Low pressure ammonia synthesis utilizing adsorptive enhancement

• US 20060039847A1
• Filed: 08/23/2004
• Published: 02/23/2006
• Est. Priority Date: 08/23/2004
• Status: Abandoned Application

• Current Assignee: Eaton Corp. (Wisconsin) (Eaton Corporation PLC.)
• Original Assignee: Eaton Corp. (Wisconsin) (Eaton Corporation PLC.)
• Inventors: Kuznicki, Steven M., Kaboord, Wayne Scott, Begale, Fred Joseph, Becher, Dawn Marie, Fellers, Daniel Woodrow
• Application Number:
  US10/924,050
• Publication Number:
  US 20060039847A1
• Time in Patent Office: Days
• US Class Current: 423/359
• CPC Class Codes: B01D 15/00 Separating processes involving the treatment of liquids with solid sorbents using liquid sorbents B01D11/00; ion exchange processes or materials, sorbent materials in general B01J, e.g. sorbents for chromatography B01J20/281; for investigating or analysing materials G01N30/00; Apparatus therefor
• CPC Class Codes: B01J 20/186 Chemical treatments in view of modifying the properties of the sieve, e.g. increasing the stability or the activity, also decreasing the activity
• CPC Class Codes: C01C 1/04 Preparation of ammonia by synthesis in the gas phasepreparation or purification of gas mixtures for ammonia synthesis C01B3/025
• CPC Class Codes: C01C 1/0458 Separation of NH3 during purge gas treatment C01C1/0476
• CPC Class Codes: Y02P 20/52 using catalysts, e.g. selective catalysts

Abstract

One aspect of the invention relates to a process for synthesizing ammonia from hydrogen and nitrogen in which an adsorbant is provided to adsorb ammonia as it is being produced. Adsorption of the product drives the ammonia synthesis reaction and allows the process to be carried out at pressures where the gas phase equilibrium conversion is too low for a conventional system to be practical. The invention is applicable to both small and large scale ammonia synthesis. A small scale ammonia synthesis plant can be a stationary or vehicle-mounted plant used to supply reducing agent for selective catalytic reduction of NOx in diesel exhaust. Ammonia can be desorbed from the adsorbant, extracted from the adsorbant, or stored and transported in its adsorbed state.

Claims

1. A process for synthesizing ammonia, comprising:

providing a vessel containing an adsorbant that adsorbs ammonia in preference to H₂ and N₂; and

bringing H₂ and N₂ together in the vessel under conditions where the H₂ and the N₂ react at a rate sufficient to bring about significant conversion to ammonia within the vessel;

wherein ammonia is adsorbed by the adsorbant simultaneously with the reaction and the adsorbant captures ammonia and thereby enhances the net conversion of H₂ and N₂ to ammonia.

2. The process of claim 1, wherein the single pass conversion rate for H₂ and N₂ through the vessel is at least about 50%.

3. The process of claim 1, wherein the conversion of H₂ and N₂ to ammonia is at least twice the equilibrium conversion in the absence of adsorbant at the temperature and pressure of the adsorbant.

4. The process of claim 1, where the vessel is maintained at a pressure of about 50 atm or less.

5. The process of claim 4, where the vessel is maintained at a pressure of about 10 atm or less.

6. The process of claim 1, wherein the vessel contains a catalyst for the reaction of H₂ and N₂ to produce ammonia and the catalyst is physically combined with the adsorbant.

7. The process of claim 6, wherein the adsorbant is the catalyst.

8. A batch ammonia synthesis process according to claim 1.

9. A vessel, an adsorbant, a nitrogen source, and a hydrogen source collectively configured to carrying out a process according to claim 1.

10. The process of claim 1, wherein the adsorbant is a molecular sieve.

11. The process of claim 10, wherein the adsorbant is a zeolite selected from the group consisting of Chabazite, faujasite, and rare earth zeolites.

12. The process of claim 11, wherein the adsorbant comprises an effective amount of Chabazite cation exchanged with lithium.

