Liquefied Natural Gas And Hydrocarbon Gas Processing

• US 20100287985A1
• Filed: 05/15/2009
• Published: 11/18/2010
• Est. Priority Date: 05/15/2009
• Status: Active Grant

• Current Assignee: Ortloff Enigneers, Ltd.
• Original Assignee: Ortloff Enigneers, Ltd.
• Inventors: Hudson, Hank M., Cuellar, Kyle T., Martinez, Tony L., Wilkinson, John D.
• Granted Patent: US 8,434,325 B2
• Time in Patent Office: Days
• US Class Current: 62/625
• CPC Class Codes: F25J 2200/02 in a single pressure main column system
• CPC Class Codes: F25J 2200/38 using pre-separation or distributed distillation before a main column system, e.g. in a at least a double column system
• CPC Class Codes: F25J 2200/50 using multiple (re-)boiler-condensers at different heights of the column
• CPC Class Codes: F25J 2200/78 Refluxing the column with a liquid stream originating from an upstream or downstream fractionator column
• CPC Class Codes: F25J 2205/02 using simple phase separation in a vessel or drum
• 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 2210/62 Liquefied natural gas [LNG]; Natural gas liquids [NGL]; Liquefied petroleum gas [LPG]
• CPC Class Codes: F25J 2230/08 Cold compressor, i.e. suction of the gas at cryogenic temperature and generally without afterstage-cooler
• CPC Class Codes: F25J 2230/60 the fluid being hydrocarbons or a mixture of hydrocarbons
• CPC Class Codes: F25J 2235/60 the fluid being (a mixture of) hydrocarbons
• 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 2270/904 by liquid or gaseous cryogen in an open loop
• CPC Class Codes: F25J 2290/40 Vertical layout or arrangement of cold equipments within in the cold box, e.g. columns, condensers, heat exchangers etc.
• CPC Class Codes: F25J 3/0209 Natural gas or substitute natural gas
• CPC Class Codes: F25J 3/0214 Liquefied 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

Abstract

A process for the recovery of heavier hydrocarbons from a liquefied natural gas (LNG) stream and a hydrocarbon gas stream is disclosed. The LNG feed stream is heated to vaporize at least part of it, then expanded and supplied to a fractionation column at a first mid-column feed position. The gas stream is expanded and cooled, then supplied to the column at a second mid-column feed position. A distillation vapor stream is withdrawn from the fractionation column below the mid-column feed positions and directed in heat exchange relation with the LNG feed stream, cooling the distillation vapor stream as it supplies at least part of the heating of the LNG feed stream. The distillation vapor stream is cooled sufficiently to condense at least a part of it, forming a condensed stream. At least a portion of the condensed stream is directed to the fractionation column as its top feed. A portion of the column overhead stream is also directed in heat exchange relation with the LNG feed stream, so that it also supplies at least part of the heating of the LNG feed stream as it is condensed to form a “lean” LNG stream. The quantities and temperatures of the feeds to the column are effective to maintain the column overhead temperature at a temperature whereby the major portion of the desired components is recovered in the bottom liquid product from the column.

Claims

1. A process for the separation of liquefied natural gas containing methane, C₂ components, and heavier hydrocarbon components and a gas stream containing methane, C₂ components, and heavier hydrocarbon components into a volatile residue gas fraction containing a major portion of said methane and said C₂ components and a relatively less volatile liquid fraction containing a major portion of said heavier hydrocarbon components wherein

(a) said liquefied natural gas is heated sufficiently to vaporize it, thereby forming a vapor stream;

(b) said vapor stream is expanded to lower pressure and is thereafter supplied to a distillation column at a first mid-column feed position;

(c) said gas stream is expanded to said lower pressure, is cooled, and is thereafter supplied to said distillation column at a second mid-column feed position;

