Classifications

• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
  • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
  • F25J1/0022—Hydrocarbons, e.g. natural gas
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
  • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
  • F25J1/0047—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
  • F25J1/003—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
  • F25J1/0057—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 after expansion of the liquid refrigerant stream 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
  • F25J1/02—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
• • 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
  • F25J1/0217—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 at least a three level refrigeration cascade with at least one MCR cycle
  • F25J1/0218—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 at least a three level refrigeration cascade with at least one MCR cycle with one or more SCR cycles, e.g. with 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
  • F25J1/0243—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
  • F25J1/0275—Construction and layout of liquefaction equipments, e.g. valves, machines adapted for special use of the liquefaction unit, e.g. portable or transportable devices
  • F25J1/0277—Offshore use, e.g. during shipping
  • F25J1/0278—Unit being stationary, e.g. on floating barge or fixed platform
• • 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.
• • 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
  • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
  • F25J1/007—Primary atmospheric gases, mixtures thereof
  • F25J1/0072—Nitrogen
• • 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
  • 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.
  • F25J1/029—Mechanically coupling of different refrigerant compressors in a cascade refrigeration system to a common 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
  • F25J2210/00—Processes characterised by the type or other details of the feed stream
  • F25J2210/04—Mixing or blending of fluids with the feed 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
  • 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
• • 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

Definitions

• the present invention relates to a device for liquefying a natural gas, a liquefaction process of a natural gas and a vessel comprising such a device. It applies, in particular, to the liquefaction at sea or on land of natural gas.
• the liquefaction of the gas allows the transport of natural gas at a lower volume compared to the transport of the non-liquefied natural gas.
• a mixture of refrigerants is compressed and then fractionated into a heavy fraction and a light fraction
• the heavy fraction being used in a first plate heat exchanger between this heavy fraction and the natural gas to cool it,
• the light fraction being used in a second plate heat exchanger between this light fraction and the cooled natural gas in order to liquefy this natural gas and
• plate exchangers are very sensitive to the distribution of fluids, which poses a problem of marinization for marine applications,
• the refrigerant mixture contains a large number of components, especially heavy compounds, these compounds crystallize in the heat exchangers at particular pressure and temperature conditions whose advent is not easily predictable and
• the process has a limited flexibility, especially in terms of operating flow and a production capacity by limited compression means.
• the cooling mixture is a mixture of nitrogen and hydrocarbons (methane, ethane, ibutane, nbutane, ipentane and npentane).
• the partial vaporization of this low-pressure mixture makes it possible to cool, liquefy the natural gas and cool the LNG produced: the low-pressure vaporization of the heavy fraction of the refrigerant mixture (gas at the top of the fractionation column) makes it possible to supply the frigories necessary for cooling at least the natural gas and
• the refrigerant mixture is completely vaporized.
• the refrigerant mixture contains too much constituent (hydrocarbons), complicating the logistics and the operational aspect.
• the storage facilities increase the weight of the installations, critical in installations at sea,
• the Cil process is based on the use of a single compression line using centrifugal compressors.
• a centrifugal compressor serves to compress a gas and consequently to raise its pressure.
• Centrifugal compressors are equipped with wheels rotating around a shaft driven by a turbine or an electric motor. These rotating wheels make it possible to transform the kinetic energy contained in the gas into potential energy in order to raise its pressure.
• the set of wheels is contained in a body called "casing" (or “envelope” in French).
• An envelope can contain a number of wheels between eight and ten at the most, and the higher the number, the more likely the compressor is to have stability problems. Compression is the heart of a liquefaction process. Indeed, each point of efficiency in addition to the compressor increases the production of liquefied natural gas.
• the financial value of a compressor is directly related to the number of envelopes. In fact, the higher the number of envelopes, the higher the investment to be made, but the greater the operational flexibility. Inversely, the decrease in the number of casings leads to a loss of operative flexibility sometimes accompanied by a loss of efficiency.
• the challenge of the present invention is therefore to provide a better compromise between efficiency and investment in order to maintain satisfactory performance over as wide a range of operation as possible.
