MX2007009824A - Plant and method for liquefying natural gas. - Google Patents

Plant and method for liquefying natural gas.

Info

Publication number
MX2007009824A
MX2007009824A MX2007009824A MX2007009824A MX2007009824A MX 2007009824 A MX2007009824 A MX 2007009824A MX 2007009824 A MX2007009824 A MX 2007009824A MX 2007009824 A MX2007009824 A MX 2007009824A MX 2007009824 A MX2007009824 A MX 2007009824A
Authority
MX
Mexico
Prior art keywords
natural gas
main
outlet
heat exchanger
cooling
Prior art date
Application number
MX2007009824A
Other languages
Spanish (es)
Inventor
Cornelis Buijs
Robert Klein Nagelvoort
Original Assignee
Shell Int Research
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 Shell Int Research filed Critical Shell Int Research
Publication of MX2007009824A publication Critical patent/MX2007009824A/en

Links

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
    • F25J1/0243—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.
    • F25J1/0292—Refrigerant compression by cold or cryogenic suction of the refrigerant 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
    • F25J1/02—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
    • 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"
    • F25J1/004—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
    • F25J1/003—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"
    • F25J1/0042—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 liquid 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
    • F25J1/0047—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 an "external" refrigerant stream in a closed vapor compression cycle
    • F25J1/0052—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 an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant 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
    • F25J1/0047—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 an "external" refrigerant stream in a closed vapor compression cycle
    • F25J1/0052—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 an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
    • F25J1/0055—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 an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream originating from an incorporated 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
    • F25J1/0211—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
    • F25J1/0214—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 as a dual level refrigeration cascade with at least one MCR 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
    • 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
    • F25J1/0214—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 as a dual level refrigeration cascade with at least one MCR cycle
    • F25J1/0215—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 as a dual level refrigeration cascade with at least one MCR cycle with one SCR cycle
    • F25J1/0216—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 as a dual level refrigeration cascade with at least one MCR cycle with one SCR cycle using a C3 pre-cooling 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
    • 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
    • F25J1/0219—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 in combination with an internal quasi-closed refrigeration loop, e.g. using a deep flash recycle 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
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0235—Heat exchange integration
    • F25J1/0237—Heat exchange integration integrating refrigeration provided for liquefaction and purification/treatment of the gas to be liquefied, e.g. heavy hydrocarbon removal from natural gas
    • F25J1/0238—Purification or treatment step is integrated within one refrigeration cycle only, i.e. the same or single refrigeration cycle provides feed gas cooling (if present) and overhead gas cooling
    • 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
    • F25J1/0237—Heat exchange integration integrating refrigeration provided for liquefaction and purification/treatment of the gas to be liquefied, e.g. heavy hydrocarbon removal from natural gas
    • F25J1/0239—Purification or treatment step being integrated between two refrigeration cycles of a refrigeration cascade, i.e. first cycle providing feed gas cooling and second cycle providing overhead gas cooling
    • F25J1/0241—Purification or treatment step being integrated between two refrigeration cycles of a refrigeration cascade, i.e. first cycle providing feed gas cooling and second cycle providing overhead gas cooling wherein the overhead cooling comprises providing reflux for a fractionation step
    • 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
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0262—Details of the cold heat exchange system
    • F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
    • F25J1/0265—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer
    • 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
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0262—Details of the cold heat exchange system
    • F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
    • F25J1/0265—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer
    • F25J1/0268—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer using a dedicated refrigeration means
    • 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
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0269—Arrangement of liquefaction units or equipments fulfilling the same process step, e.g. multiple "trains" concept
    • F25J1/0271—Inter-connecting multiple cold equipments within or downstream of the cold box
    • 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
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0274—Retrofitting or revamping of an existing liquefaction unit
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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
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    • 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.
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    • F25J1/0284—Electrical motor as the prime mechanical driver
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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.
    • F25J1/0285—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings
    • F25J1/0287—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings including an electrical motor
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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.
    • F25J1/0295—Shifting of the compression load between different cooling stages within a refrigerant cycle or within a cascade refrigeration 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/60—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being hydrocarbons or a mixture of hydrocarbons
    • 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

Abstract

Plant and method for liquefying natural gas. The plant comprises a common pre-cooling heat exchanger train (1), two natural gas liquids extraction units (100, 100') and two main heat exchangers (200, 200') to cool the overhead light fraction from its corresponding natural gas liquids extraction unit to liquefaction.

