GB2522421A - LNG production process - Google Patents

LNG production process Download PDF

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Publication number
GB2522421A
GB2522421A GB1401073.0A GB201401073A GB2522421A GB 2522421 A GB2522421 A GB 2522421A GB 201401073 A GB201401073 A GB 201401073A GB 2522421 A GB2522421 A GB 2522421A
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Prior art keywords
stream
gas
heat exchanger
bar
gas stream
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GB1401073.0A
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GB2522421B (en
GB201401073D0 (en
Inventor
Anthony Dwight Maunder
Geoffrey Frederick Skinner
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Gasconsult Ltd
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Gasconsult Ltd
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Priority to GB1401073.0A priority Critical patent/GB2522421B/en
Publication of GB201401073D0 publication Critical patent/GB201401073D0/en
Priority to PCT/GB2015/000006 priority patent/WO2015110779A2/en
Publication of GB2522421A publication Critical patent/GB2522421A/en
Application granted granted Critical
Publication of GB2522421B publication Critical patent/GB2522421B/en
Expired - Fee Related legal-status Critical Current
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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0035—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0035—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work
    • F25J1/0037—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work of a return stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0201—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using only internal refrigeration means, i.e. without external refrigeration
    • F25J1/0202—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using only internal refrigeration means, i.e. without external refrigeration in a quasi-closed internal refrigeration loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/60—Natural gas or synthetic natural gas [SNG]
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/60—Methane
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/04—Internal refrigeration with work-producing gas expansion loop
    • F25J2270/06—Internal refrigeration with work-producing gas expansion loop with multiple gas expansion loops

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

A process comprising cooling a methane rich gas stream 1 in a first heat exchanger A, dividing the cooled stream into at least two parts 4, 11, passing the first part into a gas expander B, reheating the expander outlet stream 5 in a first cold passage of a second heat exchanger C and in a first cold passage of the first exchanger A, at least partially compressing D and recycling 10 the reheated expander outlet stream. The second part 11 of the stream is cooled in the second heat exchanger C to form a condensed stream 12, the next steps are passing the condensed stream to a pressure reduction turbine F, separating G the outlet stream from the pressure reduction turbine into liquid 14 and vapour 15 fractions, reheating the vapour fraction in a second cold passage of the second heat exchanger C and in a second cold passage of the first exchanger A, at least partially compressing H and recycling 21 the reheated vapour fraction, collecting the liquid fraction 14 for use as product. The product is a methane-rich liquid.

