Cryogenic separation of lean and rich gas streams

• US 4,331,461 A
• Filed: 03/10/1978
• Issued: 05/25/1982
• Est. Priority Date: 03/10/1978
• Status: Expired due to Term

• Current Assignee: Phillips Petroleum Company (ConocoPhillips)
• Original Assignee: Phillips Petroleum Company (ConocoPhillips)
• Inventors: Bailey, Dunn M., Karbosky, Joseph T.
• Primary Examiner(s): Yudkoff, Norman
• Application Number:
  US05/885,402
• Time in Patent Office: 1,537 Days
• Field of Search: 62/28, 62/27, 62/23, 62/26, 62/24, 62/31, 62/38, 62/39
• US Class Current: 62/630
• CPC Class Codes: C07C 7/00 Purification; Separation; Use of additives working-up undefined gaseous mixtures obtained by cracking hydrocarbon oils C10G70/00
• CPC Class Codes: C07C 7/09 by fractional condensation
• CPC Class Codes: F25J 2200/02 in a single pressure main column system
• CPC Class Codes: F25J 2200/70 Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
• CPC Class Codes: F25J 2200/74 Refluxing the column with at least a part of the partially condensed overhead gas
• CPC Class Codes: F25J 2205/04 in the feed line, i.e. upstream of the fractionation step
• CPC Class Codes: F25J 2210/02 Multiple feed streams, e.g. originating from different sources
• CPC Class Codes: F25J 2240/02 Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
• CPC Class Codes: F25J 2245/02 Recycle of a stream in general, e.g. a by-pass stream
• CPC Class Codes: F25J 2260/60 Integration in an installation using hydrocarbons, e.g. for fuel purposes
• CPC Class Codes: F25J 2270/02 Internal refrigeration with liquid vaporising loop
• CPC Class Codes: F25J 2270/12 External refrigeration with liquid vaporising loop
• CPC Class Codes: F25J 2270/60 Closed external refrigeration cycle with single component refrigerant [SCR], e.g. C1-, C2- or C3-hydrocarbons
• CPC Class Codes: F25J 3/0209 Natural gas or substitute natural gas
• CPC Class Codes: F25J 3/0233 separation of CnHm with 1 carbon atom or more
• CPC Class Codes: F25J 3/0238 separation of CnHm with 2 carbon atoms or more
• CPC Class Codes: F25J 3/0257 separation of nitrogen from air F25J3/04, production of nitrogen in general C01B21/00
• CPC Class Codes: F25J 3/069 of helium

Abstract

A process for simultaneously, cryogenically separating natural gas liquids from a lean natural gas stream and a rich natural gas stream; including, compressing the lean gas feed, cooling the compressed lean gas feed, separating the cooled lean gas feed to form a vapor phase and a liquid phase, expanding the vapor phase lean gas feed, separating the expanded vapor phase lean gas feed to form a second vapor phase and a second liquid phase, fractionating the second vapor phase lean gas feed to form a methane-enriched, low pressure bottoms fraction and a nitrogen-enriched, high pressure overhead fraction, flashing a portion of the methane-enriched bottoms fraction and passing the same in countercurrent, indirect heat exchange with the nitrogen-enriched overhead fraction, to cool the same and produce a vapor phase nitrogen-enriched product and a liquid phase reflux for the fractionator, passing the remainder of the methane-enriched bottoms fraction, the flashed methane-enriched bottoms fraction and the vapor phase nitrogen-enriched fraction in countercurrent heat exchange with the lean gas feed, compressing the rich gas feed, cooling the compressed rich gas feed, fractionating the cooled rich gas feed and the liquid phases separated from the lean gas feed to form a methane-enriched overhead fraction and a natural gas liquids bottoms product and combining the methane-enriched overhead with a portion of the methane-enriched bottoms product from the lean gas feed, prior to the passage of the latter in heat exchange with the lean gas feed. The methane-enriched streams are combined, following their use as heat exchange media, to form a pipeline quality natural gas product and the nitrogen-enriched vapor phase can be utilized as a low BTU fuel gas for the plant.

