Methods for producing synthesis gas for ammonia production

Patent metadata

Field	Value
Publication number	US-9475696-B2
Application number	US-201414187663-A
Country	US
Kind code	B2
Filing date	Feb 24, 2014
Priority date	Feb 24, 2014
Publication date	Oct 25, 2016
Grant date	Oct 25, 2016

Abstract

A method for producing synthesis gas and ammonia by forming a synthesis gas mixture; separating solids from the synthesis gas mixture; subjecting the synthesis gas mixture to a shift reaction and separating the reaction products by a pressure swing adsorption unit. The hydrogen and nitrogen separated in the pressure swing adsorption unit are fed to an ammonia reactor to produce ammonia.

First claim

Having thus described the invention, what we claim is:

1. A method for producing synthesis gas for the production of ammonia comprising the steps:
a) Feeding a hydrocarbon and steam to a reformer;
b) Feeding the reaction products of the reformer to a separation unit whereby solids are separated from gases;
c) Feeding the solids to a regenerator and the gases to a shift reactor;
d) Recycling a flue gas stream comprising carbon dioxide, steam, nitrogen, and CaO from the regenerator through a cyclone to the reformer;
e) Feeding the products of the shift reactor to a pressure swing adsorption unit;
f) Feeding hydrogen and nitrogen separated from the gases in step e) to an ammonia reactor; and
g) Recovering ammonia from the ammonia reactor.

2. The method as claimed in claim 1 wherein the hydrocarbon is selected from the group consisting of methane, conventional and unconventional gases, Naphtha and liquid hydrocarbons.

3. The method as claimed in claim 1 wherein the reformer is a fluidized bed reactor.

4. The method as claimed in claim 3 wherein the fluidized bed reactor contains a solid nickel based catalyst and a calcium oxide powder.

5. The method as claimed in claim 1 wherein in step c) the solids are calcium carbonate and calcium oxide and the gases are a synthesis gas mixture.

6. The method as claimed in claim 1 wherein the shift reactor is selected from the group consisting of low temperature and high temperature shift.

7. The method as claimed in claim 1 wherein the regenerator produces CaO from calcium carbonate.

8. The method as claimed in claim 5 wherein the synthesis gas mixture comprises nitrogen, hydrogen, methane and carbon monoxide.

9. The method as claimed in claim 8 wherein the synthesis gas mixture is fed through a solid gas filter and a heat exchanger prior to being fed to the pressure swing adsorption unit.

10. The method as claimed in claim 9 wherein the pressure swing adsorption unit separates the synthesis gas mixture into a stream comprising carbon dioxide and methane and a stream comprising hydrogen and nitrogen.

11. The method as claimed in claim 10 wherein the stream comprising carbon dioxide and methane is fed to the regenerator and the stream comprising hydrogen and nitrogen is fed to the ammonia reactor.

12. The method as claimed in claim 11 wherein the stream comprising nitrogen and hydrogen is in a ratio of 3 to 4.

13. The method as claimed in claim 1 wherein ammonia is recovered as both liquid ammonia and gaseous ammonia.

14. A method for producing ammonia comprising the steps:
a) Feeding a hydrocarbon and steam to a reformer;
b) Feeding the reaction products of the reformer to a separation unit whereby solids are separated from gases;
c) Feeding the solids to a regenerator and the gases to a shift reactor;
d) Recycling a flue gas stream comprising carbon dioxide, steam, nitrogen, and CaO from the regenerator through a cyclone to the reformer;
e) Feeding the products of the shift reactor to a pressure swing adsorption unit.

15. The method as claimed in claim 14 wherein the hydrocarbon is selected from the group consisting of methane, conventional and unconventional gases, naphtha and liquid hydrocarbons.

16. The method as claimed in claim 14 wherein the reformer is a fluidized bed reactor.

17. The method as claimed in claim 16 wherein the fluidized bed reactor contains a solid nickel based catalyst and a calcium oxide powder.

18. The method as claimed in claim 14 wherein in step c) the solids are calcium carbonate and calcium oxide and the gases are a synthesis gas mixture.

19. The method as claimed in claim 14 wherein the shift reactor is selected from the group consisting of low temperature and high temperature shift.

20. The method as claimed in claim 14 wherein the regenerator produces CaO from calcium carbonate.

21. The method as claimed in claim 18 wherein the synthesis gas mixture comprises nitrogen, hydrogen, methane and carbon monoxide.

22. The method as claimed in claim 21 wherein the synthesis gas mixture is fed through a solid gas filter and a heat exchanger prior to being fed to the pressure swing adsorption unit.

23. The method as claimed in claim 22 wherein the pressure swing adsorption unit separates the synthesis gas mixture into a stream comprising carbon dioxide and methane and a stream comprising hydrogen and nitrogen.

24. The method as claimed in claim 23 wherein the stream comprising carbon dioxide and methane is fed to the regenerator and the stream comprising hydrogen and nitrogen is fed to the ammonia reactor.

25. The method as claimed in claim 24 wherein the stream comprising nitrogen and hydrogen is in a ratio of 3 to 4.

26. The method as claimed in claim 14 wherein ammonia is recovered as both liquid ammonia and gaseous ammonia.

Assignees

• Mabrouk Rachid
• Krishnamurthy Ramachandran
• Linde Ag

Inventors

• Mabrouk Rachid
• Krishnamurthy Ramachandran

Classifications

• C01B3/42

  using moving solid particles, e.g. fluidised bed technique · CPC title

• C01B2203/068

  Ammonia synthesis · CPC title

• C01B2203/0233

  the reforming step being a steam reforming step · CPC title

• C01C1/0405

  from N2 and H2 in presence of a catalyst · CPC title

• C01B2203/1241

  Natural gas or methane · CPC title