Description

PLANT AND METHOD FOR LIQUEURING NATURAL GAS FIELD OF THE INVENTION The present invention relates to a plant and a method for liquefying natural gas. BACKGROUND OF THE INVENTION US Patent 6,389,844 describes a plant and method for liquefying natural gas. The plant in accordance with US Patent 6,389,844 comprises a single common pre-cooling cycle followed by two main liquefaction cycles arranged in parallel operating simultaneously, wherein the natural gas flowing through the plant is liquefied and subcooled. Because the pre-cooling cycle attends two main liquefaction cycles, the depth to which natural gas can be precooled is usually reduced. Another plant for the production of liquefied natural gas is described in the North American Patent Application 2005/0005635. Different specifications of liquefied natural gas, in particular with respect to the calorific value, are demanded in several markets. SUMMARY OF THE INVENTION In order to satisfy these demands, the plant for liquefying natural gas in accordance with the present invention comprises: Ref .: 184230 - a pre-cooling heat exchanger train with a precooling refrigerant circuit to extract heat from natural gas in the pre-cooling heat exchanger train, and has an inlet for natural gas and an outlet for precooled natural gas; a distributor for dividing the natural gas stream into at least a first and a second natural gas substream; - at least two extraction units of natural gas liquids each conditioned with an extraction unit inlet arranged to receive one of the natural gas substreams, and comprising a heavy fraction outlet, and an upper outlet of light fraction; and - at least two main cryogenic systems each comprise a main heat exchanger having a first hot side having an inlet connected to the upper outlet of light fraction of at least one of the gas liquid extraction units natural and one outlet for liquefied natural gas, and each comprises a main refrigerant circuit for extracting heat from the natural gas flowing through the first hot side of the corresponding main heat exchanger. The method for liquefying a stream of natural gas in accordance with the present invention comprises: - precooling the natural gas stream in a heat exchanger train against a precooling refrigerant that is circulated in a precooling refrigerant circuit; - dividing the natural gas stream into at least one first and second natural gas substreams; simultaneously separating each of the first and second subcurrents of natural gas in a liquid heavy fraction, and a vaporized upper light fraction; - additionally cooling the vaporized upper light fractions in a total condensation against a main refrigerant in at least two main cryogenic systems, by which in each main cryogenic system the main refrigerant is circulated in a main refrigerant circuit; and - extracting a stream of liquefied natural gas therefrom. The precooling refrigerant circuit now assists two main refrigerant circuits, but each main refrigerant circuit is assisted by its own natural gas liquid extraction unit. In this way the liquefaction capacity is not limited by the capacity to extract liquids from natural gas. It has been surprisingly discovered that it is possible to extract natural gas liquids downstream of the pre-cooling or the pre-cooling heat exchanger train, while due to a higher natural gas flow rate, the pre-cooling temperature is lower than in the case where the pre-cooling is followed by a single main heat exchanger with a single main refrigerant cycle. Another advantage of the invention is that the natural gas extraction units have not had to be increased in size to receive the higher flow rate. It has been discovered that in high productions of natural gas, the viability limit of the construction and transport of high pressure separation columns is reached. This problem is treated with the supply of two smaller columns arranged in parallel and operated simultaneously. It can still be assumed that the additional capital cost (CAPEX) resulting from the supply of two or more units of extraction of relatively small natural gas liquids in parallel, is less than that of a large unit of extraction of conditioned natural gas liquids. to handle the full flow of natural gas. The invention includes not only a first group of embodiments wherein each of the main heat exchangers receives the vaporized upper light fraction exclusively from one of the natural gas liquid extraction units, but also a second group of embodiments wherein each of the main heat exchangers receives parts of the vaporized upper light fraction of the two or more natural gas liquid extraction units. An advantage of the first group of modalities is that the configuration of the equipment is relatively simple; an advantage of the second group of modalities is that a possible maldistribution is eliminated in the form of small variations in for example the composition or in the temperature of the respective vaporized upper light fractions. The distributor for dividing the natural gas stream into at least one first and second natural gas substreams may be located downstream of the precooling heat exchanger train or upstream thereof. In this way, the division of the natural gas stream into first and second subcurrents can be done before or after pre-cooling. Where the precooling heat exchanger train comprises two or more heat exchangers arranged in series, or the precooling is performed in two or more serial stages, the distributor can be located between two heat exchangers in the train to divide the current of natural gas between the consecutive pre-cooling stages. An advantage of dividing the natural gas stream into two subcurrents upstream of a pre-cooling stage final is that the natural gas stream can be divided into the first and second subcurrents of natural gas before it is partially condensed due to pre-cooling which reduces the probability of maldistribution. This advantage is also achieved in a plant and method for liquefying natural gas according to what is currently claimed but without the at least two natural gas liquid extraction units and separating each of the first and second natural gas substreams in one. heavy liquid fraction. BRIEF DESCRIPTION OF THE FIGURES The invention will now be described by way of example in greater detail with reference to the appended Figures, wherein the Figure shows a general schematic flow diagram of the first group of embodiments of the invention; Figure lb shows a general schematic flow chart of the second group of embodiments of the invention; Figure 2 schematically shows the plant and liquefaction process according to the present invention; Figure 3 schematically shows a more specific embodiment of the plant and process according to the present invention; and Figure 4 schematically shows a final expansion unit to be used in combination with the modalities.
DETAILED DESCRIPTION OF THE INVENTION Reference is made with respect to Figures la and Ib. The plant for liquefying natural gas in accordance with the present invention comprises a train of heat exchangers of precooling of natural gas 1, a distributor 4, two main cryogenic systems 200 and 200 ', and two units of extraction of liquids of natural gas 100 and 100 '. The pre-cooling heat exchanger train has an inlet line 90 for natural gas and an outlet line 19 for precooled natural gas. The distributor 4 is connected to the outlet line 19 and has at least two outlets 27, 27 J Each of the natural gas liquid extraction units 100, 100 'is connected to a line 27 or 27', and has a discharge line 108, 108 'to discharge a heavy fraction, a discharge line 127, 127' to discharge a higher light fraction. The heavy fraction comprises a natural gas liquid that is enriched with heavier components such as C3 + components, the upper light fraction comprises a poorer unenriched mixture of these heavier components, and must be liquefied. Each main cryogenic system 200, 200 'is associated with a discharge line 95, 95' for discharging liquefied natural gas. In Figure la, a generic modality is shown where each of the main cryogenic systems 200, 200 'is exclusively associated with one of the natural gas liquid extraction units 100, 100'. In Figure lb, a generic embodiment is shown in which the product streams from the natural gas liquid extraction units 100 and 100 'in the respective lines 127 and 127' are gathered together and redistributed in a second distribution box 44 In this embodiment, each main cryogenic system 200 and 200 'thereby receives portions of the vaporized upper light fraction from both natural gas liquid extraction units 100 and 100'. Now with reference to a more detailed embodiment according to that shown in Figure 2, the natural gas precooling heat exchanger train 1 may comprise a precooling heat exchanger 2 but conveniently comprises a set of two or more heat exchangers. heat arranged in series and / or parallel, wherein the precooling refrigerant is allowed to evaporate at one or more pressure levels. For the purpose of simplifion, the precooling heat exchanger train 1 will henceforth be represented in the form of a precooling heat exchanger 2. The natural gas precooling heat exchanger 2 has a hot side shown schematically in the form of a tube 12 having an inlet 13 for gas natural and an outlet 14 for pre-cooled natural gas. The tube 12 is arranged on the cold side 15, which may be a cover side 15, of the natural gas precooling heat exchanger 2. The plant according to the invention typically also comprises a precooling coolant circuit 3. The precooling refrigerant circuit 3 comprises a precooling refrigerant compressor 31 having an inlet 33 and an outlet 34. The outlet 34 is connected via the conduit 35 to a cooler 36, which may be an air cooler or an air cooler. water cooler. The conduit 35 is extended by an expansion device, provided here in the form of a regulating valve 38, to the inlet 39 of the cold side 15 of the natural gas precooling heat exchanger 2. The outlet 40 of the cold side 15 is connected by way of the return duct 41 to the inlet 33 of the precooling refrigerant compressor 31. Conveniently, the precooling refrigerant circuit comprises four pressure levels for precooling the natural gas stream in two or three or four stages. The pre-cooling refrigerant configuration can be provided in accordance with US Patent 6,637,238, which is incorporated herein by reference.