Claims

1. A process for cyrogenically separating a lean natural gas feed, containing a predominant amount of methane and a significant amount of nitrogen, and a separate rich natural gas feed, containing a predominant amount of ethane and higher molecular weight hydrocarbons;

comprising, liquefying at least a portion of said lean gas feed, vaporizing at least a portion of said liquefied lean gas feed to produce a nitrogen-enriched gas product, and recovering a methane-enriched liquid product and an ethane and higher molecular weight hydrocarbon-enriched liquid product; and

, simultaneously with said processing of said lean natural gas feed, liquefying at least a portion of said rich gas feed, vaporizing at least a portion of said liquefied rich gas feed and said ethane and higher molecular weight hydrocarbon-enriched liquid in a single vaporization step to produce a methane-enriched gas product, and recovering a natural gas liquids product.

2. A process in accordance with claim 1 wherein at least a portion of the energy necessary to liquefy the lean gas feed is provided by countercurrently passing at least a portion of the methane-enriched liquid product in indirect heat exchange with said lean gas feed.

3. A process in accordance with claim 2 wherein the methane-enriched gas product is combined with the methane-enriched liquid product prior to passing said methane-enriched liquid product in heat exchange with the lean gas feed.

4. A process in accordance with claim 1 wherein at least a portion of the energy necessary to liquefy the lean gas feed is provided by countercurrently passing at least a portion of the nitrogen-enriched gas product in indirect heat exchange with said lean gas feed.

5. A process in accordance with claim 4 wherein at least a second portion of the energy necessary to liquefy the lean gas feed is provided by cooling said lean gas feed by not more than about 40°

F. with an external heat exchange medium.

6. A process in accordance with claim 1 wherein at least a portion of the energy necessary to liquefy the lean gas feed is provided by compressing the lean gas feed.

7. A process in accordance with claim 1 wherein at least a portion of the energy necessary to liquefy the lean gas feed is provided by countercurrently and separately passing at least a portion of the methane-enriched liquid product and at least a portion of the nitrogen-enriched gas product in indirect heat exchange with said lean gas feed.

8. A process in accordance with claim 1 wherein at least a portion of the energy necessary to vaporize the liquefied lean gas feed is provided by expanding said liquefied lean gas feed.

9. A process in accordance with claim 8 wherein the ethane and higher molecular weight hydrocarbon-enriched liquid is produced by separating a first portion of said ethane and higher molecular weight hydrocarbon-enriched liquid from the liquefied lean gas feed, prior to the expansion of said liquefied lean gas feed and separating the remainder of the ethane and higher molecular weight hydrocarbon-enriched liquid from the expanded lean gas feed.

10. A process in accordance with claim 9 wherein at least a portion of the expanded lean gas feed, remaining after the separation of the ethane and higher molecular weight hydrocarbon-enriched liquid, is at least partially reliquefied and said reliquefied remainder of the lean gas feed is at least partially vaporized to produce the methane-enriched liquid product and the nitrogen-enriched gas product.

11. A process in accordance with claim 10 wherein the energy necessary to reliquefy the remainder of the lean gas feed and at least a portion of the energy necessary to liquefy the lean gas feed, prior to the expansion of said lean gas feed, are provided by countercurrently passing at least a portion of the methane-enriched liquid product in indirect heat exchange with said remainder of said lean gas feed and said lean gas feed.

12. A process in accordance with claim 11 wherein the methane-enriched gas product is combined with the portion of the methane-enriched liquid product, after heat exchange of said portion of said methane-enriched liquid product with the remainder of the lean gas feed.

