Ammonia production process utilizing enhanced boiling surface in refrigeration zone

• US 4,869,888 A
• Filed: 03/29/1988
• Issued: 09/26/1989
• Est. Priority Date: 03/29/1988
• Status: Expired due to Fees

• Current Assignee: UOP Des Plaines Illinois A NY General Partnership
• Original Assignee: UOP Llc (Honeywell International Inc.)
• Inventors: O'Neill, Patrick S.
• Primary Examiner(s): Doll, John
• Assistant Examiner(s): Langel, Wayne A.
• Application Number:
  US07/174,970
• Time in Patent Office: 546 Days
• Field of Search: 423/359
• US Class Current: 423/359
• CPC Class Codes: C01C 1/047 by condensation
• CPC Class Codes: Y02P 20/52 using catalysts, e.g. selective catalysts

Abstract

This invention pertains to the field of producing ammonia. More specifically, the present invention relates to reducing the costs of producing a unit amount of ammonia, particularly the energy costs, by the utilization of an enhanced boiling surface in the refrigeration zone of the process.

Claims

1. In a process for producing ammonia which comprises:

(a) reacting a nitrogen-hydrogen ammonia synthesis gas stream in the presence of an ammonia synthesis catalyst at conditions effecting partial conversion to ammonia; and

(b) cooling the reacted synthesis gas stream to a temperature below the dewpoint of ammonia so as to condense said ammonia by indirect heat exchange with ammonia refrigerant in at least two or more stages of cooling wherein each successive stage cools the reacted synthesis gas to a lower temperature with the last stage of cooling providing the lowest reacted synthesis gas temperature T, said indirect heat exchange having an overall heat transfer coefficient U_o, and wherein the ammonia refrigerant is provided by a compressor having at least two or more stages of compression, each stage of compression requiring a corresponding respective amount of compression energy to compress the ammonia such that a total amount of energy E is expended for compression and each stage of compression having an inlet suction pressure and an outlet discharge pressure;

the improvement which comprises decreasing the amount of compression energy expended per unit amount of ammonia produced in the process by;

(i) providing heat exchange apparatus for cooling the reacted synthesis gas with ammonia refrigerant having a thermally conductive wall with an enhanced boiling surface on one side of said wall in at least the last stage of cooling such that the ammonia refrigerant is in contact with the said enhanced boiling surface during the indirect heat exchange; and

(ii) increasing the suction pressure to at least the first stage of compression.

2. The process of claim 1, wherein the temperature T in the last stage of cooling is reduced to obtain more condensation of liquid ammonia product.

3. The process of claim 2, wherein the temperature T is reduced to a value in the range of from about -10°

to about -25°

F.

4. The process of claim 2, wherein the temperature T is reduced to a value in the range of from about -23°

to about -25°

F.

5. The process of claim 1, wherein the cold end temperature approach of the last stage of cooling is less than about 5°

F.

6. The process of claim 5, wherein the cold end temperature approach of the last stage of cooling is less than or equal to about 3°

F.

7. The process of claim 1, wherein the total amount of compressor energy E is reduced by maintaining the temperature T in the last cooling stage constant to thereby maintain the same level of ammonia condensation.

8. The process of claim 1, wherein all of the cooling stages are provided with an enhanced boiling surface such that the ammonia refrigerant is in contact with the said enhanced surface.

9. The process of claim 1, wherein the overall heat transfer coefficient U_o is increased by a factor of from at least about 2.0 to about 3.0.

10. The process of claim 1, wherein the overall heat transfer coefficiient U_o is increased to a value of from about 250 to 500 (BTU/hr)/(ft² °

F.).

11. The process of claim 1, wherein the condensed ammonia product is utilized as the ammonia refrigerant.

12. The process of claim 1, wherein the pressure is in the range of from about 1,800 to about 2,300 psia.

13. The process of claim 12, wherein the pressure is in the range of from about 2,100 to 2,200 psia.

14. The process of claim 1, wherein the enhanced boiling surface is a porous boiling layer.

15. The process of claim 14, wherein the porous boiling layer is constructed of thermally conductive particles bonded together to form interconnected pores of capillary size having an equivalent pore radius of less than about 6.0 mils.