Description

I
Description
LNG Production Process
S Field of the Invention
This invention relates to a process for liquefying a methane-rich gas and more particularly but not exclusively relates to a method of producing liquefied natural gas (LNG) comprising a gas expander and a liquid pressure reduction machine or turbine.
Backciround to the Invention A market is emerging for small-scale liquefaction of natural gas for local use, for instance as a transportation fuel, especially for heavy goods vehicles.
As these small liquefaction units are usually required to operate without the presence of an attendant, liquefaction processes requiring evaporation and storage of liquid hydrocarbon refrigerants are not very suitable, particularly on grounds of safety.
Consequently, liquefaction processes based on use of methane or nitrogen gas expanders have been preferred for these small unmanned liquefiers.
However such gas expander liquefaction processes based on use of a methane or nitrogen expander generally have a low thermal efficiency, requiring substantially more compression power per unit of LNG produced when compared with large base-load LNG plants.
Summary of the Invention
S According to the present invention there is provided a process for the production of a methane-rich liquid which comprises 1) providing a methane-rich gas stream having a pressure of from 40 bar to bar (4 MPa to 12 MPa), which typically has a temperature of from -10 to o 60°C, 2) cooling said gas stream in a first heat exchanger by at least 10°C, 3) dividing the gas stream from step 2 into at least first and second parts, 4) passing said first part through a gas expansion machine or turbine having an outlet pressure of from 3 bar to 20 bar (0.3 MPa to 2MPa) and an outlet temperature of from -70 to -130°C, 5) passing the outlet stream from step 4) successively through a second heat exchanger and the first heat exchanger, and 6) at least partially recycling said stream from step 5), wherein: 7) the second part from step 3) is cooled in the second heat exchanger to a temperature in the range -70 to -130°C, at which it is substantially condensed, 8) passing the liquid fraction of the cooled gas stream from the second heat S exchanger through a pressure reduction machine or turbine having an outlet pressure in the range 1 bar to 20 bar (0.1 MPa to 2 MPa), 9) separating the two phase stream from said pressure reduction machine or turbine into a methane-rich liquid product and a vapour, and optionally, 10) passing the outlet vapour stream from step 9) successively through the second heat exchanger and first heat exchanger, and optionally 11) at least partially recycling said stream from step 10).
The present invention describes a natural gas liquefaction process comprising a step of expanding a methane rich gas in an expansion machine or turbine and a second step of reducing the pressure of a methane rich liquid through a pressure reduction machine or turbine, thereby materially reducing the compression power required per unit of LNG produced compared with a process comprising a gas expansion machine or turbine alone.
Small scale LNG production units frequently are required to deliver the liquefied product at above atmospheric pressure, and accordingly the invention described herein produces liquid typically at a pressure of around 3 bar (0.3MPa). The invention may however be adapted to produce LNG product at nearer to atmospheric pressure, as outlined in the Description below.
S
Where pressures are referred to, these are absolute values.
Description of Preferred Embodiments
O Reference is made to the accompanying Figurel.
A feed stream of methane rich gas (1) with acid gases and water vapour substantially removed, a pressure typically between 40 bar and 120 bar (4 MPa and 12 MPa) and a temperature generally between -20 and 60°C, S typically between 10 and 50°C, is mixed with a recycle gas (10) described below. The resulting mixture (2) is cooled by at least 10°C in a passage of a first heat exchanger (A). For instance, if the first heat exchanger inlet temperature is 42°C, the corresponding outlet from the exchanger would be around -7°C, if the inlet temperature is 0°C the outlet would be around -20°C and if -10°C the outlet would be around -24°C. Thus as the feed plus recycle temperature drops, so does the duty of the first heat exchanger.
The cooled mixture (3) is then divided. One part (4) is admitted to an expansion machine or turbine (B), having outlet pressure typically between 3 bar and 20 bar (0.3 MPa and 2 MPa) and outlet temperature typically between -80 and -110°C. This stream (5) is reheated in a first cold passage of a second heat exchanger (C) and then further reheated (6) in a first cold passage of heat exchanger (A). The reheated stream (7) having a temperature close to the temperature of the inlet gas stream to the first heat exchanger (2) is mixed with compressed flash gas (21) described below and flows (8) to a recycle compressor (D). The compressor outlet stream (9) is cooled (10) in a recycle cooler (E) to form the above mentioned recycle gas.
0 Some variations of the above described flow scheme are foreseen, as instances: 1. the feed gas (1) may be introduced by mixing with stream (8) or at an intermediate pressure in compressor (D); 2. the recycle gas (10) may be cooled separately from the feed gas (1) in b a second hot passage in heat exchanger (A) and then divided, one part flowing to expansion turbine (B) and another part being combined with the cooled feed gas (3); 3. if the feed gas (1) has a significant content of C3+ hydrocarbon, this may in part be removed by a separator typically provided downstream of heat exchanger (A); 4. where a external demand exists for medium pressure fuel gas, this may be extracted from streams (7) or (8); 5. any part or all of the feed and/or compressor suction and/or recycle streams may be cooled separately, or after mixing (2), typically to a temperature of between 10 to -20°C before entering heat exchanger A, by means of an absorption chiller or a mechanical refrigeration cycle or a combination thereof.
S Another part (11) of the above mentioned cooled mixture (3) is cooled in a passage of second heat exchanger (C), emerging as a condensed liquid or cooled supercritical fluid at a temperature (12) typically between -80°C and - 110°C. This stream flows to a pressure reduction machine or turbine (F), emerging (13) at a pressure between 1 bar and 10 bar (0.1 MPa and 1.0 0 MPa).
This two-phase stream flows to vapour/liquid separator (G). The vapour (15) is reheated in a second cold passage of heat exchanger (C) and then is further reheated (16) in a second cold passage of heat exchanger (A) S emerging (17) at a temperature close to the temperature of the mixture of feed gas and recycle gas (2). Stream (17) may optionally be discharged from the process (18), for instance for use as a fuel, or compressed all or in part (19) in a flash gas compressor (H). The compressed stream (20) is cooled (21) in a flash gas cooler (I) and mixed with recycle gas (7) as described above.
The liquid phase (14) may comprise the liquefied methane rich product from the process. This liquefied methane stream may be further depressurised in a valve or expansion machine or turbine, for instance into an atmospheric pressure storage tank. The resulting low pressure flash gas may be reheated in a third cold passage of heat exchanger (C) and then further reheated in a third cold passage of heat exchanger (A) emerging at a temperature close to the temperature of the mixture of feed gas and recycle gas (2).
S The aforementioned first and second heat exchangers may be combined into a single heat exchange unit such as a brazed aluminium plate4in core construction, such single heat exchange unit containing internal streams corresponding to streams 3), 6), 11) and 16) in Fig. 1 with a stream corresponding to stream 4) taken out of the heat exchange unit at an O intermediate point as also shown in Fig.1.
A typical set of values of pressure and temperature for streams in Figure 1 are as below.
Name 1 2 3 4 5 6 Pressure (bar) 65.0 65.0 64.6 64.6 12.0 11.9 Temperature (C) 45.0 42.5 -6.9 -6.9 -90.6 -32.9 Name 7 8 9 10 11 12 Pressure (bar) 11.7 11.7 65.3 65.0 64.6 64.4 Temperature (C) 39.5 39.8 80.3 42.0 -6.9 -88.6 Name 13 14 15 16 17 18 Pressure (bar) 3.00 3.00 3.00 2.98 2.95 2.95 Temperature (C) -147.1 -147.1 -147.1 -32.9 39.5 39.5 Name 19 20 21 Pressure (bar) 2.95 11.8 11.7 Temperature (C) 39.5 98.0 42.0 Any part or all of the feed (1), recycle gas (10), mixture thereof (2) and/or compressor suction streams may be cooled by means of external refrigeration system, such as an absorption refrigeration cycle or a mechanical refrigeration cycle. In the case of an absorption refrigeration cycle, the heat requirement of the refrigeration system may be supplied by the exhaust heat of a gas engine S or a gas turbine, such gas engines or turbines typically being used for supplying power to the process compressors. The said cooling of either feed and/or recycle streams and/or compressor suction streams by means of an external refrigeration system may be combined with removal of carbon dioxide and/or other impurities from the feed gas.

