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4,861,360 5 sorber 136 to form stream 133 which feeds to the Ab sorber Feed Chiller 134. Stream 133 is chilled in the Absorber Feed Chiller 134 to temperatures of 10° to —35° F. Part of the carbon dioxide and ethane are con densed and dissolved inthe methanol and exitsthe Ab sorber Feed Chiller 134 instream 135. Stream 135 isfed tothebottomoftheMethanolAbsorber136.The vapor and liquid are separated in the bottom of the Methanol Absorber 136. The uncondensed methane carbon diox ide and ethane gas ?ow up the absorber countercurrent to the downcoming “lean” methanol, which absorbs the carbon dioxide. ethane and not the methane. In this context, “lean” methanol means methanol that has been essentially stripped free of ethane. carbon dioxide and other hydrocarbons. The “lean” methanol feeds the top of the Methanol Absorber 136 in stream 200 at tempera tures of --35° to 10° F. The methanol rate isadjusted on the basis of absorbing the carbon dioxide and rejecting ‘the methane-and-lighter components. This is approxi matelybetweentwoandthreetoonemolalratioof20 dioxidethatmaybedisplacedtothetopoftheDeeth anizer 156 during the distillation. The mixture in stream 149 is chilled to temperatures of 0° to 30° F. in a Deeth anizer Re?ux Condenser 150 using the propane or freon refrigeration (not shown in detail). The mixture exits methanol to carbon dioxide. The Methanol Absorber 136 is operated at pressures of 400 to 500 psia. The methane-and-lighter lighter component such as nitro gen exit the top of the Methanol Absorber 136 in stream 137attemperaturesof—10°to25°F.abovethetemper 25 theDeethanizerRe?uxCondenser150and?owstoa ature of the “lean” methanol in stream 200. Stream 137 cross-exchanges with the feed gas in Exchanger 107 and exits to the pipeline in stream 138 at temperatures of 80° to 110° F. Re?ux Accumulator 152 via stream 151. The liquid is separated from the vapor in the Re?ux Accumulator 152andthen?owstoaRe?uxPump 154viastream153, and ispumped to the Deethanizer 156 via stream 155, The“rich”methanol,whichisthemethanolcontain 30 EthaneexitstheRe?uxAccumulator152asagasin ing the absorbed carbon dioxide, ethane and other heavier hydrocarbons, leaves the bottom of the Metha nol Absorber 136 in stream 140 at temperatures of 10° to -40° F. This “rich” methanol stream 140 is cross exchanged in a Lean-Rich Methanol Cross-Exchanger 35 146 with the “lean” methanol from stream 162 to heat the “rich” methanol to a temperature of 80° F which exits in stream 147 and correspondingly reduces the “lean” methanol to a temperature level of - 10° to 20° F.,recoveringthecryogenicrefrigerantenergy.The40 ?owinginstream166.Thisheatorenergyexchangeis made by a Deethanizer Bottoms/Methanol Exchanger 160. The purpose isto recover heat energy and cool the “lean” methanol. “rich” methanol in stream 145 is reduced in pressure to 300 to 375 psia by a pressure control valve 201, which is controlled by a Pressure Controller 202. The “rich” methanol stream 145 subsequently feeds a Deethanizer 156. This feed stream 145 is fed near the top of the 45 Bottoms/Methanol Exchanger 160 in stream 159 to a Deethanizer 145 on the top third or fourth tray. Stream131isfedtotheNGL Tower170toseparate ?nal or Deethanizer Trim Reboiler 158 where the Deethanizer 156 bottoms ?uid isfurther heated to tem peratures of 150° to 210° F. using steam (not shown in detail) or some other suitable heat source. The vapor generated by the Trim Reboiler is returned to the Deethanizer 156 via stream 157. The liquid carbon diox ide and methanol exit the Deethanizer Trim Reboiler 158 instream 167 where itiscooled to 120° F. or lessby the Air Cooler 168. The cooled liquids exits the Air the carbon dioxide and ethane from the propane-and heavier hydrocarbons. The overhead gas from NLG Tower170instream171isfedtoanNGL TowerRe ?ux Condenser 172 where the stream is refrigerated with propane or freon (not shown in detail), to tempera tures of 0° to 50° F. The partially condensed ?uid from theRe?uxCondenser172isfedtoanNGLRe?ux Accumulator174viastream173.Thevaporisseparated55 Cooler168viastream169.Assetoutabove,otherkinds fromtheliquidinNGL Re?uxAccumulator174.The liquid reflux ?ows from the Re?ux Accumulator 174 viastream175toanNGL Re?uxPump176andsubse quentlypumpedtotheNGL Tower170viastream177. The vapor from the Re?ux Accumulator 174 exits in stream 199 to the Deethanizer 156. This vapor acts as a stipping medium and is fed near the lower part of the Deethanizer 156. -' of media or exhanges, such as in this case a water cooled exchanger could be used without departing from the invention. The cooledliquidinstream169isfedtotheCO2/Me thanol Splitter 189. The carbon dioxide is separated from the methanol in the COg/Methanol Splitter 189. The overhead gas exits from the cOg/Methanol Splitter in stream 178 and is chilled by the freon or propane refrigerant (not shown in detail) in a Cog/Methanol TheliquidbottomsexittheNGLTowerinstream 193and?owstoanNGL TowerReboiler194.Heatis65 SplitterCondenser179toatemperatureof0°to40°F. providedtotheNGL TowerReboiler194usingsteam (not shown in detail) or some other suitable heat me dium.The liquidinstream193isheatedintheNGL The chilled stream exits the Cog/Methanol Splitter Condensor 179 via stream 180 and ?ows to the CO7] Methanol Re?ux Accumulator 181. The vapor and 6 Tower Reboiler 194 to a temperature of 200° to 250° F. wherepartoftheliquidisvaporized.The vaporreturns totheNGLTowerviastream195.Theunvaporized liquid exits in stream 196 and is subsequently cooled by the Air Cooler 197 to a temperature of 120° F. or less. The cooled liquid from the Air Cooler 197 exits the system as the propane-and-heavier product via stream 198. Those skilled in the art, will recognize that there are other suitable means of cooling stream 197, such as a water cooled heat exchanger, as well as many ways and alternate refrigerants to use for cooling and heating the other process streams. The Deethanizer 156 separates the ethane from the carbon dioxide and the methanol. The overhead from Deethanizer 156 exits in stream 148 and is combined with a split stream 144 of the recycled “lean” methanol from stream 147 to form stream 149. The purpose ofthis combination is to preferentially reabsorb any carbon stream 187 at temperatures of 0° to 35° F., to cross exchange with the incoming feed gas 117 in exchanger 118.The ethaneexitstheplantinstream188attempera tures 80° to 110° F.. The Deethanizer Tower 156 bottoms feed a Deeth anizer Tower Reboiler 158 via stream 161 at 90° to 120° F. The bottoms in stream 161 are heated to a tempera ture of 130° to 190° F. by a cross-exchange with hot “lean” methanol from a CO?Methanol Splitter 189 The Deethanizer 156 bottoms exit the DeethanizerPDF Image | CARBON DIOXIDE ABSORPTION METHANOL PROCESS
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