• the Cil process compression trains comprise a low and medium pressure section and a high pressure compression section.
• the compression stages are grouped into one, two or three envelopes.
• the low and medium pressure section makes it possible to compress the low-pressure refrigerant mixture at the outlet of the cryogenic exchange line.
• the high pressure section compresses the light fraction of the refrigerant mixture that will provide the necessary frigories for the liquefaction and subcooling of the liquefied natural gas.
• the actuation, by the same shaft, low and high pressure sections in the compression train, causes a single rotation speed between the turbines of these sections.
• This rotation speed can be differentiated by the use of multiplication mechanisms between the speed of rotation of the turbines with respect to the single shaft.
• the rotational speeds are necessarily proportional or identical, if necessary, which renders the compression train non-flexible when the flow rates entering each section are not identical or proportional. This can cause mechanical stability problems.
• systems as described in WO 201 1/039279 are known. Such systems separate a hydrocarbon stream in a first fractionator to produce a first overhead hydrocarbon stream and a first low hydrocarbon stream.
• the overhead stream is liquefied and at least a portion is subsequently cooled by a refrigerant to provide a cooled liquefied hydrocarbon stream and a hot refrigerant stream.
• the cooled liquefied hydrocarbon stream is then expanded and stored.
• This document thus teaches a liquefaction method using three different compounds of pure refrigerants, circulating in separate cooling circuits. This teaching is complex to implement, especially from the operational point of view, the supply / logistics, and requires an important space to be implemented.
• this technology imposes a surface ratio to be respected between the lower part and the upper part; this limits the operational flexibility of this technology
• the present invention aims to remedy all or part of these disadvantages.
• the present invention provides a device for liquefying a natural gas, comprising: a compressor of a first vaporized refrigerant chemical mixture, a means for fractionating the compressed mixture into a heavy fraction and a light fraction,
• the device When the third exchange body is positioned upstream of the natural gas inlet in the first exchange body, the device makes it possible to carry out a pre-cooling of the natural gas before the cooling carried out by the first exchange body.
• the device When the third exchange body is positioned downstream of the liquefied natural gas outlet of the second exchange body, the device has an increased capacity.
• This configuration combines the advantages of the classic Cil configuration by reducing its disadvantages, in particular by:
• the present invention uses a single initial refrigerant mixture which, thanks to one or two fractionations is decomposed into two or three mixtures circulating in a single closed circuit.
• the number of equipment used is significantly reduced and the control simplified.
• the third exchange body is positioned upstream of the natural gas inlet in the first exchange body, the device comprising: a means for cooling the second compressed compound and
• the second chemical compound is a pure body composed of nitrogen, propane and / or ammonia or a mixture of nitrogen and propane.
• the first refrigerant mixture comprises nitrogen and methane and at least one of:
• heavy compounds are used in the first refrigerant mixture, these compounds having the advantage of ensuring the vaporization of the first mixture before entering the first compressor.
• the third exchange body is positioned upstream of the inlet of the natural gas in the first exchange body, the device comprising, downstream of the liquefied natural gas outlet of the second exchange body :
• the device which is the subject of the present invention comprises, between an outlet for the second compound of the cooling means of the second compound and the third exchange body, a cooling circuit of the second compound by the heavy fraction of the first mixture. inside the first exchange body.
• a portion of the cooling circuit is configured to cool the second compound by heat exchange with the light fraction of the first mixture in the second exchange body.
• the first exchange body and / or the second exchange body is a wound heat exchanger.
• the cooling means of the second compound is a heat exchanger between the second compound and water.
• the present invention relates to a vessel, which comprises a device for liquefying a natural gas object of the present invention.
• the present invention relates to a process for liquefying a natural gas, comprising:
• FIG. 1 represents, schematically, a first particular embodiment of the device that is the subject of the present invention
• FIG. 2 represents, schematically, a particular embodiment of the ship which is the subject of the present invention
• FIG. 3 represents, schematically and in the form of a logic diagram, a first particular sequence of steps of the method that is the subject of the present invention
• FIG. 4 schematically represents a second particular embodiment of the device that is the subject of the present invention
• FIG. 5 represents, schematically and in the form of a logic diagram, a second particular sequence of steps of the method that is the subject of the present invention
• FIG. 6 schematically represents a third particular embodiment of the device that is the subject of the present invention
• FIG. 7 represents, schematically, a particular embodiment of the compressors of the device which is the subject of the present invention.