The distributor 4 has an inlet 18 connected via conduit 19 to outlet 14 to receive precooled natural gas and two outlets 22 and 23. Alternatively, not shown here, distributor 4 can be provided upstream of a final precooling stage. , whereby the two outlets 22 and 23 are connected to the inlets of two parallel hot sides in the final precooling stage whereby the streams flowing through these parallel hot sides can exchange heat against the precooling coolant in the pre-cooling refrigerant circuit. Each main cryogenic system 200, 200 'contains a main heat exchanger 5, 5', and a main refrigerant circuit 9, 9 '. Each main heat exchanger 5, 5 'comprises a first hot side 25, 25' having an inlet 26, 26 '. The inlet 26 of the first hot side 25 is connected to the outlet 22 of the distributor 4 through the natural gas liquid extraction unit 100 by means of the conduits 27 and 127, and the inlet 26 'of the first hot side 25' it is connected to the outlet 23 by the natural gas liquid extraction unit 100 'by means of the conduits 27' and 127 '. Each first hot side 25, 25 'has an outlet 28, 28' in the upper part of the main heat exchanger 5, 5 'for liquefied natural gas. The first hot side 25, 25 'is lod in the cold side 29, 29 'of the main heat exchanger 5, 5', whose cold side 29, 29 'has an outlet 30, 30'. The main heat exchangers 5 and 5 'are each associated with a liquefaction refrigerant circuit 9 respectively 9'. Each liquefaction refrigerant circuit 9, 9 'comprises a liquefying refrigerant compressor 50, 50' having an inlet 51, 51 'and an outlet 52, 52'. The inlet 51, 51 'is connected by means of a return duct 53, 53' to the outlet 30, 30 'of the cold side 29, 29' of the main heat exchanger 5, 5 '. The outlet 52, 52 'is connected via the conduit 54, 54' to a cooler 56, 56 ', which can be an air cooler or a water cooler, and the hot side 57, 57' of a heat exchanger. cooling heat 58, 58 'to a separator 60, 60 J Each separator 60 has an outlet 61, 61' for liquid at its lower end and an outlet 62, 62 'for gas at its upper end.
Each heat exchanger 58, 58 'includes a cold side 85, 85' having an inlet 139, 139 'and an outlet 140, 140' to allow the entry of an auxiliary refrigerant and the discharge of spent auxiliary refrigerant. The cold side 85 is included in an auxiliary refrigerant cycle for which many options are feasible, among which are the following: One option is that the auxiliary refrigerant cycle is incorporated as a parallel cycle as described in the aforementioned US Patent 6,389,844, incorporated herein by reference, which utilizes the precooling refrigerant compressor 31 and a cooler 36, through which the inlet 139, 139 'is connected to the line 37 by an expansion device such as a regulator valve, and outlet 140, 140 'is connected to line 41. In another option, a separate auxiliary refrigerant circuit is provided as described in the aforementioned US Patent Application Publication 2005/0005635, incorporated herein by reference. reference, which utilizes an auxiliary refrigerant compressor to feed each of the refrigerant heat exchangers 58, 58 'in parallel or using an auxiliary refrigerant compressor adapted for each refrigerant heat exchanger 58, 58'. In yet another option, for which reference is made to Figures 2 and 3 of US Pat. No. 6,389,844 already incorporated in the present specification, the natural gas precooling heat exchanger 2 and the refrigerant heat exchangers 58 and 58 ' shown in Figure 2 are combined in an integrated heat exchanger, whereby hot sides 57 and 57 'are incorporated in the form of additional hot tube packages in one or more of the precooling heat exchangers 2 of the precooling heat exchangers 1.
