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7 liquid are separated in COz/Methanol Re?ux Accumu lator 181. The carbon dioxide vapor or gas exits the accumulator via stream 185 to flow to Feed Gas to Carbon Dioxide Exchanger 103. The carbon dioxide in stream 185 is heated to 80° to 100° F. by a cross exchange of energy with the feed gas 102. The heated carbon dioxide exits the plant in stream 186. The liquid re?ux flows from the Reflux Accumulator 181 to a Cog/Methanol Re?ux Pump 183 via stream 182 and is pumped to the COg/Methanol Splitter 189 via stream 184. 8 This partially condenses some of the carbon dioxide and ethane both of which are absorbed or dissolved into the “lean” methanol. The refrigeration removes the heat of solution or absorption and effectively reduces the “lean” methanol rate. The mixture is fed to the bottom of the Methanol Absorber 136 where the gas and liquid separate. The gas flows upward, countercurrent to the downcoming “lean” methanol fed at the top of the Methanol Absorber 136. This “lean” methanol has been chilled to a temperature of 0° to —40° F. The “lean” methanol rate is based on a molal ratio of carbon diox ide to methanol of between two and three to one. The carbon dioxide and ethane both are more soluble in methanol than methane or the lighter components. Con sequently, these components are dissolved or absorbed in the “lean” methanol. The separated liquid leaves the bottom of the Methanol Absorber 136 as a liquid at temperatures of 10° to 20° degrees above the inlet 4,861,360 The CO7/Methanol Splitter 189 bottoms stream 192 isheatedfrom300°to350°F.toatemperatureof320° to 380° F. by a COZ/Methanol Splitter'Reboiler 191. Steam or some other suitable means of heat is required for the Cop/Methanol Splitter Reboiler 191. Part of the ?uid is vaporized and returned to the CO9/Methanol Splitter 189 via stream 190. The hot “lean” methanol liquidexitstheCog/MethanolSplitterReboiler191in “lean”methanol.HydrogenSul?deisalsoverysoluble stream166.Thishot“lean”methanolinstream166is20 inmethanolandifanyispresent,itwillbedissolvedin cross-exchangedintheDeethanizerBottoms/Methanol Exchanger 160 to cool the “lean” methanol and reduce the heat energy load. The cooled “lean” methanol exits the Deethanizer Bottoms/Methanol Exchanger 160 via stream165totheLeanMethanolPump203,wherethe25 NGL Tower170.Theethaneandcarbondioxideare pressure is elevated to a level of 500 to 650 psia in stream 164. The “lean” methanol is further cooled to 120° F. by the Air Cooler 163 and subsequently cross exchanged with the “rich” methanol to recover the refrigeratedenergyintheLean-RichMethanolEx 30of300to500psia.ThebottomfromtheNGLTower changer 146. The cooled “lean” methanol exits the Lean-Rich Methanol Exchanger 146 via stream 147. The “lean” methanol in stream 147 is split into two streams. One stream 142 is further refrigerated to a temperature level of 0° to -35° F. by a Methanol Chiller 141 using an external refrigeration source such as freon or propane (not shown in detail). The chilled “lean” methanol flows from the Mmethanol Chiller 141 via stream 200 to thetopoftheMethanolAbsorber136.Theotherstream40 discussedabove,thepresenceofthemethanol,apolar 144 from stream 147 iscombined with the overhead gas instream 148 and ?ows to the Deethanizer Re?ux Con denser 152. This completes the recycle of the methanol molecular. serves to invert the relative volatility ratio of carbon dioxide and ethane causing the ethane to be come thelightercomponent. On thisbasis,theethaneis system. ' Inoperation,themethane,lightercomponents,to 45 distilledorstrippedfromthecarbondioxideandmetha gether with most of the carbon dioxide and some eth ane,areseparatedfromthepropane-and-heavierhydro carbons in CO2 Splitter 127. Approximately ?fteen to nol as the top product. This presence of the methanol also serves to increase the relative volatility ratio of ethane to carbon dioxide, making the separation of eth ane from the carbon dioxide methanol mixture much twenty percent of the incoming carbon dioxide and twentyfivetothirty?vepercentoftheincomingeth 50 lessdifficult.Thisethanemayberecombinedwiththe ane isdistributed to the bottoms product. The efficiency of the separation with respect to carbon dioxide and ethane distribution between the top and bottom prod uctsisnotcritical.An effectiveseparationofthepro pane-and-heavierhydrocarbonsfromthemethane-and 55 lightercomponentsisimportant.Theheavierhydrocar bons are difficult to separate from methanol. In fact, the pentane-and-heavier hydrocarbons would form an aze otrope with methanol, Fortunately this separation is veryeasytoachieve.Duetothismethodofseparation,60 the operating temperatures and pressure of —40° to 0° F. and 400 to 550 psia in the CO2 Splitter 127 are such that solidi?cation of carbon dioxide will not occur. methane product or maintained separately. The Deeth anizer 156 is operated at pressures of 300 to 500 psia with top temperatures of 10° to 35° F. and correspond ing bottom temperatures 100° to 200° F. The bottoms from the Deethanizer 156, carbon diox ide and methanol, are fed to the COg/Methanol Splitter 189, The carbon dioxide is distilled as the overhead product and may be recovered as a liquid or vapor. If hydrogen sul?de is present, it will become a art of the carbondioxideproduct.Themethanolbottomsproduct stripped of carbon dioxide and other hydrocarbons becomes the “lean” methanol. Itiscooled to 120° F. and recycled to the system. The Cog/Methanol Splitter is operatedatpressuresof300to400psiawithtoptemper The overhead gas product from this distillation con tainingmethane,lightercomponents,carbondioxide,65 aturesof—~l5°to25°F.andcorrespondingbottoms and ethane is mixed with liquid withdrawn at the bot tom chimney tray of Methanol Absorber 136. The mix ture is refrigerated to a temperature of —40" to 0“ F. temperatures 300° to 400° F. Typical operating conditions, product distributions and flow rates are illustrated in Table I. themethanol.The “rich”methanoliscross-exchanged with the “lean” methanol to recover the cryogenic energy and warm the “rich” methanol. The bottoms from the CO2 Splitter 127 is fed to the distilledintheNGL Tower170asatopgasproduct'at temperatureof0°to30°F.Ifhydrogensul?deispresent it will become a part of the ethane and carbon dioxide product.TheNGL Tower170isoperatedatpressures 170 is cooled to 120° F. to exit the system as a propane and-heavierhydrocarbonproductliquid. The warmed bottoms “rich” methanol from the Methanol Absorber 136 are fed on the top third or fourth tray of the Deethanizer 156. The overhead gas productfromtheNGL Tower170isfedatthebottom oftheDeethanizer156.A smallamount,approximately ten to twenty percent of the total “lean” methanol, is fed at the top of the Deethanizer 156 in stream 144. AsPDF Image | CARBON DIOXIDE ABSORPTION METHANOL PROCESS
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