US20140083132A1 - Process for liquefaction of natural gas - Google Patents

Process for liquefaction of natural gas Download PDF

Info

Publication number
US20140083132A1
US20140083132A1 US14/118,945 US201214118945A US2014083132A1 US 20140083132 A1 US20140083132 A1 US 20140083132A1 US 201214118945 A US201214118945 A US 201214118945A US 2014083132 A1 US2014083132 A1 US 2014083132A1
Authority
US
United States
Prior art keywords
heat exchanger
expander
stream
gas
natural gas
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Abandoned
Application number
US14/118,945
Inventor
Anthony Dwight Maunder
Geoffrey Frederick Skinner
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Gasconsult Ltd
Original Assignee
Gasconsult Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Gasconsult Ltd filed Critical Gasconsult Ltd
Assigned to GASCONSULT LIMITED reassignment GASCONSULT LIMITED ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: MAUNDER, ANTHONY DWIGHT, SKINNER, GEOFFREY FREDERICK
Publication of US20140083132A1 publication Critical patent/US20140083132A1/en
Abandoned legal-status Critical Current

Links

Images

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
    • F25J1/02—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
    • F25J1/0211—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 a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
    • 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
    • F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
    • 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
    • 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
    • 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
    • F25J1/0225—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 other external refrigeration means not provided before, e.g. heat driven absorption chillers
    • F25J1/0227—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 other external refrigeration means not provided before, e.g. heat driven absorption chillers within a refrigeration cascade
    • 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
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0229—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock
    • F25J1/023—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock for the combustion as fuels, i.e. integration with the fuel gas system
    • 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
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0235—Heat exchange integration
    • F25J1/0242—Waste heat recovery, e.g. from heat of compression
    • 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
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0244—Operation; Control and regulation; Instrumentation
    • F25J1/0254—Operation; Control and regulation; Instrumentation controlling particular process parameter, e.g. pressure, temperature
    • 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
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0281—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc. characterised by the type of prime driver, e.g. hot gas expander
    • 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
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0281—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc. characterised by the type of prime driver, e.g. hot gas expander
    • F25J1/0283—Gas turbine as the prime mechanical driver
    • 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
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/62—Separating low boiling components, e.g. He, H2, N2, Air
    • 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
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/64—Separating heavy hydrocarbons, e.g. NGL, LPG, C4+ hydrocarbons or heavy condensates in general
    • 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/80—Hot exhaust gas turbine combustion engine
    • F25J2240/82—Hot exhaust gas turbine combustion engine with waste heat recovery, e.g. in a combined cycle, i.e. for generating steam used in a Rankine cycle
    • 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
    • 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
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/906—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by heat driven absorption chillers