Instead of a stage, the integrated pre-cooling heat exchanger train may comprise two or three or more stages in series, as described with specific reference to Figure 3 in US Patent 6,389,844 already incorporated by reference. Each liquefying refrigerant circuit 9, 9 'further includes a first conduit 65, 65' extending from the outlet 61, 61 'to the inlet of a second hot side 67, 67' extending to a midpoint of the exchanger of main heat 5, 5 ', a conduit 69, 69', an expansion device 70, 70 'and an injection nozzle 73, 73'. Each liquefying refrigerant circuit 9, 9 'further includes a second conduit 75, 75' extending from the outlet 62, 62 'to the inlet of a third hot side 77, 77' extending to the top of the exchanger of main heat 5, 5 ', a conduit 79, 79', an expansion device 80, 80 'and an injection nozzle 83, 83'. The two natural gas liquid extraction units 100 and 100 'each comprise a distillation column 105 respectively 105'. The distillation column 105, 105 'is conditioned with a distillation column inlet 107, 107', which in the present embodiment is at the same time the extraction unit inlet which is connected to the distributor 4. Specifically, distillation column input 107 is connected to outlet 22 of distributor 4 via conduit 27, and distillation column input 107 'is connected to outlet 23 via conduit 27'. The extraction unit outputs are supplied in the form of lines 127 and 127 'respectively. Distillation column 105, 105 'further has a heavy fraction outlet 109, 109' for discharging a liquid (to line 108, 108 ') separated from the natural gas stream pre-cooled in the corresponding line 27, 27', and an upper outlet of light fraction 111, 111 'to discharge a vapor separated from the stream of natural gas precooled in the corresponding line 27, 27'. A fractionation unit (not shown), whether operating in the parallel heavy fractions or in the combined heavy fractions, can be connected to the heavy fraction output 109, 109 '. The distillation column 105, 105 'is in accordance with that shown in Figure 2, it is conditioned only with a rectification section. Although not required by this invention, the distillation column can also be conditioned with a rectification section and an etching section, by adding an evaporator to raise the temperature at the bottom of the column. Also a Absorption section can be conditioned in the distillation column if necessary. The distillation column can be a forced separation column. The natural gas liquid extraction unit 100, 100 'further comprises an upper heat exchanger unit 113, 113', an upper separator 117, 117 'in the shape of a reflux drum, and a reflux pump 119, 119 ' The reflux drum 117, 117 'comprises a liquid reflux outlet 121, 121', and a vapor outlet 123, 123 '. The upper output of light fraction 111, 111 'is connected to a hot side 116, 116' of the upper heat exchanger unit 113, 113 ', from which the cold side 112, 112' can be exposed to a cold stream 115, 115 J The hot side outlet of the upper heat exchanger 113, 113 'is connected to the reflow drum 117, 117'. The liquid reflux outlet 121, 121 'is connected to a suction side of the reflux pump 119, 119' of which a pressure side is connected to a reflux inlet 125, 125 'conditioned in the distillation column corresponding 105, 105 '. The steam outlet 123, 123 'is connected to the line 127, 127 J Conveniently the main refrigerant circuits 9 and 9' are identical with each other and thus are the main heat exchangers 5 and 5 'and the heat exchanger units. extraction of natural gas liquids 100 and 100 '.
During normal operation, natural gas is supplied to the precooling heat exchanger train 1 via the inlet 13 of the hot side 14 of the natural gas precooling heat exchanger 2 through the conduit 90. Normally, depending on the composition of the natural gas, the natural gas is partially condensed in the precooling heat exchanger train 1. The precooling refrigerant is withdrawn from the outlet 40 on the cold side 15 of the natural gas precooling heat exchanger 2, compressed in the compressor of precooling coolant 31 to an elevated pressure, condensed in the condenser 36 and allowed to expand in the expansion device 38 to a low pressure. On the cold side 15 the expanded precooling refrigerant is allowed to evaporate at low pressure and in this way the heat is extracted from the natural gas. The precooled natural gas withdrawn from the hot side 14 is led to the distributor 4 through the conduit 19, where it is divided into at least a first and a second precooled natural gas substream. The amounts of natural gas that pass through conduits 27 and 27 'are conveniently equal with one another. Through conduits 27 and 27 'the respective first and second precooled natural gas streams are supplied to the entries 107 and 107 'of the natural gas liquid extraction units 100 and 100'. Here, each of the first and second precooled natural gas substreams are fed into their respective distillation columns 105 and 105 'where they are simultaneously separated, typically by distillation or forced separation, into a heavy fraction comprising the condensed part of the corresponding undercurrent, and a vaporized upper light fraction. Depending on the temperature in the distillation column, the vaporized upper light fraction is de-enriched for C3 + components that include propane and contains predominantly methane, and frequently also C2 components that include ethane, and nitrogen. The vaporized light overhead stream leaves the distillation column 105, 105 'through the upper outlet of light fraction 111, 111' after which it is fed to the hot side 116, 116 'of the upper heat exchanger 113, 113' in where it is partially condensed in a partially condensed overhead stream comprising a mixture of light condensate and light steam. The partially condensed upper stream is fed to the reflow drum 117, 117 'where the light condensate is separated from the light steam. The light condensate is removed from the reflux drum 117, 117 'by the liquid reflux outlet 121, 121', and fed to a reflux of cold liquid into the distillation column 105, 105 '. The light steam is extracted from the steam outlet 123, 123 'and fed to the inlets 26 and 26' of the first hot sides 25 and 25 'of the main heat exchangers 5 and 5'. On the first hot side 25, 25 'the vaporized light fraction of the natural gas is liquefied and subcooled. Subcooled natural gas is withdrawn through conduits 95 and 95 '. Subcooled natural gas is conducted to a unit for further treatment, of which some options will be discussed later in this specification, and to tanks for storing liquefied natural gas (not