Liquefied natural gas and hydrocarbon gas processing

• US 8,794,030 B2
• Filed: 03/08/2013
• Issued: 08/05/2014
• Est. Priority Date: 05/15/2009
• Status: Expired due to Fees

• Current Assignee: Ortloff Enigneers, Ltd.
• Original Assignee: Ortloff Enigneers, Ltd.
• Inventors: Martinez, Tony L., Wilkinson, John D., Hudson, Hank M., Cuellar, Kyle T.
• Primary Examiner(s): Pettitt, John F
• Assistant Examiner(s): LANDEROS, IGNACIO EMMANUEL
• Application Number:
  US13/790,873
• Publication Number:
  US 20130283853A1
• Time in Patent Office: 515 Days
• Field of Search: 626/17, 626/18, 626/20, 626/30, 626/32
• US Class Current: 62/621
• CPC Class Codes: F25J 2200/02 in a single pressure main column system
• CPC Class Codes: F25J 2200/30 using a side column in a single pressure 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 2200/72 Refluxing the column with at least a part of the totally condensed overhead gas
• CPC Class Codes: F25J 2200/76 Refluxing the column with condensed overhead gas being cycled in a quasi-closed loop refrigeration cycle
• 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 2210/06 Splitting of the feed stream, e.g. for treating or cooling in different ways
• 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 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 2290/50 Arrangement of multiple equipments fulfilling the same process step in parallel
• 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
• CPC Class Codes: F25J 3/0615 : Liquefied natural gas

Abstract

A process for recovering heavier hydrocarbons from a liquefied natural gas (LNG) stream and a hydrocarbon gas stream is disclosed. The LNG stream is heated to vaporize at least part of it, expanded, and supplied to a fractionation column at a first mid-column feed position. The gas stream is expanded, cooled, and supplied to the column at a second mid-column feed position. A distillation vapor stream is withdrawn from the column below the mid-column feed positions and cooled by the LNG stream sufficiently to condense at least a part of it, with at least a portion of the condensed stream directed to the column at an upper mid-column feed position. A portion of the column overhead stream is cooled by the LNG feed stream to condense it and form both a “lean” LNG stream and a reflux stream that is supplied to the column at a top column feed position.

Claims

1. A process for the separation of liquefied natural gas containing methane and heavier hydrocarbon components and a gas stream containing methane and heavier hydrocarbon components into a volatile residue gas fraction containing a major portion of said methane 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 and form thereby a first condensed stream, with said cooling supplying at least a portion of said heating of said liquefied natural gas;

(e) at least a portion of said first condensed stream is supplied to said distillation column at an upper mid-column feed position;

(f) an overhead distillation 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 first portion is compressed to higher pressure;

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

(h) said second condensed stream is divided into at least a volatile liquid stream and a reflux stream;

(i) said reflux stream is further cooled, with said cooling supplying at least a portion of said heating of said liquefied natural gas;

(j) said further cooled reflux stream is supplied to said distillation column at a top column feed position;

(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 second portion is heated, with said heating supplying at least a portion of said cooling of said expanded gas stream;

(m) said vaporized volatile liquid stream and said heated second portion are combined to form said volatile residue gas fraction containing a major portion of said methane; 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.

2. The process according to claim 1, 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 said vapor stream and a liquid stream; and

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

3. The process according to claim 1, wherein

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

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

(c) said further vapor stream is cooled and thereafter supplied to said distillation column at said second mid-column feed position;

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

(e) said distillation vapor stream is withdrawn from a region of said distillation column below said expanded˜

vapor stream and said cooled further vapor stream.

4. The process according to claim 1, 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 said vapor stream and a first liquid stream;

(c) 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;

(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 further vapor stream and a second liquid stream;

(f) said further vapor stream is cooled and thereafter supplied to said distillation column at said second mid-column feed position;

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

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

(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; and

(d) said second portion is heated, with said heating supplying at least a portion of said cooling of said gas stream.

6. The process according to claim 3 wherein

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

thereby forming said further vapor stream and said liquid stream;

(b) said further 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 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 vapor stream and said expanded further vapor stream;

(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; and

(f) said second portion is heated, with said heating supplying at least a portion of said cooling of said gas stream.

7. The process according to claim 4 wherein

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

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

(b) said further 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 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 further vapor stream;

(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; and

(f) said second portion is heated, 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 second portion is compressed to higher pressure;

(b) said compressed second portion is heated, with said heating supplying at least a portion of said cooling of said expanded gas stream; and

(c) said vaporized volatile liquid stream and said heated compressed second portion are combined to form said volatile residue gas fraction.

9. The process according to claim 1, 2, 3, 4, 6, or 7 wherein said volatile residue gas fraction contains a major portion of said methane and C2 components.

10. The process according to claim 5 wherein said volatile residue gas fraction contains a major portion of said methane and C₂ components.

11. The process according to claim 8 wherein said volatile residue gas fraction contains a major portion of said methane and C₂ components.