13. A process in accordance with claim 10 wherein the energy necessary to reliquefy the remainder of the lean gas feed and at least a portion of the energy necessary to liquefy the lean gas feed, prior to the expansion of said lean gas feed, are provided by countercurrently passing at least a portion of the nitrogen-enriched gas product in indirect heat exchange with said remainder of said lean gas feed and said lean gas feed.

14. A process in accordance with claim 10 wherein the energy necessary to reliquefy the remainder of the lean gas feed and at least a portion of the energy necessary to liquefy the lean gas feed, prior to the expansion of said lean gas feed, are provided by countercurrently and separately passing the methane-enriched liquid product and at least a portion of the nitrogen-enriched gas product in indirect heat exchange with said remainder of said lean gas feed and said lean gas feed.

15. A process in accordance with claim 14 wherein the methane-enriched gas product is combined with the portion of the methane-enriched liquid product, after heat exchange of said portion of said methane-enriched liquid product with the remainder of the lean gas feed.

16. A process in accordance with claim 8 wherein at least a portion of the methane-enriched liquid product is compressed.

17. A process in accordance with claim 16 wherein at least a portion of the energy necessary to compress the methane-enriched liquid product is provided by the expansion of the liquefied lean gas feed.

18. A process in accordance with claim 1 wherein at least a portion of the methane-enriched liquid product is countercurrently passed in indirect heat exchange with the nitrogen-enriched gas product to condense a portion of said nitrogen-enriched gas product and said condensed portion of said nitrogen-enriched gas product is countercurrently contacted with the vapors of the liquefied lean gas feed during the partial vaporization of said liquefied lean gas feed.

19. A process in accordance with claim 18 wherein at least a portion of the energy necessary to liquefy the lean gas feed is provided by countercurrently and separately passing the portion of the methane-enriched liquid product, after heat exchange with the nitrogen-enriched gas product, and the remainder of the methane-enriched liquid product in indirect heat exchange with said lean gas feed.

20. A process in accordance with claim 19 wherein the methane-enriched gas product is combined with the remainder of the methane-enriched liquid product prior to passing said remainder of said methane-enriched liquid product in heat exchange with the lean gas feed.

21. A process in accordance with claim 18 wherein at least a portion of the energy necessary to liquefy the lean gas feed is provided by countercurrently passing the uncondensed portion of the nitrogen-enriched gas product in indirect heat exchange with said lean gas feed.

22. A process in accordance with claim 21 wherein at least a second portion of the energy necessary to liquefy the lean gas feed is provided by cooling said lean gas feed by not more than about 40°

F. with an external heat exchange medium.

23. A process in accordance with claim 18 wherein at least a portion of the energy necessary to liquefy the lean gas feed is provided by compressing the lean gas feed.

24. A process in accordance with claim 18 wherein at least a portion of the energy necessary to liquefy the lean gas feed is provided by countercurrently and separately passing the portion of the methane-enriched liquid product, the remainder of the methane-enriched liquid product and the uncondensed portion of the nitrogen-enriched gas product in indirect heat exchange with said lean gas feed.

25. A process in accordance with claim 18 wherein a portion of the energy necessary to vaporize the liquefied lean gas feed is provided by expanding said liquefied lean gas feed.

26. A process in accordance with claim 25 wherein the ethane and higher molecular weight hydrocarbon-enriched liquid product is produced by separating a first portion of said ethane and higher molecular weight hydrocarbon-enriched product from the liquefied lean gas feed, prior to the expansion of said liquefied lean gas feed, and separating the remainder of the ethane and higher molecular weight hydrocarbon-enriched product from the expanded lean gas feed.

27. A process in accordance with claim 26 wherein expanded lean gas feed, remaining, after the separation of the ethane and higher molecular weight hydrocarbon-enriched liquid product, is at least partially reliquefied and said reliquefied remainder of the lean gas feed is at least partially vaporized to produce the methane-enriched liquid product and the nitrogen-enriched gas product.