shown). The main refrigerant is withdrawn from the outlet 30, 30 'of the cold side 29, 29' of the main heat exchanger 5, 5 ', compressed to an elevated pressure in the liquefying refrigerant compressor 50, 50'. The heat from the compression is removed in the cooler 56, 56 'and additional heat is removed from the main coolant in the coolant heat exchanger 58, 58' to obtain partially condensed coolant. The partially condensed main refrigerant is then separated in the separator 60, 60 'in a liquid, heavy fraction, and a light, gaseous fraction, whose fractions are further cooled in the second and third hot sides 67, 67' and 77, 77 'respectively to obtain liquefied and subcooled fractions at elevated pressure. The subcooled refrigerants are then allowed to expand in the expansion devices 70, 70 'and 80, 80' to a lower pressure. In this pressure the refrigerant is allowed to evaporate on the cold side 29, 29 'of the main heat exchanger 5, 5' to extract heat from the natural gas passing through the first cold side 25, 25 '. The cold stream 115, 115 ', or upper stream of refrigerant 115, 115', required to condense the reflux of liquid out of the vaporized upper light fraction may come from any suitable source. For example, it can be fed with a current derived from cycle 3, or can be integrated as a pressure level in cycle 3. In the latter case hot side 116, 116 'can be integrated parallel to hot side 12 within a integrated heat exchanger, or the hot side 116, 116 'may be part of a separate heat exchanger unit 113, 113' through which the precooling refrigerant is fed into the cold side 112, 112 '. Alternatively, the upper coolant stream 115, 115 'can be fed with a current derived from the main coolant, for example from line 65, 65'. This can be achieved with an arrangement where the cold side 115, 115 'of the upper heat exchanger is in fluid communication with at least one of at least two main refrigerant circuits 9, 9 '. An advantage of the indirect heat exchanging the vaporized upper light fraction with the main refrigerant in at least one of the at least two main refrigerant circuits 9, 9 'is that the temperature of the pre-cooled natural gas stream is at a low point. as possible which helps achieve a deeper extraction of C3 + in the separation of natural gas liquids. In addition, the temperature of the liquid reflux stream leaving the outlet 121, 121 'may be lower to increase the recovery of C3 +. Other options are formed by any combination of two or more of the described options for cooling the vaporized upper light fraction, in particular a combination involving an integration of the hot side 116, 116 'in another heat exchanger followed by a separate upper unit of heat exchanger 113, 113 'arranged downstream of the integrated. It has been found that the temperature of the pre-cooled natural gas is around -25 ° C when the compressor drive power for each of the main refrigerant circuits 9, 9 'and the compressor drive energy for the refrigerant circuit of pre-cooling 3 are equal and the plant is operated at Maximum capacity. The pressure of the pre-cooled natural gas is typically between 4 MPa and 6 MPa (40 and 60 bar). Preferably the temperature of the liquid reflux stream is between -25 ° C and -65 ° C, whereby upon lowering the temperature most of the C3 + components are separated out of the pre-cooled natural gas. More preferably, the temperature of the reflux stream of liquid is lower than -31 ° C. A percentage of 40 to 45% propane recovery is feasible with a cold reflux temperature of about -45 ° C, using a main refrigerant for the upper cooling in the upper heat exchanger 113, 113 '. This depends on the pressure and composition of the gas. Reference is now made to Figure 3 which shows a modality involving a specific example of the use of main refrigerant from one of the main refrigerant circuits 9, 9 'to cool the vaporized upper light fraction extracted from the upper separator 117, 117 '. The hot side 116, 116 'is integrated into the main heat exchanger. Figure 3 largely corresponds to Figure 2 but in this the natural gas liquid extraction units 100, 100 'have been replaced by an alternative embodiment of natural gas liquids extraction unit 110, 110'. Since Figure 3 corresponds to Figure 2 it will not be described again, but the general reference is made instead to the corresponding parts of Figure 2.
The main cryogenic heat exchangers 5, 5 'have been replaced by a modified version 55, 55', where the hot face 25, 25 'is divided into an upstream part 24, 24' and a downstream part 24a, 24a ' In the alternative mode, the upper output of light fraction 111, 111 'is connected to the inlet 26, 26' of the corresponding upstream part 24, 24 'via the conduit 126, 126'. The outlet of the upstream part 24, 24 'is connected to the reflux drum 117, 117' and the steam outlet 123, 123 'of the reflux drum 117, 117' is connected to the corresponding inlet of the downstream part 24a, 24a 'on the hot side 25, 25' through the duct 127, 127 '. As with the main heat exchanger 5, 5 ', the downstream part 24a, 24a' has an outlet 28, 28 'in the upper part of the main heat exchanger 55, 55' for the liquefied natural gas. During the normal operation of the alternative mode, the cold required to condense the reflux of liquid out of the vaporized upper light fraction is provided by the main refrigerant. In another embodiment (not shown) the natural gas liquid extraction unit 100, 100 'and / or 110, 110' and the separation of partially condensed natural gas substreams into a heavy fraction comprising the condensed part of the corresponding substream, and a vaporized upper light fraction, takes a form in accordance with the modalities thereof as described in Publication WO 2004 / 069384, incorporated herein by reference. In particular, the reflux of cold liquid in such embodiments is divided into first and second reflux streams of which the first is introduced into the upper part of the forced separation column and the second at a mid-point. In the embodiments described above, the precooling refrigerant is conveniently a single-component refrigerant, such as propane, or a mixture of hydrocarbon components or other convenient refrigerant used in a compression-cooling cycle or in an absorption-cooling cycle. . The main refrigerant is conveniently a multi-component refrigerant comprising nitrogen, methane, ethane, propane and butane. Conveniently, the refrigerant heat exchangers 58 and 58 'comprise a set of two or more heat exchangers arranged in series, wherein the precooling refrigerant is allowed to evaporate at one or more pressure levels.
