Method of liquefying natural gas

• US 5,036,671 A
• Filed: 02/06/1990
• Issued: 08/06/1991
• Est. Priority Date: 02/06/1990
• Status: Expired due to Fees

• Current Assignee: Liquid Company SUB 2 Engineering Incorporated
• Original Assignee: Liquid Company SUB 2 Engineering Incorporated
• Inventors: Garcia, Luc, Nelson, Warren L.
• Primary Examiner(s): Capossela, Ronald C.
• Application Number:
  US07/475,908
• Time in Patent Office: 546 Days
• Field of Search: 62/11, 62/38, 62/39, 62/23, 62/48.2
• US Class Current: 62/612
• CPC Class Codes: F25J 1/0022 Hydrocarbons, e.g. natural gas
• CPC Class Codes: F25J 1/004 by flash gas recovery F25J1/0267 takes precedence
• CPC Class Codes: F25J 1/0045 by vaporising a liquid return stream
• CPC Class Codes: F25J 1/0055 originating from an incorporated cascade
• CPC Class Codes: F25J 1/0219 in combination with an internal quasi-closed refrigeration loop, e.g. using a deep flash recycle loop
• CPC Class Codes: F25J 2220/62 Separating low boiling components, e.g. He, H2, N2, Air
• CPC Class Codes: F25J 2220/64 Separating heavy hydrocarbons, e.g. NGL, LPG, C4+ hydrocarbons or heavy condensates in general
• CPC Class Codes: F25J 2245/90 the recycled stream being boil-off gas from storage
• CPC Class Codes: F25J 2290/62 Details of storing a fluid in a tank

Abstract

A method of producing a methane-rich liquid stream from a stream of natural gas predominantly consisting of methane and also containing nitrogen, entailing:

(a) supplying said natural gas stream at a pressure above atmospheric pressure,

(b) cooling and liquefying said natural gas stream using one or more refrigeration cycles, and

(c) expanding said liquefied natural gas to lower pressure in two or more stages in series, phase separating the gas and liquid phases produced during the expansion, thereby concentrating the nitrogen into the vapor phase, and producing a methane-rich liquefied natural gas.

Claims

1. A method of producing a methane-rich liquid stream from a stream of natural gas predominantly consisting of methane and also containing nitrogen, comprising:

(a) supplying said natural gas stream at a pressure above atmospheric pressure,

(b) cooling and liquefying said natural gas stream using one or more refrigeration cycles,

(c) expanding said liquefied natural gas to lower pressure in two or more stages in series, phase separating the gas and liquid phases produced during the expansion, thereby concentrating the nitrogen into the gas phases and producing a methane-rich and nitrogen depleted liquefied natural gas, and

(d) reheating the gas phases enriched in nitrogen, and sending them out of the plant as nitrogen-enriched product streams.

2. The method as a claimed in claim 1, in which the last stage of expansion of the liquid natural gas takes place in a liquid natural gas storage tank maintained slightly above atmospheric pressure.

3. The method as claimed in claim 2, in which the second to the last stage of expansion takes place at a pressure controlled just sufficiently high enough to be able to send the liquid collected in this phase separator to the storage tank.

4. The method as claimed in claim 1, which further comprises a step of recompressing some of the expansion gases to the pressure of the natural gas and recycling this gas into the natural gas being liquefied.

5. The method as claimed in claim 1, wherein said natural gas stream in step a) is supplied at a pressure of about 150 to 1,200 psig.

6. The method as claimed in claim 1, wherein said natural gas stream in step (b) is cooled and liquefied to a temperature between about -100°

C. to -150°

C.

7. The method as claimed in claim 1, wherein said liquefied natural gas in step (c) is expanded to a final lower pressure of about 30 psig to 0 psig.

8. The method as claimed in claim 1, wherein said methane-rich liquefied natural gas has less than 0.8 molar % of nitrogen in the final liquid phase.

9. The method as claimed in claim 1, which further comprises recovering said nitrogen-enriched product streams.

10. The method as claimed in claim 1, wherein further comprises using said nitrogen-enriched product streams as fuel gas.

11. A method of producing a methane-rich liquid stream from a stream of natural gas predominantly consisting of methane and also containing nitrogen, comprising:

(a) supplying said natural gas stream at a pressure above atmospheric pressure,

(b) providing a multicomponent refrigeration fluid composed of a mixture of components each having different boiling points,

(c) compressing said multicomponent refrigeration fluid to a pressure within the range of about 250 to 1,200 psig,

(d) cooling and partially condensing said multicomponent refrigeration fluid by passing it through a compressor aftercooler in heat exchange with a cooling fluid,

(e) separating the liquid and vapor phases produced in the compressor aftercooler in a phase separator,

(f) condensing and subcooling the vapor from the phase separator in a heat exchange apparatus, expanding the stream to low pressure and vaporizing and reheating it in heat exchange with itself and other streams in the heat exchange apparatus,

(g) subcooling the liquid from the phase separator in the heat exchange apparatus, expanding it to low pressure, combining it with liquefied, expanded and reheated vapor from the phase separator,

(h) vaporizing and reheating the combined stream in the heat exchange apparatus by heat exchange with itself and other streams passing through the heat exchange apparatus,

(i) returning the vaporized and reheated stream for recompression according to step (c),

(j) liquefying at least the major portion of the natural gas stream in the heat exchange apparatus,

(k) expanding said liquefied natural gas to lower pressure in two or more stages in series, phase separating the gas and liquid phases produced during expansion, thereby concentrating the nitrogen into the gas phases and producing a methane-rich and nitrogen depleted liquefied natural gas, and

(l) reheating the gas phases enriched in nitrogen, and sending them out of the plant as nitrogen-enriched product streams.

12. The method as claimed in claim 11, in which the last stage of expansion of the liquid natural gas takes place in a liquid natural gas storage tank maintained slightly above atmospheric pressure.

13. The method as claimed in claim 12, in which the second to the last stage of expansion takes place at a pressure controlled just sufficiently high enough to be able to send the liquid collected in this phase separator to the storage tank.

14. The method as claimed in claim 11, which further comprises a step of recompressing some of the expansion gases to the pressure of the natural gas and recycling this gas into the natural gas being liquefied.

15. The method as claimed in claim 11, wherein said natural gas stream in step a) is supplied at a pressure of about 150 to 1,200 psig.

16. The method as claimed in claim 11, wherein said multicomponent refrigeration fluid is such that, when recycled between the two pressures, it is capable of cooling, liquefying and subcooling the natural gas and rejecting heat thus removed from the natural gas.

17. The method as claimed in claim 11, wherein said compression in step (c) is effected to a pressure of about 300 to 600 psia.

18. The method as claimed in claim 11, wherein said cooling fluid in step (d) is air or water.

19. The method as claimed in claim 11, wherein said stream expansion of step (f) is effected to a pressure of about 250 to 1,200 psig.

20. The method as claimed in claim 11, wherein said liquefied natural gas in step k) is expanded to a final lower pressure of about 30 to 0 psig.

21. The method as claimed in claim 11, wherein said multicomponent refrigeration fluid comprises nitrogen methane, ethylene, propane, butane and isopentane.

22. The method as claimed in claim 11, which further comprises recovering said nitrogen-enriched product streams.

23. The method as claimed in claim 11, wherein said natural gas stream in step a) is supplied at a pressure of about 50 to 1,200 psig.

24. The method as claimed in claim 11, wherein said natural gas stream in step (j) is cooled and liquified to a temperature between -100°

C. to -150°

C.

25. The method as claimed in claim 11, which further comprises using said nitrogen-enriched product streams as fuel gas.