16. The process of claim 14, wherein the porous boiling layer is formed by mechanically working the wall surface.

17. The process of claim 1, wherein the enhanced boiling surface provides a boiling film heat transfer coefficient of greater than about 2,000 (BTU/hr)/(ft² °

F.).

18. The process of claim 1, wherein the suction pressure at each stage of the compressor is raised.

19. The method for decreasing energy expended per unit amount of ammonia produced in an ammonia production process which comprises:

(a) reacting a nitrogen-hydrogen ammonia synthesis gas stream in the presence of an ammonia synthesis catalyst at conditions effecting partial conversion to ammonia;

(b) passing the reacted synthesis gas containing gaseous ammonia through two or more stages of cooling by indirect heat exchange with ammonia refrigerant to a temperature below the dewpoint of the ammonia to obtain condensed ammonia product;

wherein at least the last stage of cooling contains a thermally conductive wall with an enhanced boiling surface on the side which is in contact with the ammonia refrigerant, said last stage of cooling having an overall heat transfer coefficient U_o, and wherein the ammonia refrigerant is provided by a compressor having two or more stages of compression requiring an input of compression energy for each stage of compression, each stage of compression having an inlet suction pressure and an outlet discharge pressure;

(c) increasing the suction pressure to at least the first stage of the compressor such that a percentage increase in ammonia condensation is greater than the corresponding percentage increase in compressor energy consumption.

20. The process of claim 19, wherein the reacted synthesis gas is cooled to a temperature in the range of from about -10°

to about -25°

F.

21. The process of claim 19, wherein the cold end temperature approach of the last stage of cooling is less than about 5°

F.

22. The process of claim 21, wherein the cold end temperature approach of the last stage of cooling is less than or equal to about 3°

F.

23. The process of claim 19, wherein all of the cooling stages are provided with an enhanced boiling surface such that the ammonia refrigerant is in contact with the said enhanced surface.

24. The process of claim 19, wherein the overall heat transfer coefficient U_o is in the range of from about 250 to 500 (BTU/hr)/(ft² °

F.).

25. The process of claim 19, wherein the condensed ammonia product is utilized as the ammonia refrigerant.

26. The process of claim 19, wherein the pressure is in the range of from about 1,800 to about 2,300 psia.

27. The process of claim 26, wherein the pressure is in the range of from about 2,100 to 2,200 psia.

28. The process of claim 19, wherein the enhanced boiling surface is a porous boiling layer.

29. The process of claim 28, wherein the porous boiling layer is constructed of thermally conductive particles bonded together to form interconnected pores of capillary size having an equivalent pore radius of less than about 6.0 mils.

30. The process of claim 28, wherein the porous boiling layer is formed by mechanically working the wall surface.

31. The process of claim 19, wherein the enhanced boiling surface provides a boiling film heat transfer coefficient of greater than about 2,000 (BTU/hr)/(ft² °

F.).

32. The process of claim 19, wherein the suction pressure at each stage of the compressor is raised.

33. In a process for producing ammonia which comprises:

(a) reacting a nitrogen-hydrogen ammonia synthesis gas stream in the presence of an ammonia synthesis catalyst at conditions effecting partial conversion to ammonia; and

(b) cooling the reacted synthesis gas stream containing gaseous ammonia to a temperature T below the dewpoint of the ammonia to obtain a condensed liquid ammonia product by indirect heat exchange with ammonia refrigerant in at least two or more stages of cooling, wherein the ammonia refrigerant is provided by a compressor having at least two or more stages of compression, each stage of compression requiring a corresponding amount of compression energy to compress the ammonia;

the improvement which comprises reducing the energy expended per unit amount of ammonia produced by increasing the amount of ammonia condensed while maintaining or reducing the overall compressor energy consumption by;

(i) providing heat exchange apparatus for cooling the reacted synthesis gas with ammonia refrigerant having a thermally conductive wall with an enhanced boiling surface on one side of said wall in at least the last stage of cooling such that the ammonia refrigerant is in contact with the said enhanced boiling surface during the indirect heat exchange; and

(ii) cooling the reacted synthesis gas to a temperature below T so as to condense more ammonia; and

(iii) increasing the suction pressure in at least the first stage of the compressor so as to maintain or reduce the overall compressor energy consumption.

