Acid gas enrichment method and system

Patent metadata

Field	Value
Publication number	US-10875769-B2
Application number	US-201615781555-A
Country	US
Kind code	B2
Filing date	Dec 7, 2016
Priority date	Dec 9, 2015
Publication date	Dec 29, 2020
Grant date	Dec 29, 2020

Abstract

A process for treating an H2S- and CO2-comprising fluid stream, in which a) the fluid stream is treated in a first absorber at a pressure of 10 to 150 bar with a first substream of a regenerated H2S-selective absorbent to obtain a treated fluid stream and an H2S-laden absorbent; b) the H2S-laden absorbent is heated by indirect heat exchange with regenerated H2S-selective absorbent; c) the heated H2S-laden absorbent is decompressed to a pressure of 1.2 to 10 bar in a low-pressure decompression vessel to obtain a first CO2-rich offgas and a partly regenerated absorbent; d) the partly regenerated absorbent is regenerated in a desorption column to obtain an H2S-rich offgas and regenerated absorbent; e) the H2S-rich offgas is fed to a Claus unit and the offgas from the Claus unit is fed to a hydrogenation unit to obtain hydrogenated Claus tail gas; f) the hydrogenated Claus tail gas and the first CO2-rich offgas are treated in a second absorber at a pressure of 1 to 4 bar with a second substream of the regenerated H2S-selective absorbent to obtain a second CO2-rich offgas and a second H2S-laden absorbent; and g) the second H2S-laden absorbent is guided into the first absorber. Also described is a plant suitable for performance of the process. The process is notable for a low energy requirement.

First claim

The invention claimed is:

1. A process for treating an H 2 S- and CO 2 -comprising hydrocarbonaceous fluid stream, in which
a) the fluid stream is treated in a first absorber at a pressure of 10 to 150 bar with a first substream of a regenerated H 2 S-selective absorbent to obtain a treated fluid stream and H 2 S-laden absorbent;
b) the H 2 S-laden absorbent is heated by indirect heat exchange with regenerated H 2 S-selective absorbent;
c) the heated H 2 S-laden absorbent is decompressed to a pressure of 1.2 to 10 bar in a low-pressure decompression vessel to obtain a first CO 2 -rich offgas and a partly regenerated absorbent;
d) the partly regenerated absorbent is regenerated in a desorption column to obtain an H 2 S-rich offgas and regenerated absorbent;
e) the H 2 S-rich offgas is fed to a Claus unit and the offgas from the Claus unit is fed to a hydrogenation unit to obtain hydrogenated Claus tail gas;
f) the hydrogenated Claus tail gas and the first CO 2 -rich ragas are treated in a second absorber at a pressure of 1 to 4 bar with a second substream of the regenerated H 2 S-selective absorbent to obtain a second CO 2 -rich offgas and a second H 2 S-laden absorbent; and
g) the second H 2 S-laden absorbent is guided into the first absorber.

2. The process according to claim 1 , wherein the H 2 S-laden absorbent is decompressed in a high-pressure decompression vessel to a pressure of 5 to 20 bar after leaving the first absorber and before the decompression in the low-pressure decompression vessel.

3. The process according to claim 1 , wherein the partly regenerated absorbent is heated by indirect heat exchange with regenerated H 2 S-selective absorbent and a partly cooled regenerated absorbent is obtained and the partly cooled regenerated absorbent is used to heat the H 2 S-laden absorbent by indirect heat exchange.

4. The process according to claim 1 , wherein the first CO 2 -rich tags and the hydrogenated Claus tail gas are cooled individually or in combination before the treatment in the second absorber.

5. The process according to claim 1 , wherein the second H 2 S-laden absorbent is guided into the first absorber below the feed point for the first substream of the regenerated H 2 S-selective absorbent.

6. The process according to claim 1 , in which the H 2 S-selective absorbent comprises an aqueous solution of at least one amine selected from the group consisting of tertiary amines and sterically hindered amines.

7. The process according to claim 6 , in which the H 2 S-selective absorbent comprises an aqueous solution of methyldiethanolamine.

8. The process according to claim 6 , wherein the absorbent comprises an acid.

9. The process according to claim 1 , wherein there is a partial H 2 S pressure of at least 0.1 bar and a partial CO 2 pressure of at least 0.2 bar in the fluid stream.

10. The process according to claim 1 , wherein the hydrogenated Claus tail gas comprises 0.5% to 5% by volume of H 2 S.

11. A plant for conducting the process of claim 1 , comprising
a) a first absorber connected via a first heat exchanger in a fluid-conducting manner to a desorption column, in order to accept a first substream of a regenerated H 2 S-selective absorbent from the desorption column,
the first absorber being designed to promote the absorption of H 2 S and CO 2 from the fluid stream into the first substream of the regenerated H 2 S-selective absorbent at a pressure of 10 to 150 bar to obtain a treated fluid stream and an H 2 S-laden absorbent;
and the first heat exchanger being designed to heat the H 2 S-laden absorbent by indirect heat exchange with regenerated H 2 S-selective absorbent from the desorption column;

b) a low-pressure decompression vessel which is connected in a fluid-conducting manner to the first heat exchanger and is designed to decompress the heated H 2 S-laden absorbent at a pressure of 1.2 to 10 bar to obtain a first CO 2 -rich offgas and a partly regenerated absorbent;
c) a line which guides the partly regenerated absorbent into the desorption column to obtain an H 2 S-rich offgas and regenerated absorbent;
d) a Claus unit which accepts the H 2 S-rich offgas, and a hydrogenation unit which accepts the offgas from the Claus unit to obtain hydrogenated Claus tail gas;
e) a second absorber which is connected in a fluid-conducting manner to the desorption column and is designed to promote the absorption of H 2 S from the hydrogenated Claus tail gas and the first CO 2 -rich offgas into a second substream of the regenerated H 2 S-selective absorbent at a pressure of 1 to 4 bar to obtain a second CO 2 -rich offgas and a second H 2 S-laden absorbent; and
f) a line which guides the second H 2 S-laden absorbent into the first absorber.

12. The plant according to claim 11 , further comprising a high-pressure decompression vessel which is designed to decompress the H 2 S-laden absorbent from the first absorber.

13. The plant according to claim 11 , further comprising a cooler designed to cool the regenerated H 2 S-selective absorbent coming from the first heat exchanger.

14. The plant according to claim 11 , wherein the low-pressure decompression vessel is connected via a second heat exchanger in a fluid-conducting manner to the desorption column, and the second heat exchanger is designed to beat the partly regenerated absorbent by indirect heat exchange with the regenerated H 2 S-selective absorbent.

Assignees

• Basf Se

Inventors

• Ingram Thomas
• Vorberg Gerald
• Sieder Georg

Classifications

• B01D53/8612

  Hydrogen sulfide · CPC title

• B01D53/1462 Primary

  Removing mixtures of hydrogen sulfide and carbon dioxide · CPC title

• C01B17/0408 Primary

  Pretreatment of the hydrogen sulfide containing gases · CPC title

• B01D2252/20431

  Tertiary amines · CPC title

• B01D2252/60

  Additives · CPC title