Definitions

  • the present invention relates to a method for liquefying methane-rich gas and, more particularly but not exclusively, relates to a method for producing liquefied natural gas (LNG).
  • LNG liquefied natural gas
  • Expander-based LNG installations are simple, compact, low in weight and can avoid the importation/preparation/storage of liquid refrigerants. These characteristics are attractive for smaller scale applications, particularly offshore, where low hydrocarbon inventory is desirable from safety considerations.
  • expander processes have certain drawbacks:
  • the working fluid typically nitrogen
  • Partially liquefying the feed gas itself in an expander, having a two-phase discharge flow, can reduce internal (recycle) gas flows and reduce power requirement.
  • an inventive step in the present application consists of identifying operating conditions for the two expanders (the precooling expander and the liquefying expander) which allow for practical production of atmospheric pressure LNG at about ⁇ 161° C. Moreover a very high pressure feed gas, which is a feature of the above-mentioned patents, is no longer required.
  • the present invention facilitates production of LNG from smaller gas fields, particularly offshore, due to its simple flow scheme, low power consumption and non-reliance on storage and use of liquid refrigerants.
  • the liquefaction process itself generally does not require process columns, for instance for refrigerant preparation, which may be less easy to operate under such operating conditions.
  • a process for liquefying natural gas or other methane-rich gases comprising:
  • this invention comprises a liquefaction process with moderate power requirement in which the necessary refrigeration, is largely supplied by work expansion of the feed gas itself. Cryogenic liquid refrigerants or other secondary working fluids such as nitrogen are therefore not required. In this way energy is extracted at a low temperature level which results in improved thermodynamic efficiency. As a result, a significant proportion of the LNG is formed directly in a work extracting expander, in addition to that formed by condensation in an exchanger which is cooled by the reheating of the cold gas from the said work expander.
  • FIGS. 1 and 2 represent flow diagrams illustrating processes in accordance with the invention.
  • FIG. 1 shows the operating features of the invention.
  • the exact flow sheet will depend upon the feed gas specification, but will generally contain these basic elements. Where pressures are stated anywhere in this application as “bar” these are bar absolute.
  • the feed natural gas (Stream 1 ) is passed through a pretreatment stage A in which components that would solidify or otherwise interfere with the downstream liquefaction process, such CO 2 , H 2 S, water vapour and mercury vapour, are removed to the extent necessary to give appropriate and conventional maximum concentrations in the pretreated gas (Stream 2 ).
  • Stream 2 is mixed with part (Stream 4 ) of the recycle gas (Stream 3 ) to form Stream 6 , which is passed through a passage in heat exchanger B, leaving as Stream 7 at a temperature typically in the range ⁇ 20° to ⁇ 60° C., preferably ⁇ 30° to ⁇ 50° C. This temperature is typically low enough to condense sufficient NGL to meet the specification for the final LNG product. Any condensed hydrocarbons in separator C are removed as Stream 8 .
  • the outlet vapour from C (Stream 9 ) is further cooled in a passage in heat exchanger D, exiting as Stream 10 at a temperature in the range ⁇ 50° to ⁇ 80° C., preferably ⁇ 60° to ⁇ 70° C.
  • the remaining part of the recycle gas (Stream 5 ) is cooled in gas expander E having an outlet Stream 11 with a temperature lower than the temperature of Stream 10 .
  • part or all of the pretreated feed gas may exit pretreatment stage A via Stream 2 a to join the recycle gas Stream 3 upstream of the point at which it is divided into Streams 4 & 5 .
  • This option may be convenient when the natural gas feed Stream 1 has only a small content of heavy hydrocarbon.
  • the pretreated feed gas may be mixed with the whole of the recycle gas and then the resulting mixture divided to supply heat exchanger B through Stream 6 and gas expander E through Stream 5 .
  • the pressure of Stream 11 will typically be around 15 bar (1.5 MPa).
  • Stream 11 enters a first cold passage in heat exchanger D, leaving as Stream 12 , which then passes through a first cold passage in heat exchanger B, emerging (Stream 13 ) at a temperature just below the temperature of Stream 6 .
  • the ratio of the flow rate of Stream 4 to the flow rate of Stream 5 is controlled so that the temperature approach between the composite hot and cold sides of heat exchangers B and D are substantially uniform throughout their lengths.
  • a large part of Stream 10 is then passed (Stream 14 ) through a second gas expander F from which it emerges as Stream 15 at a pressure between 3 bar (0.3 MPa) and 20 bar (2 MPa), preferably between 5 bar (0.5 MPa) and 15 bar (1.5 MPa) and in a partly liquefied state.
  • Stream 15 then enters vapour-liquid separator G.
  • the liquid phase from Separator G (Stream 16 ) is then typically let down in a pressure reduction device H such as a valve or a turbine.
  • the outlet from H (Stream 17 ) which is typically at or close to atmospheric pressure, is delivered into the LNG Tank I.
  • a conventional nitrogen stripping column (not shown) may be used, typically employing the sensible heat of Stream 16 for reboiling.
  • Stream 10 flows as Stream 23 through a hot side passage in heat exchanger J, wherein it is liquefied by indirect heat exchange with the vapour from separator G (Stream 18 ), emerging as Stream 24 .
  • This is then typically let down in pressure through pressure reduction device K, such as a valve or a turbine.
  • the outlet from K is routed either to vapour-liquid separator G, shown in broken line as Stream 25 a , or preferably as Stream 25 b to the LNG tank I.
  • This second option helps to reduce accumulation of nitrogen in the recycle gas.
  • Stream 18 having been heated in a first cold passage in heat exchanger J, emerges as Stream 19 . It is then further heated in a second cold passage in heat exchanger D, emerging as Stream 20 , which is then further heated in a second cold passage in heat exchanger B, emerging as Stream 21 at a temperature slightly below the temperature of Stream 6 .
  • Streams 13 and 21 are compressed in recycle compressor N, from which the outlet Stream 34 is cooled typically with cooling water in cooler O.
  • Compressor N may consist of more than one stage with intercoolers. Streams 13 and 21 will not have the same pressure and may enter at different compressor stages.
  • the outlet stream from P forms the above-mentioned recycle gas Stream 3 .
  • vapour comprising mainly methane together with most of the nitrogen content of the feed gas.
  • this vapour (Stream 26 ), optionally combined with boil-off vapour resulting from heat leak into tank I, is heated in a second cold passage in heat exchanger J to form Stream 27 , then in a third cold passage in heat exchanger D to give Stream 28 and finally in a third cold passage in heat exchanger B, emerging as Stream 29 at a temperature slightly below the temperature of Stream 6 .
  • a conventional booster blower (also not shown) may be provided in Stream 26 to ensure that the pressure of Stream 29 does not fall below atmospheric pressure.
  • Stream 29 may typically be used as fuel gas.
  • Part or all of Stream 29 optionally may be compressed for return to the recycle gas in a low pressure compressor L, leaving as Stream 31 .
  • This stream is cooled in cooler M, from which the outlet (Stream 32 ) joins Stream 21 to form Stream 22 , which then enters the suction of recycle compressor N instead of Stream 21 alone if this option is not used.
  • a further option is to withdraw recycle gas (Stream 33 ) at a convenient point from compressor N typically for use as gas turbine fuel. It may be convenient to use Stream 29 or Stream 33 as stripping gas for regeneration of adsorbents in the pretreatment stage A, prior to their ultimate combustion as fuels.
  • FIG. 2 shows a preferred embodiment of the invention in which expanders E and F have essentially the same outlet pressure of between 3 bar (0.3 MPa) and 20 bar (2 MPa), preferably between 5 bar (0.5 MPa) and 15 bar (1.5 MPa).
  • the outlet stream from expander E (Stream 11 ) is then combined with Stream 19 to form Stream 19 a , which enters heat exchanger D in place of Stream 19 in FIG. 1 .
  • the heat exchangers B and D then have only three passages, simplifying the construction of the exchanger and the operation of the plant.

Landscapes

  • 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)
  • Combustion & Propulsion (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

A process comprising: cooling natural gas with a heat exchanger and a first expander. The heat exchanger cools the feed natural gas to temperature higher than the outlet temperature of the expander, reheating the expander outlet stream in a first cold passage of the heat exchanger to slightly below the temperature of the feed natural gas to the heat exchanger, passing the cold outlet stream from the heat exchanger into a second expander wherein it is partly liquefied, separating the outlet stream of second expander into liquid and vapour fractions, collecting the liquid fraction for use as LNG product, reheating the vapour fraction in a second cold side passage of the heat exchanger to substantially the same temperature as the temperature of the feed natural gas to the heat exchanger, recycling the reheated vapour fraction partly as feed to the first expander and partly as feed to the heat exchanger.