Claims (16)

  1. Claims 1. A process for the production of a methane-rich liquid which comprises 1) providing a methane-rich gas stream having a pressure of from 40 bar to bar (4 MPa to 12 MPa), 2) cooling said gas stream in a first heat exchanger by at least 10°C, O 3) dividing the gas stream from step 2) into at least first and second parts, 4) passing said first part through a gas expansion machine or turbine having an outlet pressure of from 3 bar to 20 bar (0.3 MPa to 2MPa) and an outlet temperature of from -70 to -130°C, 5) passing the outlet stream from step 4) successively through a second heat exchanger and the first heat exchanger, and 6) at least partially recycling said stream from step 5), wherein: 7) the second part from step 3) is cooled in the second heat exchanger to a temperature in the range -70 to -130°C, at which it is substantially condensed, 8) passing the liquid fraction of the cooled gas stream from the second heat exchanger through a pressure reduction machine or turbine having an outlet pressure in the range 1 bar to 20 bar (0.1 MPa to 2 MPa), 9) separating the two phase stream from said pressure reduction machine or turbine into the methane-rich liquid product and a vapour.S
  2. 2. A process as claimed in Claim 1 in which the temperature of the gas stream in step 1) is in the range from -10 to 60°C.
  3. 3. A process as claimed in Claim 1 or Claim 2 in which the stream from step 0 5) is compressed and mixed with the stream from step 1).
  4. 4. A process as claimed in Claim 1 or Claim 2 in which the stream from step 5) is mixed with a gas stream that is compressed to provide the stream of step 1).
  5. 5. A process as claimed in Claim 1 or Claim 2 in which the stream from step 5) is compressed and then cooled separately from the gas stream in step 2) in the first heat exchanger and then divided into two parts; a first part passing to the gas expansion machine or turbine of step 4) and a second part being combined with said second part of step 3).
  6. 6. A process as claimed in any preceding claim in which the gas stream of step 1) comprises a significant content of Cye-hydrocarbon which is removed from the gas stream downstream of the first heat exchanger.
  7. 7. A process as claimed in any preceding claim in which at least a part of the gas stream from step 5) is used as fuel gas.
  8. 8. A process as claimed in Claim 7 in which the gas stream from step 5) is discharged from the process and/or compressed and recycled.
  9. 9. A process as claimed in any preceding claim in which the vapour fraction from step 9) is passed successively through the second heat exchanger and O the first heat exchanger.
  10. 10. A process as claimed in any preceding claim in which part of the vapour gas stream from step 9) is used as fuel gas.
  11. 11. A process as claimed in any preceding claim in which the said first exchanger cold outlet temperature is in the range of 0°C to -30°C.
  12. 12. A process as claimed in any preceding claim in which the said second exchanger cold outlet temperature is in the range of -80°C to -110°C.
  13. 13. A process as claimed in any preceding claim in which the said gas expansion machine or turbine has outlet pressure in the range 3 bar to 20 bar (0.3 MPa to 2 MPa) and an outlet temperature of from -80°C to -110°C.
  14. 14. A process as claimed in any preceding claim in which any part or all of the feed and/or compressor suction and/or recycle streams is cooled by means of an external refrigeration cycle.
  15. 15. A process as claimed in any preceding claim in which the heat requirement for an absorption refrigeration system is supplied by gas engine or gas turbine exhaust heat, such gas engines or turbines which may be used for supplying power to the process compressors.O
  16. 16. A process as claimed in any preceding claim wherein such cooling of either feed and/or compressor suction and/or recycle streams is combined with removal of carbon dioxide and/or other impurities.
GB1401073.0A 2014-01-22 2014-01-22 LNG production process Expired - Fee Related GB2522421B (en)

