Acid gas scrubbing methods featuring amine phase separation for hydrogen sulfide capture
Capture of hydrogen sulfide from a gas mixture may be accomplished using an aqueous solution comprising an amine. Certain sterically hindered amines may selectively form a reaction product with hydrogen sulfide under kinetically controlled contacting conditions and afford a light phase and a heavy phase above a critical solution temperature, wherein the hydrogen sulfide may be present in either phase. Upon separation of the light phase from the heavy phase, processing of one of the phases may take place to remove hydrogen sulfide therefrom. Recycling of the amine to an absorber tower may then take place to promote capture of additional hydrogen sulfide.
1. A method comprising:
contacting a gas mixture comprising hydrogen sulfide with an aqueous solution comprising an amine in an absorber tower under kinetically controlled contacting conditions; wherein the amine has a higher binding selectivity for hydrogen sulfide than for carbon dioxide under the kinetically controlled contacting conditions, wherein binding selectivity for hydrogen sulfide over carbon dioxide is specified by the ratio
(
[
H
2
S
]
/
[
CO
2
]
)
aqueous
solution
(
[
H
2
S
]
/
[
CO
2
]
)
gas
mixture
wherein ([H 2 S]/[CO 2 ]) aqueous solution is a molar ratio of hydrogen sulfide to carbon dioxide in the aqueous solution and ([H 2 S]/[CO 2 ]) gas mixture is a molar ratio of hydrogen sulfide to carbon dioxide in the gas mixture, wherein the ratio is greater than or equal to 8; and wherein the aqueous solution undergoes liquid phase separation above a critical solution temperature;
forming a reaction product of the hydrogen sulfide and the amine in the aqueous solution;
heating the aqueous solution to a temperature greater than or equal to the critical solution temperature, thereby forming a light phase comprising the amine and a heavy phase comprising water; wherein a majority of the reaction product of the hydrogen sulfide and the amine is present in either the light phase or the heavy phase;
separating the light phase from the heavy phase;
processing one of the light phase or the heavy phase to remove at least some hydrogen sulfide therefrom; and
after separating the light phase from the heavy phase, recycling at least a portion of the light phase to the absorber tower.
2. The method of claim 1 , wherein the amine comprises a sterically hindered secondary amine comprising at least one tertiary alkyl group bound to a nitrogen atom of the amine, a tertiary amine, or any combination thereof.
3. The method of claim 1 , wherein the amine has a critical solution temperature of about 140° C. or below and comprises at least one secondary or tertiary amine represented by a structure selected from the group consisting of
4. The method of claim 1 , wherein the gas mixture further comprises carbon dioxide, and a reaction product of the carbon dioxide and the amine is formed in the aqueous solution;
wherein the reaction product of the carbon dioxide and the amine is present in either the same phase or a different phase than the reaction product of the hydrogen sulfide and the amine.
5. The method of claim 1 , wherein separating the light phase from the heavy phase takes place by density liquid separation.
6. The method of claim 1 , wherein the aqueous solution has an amine concentration ranging from about 15 wt % amine to about 70 wt % amine.
7. The method of claim 1 , wherein the heavy phase is processed in a regeneration tower to remove at least some hydrogen sulfide therefrom.
8. The method of claim 7 , further comprising:
returning at least a portion of the heavy phase to the absorber tower after removing at least some hydrogen sulfide therefrom.
9. The method of claim 1 , wherein the gas mixture further comprises carbon dioxide, a reaction product of the carbon dioxide and the amine is formed in the aqueous solution, and a majority of the reaction product of the carbon dioxide and the amine is present in the heavy phase.
10. The method of claim 9 , further comprising:
processing the heavy phase to remove at least some carbon dioxide therefrom.
11. The method of claim 10 , further comprising:
returning at least a portion of the heavy phase to the absorber tower after removing at least some carbon dioxide therefrom.
12. The method of claim 11 , wherein the light phase and the heavy phase are returned to the absorber tower together in a combined stream.
13. The method of claim 11 , wherein the light phase and the heavy phase are returned to the absorber tower in separate streams.
14. The method of claim 1 , wherein the gas mixture and the aqueous solution are contacted under countercurrent conditions in the absorber tower.
15. The method of claim 1 , wherein the kinetically controlled contacting conditions comprise a residence time of about 2 minutes or less in the absorber tower.
16. The method of claim 1 , wherein the kinetically controlled contacting conditions comprise a temperature of about 30° C. to about 80° C.
17. The method of claim 1 , wherein processing one of the light phase or the heavy phase takes place in a regeneration tower at a temperature of about 110° C. to about 150° C.
18. The method of claim 1 , wherein the critical solution temperature is about 50° C. or greater.
19. The method of claim 1 , wherein the aqueous solution further comprises triethylene glycol monomethyl ether (MTEG), sulfolane, phosphoric acid, sulfuric acid, or any combination thereof.