Production of pure hydrogen from ammonia rich sour water stripper overhead

Patent metadata

Field	Value
Publication number	US-10112829-B2
Application number	US-201615000389-A
Country	US
Kind code	B2
Filing date	Jan 19, 2016
Priority date	Jan 19, 2016
Publication date	Oct 30, 2018
Grant date	Oct 30, 2018

Abstract

A method of producing hydrogen comprising receiving a sour gas comprising CO2, H2S, and ammonia from a sour water stripper; introducing the sour gas to an absorption system to produce an ammonia rich gas and a sulfide rich gas, wherein the ammonia rich gas comprises ammonia and CO2, and wherein the sulfide rich gas comprises H2S and CO2; compressing the ammonia rich gas in a compressing unit to a pressure of 400-600 psig to produce a compressed ammonia rich gas; introducing the compressed ammonia rich gas to an ammonia cracker unit comprising a catalyst to produce a cracked gas, wherein the ammonia cracker unit is characterized by a cracking temperature of 450-550° C., and wherein the cracked gas comprises hydrogen, nitrogen, and CO2; and introducing the cracked gas to a PSA unit to produce hydrogen and a PSA tail gas, wherein the PSA tail gas comprises nitrogen and CO2.

First claim

What is claimed is:

1. A method of producing hydrogen comprising:
(a) receiving a sour gas from a sour water stripper, wherein the sour gas comprises carbon dioxide, hydrogen sulfide, and ammonia;
(b) introducing the sour gas to a solvent based, absorption system to produce an ammonia rich gas and a sulfide rich gas, wherein the ammonia rich gas comprises ammonia and carbon dioxide, and wherein the sulfide rich gas comprises hydrogen sulfide and carbon dioxide;
(c) compressing at least a portion of the ammonia rich gas in a compressing unit to a pressure of from about 400 psig to about 600 psig to produce a compressed ammonia rich gas;
(d) introducing at least a portion of the compressed ammonia rich gas to an ammonia cracker unit to produce a cracked gas, wherein the ammonia cracker unit comprises a catalyst, wherein the ammonia cracker unit is characterized by a cracking temperature of from about 450° C. to about 550° C., wherein the cracked gas comprises hydrogen, nitrogen, and carbon dioxide, wherein the ammonia rich gas is heated in the compressing unit, and wherein the cracked gas exchanges heat with the compressing unit to produce a cooled cracked gas; and
(e) introducing a gas stream consisting of the cooled cracked gas to a pressure swing adsorption (PSA) unit to produce hydrogen and a PSA tail gas, wherein the PSA tail gas comprises nitrogen and carbon dioxide.

2. The method of claim 1 , wherein the sour gas is characterized by a pressure of from about 5 psig to about 50 psig.

3. The method of claim 1 , wherein the sour gas is generated by a sour gas source, wherein the sour gas source comprises a sour water stripper, an acid gas removal unit, a low-temperature gasification unit, a hydroprocessing unit that is configured to receive a feedstock containing equal to or greater than about 2,000 ppm nitrogen, or combinations thereof.

4. The method of claim 1 , wherein the sour gas comprises ammonia in an amount of equal to or greater than about 10 mol %.

5. The method of claim 1 , wherein the ammonia rich gas comprises sulfur in an amount of less than about 50 ppmv.

6. The method of claim 1 , wherein the absorption system comprises an absorption unit and a solvent regeneration unit, wherein the absorption unit comprises an absorber solvent, wherein the sour gas is introduced to the absorption unit to produce the ammonia rich gas and a sulfide rich solvent, wherein the sulfide rich solvent comprises at least a portion of the hydrogen sulfide of the sour gas and a portion of the carbon dioxide of the sour gas, and wherein the ammonia rich gas comprises at least a portion of the ammonia of the sour gas and another portion of the carbon dioxide of the sour gas.

7. The method of claim 6 , wherein the absorber solvent comprises diglycolamine; a basic amine, methylethylamine, piperazine, 2-methylpiperazine; blends of methyl diethanolamine with a basic amine; or combinations thereof.

8. The method of claim 6 , wherein at least a portion of the sulfide rich solvent is introduced to the solvent regeneration unit to produce the sulfide rich gas and the absorber solvent.

9. The method of claim 8 , wherein a portion of the absorber solvent produced in the solvent regeneration unit is recycled to the absorption unit.

10. The method of claim 8 , wherein a portion of the absorber solvent produced in the solvent regeneration unit is sent to a reboiler to produce absorber solvent vapors, and wherein at least a portion of the absorber solvent vapors is recycled to the solvent regeneration unit.

11. The method of claim 1 , wherein the ammonia rich gas contains equal to or greater than about 50 mol % of the ammonia of the sour gas, and wherein the sulfide rich gas contains less than about 50 mol % of the ammonia of the sour gas.

12. The method of claim 1 , wherein at least a portion of the sulfide rich gas is introduced to a sulfur recovery unit to produce sulfur.

13. The method of claim 1 , wherein at least a portion of the ammonia rich gas is further introduced to a sulfur removal unit to produce a purified ammonia rich gas, wherein the purified ammonia rich gas comprises sulfur in an amount of less from about 10 ppmv to about 50 ppmv.

14. The method of claim 13 , wherein at least a portion of the purified ammonia rich gas is compressed to a pressure of from about 400 psig to about 600 psig to produce the compressed ammonia rich gas.

15. The method of claim 1 , wherein the cracked gas has a temperature of from about 450° C. to about 550° C., and wherein the cooled cracked gas has a temperature of from about 150° C. to about 200° C.

16. The method of claim 1 , wherein at least a portion of the cooled cracked gas is introduced to the PSA unit to produce the hydrogen and the PSA tail gas.

17. The method of claim 1 , wherein the compressed ammonia rich gas has a temperature of from about 250° C. to about 500° C.

18. The method of claim 1 , wherein at least a portion of the PSA tail gas is contacted with a fuel used for heating the ammonia cracker unit.

19. The method of claim 1 , wherein the PSA tail gas is characterized by a pressure of from about 5 psig to about 50 psig.

20. The method of claim 1 , wherein the hydrogen is characterized by a pressure of from about 375 psig to about 575 psig.

21. The method of claim 1 , wherein the hydrogen is characterized by a purity of equal to or greater than about 99%.

22. The method of claim 1 , wherein a molar ratio of ammonia to hydrogen sulfide in the sour gas is equal to or greater than about 1:1.

23. The method of claim 1 , wherein the sour gas is produced in the sour water stripper.

24. The method of claim 1 , wherein the catalyst is a nickel-based catalyst.

Assignees

• Fluor Tech Corp

Inventors

• Ravikumar Ravi
• Mathias Paul M

Classifications

• C01B17/04 Primary

  from gaseous sulfur compounds including gaseous sulfides · CPC title

• C01B3/04 Primary

  by decomposition of inorganic compounds (reversible storage of hydrogen C01B3/0018) · CPC title

• C01B3/047 Primary

  Decomposition of ammonia · CPC title

• C01B2203/0465

  Composition of the impurity · CPC title

• C01B17/0408

  Pretreatment of the hydrogen sulfide containing gases · CPC title