34. In a process for producing ammonia which comprises;

(a) reacting a nitrogen-hydrogen ammonia synthesis gas stream in the presence of an ammonia synthesis catalyst at conditions effecting partial conversion to ammonia; and

(b) cooling the reacted synthesis gas stream containing gaseous ammonia to a temperature T below the dewpoint of the ammonia to obtain a condensed liquid ammonia product by indirect heat exchange with ammonia refrigerant in at least two or more stages of cooling, wherein the ammonia refrigerant is provided by a compressor having at least two or more stages of compression, each stage of compression requiring a corresponding amount of compression energy to compress the ammonia;

the improvement which comprises reducing the energy expended per unit of ammonia produced by maintaining the ammonia obtained substantially constant while reducing the overall compressor energy consumption by;

(i) providing heat exchange apparatus for cooling the reacted synthesis gas with ammonia refrigerant having a thermally conductive wall with an enhanced boiling surface on one side of such wall in at least the last stage of cooling such that the ammonia refrigerant is in contact with the said enhanced boiling surface during the indirect heat exchange; and

(ii) cooling the reacted synthesis gas to essentially the same temperature T so as to obtain a substantially constant amount of ammonia condensation; and

(iii) increasing the suction pressure in at least the first stage of the compressor so as to decrease the overall compressor energy consumption.

35. In a process for the production of ammonia comprising:

(a) compressing a hydrogen-nitrogen ammonia synthesis gas stream to a pressure greater than about 1800 psia;

(b) combining the compressed synthesis gas with a reacted synthesis gas stream containing hydrogen, nitrogen, and gaseous ammonia from step (i);

(c) passing a first portion of the combined stream to a heat exchanger which is in indirect heat exchange with a vapor phase stream containing hydrogen, nitrogen, and gaseous ammonia obtained from step (g) to cool the first portion of the combined stream;

(d) passing a second portion of the combined stream to at least one cooling stage cooled with ammonia refrigerant;

(e) recombining the cooled first and second portions of combined stream;

(f) passing the recombined stream to a final cooling stage to reduce the temperature of the recombined stream to a temperature T₁ and providing a mixture containing liquid ammonia, gaseous ammonia, hydrogen, and nitrogen;

(g) separating the liquid ammonia from the vapor portion of the mixture in a first separating zone to form a vapor phase of gaseous ammonia, hydrogen and nitrogen and a liquid ammonia phase;

(h) passing the vapor phase in indirect heat exchange with the first portion of the combined stream in accordance with step (c);

(i) reacting the vapor phase in the presence of an ammonia synthesis catalyst at conditions effecting conversion of the hydrogen and nitrogen to gaseous ammonia and form the reacted synthesis gas stream of step (b);

wherein the ammonia refrigerant in the cooling stages is provided by a compressor having at least two or more stages of compression;

the improvement which comprises reducing the energy expended per unit of ammonia produced by;

(i) providing at least the final ammonia refrigerant cooling stage with a thermally conductive wall having an enhanced boiling surface on the side which is in contact with the ammonia refrigerant said that the overall heat transfer coefficient is increased by a factor of at least 2.0 to 3.0;

(ii) reducing the temperature of the recombined stream to a temperature T₂ which is less than T₁ such that more ammonia is condensed;

(iii) increasing the amount of the first portion of the combined stream passed to the heat exchanger; and

(iv) increasing the suction pressure to at least the first stage of the compressor.