(d) a distillation vapor stream is withdrawn from a region of said distillation column below said expanded vapor stream and said expanded cooled gas stream, whereupon said distillation vapor stream is cooled sufficiently to at least partially condense it, forming thereby a condensed stream and a stream containing any remaining vapor, with said cooling supplying at least a portion of said heating of said liquefied natural gas;

(e) at least a portion of said condensed stream is supplied to said distillation column as a reflux stream at a top column feed position;

(f) an overhead vapor stream is withdrawn from an upper region of said distillation column and divided into at least a first portion and a second portion, whereupon said second portion is compressed to higher pressure;

(g) said compressed second portion is cooled sufficiently to at least partially condense it and form thereby a volatile liquid stream, with said cooling supplying at least a portion of said heating of said liquefied natural gas;

(h) said volatile liquid stream is heated sufficiently to vaporize it, with said heating supplying at least a portion of said cooling of said expanded gas stream;

(i) said first portion is heated, with said heating supplying at least a portion of said cooling of said distillation vapor stream;

5. The process according to claim 1 or 2 wherein

(a) said gas stream is cooled, is expanded to said lower pressure, and is thereafter supplied to said distillation column at said second mid-column feed position;

(b) said distillation vapor stream is withdrawn from a region of said distillation column below said expanded vapor stream and said cooled expanded gas stream; and

(c) said volatile liquid stream is heated sufficiently to vaporize it, with said heating supplying at least a portion of said cooling of said gas stream.

8. The process according to claim 1, 2, 3, or 4 wherein

(a) said any remaining vapor stream and said heated first portion are combined to form a residue vapor stream;

and

(b) said residue vapor stream is compressed to higher pressure and thereafter combined with said vaporized volatile liquid stream to form said volatile residue gas fraction.

9. The process according to claim 1, 2, 3, 4, 6, or 7 wherein

(a) said condensed stream is divided into at least a first reflux stream and a second reflux stream;

(b) said first reflux stream is supplied to said distillation column at said top feed position; and

(c) said second reflux stream is supplied to said distillation column at a mid-column feed location in substantially the same region wherein said distillation vapor stream is withdrawn.

10. The process according to claim 5 wherein

(a) said condensed stream is divided into at least a first reflux stream and a second reflux stream;

(b) said first reflux stream is supplied to said distillation column at said top feed position; and

(c) said second reflux stream is supplied to said distillation column at a mid-column feed location in substantially the same region wherein said distillation vapor stream is withdrawn.

11. The process according to claim 8 wherein

(a) said condensed stream is divided into at least a first reflux stream and a second reflux stream;

(b) said first reflux stream is supplied to said distillation column at said top feed position; and

(c) said second reflux stream is supplied to said distillation column at a mid-column feed location in substantially the same region wherein said distillation vapor stream is withdrawn.

12. The process according to claim 1, 2, 3, 4, 6, or 7 wherein a distillation liquid stream is withdrawn from said distillation column at a location above the region wherein said distillation vapor stream is withdrawn, whereupon said distillation liquid stream is heated and said heated distillation liquid stream is thereafter redirected into said distillation column at a location below the region wherein said distillation vapor stream is withdrawn.

13. The process according to claim 5 wherein a distillation liquid stream is withdrawn from said distillation column at a location above the region wherein said distillation vapor stream is withdrawn, whereupon said distillation liquid stream is heated and said heated distillation liquid stream is thereafter redirected into said distillation column at a location below the region wherein said distillation vapor stream is withdrawn.

14. The process according to claim 8 wherein a distillation liquid stream is withdrawn from said distillation column at a location above the region wherein said distillation vapor stream is withdrawn, whereupon said distillation liquid stream is heated and said heated distillation liquid stream is thereafter redirected into said distillation column at a location below the region wherein said distillation vapor stream is withdrawn.

15. The process according to claim 9 wherein a distillation liquid stream is withdrawn from said distillation column at a location above the region wherein said distillation vapor stream is withdrawn, whereupon said distillation liquid stream is heated and said heated distillation liquid stream is thereafter redirected into said distillation column at a location below the region wherein said distillation vapor stream is withdrawn.