The main heat exchangers 5 and 5 'and 55 and 55' may be of any suitable design, such as a rotary heat exchanger or a plate-fin heat exchanger. In the embodiments according to that described with reference to Figures 2 and 3, the main heat exchangers 5, 5 ', 55, 55' have a second and a third hot side, 67, 67 'and 77, 77', respectively. In an alternative embodiment, the main heat exchanger has only one hot side in which the second and third hot sides are combined. In this case the partially condensed main coolant is supplied directly to the third hot side 77, 77 ', without separating it into a liquid, heavy fraction, and a light, gaseous fraction. The compressors 31, 50 and 50 'can be multi-stage compressors with an intercooling, or a combination of compressors in series with an intercooling between two compressors, or a combination of compressors in parallel. The compressors 31, 50 and 50 'in the precooling refrigerant circuit 3 and the two main refrigerant circuits 9 and 9' can be turbine driven or electric motor driven, or a turbine / electric motor combined drive. Conveniently the turbine (not shown) in the precooling refrigerant circuit is a turbine of steam. In this case conveniently, the steam required to drive the steam turbine is generated with the heat released from the cooling of the gas turbine extractors (not shown) of the main refrigerant circuits. The present invention provides a plant for liquefying natural gas that can be expanded, wherein in a first stage a single train is constituted with a capacity of 100% liquefaction, and wherein in a second stage the second main heat exchanger and the second liquefaction refrigerant circuit of the same size equal to the first can be added to expand the liquefaction capacity to between approximately 140 and approximately 160%, while the C3 + components of natural gas can be controlled. An advantage of the present invention is that the pre-cooling and liquefaction conditions, for example the refrigerant compositions, can be easily adapted so that an efficient operation is achieved. Moreover, in case one of the liquefaction circuits has to be left out of operation, the conditions can be adapted to work efficiently with a single liquefaction train. The calculations have also shown that the efficiency of liquefaction (amount of liquefied gas produced per unit of work performed by the compressors) is not affected adverse by the use of a pre-cooling refrigerant circuit that assists two main refrigerant circuits. The liquefaction capacity can be further extended by the supply of at least one final expansion unit, connected to the outlet conduits 95, 95 'for liquefied natural gas. Figure 4 shows an embodiment of such a final expansion unit that can be added to any of the plants described above. Each conduit 95, 95 'is connected to a final expansion expander 97, 97' and a regulating valve 99, 99 '. The low pressure ends discharge into conduits 101, 101 'which both connect to a final expansion gas separator 103. Alternatively, the junction where the liquefied natural gas in conduits 95 and 95' is combined upstream of a single final expansion expander (not shown). The final expansion gas separator is supplied with a final expansion gas outlet 133 and a liquefied natural gas outlet 135. An optional pump 137 can be conditioned to carry the liquefied natural gas to any desired pressure before discharging it into the line 138 for transport or storage. The expanded gas outlet 133 is connected to a compressor 139. The high pressure outlet of the compressor 139 it is connected to a cooler 141, which can be an environmental cooler. A heat exchanger 143 is supplied upstream of the compressor 139 to have the ability to maintain the cold created in the final expansion gas. During normal operation, the pressure in the liquefied natural gas is lowered in the final expansion expander 97, 97 'and the regulating valve 99, 99', preferably at atmospheric or near atmospheric conditions. This expansion lowers the temperature of the liquefied natural gas, and final expansion gas is also formed in the process. Typically, the temperature is lowered by approximately 10 ° C when the expanded pressure drops from 5 MPa (50 bar) to atmospheric pressure. Due to a further drop in temperature, more liquefied natural gas can be produced with a certain cooling energy in the pre-cooling train 1 and the main cryogenic systems 200, 200 '. The final expansion gas is separated from the liquefied natural gas in the final expansion gas separator 103. The final expansion gas exiting the final expansion gas separator 103 is compressed to a pressure by which it can be discharged through line 145 for additional use, for example as fuel gas. The cold present in the final expansion gas can be retained by heat exchanger 143, for example to precool the main refrigerant. In that case, the heat exchanger 143 could be included in the main refrigerant circuits 9, 9 '. For the purpose of further increasing the capacity of the plant, an optional final expansion gas feedback loop can be supplied through which a portion of the final expansion gas in line 145 is at least partially condensed and reinjected inside. of the liquefied natural gas stream upstream of the final expansion separator 103. For this purpose, the optional feedback circuit may comprise an additional compressor 147, of which the low pressure terminal is connected to line 145. The high-end terminal pressure of the additional compressor 147 is connected to a line upstream of the final expansion gas separator, consecutively by means of an optional additional cooler 149, a heat exchanger 143 and an expansion device such as a regulating valve 151. With reinjection optional, additional compressors 139 and 147 provide extra points where the service d Cooling can be introduced into the process and the cooling temperature in the main refrigerant circuits can be increased. Due to the extra cooling service added in this way it can be produced a higher quantity of liquid natural gas. Calculations have shown that 4 to 5% additional liquefaction capacity can be achieved with the final expansion system that includes optional recycling. Other final expansion or expanded systems may be used instead of those described here. The final expansion system according to what is described in the US Patent 5,893,274 is included as a reference. It is noted that in relation to this date, the best method known to the applicant to carry out the aforementioned invention, is that which is clear from the present description of the invention.

Claims (9)

  1. CLAIMS Having described the invention as above, the content of the following claims is claimed as property: 1. A plant for liquefying natural gas, characterized in that it comprises: - a pre-cooling heat exchanger train with a pre-cooling refrigerant circuit to extract natural gas heat in the pre-cooling heat exchanger train, which has an inlet for natural gas and an outlet for pre-cooled natural gas; a distributor for dividing the natural gas stream into at least a first and a second natural gas substream; - at least two extraction units of natural gas liquids each conditioned with an extraction unit inlet arranged to receive one of the natural gas substreams, and comprising a heavy fraction outlet, and an upper outlet of light fraction; and - at least two main cryogenic systems each comprise a main heat exchanger having a first hot side having an inlet connected to the upper outlet of light fraction of at least one of the gas liquid extraction units natural gas and an outlet for liquefied natural gas, and each one comprises a
  2. main coolant circuit to extract heat from natural gas flowing through the first hot side of the corresponding main heat exchanger. The plant according to claim 1, characterized in that each of the natural gas liquid extraction units is conditioned with a reflux inlet arranged to receive a reflux of liquid from a liquid reflux outlet of a top separator , the upper separator is conditioned with an inlet in fluid communication with the upper outlet of light fraction and a vapor outlet in fluid communication with the corresponding main cryogenic heat exchanger.