28. A process in accordance with claim 27 wherein the energy necessary to reliquefy the remainder of the lean gas feed and at least a portion of the energy necessary to liquefy the lean gas feed, prior to the expansion of said lean gas feed, are provided by countercurrently and separately passing the portion of the methane-enriched liquid product, after heat exchange with the nitrogen-enriched gas product, and the remainder of the methane-enriched liquid product in indirect heat exchange with said remainder of said lean gas feed and said lean gas feed.

29. A process in accordance with claim 28 wherein the methane-enriched gas product is combined with the portion of the methane-enriched liquid product, after heat exchange of said portion of said methane-enriched liquid product with the remainder of the lean gas feed.

30. A process in accordance with claim 27 wherein the energy necessary to reliquefy the remainder of the lean gas feed and at least a portion of the energy necessary to liquefy the lean gas feed, prior to the expansion of said lean gas feed, are provided by countercurrently passing the uncondensed portion of the nitrogen-enriched gas product in indirect heat exchange with said remainder of said lean gas feed and said lean gas feed.

31. A process in accordance with claim 27 wherein the energy necessary to reliquefy the remainder of the lean gas feed and at least a portion of the energy necessary to liquefy the lean gas feed, prior to the expansion of said lean gas feed, are provided by countercurrently and separately passing the portion of the methane-enriched liquid product, after heat exchange with the nitrogen-enriched gas product, the remainder of the methane-enriched liquid product and the uncondensed portion of the nitrogen-enriched gas product in indirect heat exchange with said remainder of said lean gas feed and said lean gas feed.

32. A process in accordance with claim 31 wherein the methane-enriched gas product is combined with the portion of the methane-enriched liquid product, after heat exchange of said portion of said methane-enriched liquid product with the remainder of the lean gas feed.

33. A process in accordance with claim 25 wherein at least a portion of the methane-enriched liquid product is compressed.

34. A process in accordance with claim 33 wherein at least a portion of the energy necessary to compress the portion of the methane-enriched liquid product is provided by the expansion of the liquefied lean gas feed.

35. A process in accordance with claim 1 wherein the ethane and higher molecular weight hydrocarbon-enriched liquid is countercurrently and directly contacted with the vapors of the rich gas feed during the vaporization of the said rich gas feed.

36. A process in accordance with claim 1 wherein at least a portion of the energy necessary to vaporize the liquefied lean gas feed is provided by expanding said liquefied lean gas feed, producing the ethane and higher molecular weight hydrocarbon-enriched liquid by separating a first portion of said ethane and higher molecular weight hydrocarbon-enriched liquid from said liquefied lean gas feed, prior to said expansion of said liquefied lean gas feed, and separating the remainder of the ethane and higher molecular weight hydrocarbon-enriched liquid from the expanded lean gas feed and said first portion of said ethane and higher molecular weight hydrocarbon-enriched liquid and said remainder of said ethane and higher molecular weight hydrocarbon-enriched liquid are sequentially, countercurrently and directly contacted with the vapors of the rich gas feed during the vaporization of said rich gas feed.

37. A process in accordance with claim 1 wherein the rich gas feed is separated into a vapor phase rich gas feed and a liquid phase rich gas feed and said vapor phase rich gas feed is countercurrently and directly contacted with the vapors from said liquid phase rich gas feed during the vaporization of said liquefied rich gas feed.

38. A process in accordance with claim 1 wherein the rich gas feed is separated into a first vapor phase rich gas feed and a first liquid phase rich gas feed, said first vapor phase rich gas feed is further separated into a second vapor phase rich gas feed and a second liquid phase rich gas feed, said first and second liquid phase rich gas feeds are combined and said second vapor phase rich gas feed is countercurrently and directly contacted with the vapors from said combined first and second liquid phase rich gas feeds during the vaporization of said combined rich gas feed.

39. A process in accordance with claim 38 wherein the first vapor phase rich gas feed is at least partially reliquefied, prior to the further separation of said first vapor phase rich gas feed.