concentration is expected to drop further as remediation proceeds,thus increasing fuel costs. For these <br /> f reasons thermal oxidation is not recommended for the Manteca site. p hydrocarbons to <br /> Similar to thermal oxidation,catalytic oxidation breaks down COMPlex etroleum hY <br /> carbon and oxygen oxides by combustion. The catalytic oxidizer operates at a lower temperature,400- <br /> and an air-to-air heat exchanger to oxidize the <br /> g00°F, by utilizing a precious metal coated catalyst <br /> contaminant stream. Because vapor phase lead can foul the cata�y er leads to reduceda lead scrubber will <br /> ienergy input <br /> if necessary. The lower operating temperature and heat excha g <br /> ence,catalytic <br /> compared to the thermal oxidizer. Hn theioins operation installation and treatmentmmended fcatalyt clt <br /> ioxidation <br /> Groundwater Technology has extensive experience n the <br /> units,and has successfully permitted them in California. The removal efficiency is comparable to thermal <br /> oxidation and carbon, and will be at least 90%. <br /> [1,.CR0l1NDW rE It <br /> TECHNOLOGY,INC, <br />