Description

    FIELD OF THE INVENTION
  • The present invention relates to a method for liquefying methane-rich gas and, more particularly but not exclusively, relates to a method for producing liquefied natural gas (LNG).
    • BACKGROUND TO THE INVENTION
  • Liquefaction of natural gas can practically be achieved by:
      • evaporation of liquid refrigerants
      • work expansion of gases in expansion machines (expanders).
  • Evaporation of liquid refrigerants gives the lowest power requirement and is the basis of the widely used Cascade and Mixed Refrigerant LNG processes.
  • Expander-based LNG installations are simple, compact, low in weight and can avoid the importation/preparation/storage of liquid refrigerants. These characteristics are attractive for smaller scale applications, particularly offshore, where low hydrocarbon inventory is desirable from safety considerations. However expander processes have certain drawbacks:
      • until recently, limited capacity and experience with expanders
      • higher power requirement
      • higher internal gas flowrates, requiring larger line diameters, etc.
  • With most expander-based processes the working fluid (typically nitrogen) remains in the vapour phase at the expander outlet.
  • Partially liquefying the feed gas itself in an expander, having a two-phase discharge flow, can reduce internal (recycle) gas flows and reduce power requirement.
  • LNG production in a liquefying expander is not a new idea (U.S. Pat. No. 2,903,858—Bocquet).
  • The present inventors previously disclosed a process (GB Patent 2393504B, U.S. Pat. No. 7,234,321) with potentially lower power requirements, wherein a liquefying expander is combined with a precooling circuit which contains a simple mixed refrigerant generated from the feed natural gas.
  • Other recent disclosures comprise precooling by a parallel/recycle gas expander followed by a liquefying expander:
      • WO 01/44735 (Minta et al) describing production of pressurised liquid natural gas (PLNG) at −112° C. from feed gas compressed to a high pressure of “above 1600 psia”.
      • US 2006/0213222 (Whitesell) describing production of LNG from a feed gas entering the process at, or compressed within, the process to a pressure of “between about 1500 psig to about 3500 psig”.
    SUMMARY OF THE INVENTION
  • Relative to the two above-mentioned patents, an inventive step in the present application consists of identifying operating conditions for the two expanders (the precooling expander and the liquefying expander) which allow for practical production of atmospheric pressure LNG at about −161° C. Moreover a very high pressure feed gas, which is a feature of the above-mentioned patents, is no longer required.
  • This results in a simplified process with improved thermal efficiency having a wide range of potential applications where the raw feed gas has a pressure as low as 40 bar (4 MPa).
  • The present invention facilitates production of LNG from smaller gas fields, particularly offshore, due to its simple flow scheme, low power consumption and non-reliance on storage and use of liquid refrigerants. The liquefaction process itself generally does not require process columns, for instance for refrigerant preparation, which may be less easy to operate under such operating conditions.
    • DESCRIPTION OF THE INVENTION
  • According to the invention, there is provided a process for liquefying natural gas or other methane-rich gases. The feed gas, generally at a pressure of from 40 (4 MPa) to 100 bar (10 MPa), is liquefied to give LNG product at approx 1 bar (0.1 MPa)/−161° C. by the expander-based plant configuration described above Sand comprising:
      • cooling feed gas and recycle gas (mentioned below) in a first step by means of a first heat exchanger and in a first work expander; the heat exchanger having an outlet temperature in the range of −50° to −80° C., preferably −60° to −70° C.; the expander having a lower outlet temperature than that of the heat exchanger; the expander having its outlet stream reheated in a cold passage of the said heat exchanger and then recompressed to form part of the above mentioned recycle gas.
      • passing the cooled outlet stream from the said first heat exchanger partly into a hot passage in a second heat exchanger, wherein it is essentially condensed, and partly into a second work expander, the said second expander having a lower outlet temperature than the cold outlet of the second heat exchanger, the second expander outlet stream containing a significant amount of liquid (typically 10-15% wt); the expander outlet being separated into a vapour fraction and a liquid fraction; the vapour fraction being reheated in cold passages in said second and first heat exchangers; then recompressed and returned to the inlet to the process as part of the above mentioned recycle gas.
      • reducing the pressure of the above mentioned separated liquid and of the condensed liquid from the hot passage from second heat exchanger (both typically around −120° C.) to around to atmospheric pressure; reheating the flashed gas evolved in further cold passages in the above heat exchangers; removing the liquid for use as LNG product.
  • It has been found that the lowest requirement for recycle gas compression power results from concentrating the extraction of mechanical work into the pressure range above 10 bar (1 MPa) approx at the outlet of the second expander. An advantage of this is that the outlet pressures from the two expanders can be equalized at around 10 bar (1 MPa), reducing the first heat exchanger to a three-passage configuration.
  • Whereas most existing LNG production relies on evaporation of liquid refrigerants to cool and condense the natural gas so as to form LNG product in heat exchanger, this invention comprises a liquefaction process with moderate power requirement in which the necessary refrigeration, is largely supplied by work expansion of the feed gas itself. Cryogenic liquid refrigerants or other secondary working fluids such as nitrogen are therefore not required. In this way energy is extracted at a low temperature level which results in improved thermodynamic efficiency. As a result, a significant proportion of the LNG is formed directly in a work extracting expander, in addition to that formed by condensation in an exchanger which is cooled by the reheating of the cold gas from the said work expander.
    • DESCRIPTION OF PREFERRED EMBODIMENTS
  • The invention will be described with reference to the accompanying drawings in which FIGS. 1 and 2 represent flow diagrams illustrating processes in accordance with the invention.
  • FIG. 1 shows the operating features of the invention. The exact flow sheet will depend upon the feed gas specification, but will generally contain these basic elements. Where pressures are stated anywhere in this application as “bar” these are bar absolute.