  3. 3. The plant according to claim 2, characterized in that an upper heat exchanger is provided upstream of the upper separator to extract heat from the upper light fraction, from the upper heat exchanger the cold side is in fluid communication with at least one of the at least two main refrigerant circuits.
  4. The plant according to claim 1, 2, or 3, characterized in that it also comprises at least one final expansion unit, connected to the outlets for the liquefied natural gas of the at least two heat exchangers and comprises at least one outlet for a final expansion gas and one outlet for liquefied natural gas.
  5. 5. A plant for liquefying natural gas according to any of claims 1-4, characterized in that the distributor has two exits, and wherein the plant comprises two extraction units of natural gas liquids and two main heat exchangers.
  6. 6. A method for liquefying a natural gas stream, characterized in that it comprises: pre-cooling the natural gas stream in a heat exchanger train against a pre-cooling refrigerant that is circulated in a pre-cooling refrigerant circuit, thereby obtaining a pre-cooled natural gas stream; - dividing the pre-cooled natural gas stream into at least one first and second natural gas substreams; simultaneously separating each of the first and second subcurrents of natural gas in a liquid heavy fraction, and a vaporized upper light fraction; further cooling the vaporized upper light fractions in a total condensation against a main refrigerant in at least two main cryogenic systems, by which in each main cryogenic system the main refrigerant is circulated in a main refrigerant circuit; and - extracting a stream of liquefied natural gas therefrom.
  7. 7. The method according to claim 6, characterized in that the additional cooling comprises partially condensing each of the vaporized upper light fractions to form a light condensate and a light vapor, separating the light condensate from the light steam, feeding the light condensate as a reflux cold in the step of simultaneously separating each of the first and second sub streams of partially condensed natural gas and further cooling the light steam in a complete condensation. The method according to claim 7, characterized in that the partial condensate of each of the vaporized upper light fractions comprises an indirect heat exchange with the main refrigerant in at least one of the at least two refrigerant circuits main. The method according to any of claims 6 to 8, characterized in that the stream of liquefied natural gas is subsequently expanded whereby a mixture comprising an additionally cooled liquefied natural gas and an expanded vapor is formed, whereby the Expanded steam is separated from still further liquefied natural gas cooled, compressed, at least partially condensed and reinjected into the liquefied natural gas stream upstream of the expanded vapor separation.
MX2007009824A 2005-02-17 2006-02-15 Plant and method for liquefying natural gas. MX2007009824A (en)

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Families Citing this family (33)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20070204649A1 (en) * 2006-03-06 2007-09-06 Sander Kaart Refrigerant circuit
WO2007131850A2 (en) * 2006-05-15 2007-11-22 Shell Internationale Research Maatschappij B.V. Method and apparatus for liquefying a hydrocarbon stream
WO2008033183A2 (en) 2006-09-11 2008-03-20 Exxonmobil Upstream Research Company Transporting and managing liquefied natural gas
WO2008034874A2 (en) * 2006-09-22 2008-03-27 Shell Internationale Research Maatschappij B.V. Method and apparatus for producing a cooled liquefied hydrocarbon stream
EP2074364B1 (en) 2006-09-22 2018-08-29 Shell International Research Maatschappij B.V. Method and apparatus for liquefying a hydrocarbon stream
EP2104824A2 (en) * 2006-10-23 2009-09-30 Shell Internationale Research Maatschappij B.V. Method and apparatus for cooling hydrocarbon streams
RU2464510C2 (en) * 2006-11-14 2012-10-20 Шелл Интернэшнл Рисерч Маатсхаппий Б.В. Method and device for hydrocarbon flow cooling
KR100948740B1 (en) * 2008-03-19 2010-03-22 현대중공업 주식회사 High Efficient Offshore Liquefied Natural Gas Production Facility Using Subcooling and Latent Heat Exchange
BRPI0918769B1 (en) * 2008-09-09 2021-01-05 Conocophillips Company system to improve gas turbine performance in a natural gas plant
US20100147024A1 (en) * 2008-12-12 2010-06-17 Air Products And Chemicals, Inc. Alternative pre-cooling arrangement
KR101187532B1 (en) * 2009-03-03 2012-10-02 에스티엑스조선해양 주식회사 boil-off gas management apparatus of electric propulsion LNG carrier having reliquefaction function
US10082331B2 (en) 2009-07-16 2018-09-25 Conocophillips Company Process for controlling liquefied natural gas heating value
CA2767369C (en) * 2009-07-21 2017-10-24 Shell Internationale Research Maatschappij B.V. Method for treating a multi-phase hydrocarbon stream and an apparatus therefor
KR101787335B1 (en) * 2010-06-30 2017-10-19 쉘 인터내셔날 리써취 마트샤피지 비.브이. Method of treating a hydrocarbon stream comprising methane, and an apparatus therefor
CN102796580A (en) * 2012-08-28 2012-11-28 安瑞科(蚌埠)压缩机有限公司 Method for stabilizing liquid mixed hydrocarbon
RU2538192C1 (en) * 2013-11-07 2015-01-10 Открытое акционерное общество "Газпром" Method of natural gas liquefaction and device for its implementation