Priority Applications (2)

Application Number Priority Date Filing Date Title
GB1401073.0A GB2522421B (en) 2014-01-22 2014-01-22 LNG production process
PCT/GB2015/000006 WO2015110779A2 (en) 2014-01-22 2015-01-12 Lng production process

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Application Number Priority Date Filing Date Title
GB1401073.0A GB2522421B (en) 2014-01-22 2014-01-22 LNG production process

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GB201401073D0 GB201401073D0 (en) 2014-03-05
GB2522421A true GB2522421A (en) 2015-07-29
GB2522421B GB2522421B (en) 2016-10-19

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Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2539955A (en) * 2015-07-03 2017-01-04 Frederick Skinner Geoffrey Process for producing liquefied natural gas
GB2541464A (en) * 2015-08-21 2017-02-22 Frederick Skinner Geoffrey Process for producing Liquefied natural gas
WO2017121042A1 (en) * 2016-01-15 2017-07-20 成都赛普瑞兴科技有限公司 Method and apparatus for liquefying methane-rich gas through expansion refrigeration
IT201800010171A1 (en) 2018-11-08 2020-05-08 Saipem Spa PROCESS FOR THE RE-LIQUEFACTION AND CONTEMPORARY DECREASE OF THE NITROGEN CONTENT IN THE BOG FOR SELF-REFRIGERATED ABSORPTION
IT202100020159A1 (en) 2021-07-28 2023-01-28 Saipem Spa BOG RECONDENSATION PROCESS THROUGH REFRIGERATION OF CRYOGENIC LIQUIDS COGENERATED IN THE LNG VAPORIZATION PROCESS
EP4365525A3 (en) * 2022-10-14 2024-08-07 Air Products and Chemicals, Inc. Semi-open loop liquefaction process

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Publication number Priority date Publication date Assignee Title
WO2017162566A1 (en) 2016-03-21 2017-09-28 Shell Internationale Research Maatschappij B.V. Method and system for liquefying a natural gas feed stream
CZ2019618A3 (en) * 2019-10-04 2020-12-16 Siad Macchine Impianti S.P.A. Natural gas processing equipment
WO2024165416A1 (en) 2023-02-10 2024-08-15 Airco Process Technology A/S Small scale expansion cycle methane liquefaction process

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20040255616A1 (en) * 2001-08-21 2004-12-23 Maunder Anthony D. Method for liquefying methane-rich gas
GB2486036A (en) * 2011-06-15 2012-06-06 Anthony Dwight Maunder Process for liquefying natural gas using low-pressure feed stream
US20130340473A1 (en) * 2011-01-06 2013-12-26 Technip France Method for producing a c3+ hydrocarbon-rich fraction and a methane- and ethane-rich stream from a hydrocarbon-rich feed stream, and related facility

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20040255616A1 (en) * 2001-08-21 2004-12-23 Maunder Anthony D. Method for liquefying methane-rich gas
US20130340473A1 (en) * 2011-01-06 2013-12-26 Technip France Method for producing a c3+ hydrocarbon-rich fraction and a methane- and ethane-rich stream from a hydrocarbon-rich feed stream, and related facility
GB2486036A (en) * 2011-06-15 2012-06-06 Anthony Dwight Maunder Process for liquefying natural gas using low-pressure feed stream

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2539955A (en) * 2015-07-03 2017-01-04 Frederick Skinner Geoffrey Process for producing liquefied natural gas
GB2541464A (en) * 2015-08-21 2017-02-22 Frederick Skinner Geoffrey Process for producing Liquefied natural gas
US20180180354A1 (en) * 2015-08-21 2018-06-28 Gasconsult Limited Process for Producing Liquefied Natural Gas
US10641548B2 (en) * 2015-08-21 2020-05-05 Gasconsult Limited Process for producing liquefied natural gas
WO2017121042A1 (en) * 2016-01-15 2017-07-20 成都赛普瑞兴科技有限公司 Method and apparatus for liquefying methane-rich gas through expansion refrigeration
IT201800010171A1 (en) 2018-11-08 2020-05-08 Saipem Spa PROCESS FOR THE RE-LIQUEFACTION AND CONTEMPORARY DECREASE OF THE NITROGEN CONTENT IN THE BOG FOR SELF-REFRIGERATED ABSORPTION
IT202100020159A1 (en) 2021-07-28 2023-01-28 Saipem Spa BOG RECONDENSATION PROCESS THROUGH REFRIGERATION OF CRYOGENIC LIQUIDS COGENERATED IN THE LNG VAPORIZATION PROCESS
EP4365525A3 (en) * 2022-10-14 2024-08-07 Air Products and Chemicals, Inc. Semi-open loop liquefaction process

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WO2015110779A3 (en) 2015-11-12

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