  • The feed natural gas (Stream 1) is passed through a pretreatment stage A in which components that would solidify or otherwise interfere with the downstream liquefaction process, such CO2, H2S, water vapour and mercury vapour, are removed to the extent necessary to give appropriate and conventional maximum concentrations in the pretreated gas (Stream 2).
  • Stream 2 is mixed with part (Stream 4) of the recycle gas (Stream 3) to form Stream 6, which is passed through a passage in heat exchanger B, leaving as Stream 7 at a temperature typically in the range −20° to −60° C., preferably −30° to −50° C. This temperature is typically low enough to condense sufficient NGL to meet the specification for the final LNG product. Any condensed hydrocarbons in separator C are removed as Stream 8. The outlet vapour from C (Stream 9) is further cooled in a passage in heat exchanger D, exiting as Stream 10 at a temperature in the range −50° to −80° C., preferably −60° to −70° C. The remaining part of the recycle gas (Stream 5) is cooled in gas expander E having an outlet Stream 11 with a temperature lower than the temperature of Stream 10. Optionally part or all of the pretreated feed gas may exit pretreatment stage A via Stream 2 a to join the recycle gas Stream 3 upstream of the point at which it is divided into Streams 4 & 5. This option may be convenient when the natural gas feed Stream 1 has only a small content of heavy hydrocarbon. In such a case the pretreated feed gas may be mixed with the whole of the recycle gas and then the resulting mixture divided to supply heat exchanger B through Stream 6 and gas expander E through Stream 5.
  • The pressure of Stream 11 will typically be around 15 bar (1.5 MPa). Stream 11 enters a first cold passage in heat exchanger D, leaving as Stream 12, which then passes through a first cold passage in heat exchanger B, emerging (Stream 13) at a temperature just below the temperature of Stream 6. The ratio of the flow rate of Stream 4 to the flow rate of Stream 5 is controlled so that the temperature approach between the composite hot and cold sides of heat exchangers B and D are substantially uniform throughout their lengths. A large part of Stream 10 is then passed (Stream 14) through a second gas expander F from which it emerges as Stream 15 at a pressure between 3 bar (0.3 MPa) and 20 bar (2 MPa), preferably between 5 bar (0.5 MPa) and 15 bar (1.5 MPa) and in a partly liquefied state. Stream 15 then enters vapour-liquid separator G. The liquid phase from Separator G (Stream 16) is then typically let down in a pressure reduction device H such as a valve or a turbine. The outlet from H (Stream 17), which is typically at or close to atmospheric pressure, is delivered into the LNG Tank I. If it is desired to reduce the nitrogen content of the product LNG, a conventional nitrogen stripping column (not shown) may be used, typically employing the sensible heat of Stream 16 for reboiling.
  • Optionally and preferably a part of Stream 10 flows as Stream 23 through a hot side passage in heat exchanger J, wherein it is liquefied by indirect heat exchange with the vapour from separator G (Stream 18), emerging as Stream 24. This is then typically let down in pressure through pressure reduction device K, such as a valve or a turbine. The outlet from K is routed either to vapour-liquid separator G, shown in broken line as Stream 25 a, or preferably as Stream 25 b to the LNG tank I. This second option helps to reduce accumulation of nitrogen in the recycle gas. Stream 18, having been heated in a first cold passage in heat exchanger J, emerges as Stream 19. It is then further heated in a second cold passage in heat exchanger D, emerging as Stream 20, which is then further heated in a second cold passage in heat exchanger B, emerging as Stream 21 at a temperature slightly below the temperature of Stream 6.
  • Streams 13 and 21 are compressed in recycle compressor N, from which the outlet Stream 34 is cooled typically with cooling water in cooler O. Compressor N may consist of more than one stage with intercoolers. Streams 13 and 21 will not have the same pressure and may enter at different compressor stages. The outlet stream from P forms the above-mentioned recycle gas Stream 3.
  • The flashing of Stream 16 across H and the flashing of Stream 24 across K will result in the evolution of vapour comprising mainly methane together with most of the nitrogen content of the feed gas. Typically this vapour (Stream 26), optionally combined with boil-off vapour resulting from heat leak into tank I, is heated in a second cold passage in heat exchanger J to form Stream 27, then in a third cold passage in heat exchanger D to give Stream 28 and finally in a third cold passage in heat exchanger B, emerging as Stream 29 at a temperature slightly below the temperature of Stream 6. A conventional booster blower (also not shown) may be provided in Stream 26 to ensure that the pressure of Stream 29 does not fall below atmospheric pressure. Stream 29 may typically be used as fuel gas.
  • Part or all of Stream 29 (Stream 30) optionally may be compressed for return to the recycle gas in a low pressure compressor L, leaving as Stream 31. This stream is cooled in cooler M, from which the outlet (Stream 32) joins Stream 21 to form Stream 22, which then enters the suction of recycle compressor N instead of Stream 21 alone if this option is not used. A further option is to withdraw recycle gas (Stream 33) at a convenient point from compressor N typically for use as gas turbine fuel. It may be convenient to use Stream 29 or Stream 33 as stripping gas for regeneration of adsorbents in the pretreatment stage A, prior to their ultimate combustion as fuels.
  • FIG. 2 shows a preferred embodiment of the invention in which expanders E and F have essentially the same outlet pressure of between 3 bar (0.3 MPa) and 20 bar (2 MPa), preferably between 5 bar (0.5 MPa) and 15 bar (1.5 MPa). The outlet stream from expander E (Stream 11) is then combined with Stream 19 to form Stream 19 a, which enters heat exchanger D in place of Stream 19 in FIG. 1. The heat exchangers B and D then have only three passages, simplifying the construction of the exchanger and the operation of the plant.
  • Although in most applications it is expected that the Streams 2 and 3 will have temperatures close to ambient temperature, cooling below this level may be advantageous. It is feasible to cool those streams, and optionally the outlet streams from compressor intercoolers and aftercoolers, by means of a mechanical refrigeration cycle or by means of an absorption refrigeration system, typically using lithium bromide (LiBr), which could receive its heat supply from the exhaust of a gas turbine, gas engine or combined cycle or anything else suitable.