13. The process of claim 1, wherein the bulk of the reaction occurs within one meter of the adsorbant.

14. The process of claim 1, further comprising regenerating the adsorbant by heating.

15. The process of claim 1, wherein bringing H₂ and N₂ together in the vessel under conditions where the H₂ and the N₂ react comprises introducing H₂ and N₂ into vessel while at least a portion of the adsorbant is at a temperature greater than that of the combined H₂ and N₂, whereby the adsorbant heats the H₂ and N₂ to a temperature at which the reaction occurs.

16. The process of claim 1, wherein the nitrogen is obtained by membrane separation from air and the nitrogen is supplied from the membrane separation process to the vessel without increasing the nitrogen pressure.

17. The process of claim 1, further comprising providing an ammonia synthesis catalyst in the vessel, wherein the ammonia synthesis catalyst is physically separate from the adsorbant, but there is no substantial pressure gradient between the catalyst and the adsorbant during reaction and adsorption.

18. The process of claim 17, wherein there is a substantial temperature gradient between the catalyst and the adsorbant during reaction and adsorption.

19. The process of claim 18, wherein the temperature gradient is at least about 75°

C.

20. The process of claim 1, wherein the adsorbant is at a temperature from about 100 to about 350°

C.

21. The process of claim 20, wherein the adsorbant is at a temperature of at least about 200°

C.

22. The process of claim 1, further comprising replacement of the adsorbant prior to regeneration of the adsorbant, wherein the vessel is not used to synthesize ammonia during replacement of the adsorbant.

23. The process of claim 1, further comprising regeneration of the adsorbant, wherein the vessel is not used to synthesize ammonia during regeneration of the adsorbant.

24. The process of claim 1, wherein the process is carried out without appreciable heat exchange between the vessel or any of its contents and any cooling fluid external to the vessel.

25. A process using ammonia, comprising:

synthesizing ammonia according to the process of claim 1;

and

using the ammonia in the process without condensing the ammonia to liquid form between the synthesis and the use.

26. The process of claim 1, further comprising a regeneration step in which the adsorbant is heated to desorb the ammonia.

27. The process of claim 26, wherein heating the adsorbant comprises heating to a temperature above the temperature condition at which the ammonia formed.

28. The process of claim 1, wherein the adsorbant is in the form of multiple units that are cycled through the vessel as the ammonia-forming reaction takes place.

29. The process of claim 1 wherein the H₂ and or N₂ are injected into the vessel at a high velocity to cause circulation within the vessel.

30. The process of claim 1, further comprising a regeneration step in which nitrogen is flowed through the vessel and carries away ammonia desorbed from the adsorbant.

31. An ammonia synthesis plant, comprising:

a reaction vessel containing an adsorbant for ammonia.

a nitrogen source configured to supply the reaction vessel with nitrogen; and

a hydrogen source configured to supply the reaction vessel with hydrogen;

wherein the reaction vessel is configured to bring about reaction of the hydrogen and the nitrogen to produce ammonia and the adsorbant is configured to adsorb the ammonia.

32. The ammonia synthesis plant of claim 31, wherein the plant is not configured to recirculate unreacted nitrogen and hydrogen exiting the vessel.

33. The ammonia synthesis plant of claim 31, wherein the adsorbant is distributed whereby the majority of void volume within the vessel is within 1 meter of the adsorbant.

34. The ammonia synthesis plant of claim 31, wherein the plant is configured to provide a single-pass conversion rate for the ammonia synthesis reaction of at least about 50%.

35. The ammonia synthesis plant of claim 31, wherein the plant is configured to provide a single-pass conversion rate for the ammonia synthesis reaction of at least twice the equilibrium conversion in the absence of the adsorbant.

36. The ammonia synthesis plant of claim 31, wherein the vessel is configured to operate at a pressure of about 50 atm or less.

37. The ammonia synthesis plant of claim 36, wherein the vessel is configured to operate at a pressure of about 10 atm or less.

38. The ammonia synthesis plant of claim 31, wherein the vessel contains a catalyst for the reaction of H₂ and N₂ to produce ammonia and the catalyst is physically combined with the adsorbant.

39. The ammonia synthesis plant of claim 38, wherein the adsorbant is the catalyst.

40. The ammonia synthesis plant of claim 31, wherein the plant is configured for batch operation.

41. The ammonia synthesis plant of claim 40, wherein the plant comprises multiple reaction vessels.

42. The ammonia synthesis plant of claim 31, wherein the adsorbant is a molecular sieve.

43. The ammonia synthesis plant of claim 42, wherein the adsorbant is a zeolite selected from the group consisting of Chabazite, faujasite, and rare earth zeolites.

