Process for separating CO2 and H2 S from hydrocarbons

Claim 2

A process for separating components of a feed gas containing CO 2 , H 2 S and C 1 and higher hydrocarbons to form a CO 2 -rich stream, an H 2 S-rich stream and a hydrocarbon-rich stream, said process comprising: (a) passing said feed gas to a plurality of membrane separation units to form a plurality of acid gas-rich streams and a hydrocarbon-rich stream; (b) compressing at least one acid gas-rich stream and passing said stream back through at least one membrane separation unit to further remove hydrocarbons and thereby form an additional hydrocarbon-rich stream; (c) combining said hydrocarbon-rich streams to form a combined hydrocarbon-rich stream containing less than 10 mole% CO 2 ; (d) separating said combined hydrocarbon-rich stream to form a methane-rich stream and a higher hydrocarbon-rich stream; (e) combining the acid gas-rich streams to form a combined acid gas-rich stream; (f) compressing said combined acid gas-rich stream; (g) contacting said combined acid gas-rich stream with a solvent capable of absorbing H 2 S thereby forming a CO 2 product stream containing less than 100 ppm H 2 S and an H 2 S-rich solvent stream; (h) passing said H 2 S-rich solvent stream through a series of flash units to remove CO 2 from the H 2 S-rich solvent stream; (i) subsequently contacting the H 2 S-rich solvent stream with the methane-rich stream in step (d) to further remove CO 2 ; and (j) thermally treating the resultant H 2 S-rich solvent stream to form an H 2 S-rich product stream having a concentration of at least 30 mole% H 2 S and a regenerated solvent stream.

Claim 3

The process in accordance with claim 1 wherein the regenerated solvent stream is recycled to absorb H 2 S from the combined acid gas-rich stream in step (g).

Claim 4

The process in accordance with claim 2 wherein the series of flash units comprises at least one thermal flash unit and at least one pressure flash unit.

Claim 5

The process in accordance with claim 3 wherein the solvent capable of absorbing H 2 S is a physical acid gas removal solvent.

Claim 6

The process in accordance with claim 4 wherein the physical acid gas removal solvent is a mixture of polyethylene glycol dimethyl ethers.

Claim 7

The process in accordance with claim 2 wherein the solvent capable of absorbing H 2 S is a chemical acid gas removal solvent.

Claim 8

The process in accordance with claim 6 wherein the chemical acid gas removal solvent is diethanolamine.

Claim 9

The process in accordance with claim 2 wherein the CO 2 product stream contains less than 60 ppm H 2 S.

Claim 10

The process in accordance with claim 8 wherein the H 2 S product stream has an H 2 S concentration of at least 35 mole % H 2 S.

Claim 11

A process for separating components of a feed gas containing acid gases and C 1 and higher hydrocarbons to form a CO 2 -rich stream, an H 2 S-rich stream and a hydrocarbon-rich stream, said process comprising: (a) passing said feed gas to a plurality of membrane separation units to form a plurality of acid gas-rich streams and hydrocarbon-rich stream; (b) compressing at least one acid gas-rich stream and passing said stream back through at least one membrane separation unit to further remove hydrocarbons and thereby form an additional hydrocarbon-rich stream; (c) combining the hydrocarbon-rich streams, and subsequently passing said combined hydrocarbon stream, containing less than about 10 mole% CO 2 , to a natural gas processing plant to form a methane-rich stream and a higher hydrocarbon-rich stream; (d) combining the acid gas-rich streams and subsequently passing said combined stream through successive step compression to a fractionation column containing a solvent capable of selectively removing H 2 S thereby forming an H 2 S-rich solvent stream and a CO 2 product stream containing less than 100 ppm H 2 S; (e) passing said H 2 S-rich solvent stream through a series of flash units to separate CO 2 from the H 2 S-rich solvent; (f) subsequently introducing said H 2 S-rich solvent stream into an H 2 S concentrator where residual CO 2 is removed from said solvent stream by contact with the methane-rich stream produced in step (c); (g) passing the resultant H 2 S-rich solvent stream to an H 2 S stripping column to form an H 2 S-rich product stream, having a concentration of at least 30 mole% H 2 S, and a regenerated solvent stream; and (h) recycling said solvent stream back to the H 2 S absorption column.

Claim 12

A process for separating components of a feed gas containing acid gases and C 1 and higher hydrocarbons to form a CO 2 -rich stream, an H 2 S-rich stream and a hydrocarbon-rich stream, said process comprising: (a) passing said feed gas to a plurality of membrane separation units to form a plurality of acid gas-rich streams and hydrocarbon-rich stream; (b) compressing at least one acid gas-rich stream and passing said stream back through at least one membrane separation unit to further remove hydrocarbons and thereby form an additional hydrocarbon-rich stream; (c) combining the hydrocarbon-rich streams, and subsequently passing said combined hydrocarbon stream, containing less than about 10 mole% CO 2 , to a natural gas processing plant to form a methane-rich stream and a higher hydrocarbon-rich stream; (d) combining the acid gas-rich streams and subsequently passing said combined stream through successive step compression to a fractionation column containing a solvent capable of selectively removing H 2 S thereby forming an H 2 S-rich solvent stream and a CO 2 product stream containing less than 100 ppm H 2 S; (e) passing said H 2 S-rich solvent stream through a series of flash units to separate CO 2 from the H 2 S-rich solvent; (f) subsequently introducing said H 2 S-rich solvent stream into an H 2 S concentrator where residual CO 2 is removed from said solvent stream by contact with the methane-rich stream produced in step (c); (g) passing the resultant H 2 S-rich solvent stream to an H 2 S stripping column to form an H 2 S-rich product stream, having a concentration of at least 30 mole% H 2 S, and a regenerated solvent stream; and (h) recycling said solvent stream back to the H 2 S absorption column.

Claim 13

The process in accordance with claim 10 wherein the solvent capable of absorbing H 2 S is a physical acid gas removal solvent.

Claim 14

The process in accordance with claim 11 wherein the series of flash units comprises at least one thermal flash unit and at least one pressure flash unit.