Claims (8)

1. A process for liquefying natural gas or other methane-rich gases comprising:
cooling feed natural gas at a pressure of from 40 to 100 bar (4 to 10 MPa) to a temperature of −50° to −80° C. by means of a heat exchanger and a first gas expander, the heat exchanger receiving the feed natural gas and having an outlet temperature higher than the outlet temperature of the expander;
reheating the expander outlet stream in a first cold passage of said heat exchanger to just below the inlet temperature of the feed natural gas to said heat exchanger, compressing and recycling;
passing part or all of the cold outlet stream from said heat exchanger into a second expander in which it is partly liquefied;
separating the outlet stream of said second expander into vapour and liquid fractions;
collecting the liquid fraction for use as LNG product,
reheating the vapour fraction in a second cold side passage of said heat exchanger to just below the inlet temperature of the feed natural gas to said heat exchanger;
recycling the said reheated vapour fraction after compression in part to the said first expander and in part to the said heat exchanger;
wherein
the outlet stream of the second expander is at a pressure between 5 and 15 bar (0.5 and 1.5 MPa).
2. The process as claimed in claim 1 in which the heat exchanger receives all the feed natural gas.
3. The process as claimed in claim 1 in which the heat exchanger receives a large part, at least 30%, of the feed natural gas.
4. The process as claimed in claim 1 in which the feed natural gas is cooled to a temperature of −60° to −70° C.
5. The modification of the process claimed in claim 1 in which the said first and second gas expanders have essentially the same outlet pressure of between 5 bar and 15 bar (0.5 and 1.5 MPa), and the outlet streams from both expanders are combined prior to final reheating, compression and recycle.
6. The process as claimed in claim 1 in which any part or all of the feed and/or compressor discharge and/or recycle streams are cooled, typically by use of an absorption refrigeration cycles such as lithium bromide (LiBr).
7. The process as claimed in claim 1 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.
8. The process as claimed in claim 1 wherein such cooling of either feed and/or recycle streams is combined with removal of carbon dioxide and/or other impurities from the feed gas.
US14/118,945 2011-06-15 2012-06-11 Process for liquefaction of natural gas Abandoned US20140083132A1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
GB1110096.3A GB2486036B (en) 2011-06-15 2011-06-15 Process for liquefaction of natural gas
GB1110096.3 2011-06-15
PCT/GB2012/000502 WO2012172281A2 (en) 2011-06-15 2012-06-11 Process for liquefaction of natural gas

Publications (1)

Publication Number Publication Date
US20140083132A1 true US20140083132A1 (en) 2014-03-27

Family

ID=44357822

Family Applications (1)

Application Number Title Priority Date Filing Date
US14/118,945 Abandoned US20140083132A1 (en) 2011-06-15 2012-06-11 Process for liquefaction of natural gas

Country Status (11)

Country Link
US (1) US20140083132A1 (en)
EP (1) EP2721358A2 (en)
JP (1) JP5984192B2 (en)
KR (1) KR101820560B1 (en)
CN (1) CN103582792B (en)
AU (1) AU2012270148B2 (en)
CA (1) CA2836628C (en)
GB (1) GB2486036B (en)
MX (1) MX346703B (en)
MY (1) MY172653A (en)
WO (1) WO2012172281A2 (en)

Cited By (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3043133A1 (en) * 2015-01-12 2016-07-13 Shell Internationale Research Maatschappij B.V. Method of removing nitrogen from a nitrogen containing stream
EP3118548A2 (en) 2015-04-24 2017-01-18 Air Products And Chemicals, Inc. Integrated methane refrigeration system for liquefying natural gas
WO2017079711A1 (en) * 2015-11-06 2017-05-11 Fluor Technologies Corporation Systems and methods for lng refrigeration and liquefaction
WO2018147973A1 (en) * 2017-02-13 2018-08-16 Exxonmobil Upstream Research Company Pre-cooling of natural gas by high pressure compression and expansion
US20190049174A1 (en) * 2016-03-21 2019-02-14 Shell Oil Company Method and system for liquefying a natural gas feed stream
US20190112008A1 (en) * 2016-03-31 2019-04-18 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Boil-off gas re-liquefying device and method for ship
EP3561421A1 (en) * 2018-04-27 2019-10-30 Air Products And Chemicals, Inc. Improved method and system for cooling a hydrocarbon stream using a gas phase refrigerant
US10866022B2 (en) 2018-04-27 2020-12-15 Air Products And Chemicals, Inc. Method and system for cooling a hydrocarbon stream using a gas phase refrigerant
US20200393196A1 (en) * 2017-12-29 2020-12-17 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Device and method for processing boil-off gas in liquefied gas regasification system
US20210088273A1 (en) * 2019-09-24 2021-03-25 High Roller E & C, LLC System and process for natural gas liquefaction
EP3943852A2 (en) 2020-06-30 2022-01-26 Air Products And Chemicals, Inc. Liquefaction system
US11255602B2 (en) * 2016-07-06 2022-02-22 Saipem S.P.A. Method for liquefying natural gas and for recovering possible liquids from the natural gas, comprising two refrigerant cycles semi-open to the natural gas and a refrigerant cycle closed to the refrigerant gas
US11536510B2 (en) 2018-06-07 2022-12-27 Exxonmobil Upstream Research Company Pretreatment and pre-cooling of natural gas by high pressure compression and expansion
US20230136307A1 (en) * 2018-08-22 2023-05-04 ExxonMobil Technology and Engineering Company Managing Make-Up Gas Composition Variation for a High Pressure Expander Process
US20230304731A1 (en) * 2020-07-30 2023-09-28 L'air Liquide, Societe Anonyme Pour L'etude Et L?Exploitation Des Procedes Georges Claude Facility and method for refrigerating a fluid
EP3479037B1 (en) * 2016-06-30 2024-02-14 Baker Hughes Oilfield Operations, LLC System and method for producing liquefied natural gas
US11911732B2 (en) 2020-04-03 2024-02-27 Nublu Innovations, Llc Oilfield deep well processing and injection facility and methods
US12025370B2 (en) 2022-10-14 2024-07-02 Air Products And Chemicals, Inc. Reverse Brayton LNG production process

