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3 of efficiency of separating the carbon dioxide and eth ane between the top and bottom product is not critical. 4 sion or other heat “H” is provided by sources not shown; and FIGS. IC and ID are a schematic ?ow diagram illus formation of carbon dioxide will take place. In a ?rst embodiment, thereafter, the overhead gas productismixedwith“lean”ethanol,obtainedfromthe bottom of a chimney tray of a downstream Methanol hydrocarbons, of the alternate embodiment of the pres ent invention. Designations “R” and “H” illustrate the locations where propane or freon or other suitable re frigeration “R” and low-level gas compression or other heat “H” isprovided by sources not shown. Designa tions “WR” illustrate the locations where warm pro pane or freon or other suitable refrigeration liquid is subcooled as it provides heat energy to the process fluid. from the carbon dioxide, ethane, methanol mixture in the third distillation column. The carbon dioxide is separated from the methanol in a fourth column. The methanol from this column becomes the “lean” metha 101'. exchange with product methane in stream 137, for stream 106, product ethane in stream 187, for stream 117, and product carbon dioxide in stream 185 for stream 102, The split is distributed on the basis of the 25 cryogenicenergythatcanberecoveredfromeachof these outgoing streams 137, 187, 185. The exchange of energy is accomplished in Feed Gas to Methane Gas Exchanger 118 for streams 117, 187, Feed Gas to Eth ane Gas Exchanger 107 for streams 106, 137, and Feed GastoCarbonDioxideExchanger103forstreams102, ' 185. The cooled feed gas from streams 102, 106, 117 is recombined in stream 111 and chilled to a temperature of 50° to —-30° F. with propane or freon or other suit able refrigeration (not shown in detail) in a Chiller 112. The chilledfeedstream113isreducedinpressuretoa level of 550 to 400 psia by a pressure control valve 114 and fed to a CO; Splitter 127 via valve ef?uent stream 115. The pressure is set and controlled by a Pressure Controller 116. The overhead gas from the CO2 Splitter 4,861,360 Consequently, carbon dioxide and ethane are found in both top and bottom products. The temperature and pressurerequiredforthisseparationissuchthatnosolid 5 methane and ethane and from propane-and-heavier Absorber, The carbon dioxide and ethane mixture is absorbed or dissolved into the methanol mixture during refrigeration. Absorption of the carbon dioxide and ethane is then accomplished in the Methanol Absorber. The:heavybottoms,propane-and-heavier,areseparated inasecondcolumn,Theremainder,carbondioxide, 5 ethane,andmethanolmixture,isfedtoanothercolumn, together with more lean methanol. The presence of the polar component methanol serves both to invert and to increase the relative volatility of carbon dioxide to eth ane- This allows the ethane to be distilled or stripped 20 117, The feed gas in streams 102, 106, 117 cross In an alternate embodiment, the heavy bottoms from the ?rst tower containing some carbon dioxide and ethane are separated from the propane and heavier hydrocarbons in a second tower. The overhead carbon dioxide and ethane from this tower are recombined with the overhead gas from the ?rst tower and compressed toapressureof600to650psia.The compressedmixture is subsequently cross-exchanged with the ?rst tower bottoms to provide reboiler heat and cool the com pressed mixture. The mixture is further chilled with external refrigeration and fed to a third tower. The methane, ethane, lighter components and roughly 15 to 20 percent of the carbon dioxide are separated from the remaining carbon dioxide as an overhead gas. The re maining80to85percentcarbondioxideisseparatedas4-0 127exitsinstream120andischilledtoatemperatureof a bottoms liquid product. Thereafter, the overhead gas product is mixed with “rich” methanol, obtained from the bottom of a down 0° to —30° F. by a C02 Splitter Re?ux Condenser 121 with propane or freon refrigeration (not shown in de tail). The ef?uent stream 122 from the Splitter Re?ux Condensor 121 ?ows to a Re?ux Accumulator 123. Part stream Methanol Absorber. The carbon dioxide and partoftheethaneisabsorbedordissolvedintothe45 ofthegasinstream122iscondensed,andthisliquidis methanol mixture and refrigerated. Absorption of the remaining carbon dioxide gas is accomplished in the Methanol Absorber using “lean” methanol. The ab sorbed carbon dioxide is subsequently separated from the methanol in a fourth tower. The methanol from this tower becomes the “lean” methanol. The separated carbon dioxide is compressed to a pressure of 600 to 650 psia and subsequently condensed and combined with the liquid carbon dioxide from the third tower as ?nal carbon dioxide product. BRIEF DESCRIPTION OF DRAWINGS For a further understanding of the nature and objects separated from the gas in the Re?ux Accumulator 123, the liquid leaving the Re?ux Accumulator 123 via stream 124. The liquid in stream 124 is pumped by a Re?uxPump 125totheCO2Splitter127viastream126. The uncondensed carbon dioxide ethane, and methane and-lighter gases exit the Re?ux Accumulator 123 via stream 132. The bottom stream 130 from C0; Splitter 127 is heated using heat from the refrigerant ?uid (not shown 55 indetail)inaCO;/SplitterReboiler129.Thepurposeis to recover the colder refrigerant energy from the pro cess ?uid in stream 130 which is at a temperature of 25° to 65° F. The refrigerant ?uid iscross-exchanged in the COg/Splitter Reboiler 129 with the process stream 130 of the present invention, reference is made to the fol~ lowingdrawingsinwhichlikepartsaregivenlikenu 60 fromtheCO2Splitter127.Theheatpartiallyvaporizes merals and wherein: A, FIGS. IA and IB are a schematic ?ow diagram illus trating the distillative separation of carbon dioxide, methane and ethane from each other and from propane and-heavier hydrocarbons, of the ?rst embodiment of the present invention. Designations “R” and “H” illus trate the locations where propane or freon or other suitable refrigeration “R” and low-level gas compres this?uid.The vaporisreturnedtotheCO2 Splitter127 via stream 128. The liquid, free of methane-and-lighter components and containing some carbon dioxide. eth ane and all of the propane-and-heavier hydrocarbons, exitsthe CO2/SplitterReboiler 129 instream 131 which isfedtoanNGL Tower170. Stream 132 is combined with liquid in stream 139 whichisfromachimneytray201ofaMethaneAb trating the distillative separation of carbon dioxide, FIRST MODE FOR CARRYING OUT THE INVENTION Referring to FIG. 1A, there is shown the feed gas stream 101 which issplitinto three streams 102, 106 andPDF Image | CARBON DIOXIDE ABSORPTION METHANOL PROCESS
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