16. The process according to claim 10 wherein a distillation liquid stream is withdrawn from said distillation column at a location above the region wherein said distillation vapor stream is withdrawn, whereupon said distillation liquid stream is heated and said heated distillation liquid stream is thereafter redirected into said distillation column at a location below the region wherein said distillation vapor stream is withdrawn.

17. The process according to claim 11 wherein a distillation liquid stream is withdrawn from said distillation column at a location above the region wherein said distillation vapor stream is withdrawn, whereupon said distillation liquid stream is heated and said heated distillation liquid stream is thereafter redirected into said distillation column at a location below the region wherein said distillation vapor stream is withdrawn.

2. A process for the separation of liquefied natural gas containing methane, C₂ components, and heavier hydrocarbon components and a gas stream containing methane, C₂ components, and heavier hydrocarbon components into a volatile residue gas fraction containing a major portion of said methane and said C₂ components and a relatively less volatile liquid fraction containing a major portion of said heavier hydrocarbon components wherein

(a) said liquefied natural gas is heated sufficiently to partially vaporize it;

(b) said partially vaporized liquefied natural gas is separated thereby to provide a vapor stream and a liquid stream;

(c) said vapor stream is expanded to lower pressure and is thereafter supplied to a distillation column at a first mid-column feed position;

(d) said liquid stream is expanded to said lower pressure and thereafter supplied to said distillation column at a lower mid-column feed position;

(e) said gas stream is expanded to said lower pressure, is cooled, and is thereafter supplied to said distillation column at a second mid-column feed position;

(f) a distillation vapor stream is withdrawn from a region of said distillation column below said expanded vapor stream and said expanded cooled gas stream, whereupon said distillation vapor stream is cooled sufficiently to at least partially condense it, forming thereby a condensed stream and a stream containing any remaining vapor, with said cooling supplying at least a portion of said heating of said liquefied natural gas;

(g) at least a portion of said condensed stream is supplied to said distillation column as a reflux stream at a top column feed position;

(h) an overhead vapor stream is withdrawn from an upper region of said distillation column and divided into at least a first portion and a second portion, whereupon said second portion is compressed to higher pressure;

(i) said compressed second portion is cooled sufficiently to at least partially condense it and form thereby a volatile liquid stream, with said cooling supplying at least a portion of said heating of said liquefied natural gas;

(j) said volatile liquid stream is heated sufficiently to vaporize it, with said heating supplying at least a portion of said cooling of said expanded gas stream;

(k) said first portion is heated, with said heating supplying at least a portion of said cooling of said distillation vapor stream;

(l) said vaporized volatile liquid stream, said any remaining vapor stream, and said heated first portion are combined to form said volatile residue gas fraction containing a major portion of said methane and said C₂ components; and

(m) the quantity and temperature of said reflux stream and the temperatures of said feeds to said distillation column are effective to maintain the overhead temperature of said distillation column at a temperature whereby the major portion of said heavier hydrocarbon components is recovered in said relatively less volatile liquid fraction by fractionation in said distillation column.

3. A process for the separation of liquefied natural gas containing methane, C₂ components, and heavier hydrocarbon components and a gas stream containing methane, C₂ components, and heavier hydrocarbon components into a volatile residue gas fraction containing a major portion of said methane and said C₂ components and a relatively less volatile liquid fraction containing a major portion of said heavier hydrocarbon components wherein

(a) said liquefied natural gas is heated sufficiently to vaporize it, thereby forming a first vapor stream;

(b) said first vapor stream is expanded to lower pressure and is thereafter supplied to a distillation column at a first mid-column feed position;

(c) said gas stream is expanded to said lower pressure and is thereafter cooled sufficiently to partially condense it;