Families Citing this family (34)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2713127A1 (en) * 2012-09-28 2014-04-02 Siemens Aktiengesellschaft Method for liquefaction of natural gas
GB2522421B (en) * 2014-01-22 2016-10-19 Dwight Maunder Anthony LNG production process
US9696086B2 (en) 2014-01-28 2017-07-04 Dresser-Rand Company System and method for the production of liquefied natural gas
TWI603044B (en) 2015-07-10 2017-10-21 艾克頌美孚上游研究公司 System and method for producing liquefied nitrogen using liquefied natural gas
TWI608206B (en) 2015-07-15 2017-12-11 艾克頌美孚上游研究公司 Liquefied natural gas (LNG) production system with increased efficiency by pre-cooling the natural gas supply stream
TWI606221B (en) 2015-07-15 2017-11-21 艾克頌美孚上游研究公司 Liquefied natural gas production system and method with greenhouse gas removal
GB2541464A (en) 2015-08-21 2017-02-22 Frederick Skinner Geoffrey Process for producing Liquefied natural gas
WO2017105680A1 (en) 2015-12-14 2017-06-22 Exxonmobil Upstream Research Company Expander-based lng production processes enhanced with liquid nitrogen
SG11201803521SA (en) 2015-12-14 2018-06-28 Exxonmobil Upstream Res Co Method of natural gas liquefaction on lng carriers storing liquid nitrogen
JP6772267B2 (en) 2015-12-14 2020-10-21 エクソンモービル アップストリーム リサーチ カンパニー Methods and systems for separating nitrogen from liquefied natural gas using liquefied nitrogen
JP6800977B2 (en) 2015-12-14 2020-12-16 エクソンモービル アップストリーム リサーチ カンパニー Precooling of natural gas by high pressure compression and expansion
CN105674686B (en) * 2016-01-15 2018-09-14 成都赛普瑞兴科技有限公司 A kind of liquefied method and device of swell refrigeration high methane gas
CN105823304B (en) * 2016-03-23 2019-02-19 成都赛普瑞兴科技有限公司 A kind of liquefied method and device of twin-stage swell refrigeration high methane gas
CN106052303A (en) * 2016-06-07 2016-10-26 成都赛普瑞兴科技有限公司 Efficient expansion refrigeration methane-rich gas liquefaction method and device
US10663115B2 (en) 2017-02-24 2020-05-26 Exxonmobil Upstream Research Company Method of purging a dual purpose LNG/LIN storage tank
CN106907273A (en) * 2017-03-15 2017-06-30 广西利维船舶制造有限公司 A kind of ship LNG vaporization system of utilization river heat supply
AU2019322808B2 (en) 2018-08-14 2022-10-13 ExxonMobil Technology and Engineering Company Conserving mixed refrigerant in natural gas liquefaction facilities
WO2020040953A2 (en) 2018-08-22 2020-02-27 Exxonmobil Upstream Research Company Heat exchanger configuration for a high pressure expander process and a method of natural gas liquefaction using the same
US11635252B2 (en) 2018-08-22 2023-04-25 ExxonMobil Technology and Engineering Company Primary loop start-up method for a high pressure expander process
WO2020106394A1 (en) 2018-11-20 2020-05-28 Exxonmobil Upstream Research Company Poly refrigerated integrated cycle operation using solid-tolerant heat exchangers
WO2020106397A1 (en) 2018-11-20 2020-05-28 Exxonmobil Upstream Research Company Methods and apparatus for improving multi-plate scraped heat exchangers
TWI746977B (en) * 2019-01-22 2021-11-21 法商液態空氣喬治斯克勞帝方法研究開發股份有限公司 Gas liquefaction method and gas liquefaction device
US11668524B2 (en) 2019-01-30 2023-06-06 Exxonmobil Upstream Research Company Methods for removal of moisture from LNG refrigerant
CA3123235A1 (en) 2019-01-30 2020-08-06 Exxonmobil Upstream Research Company Methods for removal of moisture from lng refrigerant
GB2582815A (en) * 2019-04-05 2020-10-07 Frederick Skinner Geoffrey Process for producing liquefied natural gas
US11465093B2 (en) 2019-08-19 2022-10-11 Exxonmobil Upstream Research Company Compliant composite heat exchangers
US20210063083A1 (en) 2019-08-29 2021-03-04 Exxonmobil Upstream Research Company Liquefaction of Production Gas
US12050054B2 (en) 2019-09-19 2024-07-30 ExxonMobil Technology and Engineering Company Pretreatment, pre-cooling, and condensate recovery of natural gas by high pressure compression and expansion
WO2021055021A1 (en) 2019-09-19 2021-03-25 Exxonmobil Upstream Research Company Pretreatment and pre-cooling of natural gas by high pressure compression and expansion
WO2021055020A1 (en) 2019-09-19 2021-03-25 Exxonmobil Upstream Research Company Pretreatment and pre-cooling of natural gas by high pressure compression and expansion
US11083994B2 (en) 2019-09-20 2021-08-10 Exxonmobil Upstream Research Company Removal of acid gases from a gas stream, with O2 enrichment for acid gas capture and sequestration
WO2021061253A1 (en) 2019-09-24 2021-04-01 Exxonmobil Upstream Research Company Cargo stripping features for dual-purpose cryogenic tanks on ships or floating storage units for lng and liquid nitrogen
GB2601173B (en) 2020-11-21 2022-11-16 Frederick Skinner Geoffrey Process for producing liquefied Hydrogen
WO2024165416A1 (en) 2023-02-10 2024-08-15 Airco Process Technology A/S Small scale expansion cycle methane liquefaction process

