Bulk CO.sub.2 recovery process
First Claim
1. A process for removing an acid gas component from a gaseous mixture containing said acid gas and hydrocarbons comprising methane, ethane and heavier hydrocarbons, said process comprising the steps of:
- (a) contacting a feed gas stream comprising said gaseous mixture with an absorbent consisting essentially of an aqueous alkanolamine solution in a contacting zone wherein said acid gas component is absorbed by said absorbent at a temperature in the range of from about 240°
F. to about 260°
F.;
(b) withdrawing a liquid stream enriched in said acid gas component from said contacting zone; and
(c) withdrawing from said contacting zone a gaseous hydrocarbon stream having a reduced concentration of said acid gas component compared to the concentration of said acid gas component in said feed gas stream.
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Accused Products
Abstract
A high temperature absorption process for bulk recovery of CO2 comprises contacting a gaseous mixture containing CO2, H2 S, and natural gas with C3 and heavier components and having a high and variable CO2 loading, with an amine absorbent solution at a temperature above 220° F. The amine absorbent solution is continuously regenerated in a multiple section flashing so as to reduce the energy requirements for regeneration and thereby making the process more suitable for bulk recovery of CO2 from gas streams associated with enhanced oil recovery projects employing CO2 for miscible flood of oil reservoirs.
58 Citations
14 Claims
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1. A process for removing an acid gas component from a gaseous mixture containing said acid gas and hydrocarbons comprising methane, ethane and heavier hydrocarbons, said process comprising the steps of:
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(a) contacting a feed gas stream comprising said gaseous mixture with an absorbent consisting essentially of an aqueous alkanolamine solution in a contacting zone wherein said acid gas component is absorbed by said absorbent at a temperature in the range of from about 240°
F. to about 260°
F.;(b) withdrawing a liquid stream enriched in said acid gas component from said contacting zone; and (c) withdrawing from said contacting zone a gaseous hydrocarbon stream having a reduced concentration of said acid gas component compared to the concentration of said acid gas component in said feed gas stream. - View Dependent Claims (2, 3, 4, 5, 6, 7, 8)
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9. A process for removing carbon dioxide from a gaseous mixture containing carbon dioxide and hydrocarbons comprising methane, ethane and which includes C3 and heavier hydrocarbons, said method comprising the steps of:
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(a) contacting a feed gas stream comprising said gaseous mixture with an absorbent consisting essentially of an aqueous methyldiethanolamine (MDEA) solution in a contacting zone and at a contacting temperature wherein said carbon dioxide is absorbed in said absorbent solution at a temperature in the range of from about 240°
F. to about 260°
F.;(b) withdrawing a liquid MDEA stream enriched in carbon dioxide from said contacting zone; (c) passing the thus withdrawn liquid MDEA stream through a first pressure reducing vessel at a temperature substantially matching the contacting temperature in said contacting zone to effect a first flashing separation of absorbed CO2 from said liquid MDEA stream; (d) withdrawing a liquid MDEA stream enriched in carbon dioxide from said first pressure reducing zone and passing the thus withdrawn liquid MDEA stream to a second pressure reducing zone; (e) effecting a second flashing separation of absorbed CO2 from said liquid MDEA stream in said second pressure reducing vessel; (f) withdrawing a liquid MDEA stream enriched in carbon dioxide from said second pressure reducing vessel and passing the thus withdrawn liquid stream to a third pressure reducing vessel; (g) effecting a third flashing separation of absorbed CO2 from said liquid MDEA stream at a temperature substantially matching the contacting temperature in said contacting zone in said third pressure reducing vessel so as to produce regenerated liquid MDEA and gaseous carbon dioxide; (i) withdrawing a regenerated liquid MDEA stream from said third pressure reducing vessel and passing the thus withdrawn regenerated liquid MDEA stream to said contacting zone to effect said contacting step in paragraph (a); and (j) withdrawing from said contacting zone a gaseous hydrocarbon stream having a reduced concentration of CO2 compared to the concentration of CO2 in said feed gas stream. - View Dependent Claims (10, 11, 12, 13, 14)
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Specification