44. The ammonia synthesis plant of claim 43, wherein the adsorbant comprises an effective amount of Chabazite cation exchanged with lithium.

45. The ammonia synthesis plant of claim 31, wherein the plant is configured to bring abut the reaction and the adsorption at substantially the same pressure.

46. The ammonia synthesis plant of claim 31, wherein the plant is configured to regenerate the adsorbant by heating.

47. The ammonia synthesis plant of claim 31, wherein the nitrogen source is an apparatus for membrane separation of nitrogen from air and the plant is configured to supply the nitrogen to the vessel without increasing the nitrogen pressure.

48. The ammonia synthesis plant of claim 31, wherein:

the reaction vessel comprises an ammonia synthesis catalyst physically separate from the adsorbant; and

the plant is configured whereby there is no substantial pressure gradient between the catalyst and the adsorbant during reaction and adsorption.

49. The ammonia synthesis plant of claim 48, wherein the plant is configured to develop a substantial temperature gradient between the catalyst and the adsorbant during reaction and adsorption.

50. The ammonia synthesis plant of claim 49, wherein the temperature gradient is at least about 75°

C.

51. The ammonia synthesis plant of claim 31, wherein the reaction vessel does not include a heat exchanger.

52. An ammonia synthesis plant according to claim 31 adapted for mounting on a vehicle.

53. An ammonia synthesis plant according to claim 31, wherein plant is configure to move the adsorbant through the reaction vessel as the ammonia-forming reaction takes place.

54. An ammonia synthesis plant according to claim 31, wherein the plant is configured to inject H₂ and or N₂ into the vessel at a high velocity to cause circulation within the vessel.

55. A method of enhancing the single pass conversion in an ammonia synthesis plant comprising:

placing an ammonia adsorbant inside the plant to adsorb ammonia as it is produced; and

intermittently inducing desorption from the adsorbant to regenerate the adsorbant.

56. The method of claim 55, wherein the adsorbant is Chabazite cation exchanged with lithium.

57. The method of claim 55, wherein inducing desorption comprises heating the adsorbant.

58. The method of claim 55, wherein inducing desorption comprises flowing N₂ over the adsobant.

59. A process of separating gaseous ammonia from other gasses, comprising:

adsorbing the ammonia on an adsorbant comprising an effective amount of Chabazite cation exchanged with lithium; and

inducing desorption of the ammonia.

60. The method of claim 59, wherein inducing desorption comprises heating the adsorbant.

61. An ammonia synthesis plant, comprising:

a plurality of ammonia synthesis reactors comprising an adsorbant that adsorbs ammonia synthesized in the reactors;

a mobile framework configured to hold the reactors and move them in sequence through a plurality of positions; and

one or more couplings adapted to provide a feed comprising hydrogen and nitrogen to the reactors in a subset of the positions;

wherein a subset is at least one, but less than all;

whereby the mobile framework is adapted to move the reactors in and out of position to receive the feed and at any given time less than all of the reactors are configured to receive the feed.

62. The ammonia synthesis plant of claim 61, wherein the mobile framework holds the plurality of reactors in a radial array and the mobile framework moves the reactors by rotating the array.

63. The ammonia synthesis plant of claim 61, further comprising:

a coupling adapted to receive an inert gas;

wherein the mobile framework is designed to alternately place each of the reactors into position to receive the inert gas and the ammonia synthesis plant is desgined to recirculate the inert gas to induce desorption of ammonia.

64. A method of synthesizing ammonia, comprising:

providing a plurality of ammonia synthesis reactors comprising an adsorbant for ammonia; and

providing an indexing system that moves the reactors whereby each of the reactors alternates through a set of positions and in one or more of the positions the reactors receive a feed comprising hydrogen and nitrogen in one or more others of the positions the reactors receive a flow of inert gas;

wherein the feed reacts in the reactors to produce ammonia that adsorbs on the adsorbant; and

the ammonia desorbs and is carried away by the flow of inert gas, whereby the adsorbant is regenerated.