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2900796A (en) * 1954-08-16 1959-08-25 Constock Liquid Methane Corp Method of liquefying natural gas
US3433026A (en) * 1966-11-07 1969-03-18 Judson S Swearingen Staged isenthalpic-isentropic expansion of gas from a pressurized liquefied state to a terminal storage state
US4758257A (en) * 1986-05-02 1988-07-19 The Boc Group Plc Gas liquefaction method and apparatus
US5651269A (en) * 1993-12-30 1997-07-29 Institut Francais Du Petrole Method and apparatus for liquefaction of a natural gas
US20100186445A1 (en) * 2007-08-24 2010-07-29 Moses Minta Natural Gas Liquefaction Process
US20120036888A1 (en) * 2007-11-05 2012-02-16 David Vandor Method and system for the small-scale production of liquified natural gas (lng) and cold compressed gas (ccng) from low-pressure natural gas
US20120204598A1 (en) * 2011-02-16 2012-08-16 Conocophillips Company Integrated waste heat recovery in liquefied natural gas facility

Family Cites Families (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2903858A (en) 1955-10-06 1959-09-15 Constock Liquid Methane Corp Process of liquefying gases
US3581511A (en) * 1969-07-15 1971-06-01 Inst Gas Technology Liquefaction of natural gas using separated pure components as refrigerants
US3677019A (en) * 1969-08-01 1972-07-18 Union Carbide Corp Gas liquefaction process and apparatus
MY122625A (en) * 1999-12-17 2006-04-29 Exxonmobil Upstream Res Co Process for making pressurized liquefied natural gas from pressured natural gas using expansion cooling
GB0120272D0 (en) 2001-08-21 2001-10-10 Gasconsult Ltd Improved process for liquefaction of natural gases
AU2003900327A0 (en) * 2003-01-22 2003-02-06 Paul William Bridgwood Process for the production of liquefied natural gas
JP4551446B2 (en) * 2004-04-26 2010-09-29 オートロフ・エンジニアーズ・リミテッド Natural gas liquefaction
US7673476B2 (en) 2005-03-28 2010-03-09 Cambridge Cryogenics Technologies Compact, modular method and apparatus for liquefying natural gas
RU2406949C2 (en) * 2005-08-09 2010-12-20 Эксонмобил Апстрим Рисерч Компани Method of liquefying natural gas
CN101228405B (en) * 2005-08-09 2010-12-08 埃克森美孚上游研究公司 Natural gas liquefaction process for producing LNG
JP2007051788A (en) * 2005-08-15 2007-03-01 Daikin Ind Ltd Refrigeration equipment
EP1939564A1 (en) * 2006-12-26 2008-07-02 Repsol Ypf S.A. Process to obtain liquefied natural gas
CN101871703A (en) * 2009-04-21 2010-10-27 刘甄 Lithium bromide absorbing type refrigeration and heat supply device

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2900796A (en) * 1954-08-16 1959-08-25 Constock Liquid Methane Corp Method of liquefying natural gas
US3433026A (en) * 1966-11-07 1969-03-18 Judson S Swearingen Staged isenthalpic-isentropic expansion of gas from a pressurized liquefied state to a terminal storage state
US4758257A (en) * 1986-05-02 1988-07-19 The Boc Group Plc Gas liquefaction method and apparatus
US5651269A (en) * 1993-12-30 1997-07-29 Institut Francais Du Petrole Method and apparatus for liquefaction of a natural gas
US20100186445A1 (en) * 2007-08-24 2010-07-29 Moses Minta Natural Gas Liquefaction Process
US20120036888A1 (en) * 2007-11-05 2012-02-16 David Vandor Method and system for the small-scale production of liquified natural gas (lng) and cold compressed gas (ccng) from low-pressure natural gas
US20120204598A1 (en) * 2011-02-16 2012-08-16 Conocophillips Company Integrated waste heat recovery in liquefied natural gas facility