(d) said partially condensed gas stream is separated thereby to provide a second vapor stream and a liquid stream;

(e) said second vapor stream is supplied to said distillation column at a second mid-column feed position;

(f) said liquid stream is heated and is thereafter supplied to said distillation column at a lower mid-column feed position;

(g) a distillation vapor stream is withdrawn from a region of said distillation column below said expanded first vapor stream and said second vapor stream, whereupon said distillation vapor stream is cooled sufficiently to at least partially condense it, forming thereby a condensed stream and a stream containing any remaining vapor, with said cooling supplying at least a portion of said heating of said liquefied natural gas;

(h) at least a portion of said condensed stream is supplied to said distillation column as a reflux stream at a top column feed position;

(i) an overhead vapor stream is withdrawn from an upper region of said distillation column and divided into at least a first portion and a second portion, whereupon said second portion is compressed to higher pressure;

(j) said compressed second portion is cooled sufficiently to at least partially condense it and form thereby a volatile liquid stream, with said cooling supplying at least a portion of said heating of said liquefied natural gas;

(k) said volatile liquid stream is heated sufficiently to vaporize it, with said heating supplying at least a portion of said cooling of said expanded gas stream;

(l) said first portion is heated, with said heating supplying at least a portion of said cooling of said distillation vapor stream;

(m) said vaporized volatile liquid stream, said any remaining vapor stream, and said heated first portion are combined to form said volatile residue gas fraction containing a major portion of said methane and said C₂ components; and

(n) the quantity and temperature of said reflux stream and the temperatures of said feeds to said distillation column are effective to maintain the overhead temperature of said distillation column at a temperature whereby the major portion of said heavier hydrocarbon components is recovered in said relatively less volatile liquid fraction by fractionation in said distillation column.

6. The process according to claim 3 wherein

(a) said gas stream is cooled sufficiently to partially condense it;

thereby forming said second vapor stream and said liquid stream;

(b) said second vapor stream is expanded to said lower pressure and is thereafter supplied to said distillation column at said second mid-column feed position;

(c) said liquid stream is expanded to said lower pressure, is heated, and is thereafter supplied to said distillation column at said lower mid-column feed position;

(d) said distillation vapor stream is withdrawn from a region of said distillation column below said expanded first vapor stream and said expanded second vapor stream; and

(e) said volatile liquid stream is heated sufficiently to vaporize it, with said heating supplying at least a portion of said cooling of said gas stream.

4. A process for the separation of liquefied natural gas containing methane, C₂ components, and heavier hydrocarbon components and a gas stream containing methane, C₂ components, and heavier hydrocarbon components into a volatile residue gas fraction containing a major portion of said methane and said C₂ components and a relatively less volatile liquid fraction containing a major portion of said heavier hydrocarbon components wherein

(a) said liquefied natural gas is heated sufficiently to partially vaporize it;

(b) said partially vaporized liquefied natural gas is separated thereby to provide a first vapor stream and a first liquid stream;

(c) said first vapor stream is expanded to lower pressure and is thereafter supplied to a distillation column at a first mid-column feed position;

(d) said first liquid stream is expanded to said lower pressure and thereafter supplied to said distillation column at a first lower mid-column feed position;

(e) said gas stream is expanded to said lower pressure and is thereafter cooled sufficiently to partially condense it;

(f) said partially condensed gas stream is separated thereby to provide a second vapor stream and a second liquid stream;

(g) said second vapor stream is supplied to said distillation column at a second mid-column feed position;

(h) said second liquid stream is heated and is thereafter supplied to said distillation column at a second lower mid-column feed position;

(i) a distillation vapor stream is withdrawn from a region of said distillation column below said expanded first vapor stream and said second vapor stream, whereupon said distillation vapor stream is cooled sufficiently to at least partially condense it, forming thereby a condensed stream and a stream containing any remaining vapor, with said cooling supplying at least a portion of said heating of said liquefied natural gas;