EP2977430A1 (en) 2014-07-24 2016-01-27 Shell Internationale Research Maatschappij B.V. A hydrocarbon condensate stabilizer and a method for producing a stabilized hydrocarbon condenstate stream
EP2977431A1 (en) 2014-07-24 2016-01-27 Shell Internationale Research Maatschappij B.V. A hydrocarbon condensate stabilizer and a method for producing a stabilized hydrocarbon condenstate stream
AU2016368494B2 (en) * 2015-12-08 2020-03-12 Shell Internationale Research Maatschappij B.V. Controlling refrigerant compression power in a natural gas liquefaction process
WO2017177317A1 (en) 2016-04-11 2017-10-19 Geoff Rowe A system and method for liquefying production gas from a gas source
US10359228B2 (en) 2016-05-20 2019-07-23 Air Products And Chemicals, Inc. Liquefaction method and system
WO2017214723A1 (en) 2016-06-13 2017-12-21 Geoff Rowe System, method and apparatus for the regeneration of nitrogen energy within a closed loop cryogenic system
FR3053771B1 (en) * 2016-07-06 2019-07-19 Saipem S.P.A. METHOD FOR LIQUEFACTING NATURAL GAS AND RECOVERING LIQUID EVENTS OF NATURAL GAS COMPRISING TWO NATURAL GAS SEMI-OPENING REFRIGERANT CYCLES AND A REFRIGERANT GAS REFRIGERANT CYCLE
CN109323126A (en) * 2017-08-01 2019-02-12 通用电气公司 Natural gas liquefaction system and method
RU2701173C1 (en) * 2019-03-06 2019-09-25 Андрей Владиславович Курочкин Plant for production of liquefied natural gas
RU2699911C1 (en) * 2019-03-06 2019-09-11 Андрей Владиславович Курочкин Plant for producing lng
RU2702683C1 (en) * 2019-04-15 2019-10-09 Андрей Владиславович Курочкин Plant for production of liquefied natural gas
RU2702682C1 (en) * 2019-04-15 2019-10-09 Андрей Владиславович Курочкин Installation for liquefied natural gas production and method of its operation
RU2702680C1 (en) * 2019-04-15 2019-10-09 Андрей Владиславович Курочкин Unit for reduction of natural gas with generation of lng
WO2020225096A1 (en) 2019-05-03 2020-11-12 Shell Internationale Research Maatschappij B.V. Method and system for controlling refrigerant composition in case of gas tube leaks in a heat exchanger
RU2750825C1 (en) * 2020-02-24 2021-07-05 Андрей Владимирович Иванов Launch vehicle with universal upper stage and propulsion system for it
AU2021225308B2 (en) 2020-02-25 2023-11-30 Shell Internationale Research Maatschappij B.V. Method and system for production optimization
EP3943851A1 (en) 2020-07-22 2022-01-26 Shell Internationale Research Maatschappij B.V. Method and system for natural gas liquefaction with improved removal of heavy hydrocarbons

Family Cites Families (21)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2384221A1 (en) * 1977-03-16 1978-10-13 Air Liquide PLATE EXCHANGER TYPE HEAT EXCHANGE ASSEMBLY
US4445916A (en) * 1982-08-30 1984-05-01 Newton Charles L Process for liquefying methane
US4541852A (en) * 1984-02-13 1985-09-17 Air Products And Chemicals, Inc. Deep flash LNG cycle
DE3528071A1 (en) * 1985-08-05 1987-02-05 Linde Ag METHOD FOR DISASSEMBLING A HYDROCARBON MIXTURE
JP3320934B2 (en) * 1994-12-09 2002-09-03 株式会社神戸製鋼所 Gas liquefaction method
MY117899A (en) * 1995-06-23 2004-08-30 Shell Int Research Method of liquefying and treating a natural gas.
DZ2671A1 (en) * 1997-12-12 2003-03-22 Shell Int Research Liquefaction process of a gaseous fuel product rich in methane to obtain a liquefied natural gas.
TW477890B (en) * 1998-05-21 2002-03-01 Shell Int Research Method of liquefying a stream enriched in methane
TW421704B (en) * 1998-11-18 2001-02-11 Shell Internattonale Res Mij B Plant for liquefying natural gas
US6347532B1 (en) * 1999-10-12 2002-02-19 Air Products And Chemicals, Inc. Gas liquefaction process with partial condensation of mixed refrigerant at intermediate temperatures
MY125082A (en) * 1999-12-15 2006-07-31 Shell Int Research Compression apparatus for gaseous refrigerant
FR2818365B1 (en) * 2000-12-18 2003-02-07 Technip Cie METHOD FOR REFRIGERATION OF A LIQUEFIED GAS, GASES OBTAINED BY THIS PROCESS, AND INSTALLATION USING THE SAME
US6742358B2 (en) * 2001-06-08 2004-06-01 Elkcorp Natural gas liquefaction
JP2003280126A (en) * 2002-01-18 2003-10-02 Fuji Photo Film Co Ltd Method for production of silver halide photographic emulsion and production apparatus therefor
US6658892B2 (en) * 2002-01-30 2003-12-09 Exxonmobil Upstream Research Company Processes and systems for liquefying natural gas
JP4032128B2 (en) * 2002-08-01 2008-01-16 東ソー株式会社 Microchannel structure, desk-size chemical plant constructed, and fine particle production apparatus using them
CN100575855C (en) * 2002-09-10 2009-12-30 Gac株式会社 Heat exchanger and manufacture method thereof
EP1549893A1 (en) * 2002-09-30 2005-07-06 BP Corporation North America Inc. Modular lng process
EP1471319A1 (en) * 2003-04-25 2004-10-27 Totalfinaelf S.A. Plant and process for liquefying natural gas
US20060260355A1 (en) * 2005-05-19 2006-11-23 Roberts Mark J Integrated NGL recovery and liquefied natural gas production
EP2074364B1 (en) * 2006-09-22 2018-08-29 Shell International Research Maatschappij B.V. Method and apparatus for liquefying a hydrocarbon stream

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RU2007130261A (en) 2009-02-20
MY141434A (en) 2010-04-30
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