• FIG. 8 represents, schematically and in the form of a logic diagram, a third particular sequence of steps of the method which is the subject of the present invention.
• FIG. 1 which is not to scale, shows a schematic view of an embodiment of the device 100 which is the subject of the present invention.
• This device 100 for liquefying a natural gas comprising:
• a compressor 105 of a first vaporized refrigerant chemical mixture means for fractionating the compressed mixture into a heavy fraction and a light fraction
• a second heat exchange body 120 between the light fraction of the first mixture and the natural gas cooled in the first exchange body to liquefy the natural gas
• a means, 140 or 145, for compressing the second vaporized compound for compressing the second vaporized compound.
• the compressor 105 is, for example, a centrifugal compressor provided with a wheel rotating around a shaft driven by a turbine or an electric motor. This rotating wheel makes it possible to transform the kinetic energy contained in the gas into potential energy in order to raise the pressure of said gas. In order to increase the compression achieved, the number of wheels is increased in order to reach a determined discharge pressure.
• the inlet pressure of the compressor 105 is, for example, of the order of at least 2 bar absolute.
• the compression ratio achieved in the compressor 105 is, for example, between 2 and 6.
• This compressor 105 is, for example, configured to compress a first refrigerant mixture which comprises nitrogen and methane and at least one of:
• the composition of the first compound is adjusted according to the composition of the natural gas to be liquefied in the device. This adjustment is made as a function of the vapor function curve, that is to say the equilibrium pressure temperature, of the composition of the natural gas along the exchange line formed of the first body 1 12 and the second 120 exchange body.
• This compressor 105 includes an inlet (not referenced) for vaporized refrigerant mixture and an outlet (not referenced) for compressed refrigerant mixture.
• the compressed refrigerant mixture is preferably cooled in a fifth heat exchanger 106.
• This heat exchanger 106 is, for example, a tubular exchanger in which the cold source is air or water.
• the colder the temperature of the source the greater the efficiency of the process.
• the maximum cooling temperature corresponds to the temperature of the air or water plus fifteen degrees Celsius.
• the cooling mixture preferably cooled in the fifth exchanger 106, is supplied by means of fractionation.
• This fraction means is, for example, a fractionation column.
• the flow entering the fractionation column is two-phase, a portion being gaseous and a portion being liquid.
• the gaseous fraction flows in the column to come out at the head and the liquid fraction in the foot.
• This means 10 fractionation comprises:
• the light fraction leaving the fractionation means 1 enters the first exchange body 1 and is cooled by the heavy fraction passing through the first exchange body 1.
• This light fraction can also, depending on the operating conditions, act as a cold source in the heat exchange occurring with the natural gas entering through the inlet 1 16 of the first exchange body 1 15.
• the fractionation means further comprises an inlet for refluxing a portion of the light fraction, this portion of light fraction is harvested, for example, from a reflux flask.
• the fractionation means 10 then preferably comprises packings, making it possible to improve the transfer of material between the gaseous flow and the liquid fraction from the reflux flask 11, which absorbs the heavier compounds of the gas fraction allowing to obtain a flow rich in nitrogen and methane at the head.
• the means 10 fractionation is preferably provided with a mesh to limit the entrainment of droplets in the gas fraction.
• This reflux flask 1 1 1 is connected to the light fraction outlet of the fractionation means 1, with or without intermediate exchange in the first body 1 15, and similarly operates by separating the light fraction of heavy fraction residues unexpectedly transported by the light fraction out of the fractionation means.
• the balloon 1 1 1 is preferably provided with a mesh to limit the entrainment of droplets in the gaseous fraction.
• the light fraction leaving the fractionation means 1, or the reflux flask 1 1 1 when such a flask 1 1 1 is present, is preferentially compressed by a second compressor 1 12.
• This second compressor 1 12 is, for example, a centrifugal compressor.
• This centrifugal compressor is preferably actuated by the turbine implemented at the compressor 105 when the compressor 105 is a centrifugal compressor.
• the pressure at the outlet of the second compressor January 12 is, for example, of the order of 40 bar absolute and the compression ratio is preferably between 2 and 4.
• the light fraction, with or without compression in the second compressor 1 12, is preferably cooled in a sixth heat exchanger 1 13.
• This heat exchanger 1 13 is, for example, a tubular exchanger in which the cold source is air or water.
• the colder the temperature of the source the greater the cooling efficiency.
• the maximum cooling temperature corresponds to the temperature of the air or water plus fifteen degrees Celsius. The resulting flow brings the cold or the frigories necessary for the cooling of the natural gas.
• the first heat exchanger 1 is, for example, a wound heat exchanger in which the light fraction acts as a cold source and the natural gas as a hot source.
• the first exchanger 1 15 and the second exchanger 120 are formed of a single wound exchanger.
• the natural gas enters the first exchanger 1 through the inlet 1 16.
• the light fraction vaporized during the exchange with the natural gas in the first exchange body 1 is preferably redirected to a balloon 1 14 configured to separate the light fraction into two parts, one being heavier than the other.
• the device 100 preferably comprises a valve 136 upstream of the tank 1 14. This valve creates, for example, an expansion of the gas portion of the first mixture of the order of 20 to 25 bar.
• the two parts of the light fraction are transmitted to the second exchange body 120, the light fraction acting as a cold source in the heat exchange made with the natural gas previously cooled in the first exchange body 1.
• the heavy part of the light fraction is, after passing through the second body 120 of exchange, relaxed in an expansion turbine 1 18 (called “expander” in English), then transmitted to the compressor 105 via the return conduit 125.
• This expansion turbine 1 18 is put in place of a valve 123 or in parallel with this valve 123.
• the heavy part of the light fraction, compressed is reinjected into the second body 120 exchange.
• the light portion of the light fraction is transmitted to the compressor 105 via the return line 125.
• the light portion of the light fraction leaves the second exchange body 120 is expanded in a valve 122, and is reinjected into the second exchange body 120 before being redirected to the compressor 105.
• the valve 122 creates a trigger to reach a pressure of about 4 to 5 bar depending on the pressure drop of the downstream circuit, for example.
• the heavy fraction of the refrigerant mixture leaving the fractionation means is passed to the first exchange body 1 and acts as a heat sink in the exchange with the natural gas.
• the device 100 comprises an expansion turbine 127 in parallel with the valve 122.
• the device 100 comprises the expansion turbine 127 and does not comprise a valve 122.
• the heavy fraction leaves the first exchange body 1 and is reinjected into this first exchange body 1, after being expanded in a pressure regulator 1 19, before being redirected to the compressor 105.
• the expander 1 19 creates a trigger to reach a pressure of about 4 to 5 bar depending on the pressure drop in the first body 1 exchange, for example.
• the return line 125 comprises, between the first exchange body 1 and the compressor 105, a balloon 126.
• This balloon 126 ensures that at the inlet of the first compressor 105, the first refrigerant mixture is exclusively in gaseous form.
• the ball 126 is preferably provided with a mesh to limit the entrainment of droplets in the gaseous fraction.
• the device 100 comprises a pipe connecting a portion of the balloon 126, intended to receive the liquid portion of the first mixture, by means of 10 fractionation.
• this pipe is provided with a pump.
• this pump is activated according to a liquid level captured by a sensor in the portion of the balloon 126 intended to receive the liquid portion of the first mixture.
• natural gas is liquefied through two successive stages of cooling.
• the first step takes place in the first exchange body 1 and the second step takes place in the second exchange body 120.
• the natural gas flows in the first body 1 15 and in the second body 120, preferably against the current of the first refrigerant mixture.
• the cooled natural gas preferably leaves the first body 1 at a temperature of about -30 ° C.
• This cooled natural gas is then preferably directed to a fractionation section (not shown) to separate any condensates from the gaseous fraction.
• the gaseous fraction is transmitted to the second body 120 to be liquefied.
• the present invention proposes the addition of a third cooling step positioned either upstream or downstream of the first two steps.
• a third exchange body 130 is positioned upstream of the inlet 1 16 of the natural gas in the first exchange body 1.
• This third exchange body 130 is, for example, a tubular exchanger using, as a cold source, a second refrigerant compound, and hot source natural gas entering the device 100 to be liquefied.
• the second chemical compound is, for example a pure body composed of nitrogen, propane and / or ammonia or a mixture of nitrogen and propane.
• this ammonia is used alone.
• a third exchange body 135 is positioned downstream of the outlet 121 of liquefied natural gas from the second exchange body 120.
• This third exchange body 135 is, for example, a tubular exchanger using, as a cold source, a second refrigerant compound, and hot source liquefied natural gas exiting in the device 100 to be stored or consumed.
• the natural gas thus liquefied can be expanded at atmospheric pressure by an expansion valve (not shown) before storage.
• the evaporation gas, called "BOG" (for "Boil-off gas”) in English, collected in the liquefied natural gas storage can be reinjected into the device 100 at the gaseous fraction leaving the fractionation section between the first body 1 15 and the second body 120 exchange.
• the second refrigerant compound is here, for example, liquid nitrogen.
• the device 100 Downstream of this third body, 130 or 135, the device 100 comprises a means, 140 or 145, for compressing the second compound.
• This compressor, 140 or 145 is for example a centrifugal compressor.
• the device 100 comprises both the upstream cooling step and the downstream cooling step.
• the third exchange body 130 is called the exchange body positioned upstream of the first exchange body 1 and the fourth exchange body 135 the exchange body positioned downstream of the second body 120. 'exchange.
• the second refrigerant mixture is called the refrigerant mixture used in the third body 130 and the third mixture refrigerates the refrigerant mixture used in the fourth exchange body.
• the device 100 comprises:
• the cooling means 150 is, for example, a heat exchanger between the second vaporized compound during heat exchange with the natural gas in the third exchange body 130 and air or water.
• the device 100 comprises, between an outlet 131 for the second compound of the means 150 for cooling the second compound and the third 130 for the exchange body, a circuit 170 for cooling the second composed of the heavy fraction of the first mixture within the first exchange body.
• This cooling circuit 170 is produced, for example, by the inlet of the second cooled compound in the first exchange body 1, the second cooled compound acting as a hot source with respect to the heavy fraction and to the possible light fraction of the first refrigerant mixture passing through this first exchange body.
• This second vaporized compound can simultaneously act as a cold source with respect to the natural gas entering the first body 1 15 through the inlet 1 16 for natural gas.
• the second vaporized compound leaves the first body 1 15, is expanded in a pressure reducer 124 and is reinjected into the first body 1 15 or in the second body 120.
• the second compound is expanded, for example, to a pressure of between 3 and 4 bar depending on the pressure drop in the upstream pipes.
• This cooling circuit 170 is intended to facilitate the cooling occurring in the cooling means 150.
• a portion of the cooling circuit 170 is configured to cool the second compound by heat exchange with the light fraction of the first mixture in the second 120 exchange body.
• the second compound cooled by heat exchange in the first exchange body 1
• the second vaporized compound then acts as a hot source with respect to the light fraction of the first refrigerant mixture passing through this second exchange body 120.
• This second vaporized compound can simultaneously act as a cold source with respect to the natural gas entered in the second exchange body 120.
• the device 100 comprises:
• the cooling means 160 is, for example, a heat exchanger between the third compressed mixture and air or water.
• natural gas Prior to the third body 130 exchange, natural gas can undergo a pretreatment.
• the compressors and compression means, 105, 1 12 and 140, implemented in this embodiment can be replaced by the compressors, 605, 610 and 620, described with reference to Figure 6 and whose functions are similar.
• FIG. 2 which is not to scale, a schematic view of an embodiment of the ship 200 which is the subject of the present invention is observed.
• This ship 200 comprises:
• FIG. 3 diagrammatically and in the form of a logic diagram shows a particular sequence of steps of the method 300 which is the subject of the present invention.
• This method 300 for liquefying a natural gas comprising:
• a step 305 for compressing a first vaporized refrigerant chemical mixture a step 310 for fractionating the compressed mixture into a heavy fraction and a light fraction
• a second heat exchange step 320 between the light fraction of the first mixture and the natural gas cooled during the first exchange step to liquefy the natural gas and a step 325 of returning the first vaporized refrigerant mixture in the heat exchange bodies to the compression step,
• a step 335 of compressing the second vaporized compound is a step 335 of compressing the second vaporized compound.
• This method 300 is realized, for example, by the implementation of the device 100 as described with reference to FIG. As will be understood, all the variants, all the examples and all the embodiments of the device 100 can also be transposed as steps within the method 300.
• FIG. 4 which is not to scale, shows a schematic view of an embodiment of the device 400 which is the subject of the present invention.
• This device 400 for liquefying a natural gas comprising:
• a second heat exchange body 120 between the light fraction of the first mixture and the natural gas cooled in the first exchange body to liquefy the natural gas
• a line 415 for injecting the evaporation gas at the inlet of the second exchange body is a line 415 for injecting the evaporation gas at the inlet of the second exchange body.
• valve 136 the valve 136.
• natural gas is liquefied through two successive stages of cooling.
• the first step takes place in the first exchange body 1 and the second step takes place in the second exchange body 120.
• the device 400 preferably comprises a fractionation section configured to remove condensates from the gas stream.
• the liquefied natural gas leaving the second body 120 through the outlet 121 passes through a regulator 405 configured to relax the liquefied natural gas at atmospheric pressure.
• the regulator 405 is, for example, a valve implementing the Joule-Tomshon effect.
• This relaxation causes the appearance of evaporation gas, or BOG.
• the BOG thus generated is collected in a collector 410 and injected, via a pipe 415, into the inlet of the second exchange body 120. This injection can take place upstream, in or downstream of the fractionation section if such a section is present.
• the collector 410 is, for example, a gas / liquid separation flask equipped with a mesh to limit the entrainment of droplets in the gas fraction.
• the pipe 415 is provided with a compressor 416 compressing the gaseous fraction leaving the collector 410.
• a third exchange body 420 is positioned upstream of the inlet 1 16 of the natural gas in the first body 15 exchange.
• This third exchange body 420 is, for example, a tubular exchanger using, as a cold source, a second refrigerant compound, and hot source natural gas entering the device 400 to be liquefied.
• the device 400 then comprises a compressor 425 of the second vaporized compound downstream of the third exchange body 420.
• This compressor 425 is, for example, a centrifugal compressor.
• the second chemical compound is, for example a pure body composed of nitrogen, propane and / or ammonia or a mixture of nitrogen and propane.
• the device 400 includes:
• a transfer line 435 for transferring the second cooled compound to the third exchange body 420.
• the cooling means 430 is, for example, a heat exchanger between the second compressed compound and water or brine.
• the device 400 comprises, between an outlet 421 for the second compound of the means 430 for cooling the second compound and the third 420 exchange body, a cooling circuit 440 for the second composed of the heavy fraction of the first mixture within the first exchange body.
• This cooling circuit 440 is produced, for example, by the inlet of the second cooled compound in the first exchange body 1, the second cooled compound acting as a hot source with respect to the heavy fraction and to the possible light fraction of the first refrigerant mixture passing through this first exchange body.
• This second cooled compound can simultaneously act as a cold source with respect to the natural gas entering the first body 1 15 through the inlet 1 16 for natural gas.
• the second vaporized compound leaves the first body 1 15, is expanded in a pressure reducer 424 and is reinjected into the first body 1 15 or in the second body 120.
• the second compound is expanded, for example, at a pressure of 3 to 4 bar at the outlet of the regulator 424.
• This cooling circuit 440 is intended to facilitate the cooling occurring in the cooling means 430.
• This circuit 440 may also include a second part, in the second body 120 exchange, as described with reference to Figure 1.
• the first refrigerant mixture comprises nitrogen and methane and at least one of:
• FIG. 5 diagrammatically shows a particular embodiment of the method which is the subject of the present invention.
• This method 500 for liquefying a natural gas comprising:
• a step 505 for compressing a first vaporized refrigerant chemical mixture a step 510 for fractionating the compressed mixture into a heavy fraction and a light fraction
• a second heat exchange step 520 between the light fraction of the first mixture and the natural gas cooled during the first exchange step to liquefy the natural gas
• a step 540 of injection of the evaporation gas at the inlet of the second exchange stage is a step 540 of injection of the evaporation gas at the inlet of the second exchange stage.
• This method 500 is realized, for example, by the implementation of the device 400 as described with reference to FIG. 4. As it is understood, all the variants, all the examples and all the embodiments of the device 400 are also can be transposed as steps in process 500.
• FIGS. 6 and 7 show diagrammatically a particular embodiment of the device 600 which is the subject of the present invention.
• This device 600 for liquefying a natural gas comprising:
• first heat exchange body 1 between the heavy fraction of the first mixture and the natural gas for cooling at least the natural gas
• second heat exchange body 120 between the compressed light fraction of the first mixture and the natural gas cooled in the first exchange body to liquefy the natural gas
• a transfer line 435 for transferring the second cooled compound to the third exchange body 420.
• envelope a casing that includes at least one compressor. Each compressor has one or more wheels.
• the third compressor 620 corresponds to the third compressor 140 as described with reference to FIG. However, this third compressor 620 is actuated by the implementation of a single turbine common with the turbine operating the first compressor 605.
• the first compressor corresponds to the first compressor 105 as described with reference to FIG.
• the fourth compressor 615 is configured to raise the pressure of the light portion of the light fraction of the first cooling mixture.
• This fourth compressor shares a single turbine common with the second compressor 610, this second compressor 610 corresponding to the second compressor 1 12 as described with reference to FIG.
• the device 600 which is the subject of the present invention comprises:
• a fourth compressor 615 centrifuge the light fraction of the first mixture, the second and fourth centrifugal compressor being actuated by a single turbine 640 common and
• the device 600 which is the subject of the present invention comprises:
• the fourth compressor 615 compressing the separated gas fraction
• the separator 650 is, for example, similar to the reflux flask 14 as described with reference to FIG.
• the regulator 625 is, for example, similar to the expansion turbine 1 18 as described with reference to FIG.
• the second chemical compound comprises nitrogen, propane and / or ammonia.
• the first refrigerant mixture comprises nitrogen and methane and at least one of:
• the device 600 comprises:
• a line 415 for injecting the evaporation gas at the inlet of the second exchange body is a line 415 for injecting the evaporation gas at the inlet of the second exchange body.
• the device 600 comprises, between an outlet 421 for the second compound of the cooling means 430 and the third exchange body 420, a circuit 440 for cooling the second compound by the heavy fraction of the first mixture inside the first exchange body.
• the first exchange body 1 and / or the second exchange body 120 is a wound heat exchanger.
• the means 430 for cooling the second compound is a heat exchanger between the second compound and water.
• FIG. 8 diagrammatically shows a particular embodiment of the method 700 that is the subject of the present invention.
• This method 700 for liquefying a natural gas comprising:
• a first heat exchange step 720 between the heavy fraction of the first mixture and the natural gas for cooling at least the natural gas
• a second heat exchange step 725 between the compressed light fraction of the first mixture and the natural gas cooled in the first exchange body to liquefy the natural gas
• a step 755 for transferring the second cooled compound to the third exchange step is a step 755 for transferring the second cooled compound to the third exchange step.
• This method 700 is realized, for example, by the implementation of the device 600 as described with reference to FIGS. 6 and 7. As can be understood, all the variants, all the examples and all the embodiments of the device 600 are also transposable as steps in the method 700.

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• 2016
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