(j) at least a portion of said condensed stream is supplied to said distillation column as a reflux stream at a top column feed position;

(k) an overhead vapor stream is withdrawn from an upper region of said distillation column and divided into at least a first portion and a second portion, whereupon said second portion is compressed to higher pressure;

(l) said compressed second portion is cooled sufficiently to at least partially condense it and form thereby a volatile liquid stream, with said cooling supplying at least a portion of said heating of said liquefied natural gas;

(m) said volatile liquid stream is heated sufficiently to vaporize it, with said heating supplying at least a portion of said cooling of said expanded gas stream;

(n) said first portion is heated, with said heating supplying at least a portion of said cooling of said distillation vapor stream;

(o) said vaporized volatile liquid stream, said any remaining vapor stream, and said heated first portion are combined to form said volatile residue gas fraction containing a major portion of said methane and said C₂ components; and

(p) the quantity and temperature of said reflux stream and the temperatures of said feeds to said distillation column are effective to maintain the overhead temperature of said distillation column at a temperature whereby the major portion of said heavier hydrocarbon components is recovered in said relatively less volatile liquid fraction by fractionation in said distillation column.

7. The process according to claim 4 wherein

(a) said gas stream is cooled sufficiently to partially condense it;

thereby forming said second vapor stream and said second liquid stream;

(b) said second vapor stream is expanded to said lower pressure and is thereafter supplied to said distillation column at said second mid-column feed position;

(c) said second liquid stream is expanded to said lower pressure, is heated, and is thereafter supplied to said distillation column at said second lower mid-column feed position;

(d) said distillation vapor stream is withdrawn from a region of said distillation column below said expanded first vapor stream and said expanded second vapor stream; and

(e) said volatile liquid stream is heated sufficiently to vaporize it, with said heating supplying at least a portion of said cooling of said gas stream.

18. A process for the separation of liquefied natural gas containing methane, C₂ components, and heavier hydrocarbon components and a gas stream containing methane, C₂ components, and heavier hydrocarbon components into a volatile residue gas fraction containing a major portion of said methane and said C₂ components and a relatively less volatile liquid fraction containing a major portion of said heavier hydrocarbon components wherein

(a) said liquefied natural gas is heated sufficiently to vaporize it, thereby forming a vapor stream;

(b) said vapor stream is expanded to lower pressure and is thereafter supplied at a first lower feed position to an absorber column that produces an overhead vapor stream and a bottom liquid stream;

(c) said gas stream is expanded to said lower pressure, is cooled, and is thereafter supplied to said absorber column at a second lower feed position;

(d) said bottom liquid stream is supplied to a stripper column at a top column feed position;

(e) a distillation vapor stream is withdrawn from an upper region of said stripper column, whereupon said distillation vapor stream is cooled sufficiently to at least partially condense it, forming thereby a condensed stream and a stream containing any remaining vapor, with said cooling supplying at least a portion of said heating of said liquefied natural gas;

(f) at least a portion of said condensed stream is supplied to said absorber column as a reflux stream at a top column feed position;

(g) said overhead vapor stream is divided into at least a first portion and a second portion, whereupon said second portion is compressed to higher pressure;

(h) said compressed second portion is cooled sufficiently to at least partially condense it and form thereby a volatile liquid stream, with said cooling supplying at least a portion of said heating of said liquefied natural gas;

(i) said volatile liquid stream is heated sufficiently to vaporize it, with said heating supplying at least a portion of said cooling of said expanded gas stream;

(j) said first portion is heated, with said heating supplying at least a portion of said cooling of said distillation vapor stream;

(k) said vaporized volatile liquid stream, said any remaining vapor stream, and said heated first portion are combined to form said volatile residue gas fraction containing a major portion of said methane and said C₂ components; and

(l) the quantity and temperature of said reflux stream and the temperatures of said feeds to said absorber column and said stripper column are effective to maintain the overhead temperatures of said absorber column and said stripper column at temperatures whereby the major portion of said heavier hydrocarbon components is recovered in said relatively less volatile liquid fraction by fractionation in said absorber column and said stripper column.

22. The process according to claim 18 or 19 wherein

(a) said gas stream is cooled, is expanded to said lower pressure, and is thereafter supplied to said absorber column at said second lower feed position;

and

(b) said volatile liquid stream is heated sufficiently to vaporize it, with said heating supplying at least a portion of said cooling of said gas stream.

25. The process according to claim 18, 19, 20, or 21 wherein

(a) said any remaining vapor stream and said heated first portion are combined to form a residue vapor stream;

and

(b) said residue vapor stream is compressed to higher pressure and thereafter combined with said vaporized volatile liquid stream to form said volatile residue gas fraction.

26. The process according to claim 18, 19, 20, 21, 23, or 24 wherein

(a) said condensed stream is divided into at least a first reflux stream and a second reflux stream;

(b) said first reflux stream is supplied to said absorber column at said top feed position;

(c) said bottom liquid stream is supplied to said stripper column at an upper mid-column feed position; and

(d) said second reflux stream is supplied to said stripper column at said top column feed position.

27. The process according to claim 22 wherein

(a) said condensed stream is divided into at least a first reflux stream and a second reflux stream;

(b) said first reflux stream is supplied to said absorber column at said top feed position;

(c) said bottom liquid stream is supplied to said stripper column at an upper mid-column feed position; and

(d) said second reflux stream is supplied to said stripper column at said top column feed position.

28. The process according to claim 25 wherein

(a) said condensed stream is divided into at least a first reflux stream and a second reflux stream;

(b) said first reflux stream is supplied to said absorber column at said top feed position;

(c) said bottom liquid stream is supplied to said stripper column at an upper mid-column feed position; and

(d) said second reflux stream is supplied to said stripper column at said top column feed position.

29. The process according to claim 18, 19, 20, 21, 23, or 24 wherein at least a portion of said bottom liquid stream is heated before said bottom liquid stream is supplied to said stripper column at said top column feed position.

30. The process according to claim 22 wherein at least a portion of said bottom liquid stream is heated before said bottom liquid stream is supplied to said stripper column at said top column feed position.

31. The process according to claim 25 wherein at least a portion of said bottom liquid stream is heated before said bottom liquid stream is supplied to said stripper column at said top column feed position.

32. The process according to claim 26 wherein at least a portion of said bottom liquid stream is heated before said bottom liquid stream is supplied to said stripper column at said upper mid-column feed position.

33. The process according to claim 27 wherein at least a portion of said bottom liquid stream is heated before said bottom liquid stream is supplied to said stripper column at said upper mid-column feed position.

34. The process according to claim 28 wherein at least a portion of said bottom liquid stream is heated before said bottom liquid stream is supplied to said stripper column at said upper mid-column feed position.

19. A process for the separation of liquefied natural gas containing methane, C₂ components, and heavier hydrocarbon components and a gas stream containing methane, C₂ components, and heavier hydrocarbon components into a volatile residue gas fraction containing a major portion of said methane and said C₂ components and a relatively less volatile liquid fraction containing a major portion of said heavier hydrocarbon components wherein

(a) said liquefied natural gas is heated sufficiently to partially vaporize it;

(b) said partially vaporized liquefied natural gas is separated thereby to provide a vapor stream and a liquid stream;

(c) said vapor stream is expanded to lower pressure and is thereafter supplied at a first lower feed position to an absorber column that produces an overhead vapor stream and a bottom liquid stream;

(d) said gas stream is expanded to said lower pressure, is cooled, and is thereafter supplied to said absorber column at a second lower feed position;

(e) said bottom liquid stream is supplied to a stripper column at a top column feed position;

(f) said liquid stream is expanded to said lower pressure and thereafter supplied to said stripper column at a mid-column feed position;

(g) a distillation vapor stream is withdrawn from an upper region of said stripper column, whereupon said distillation vapor stream is cooled sufficiently to at least partially condense it, forming thereby a condensed stream and a stream containing any remaining vapor, with said cooling supplying at least a portion of said heating of said liquefied natural gas;

(h) at least a portion of said condensed stream is supplied to said absorber column as a reflux stream at a top column feed position;

(i) said overhead vapor stream is divided into at least a first portion and a second portion, whereupon said second portion is compressed to higher pressure;

(j) said compressed second portion is cooled sufficiently to at least partially condense it and form thereby a volatile liquid stream, with said cooling supplying at least a portion of said heating of said liquefied natural gas;

(k) said volatile liquid stream is heated sufficiently to vaporize it, with said heating supplying at least a portion of said cooling of said expanded gas stream;

(l) said first portion is heated, with said heating supplying at least a portion of said cooling of said distillation vapor stream;

(m) said vaporized volatile liquid stream, said any remaining vapor stream, and said heated first portion are combined to form said volatile residue gas fraction containing a major portion of said methane and said C₂ components; and

(n) the quantity and temperature of said reflux stream and the temperatures of said feeds to said absorber column and said stripper column are effective to maintain the overhead temperatures of said absorber column and said stripper column at temperatures whereby the major portion of said heavier hydrocarbon components is recovered in said relatively less volatile liquid fraction by fractionation in said absorber column and said stripper column.

20. A process for the separation of liquefied natural gas containing methane, C₂ components, and heavier hydrocarbon components and a gas stream containing methane, C₂ components, and heavier hydrocarbon components into a volatile residue gas fraction containing a major portion of said methane and said C₂ components and a relatively less volatile liquid fraction containing a major portion of said heavier hydrocarbon components wherein

(a) said liquefied natural gas is heated sufficiently to vaporize it, thereby forming a first vapor stream;

(b) said first vapor stream is expanded to lower pressure and is thereafter supplied at a first lower feed position to an absorber column that produces an overhead vapor stream and a bottom liquid stream;

(c) said gas stream is expanded to said lower pressure and is thereafter cooled sufficiently to partially condense it;

(d) said partially condensed gas stream is separated thereby to provide a second vapor stream and a liquid stream;

(e) said second vapor stream is supplied to said distillation column at a second lower feed position;

(f) said bottom liquid stream is supplied to a stripper column at a top column feed position;

(g) said liquid stream is heated and is thereafter supplied to said stripper column at a mid-column feed position;

(h) a distillation vapor stream is withdrawn from an upper region of said stripper column, whereupon said distillation vapor stream is cooled sufficiently to at least partially condense it, forming thereby a condensed stream and a stream containing any remaining vapor, with said cooling supplying at least a portion of said heating of said liquefied natural gas;

(i) at least a portion of said condensed stream is supplied to said absorber column as a reflux stream at a top column feed position;

(j) said overhead vapor stream is divided into at least a first portion and a second portion, whereupon said second portion is compressed to higher pressure;

(k) said compressed second portion is cooled sufficiently to at least partially condense it and form thereby a volatile liquid stream, with said cooling supplying at least a portion of said heating of said liquefied natural gas;

(l) said volatile liquid stream is heated sufficiently to vaporize it, with said heating supplying at least a portion of said cooling of said expanded gas stream;

(m) said first portion is heated, with said heating supplying at least a portion of said cooling of said distillation vapor stream;

(n) said vaporized volatile liquid stream, said any remaining vapor stream, and said heated first portion are combined to form said volatile residue gas fraction containing a major portion of said methane and said C₂ components; and

(o) the quantity and temperature of said reflux stream and the temperatures of said feeds to said absorber column and said stripper column are effective to maintain the overhead temperatures of said absorber column and said stripper column at temperatures whereby the major portion of said heavier hydrocarbon components is recovered in said relatively less volatile liquid fraction by fractionation in said absorber column and said stripper column.

23. The process according to claim 20 wherein

(a) said gas stream is cooled sufficiently to partially condense it;

thereby forming said second vapor stream and said liquid stream;

(b) said second vapor stream is expanded to said lower pressure and is thereafter supplied to said absorber column at said second lower feed position;

(c) said liquid stream is expanded to said lower pressure, is heated, and is thereafter supplied to said stripper column at said mid-column feed position; and

(d) said volatile liquid stream is heated sufficiently to vaporize it, with said heating supplying at least a portion of said cooling of said gas stream.

21. A process for the separation of liquefied natural gas containing methane, C₂ components, and heavier hydrocarbon components and a gas stream containing methane, C₂ components, and heavier hydrocarbon components into a volatile residue gas fraction containing a major portion of said methane and said C₂ components and a relatively less volatile liquid fraction containing a major portion of said heavier hydrocarbon components wherein

(a) said liquefied natural gas is heated sufficiently to partially vaporize it;

(b) said partially vaporized liquefied natural gas is separated thereby to provide a first vapor stream and a first liquid stream;

(c) said first vapor stream is expanded to lower pressure and is thereafter supplied at a first lower feed position to an absorber column that produces an overhead vapor stream and a bottom liquid stream;

(d) said gas stream is expanded to said lower pressure and is thereafter cooled sufficiently to partially condense it;

(e) said partially condensed gas stream is separated thereby to provide a second vapor stream and a second liquid stream;

(f) said second vapor stream is supplied to said distillation column at a second lower feed position;

(g) said bottom liquid stream is supplied to a stripper column at a top column feed position;

(h) said first liquid stream is expanded to said lower pressure and thereafter supplied to said stripper column at a first mid-column feed position;

(i) said second liquid stream is heated and is thereafter supplied to said stripper column at a second mid-column feed position;

(j) a distillation vapor stream is withdrawn from an upper region of said stripper column, whereupon said distillation vapor stream is cooled sufficiently to at least partially condense it, forming thereby a condensed stream and a stream containing any remaining vapor, with said cooling supplying at least a portion of said heating of said liquefied natural gas;

(k) at least a portion of said condensed stream is supplied to said absorber column as a reflux stream at a top column feed position;

(l) said overhead vapor stream is divided into at least a first portion and a second portion, whereupon said second portion is compressed to higher pressure;

(m) said compressed second portion is cooled sufficiently to at least partially condense it and form thereby a volatile liquid stream, with said cooling supplying at least a portion of said heating of said liquefied natural gas;

(n) said volatile liquid stream is heated sufficiently to vaporize it, with said heating supplying at least a portion of said cooling of said expanded gas stream;

(o) said first portion is heated, with said heating supplying at least a portion of said cooling of said distillation vapor stream;

(p) said vaporized volatile liquid stream, said any remaining vapor stream, and said heated first portion are combined to form said volatile residue gas fraction containing a major portion of said methane and said C₂ components; and

(q) the quantity and temperature of said reflux stream and the temperatures of said feeds to said absorber column and said stripper column are effective to maintain the overhead temperatures of said absorber column and said stripper column at temperatures whereby the major portion of said heavier hydrocarbon components is recovered in said relatively less volatile liquid fraction by fractionation in said absorber column and said stripper column.

24. The process according to claim 21 wherein

(a) said gas stream is cooled sufficiently to partially condense it;

thereby forming said second vapor stream and said second liquid stream;

(b) said second vapor stream is expanded to said lower pressure and is thereafter supplied to said absorber column at said second lower feed position;

(c) said second liquid stream is expanded to said lower pressure, is heated, and is thereafter supplied to said stripper column at said second mid-column feed position; and

(d) said volatile liquid stream is heated sufficiently to vaporize it, with said heating supplying at least a portion of said cooling of said gas stream.