Cited By (30)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3043133A1 (en) * 2015-01-12 2016-07-13 Shell Internationale Research Maatschappij B.V. Method of removing nitrogen from a nitrogen containing stream
US9863697B2 (en) 2015-04-24 2018-01-09 Air Products And Chemicals, Inc. Integrated methane refrigeration system for liquefying natural gas
EP3118548A2 (en) 2015-04-24 2017-01-18 Air Products And Chemicals, Inc. Integrated methane refrigeration system for liquefying natural gas
EP3118548A3 (en) * 2015-04-24 2017-05-03 Air Products And Chemicals, Inc. Integrated methane refrigeration system for liquefying natural gas
US12313337B2 (en) 2015-11-06 2025-05-27 Fluor Technologies Corporation Systems and methods for LNG refrigeration and liquefaction
WO2017079711A1 (en) * 2015-11-06 2017-05-11 Fluor Technologies Corporation Systems and methods for lng refrigeration and liquefaction
US20190049174A1 (en) * 2016-03-21 2019-02-14 Shell Oil Company Method and system for liquefying a natural gas feed stream
US20190112008A1 (en) * 2016-03-31 2019-04-18 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Boil-off gas re-liquefying device and method for ship
US12006017B2 (en) 2016-03-31 2024-06-11 Hanwha Ocean Co., Ltd. Boil-off gas reliquefication apparatus and method for vessel
US11760462B2 (en) 2016-03-31 2023-09-19 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Boil-off gas re-liquefying device and method for ship
EP3479037B1 (en) * 2016-06-30 2024-02-14 Baker Hughes Oilfield Operations, LLC System and method for producing liquefied natural gas
US11255602B2 (en) * 2016-07-06 2022-02-22 Saipem S.P.A. Method for liquefying natural gas and for recovering possible liquids from the natural gas, comprising two refrigerant cycles semi-open to the natural gas and a refrigerant cycle closed to the refrigerant gas
WO2018147973A1 (en) * 2017-02-13 2018-08-16 Exxonmobil Upstream Research Company Pre-cooling of natural gas by high pressure compression and expansion
US20180231303A1 (en) * 2017-02-13 2018-08-16 Fritz Pierre, JR. Pre-Cooling of Natural Gas by High Pressure Compression and Expansion
US20200393196A1 (en) * 2017-12-29 2020-12-17 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Device and method for processing boil-off gas in liquefied gas regasification system
RU2743094C2 (en) * 2018-04-27 2021-02-15 Эр Продактс Энд Кемикалз, Инк. Improved method and system for cooling a hydrocarbon flow using a gas-phase coolant
EP3561421A1 (en) * 2018-04-27 2019-10-30 Air Products And Chemicals, Inc. Improved method and system for cooling a hydrocarbon stream using a gas phase refrigerant
AU2019202815B2 (en) * 2018-04-27 2021-03-11 Hercules Project Company Llc Method and system for cooling a hydrocarbon stream using a gas phase refrigerant
US10866022B2 (en) 2018-04-27 2020-12-15 Air Products And Chemicals, Inc. Method and system for cooling a hydrocarbon stream using a gas phase refrigerant
CN110411146A (en) * 2018-04-27 2019-11-05 气体产品与化学公司 Improved method and system for cooling a hydrocarbon stream using a vapor phase refrigerant
US10788261B2 (en) 2018-04-27 2020-09-29 Air Products And Chemicals, Inc. Method and system for cooling a hydrocarbon stream using a gas phase refrigerant
US11536510B2 (en) 2018-06-07 2022-12-27 Exxonmobil Upstream Research Company Pretreatment and pre-cooling of natural gas by high pressure compression and expansion
US12050056B2 (en) * 2018-08-22 2024-07-30 ExxonMobil Technology and Engineering Company Managing make-up gas composition variation for a high pressure expander process
US20230136307A1 (en) * 2018-08-22 2023-05-04 ExxonMobil Technology and Engineering Company Managing Make-Up Gas Composition Variation for a High Pressure Expander Process
US20210088273A1 (en) * 2019-09-24 2021-03-25 High Roller E & C, LLC System and process for natural gas liquefaction
US11911732B2 (en) 2020-04-03 2024-02-27 Nublu Innovations, Llc Oilfield deep well processing and injection facility and methods
US11499775B2 (en) 2020-06-30 2022-11-15 Air Products And Chemicals, Inc. Liquefaction system
EP3943852A2 (en) 2020-06-30 2022-01-26 Air Products And Chemicals, Inc. Liquefaction system
US20230304731A1 (en) * 2020-07-30 2023-09-28 L'air Liquide, Societe Anonyme Pour L'etude Et L?Exploitation Des Procedes Georges Claude Facility and method for refrigerating a fluid
US12025370B2 (en) 2022-10-14 2024-07-02 Air Products And Chemicals, Inc. Reverse Brayton LNG production process

Also Published As

Publication number Publication date
JP2014522477A (en) 2014-09-04
WO2012172281A4 (en) 2014-01-09
MY172653A (en) 2019-12-09
MX2013014870A (en) 2015-06-15
GB2486036A (en) 2012-06-06
JP5984192B2 (en) 2016-09-06
KR101820560B1 (en) 2018-01-19
AU2012270148A1 (en) 2013-11-28
CN103582792A (en) 2014-02-12
WO2012172281A3 (en) 2013-12-05
GB201110096D0 (en) 2011-07-27
CA2836628A1 (en) 2012-12-20
CA2836628C (en) 2019-06-25
MX346703B (en) 2017-03-28
KR20140043745A (en) 2014-04-10
CN103582792B (en) 2016-06-22
GB2486036B (en) 2012-11-07
AU2012270148B2 (en) 2017-12-07
WO2012172281A2 (en) 2012-12-20
EP2721358A2 (en) 2014-04-23

Similar Documents

Publication Publication Date Title
CA2836628C (en) Process for liquefaction of natural gas
US6751985B2 (en) Process for producing a pressurized liquefied gas product by cooling and expansion of a gas stream in the supercritical state
US8250883B2 (en) Process to obtain liquefied natural gas
JP5547967B2 (en) Liquefied natural gas production system and method
EP2564139B1 (en) Process and apparatus for the liquefaction of natural gas
JP2019526770A (en) Process for liquefying natural gas and recovering any liquid from natural gas, comprising two semi-open refrigerant cycles using natural gas and one closed refrigerant cycle using gas refrigerant
US20100175423A1 (en) Methods and apparatus for liquefaction of natural gas and products therefrom
CA2960195A1 (en) Production of low pressure liquid carbon dioxide from a power production system and method
WO2015069138A2 (en) Natural gas liquefaction method and unit
MX2012004349A (en) Complete liquefaction methods and apparatus.
US20210088275A1 (en) Pretreatment and Pre-Cooling of Natural Gas by High Pressure Compression and Expansion
WO2015110779A2 (en) Lng production process
US11806639B2 (en) Pretreatment and pre-cooling of natural gas by high pressure compression and expansion
EP2796819B1 (en) Method and apparatus for the liquefaction of natural gas
WO2007148122A2 (en) Process and device for producing lng
CN104412055B (en) Method for controlling temperature to liquefy gas and production equipment using the method
WO2006135363A1 (en) Apparatus and methods for processing hydrocarbons to produce liquified natural gas

Legal Events

Date Code Title Description
AS Assignment

Owner name: GASCONSULT LIMITED, UNITED KINGDOM

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:MAUNDER, ANTHONY DWIGHT;SKINNER, GEOFFREY FREDERICK;REEL/FRAME:031638/0222

Effective date: 20131111

STPP Information on status: patent application and granting procedure in general

Free format text: NON FINAL ACTION MAILED

STPP Information on status: patent application and granting procedure in general

Free format text: RESPONSE TO NON-FINAL OFFICE ACTION ENTERED AND FORWARDED TO EXAMINER

STPP Information on status: patent application and granting procedure in general

Free format text: RESPONSE TO NON-FINAL OFFICE ACTION ENTERED AND FORWARDED TO EXAMINER

STPP Information on status: patent application and granting procedure in general

Free format text: FINAL REJECTION MAILED

STPP Information on status: patent application and granting procedure in general

Free format text: ADVISORY ACTION MAILED

STCB Information on status: application discontinuation

Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION