Classifications

• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
  • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
  • F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
  • 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
• • 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
  • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
  • F25B40/00—Subcoolers, desuperheaters or superheaters
• • 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
  • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
  • F25B40/00—Subcoolers, desuperheaters or superheaters
  • F25B40/02—Subcoolers
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
  • F25J1/0002—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
  • F25J1/005—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 expansion of a gaseous 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
  • F25J1/003—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
  • F25J1/0057—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
  • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
  • F25J1/008—Hydrocarbons
  • F25J1/0087—Propane; Propylene
• • 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
  • F25J1/008—Hydrocarbons
  • F25J1/0092—Mixtures of hydrocarbons comprising possibly also minor amounts of 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
  • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
  • F25J1/0097—Others, e.g. F-, Cl-, HF-, HClF-, HCl-hydrocarbons etc. or mixtures thereof
• • 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
  • F25J1/0217—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
• • 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
  • F25J1/0279—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.
  • F25J1/0285—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings
  • F25J1/0288—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings using work extraction by mechanical coupling of compression and expansion of the refrigerant, so-called companders
• • 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
  • F25J2270/00—Refrigeration techniques used
  • F25J2270/14—External refrigeration with work-producing gas expansion loop
  • F25J2270/16—External refrigeration with work-producing gas expansion loop with mutliple gas expansion loops of the same refrigerant
• • 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
  • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
  • F25J2290/10—Mathematical formulae, modeling, plot or curves; Design methods

Definitions

• the present invention relates to a method of subcooling an LNG stream obtained by cooling by means of a first refrigeration cycle, the method being of the type comprising the following steps:
• An object of the invention is therefore to provide an autonomous method of sub-cooling a stream of LNG, which has an improved efficiency and which can easily be implemented in units of various structures.
• the subject of the invention is a subcooling process of the aforementioned type, characterized in that the refrigerant fluid is formed by a mixture of fluids comprising nitrogen.
• the method according to the invention can comprise one or more of the following characteristics, taken in isolation or in any technically possible combination:
• the refrigerant comprises nitrogen and at least one hydrocarbon
• the cooling fluid contains nitrogen and methane
• the cooling fluid coming from the compression apparatus is placed in heat exchange relation with a secondary refrigerant circulating in the second heat exchanger, the secondary refrigerant undergoing a third refrigeration cycle wherein it is compressed at the outlet of the second heat exchanger, cooled and condensed at least partially, and then expanded before vaporizing in the second heat exchanger;
• the secondary refrigerant fluid comprises propane
• the subcooling stream from the step is put into a heat exchange relationship with the coolant stream in a third heat exchanger; (iii ⁇ ) introducing the subcooling stream from the third heat exchanger into the cold turbine;
• the secondary turbine is coupled to a compressor of the compression apparatus: during step (iv), the cooling fluid is maintained substantially in gaseous form in the cold turbine;
• the refrigerant fluid is liquefied to more than 95% by mass in the cold turbine
• the subcooling current coming from the third heat exchanger is cooled before it passes through the cold turbine by heat exchange with the refrigerant circulating in the first heat exchanger at the outlet of the cold turbine;
• the cooling fluid contains a C 2 hydrocarbon
• the high pressure is greater than about 70 bars and the low pressure is less than about 30 bars.
• the subject of the invention is also a sub-cooling installation of a stream of LNG originating from a liquefaction unit comprising a first refrigeration cycle, the installation being of the type comprising: means for sub-cooling the stream LNG system comprising a first heat exchanger for putting the LNG stream in heat exchange relation with a refrigerant fluid; and
• a second closed refrigeration cycle independent of the first cycle and comprising: a second heat exchanger comprising means for circulating the refrigerant fluid issuing from the first heat exchanger;
• the installation according to the invention may comprise one or more of the following characteristics taken separately or in any technically possible combination:
• the refrigerant comprises nitrogen and at least one hydrocarbon;
• the cooling fluid contains nitrogen and methane;
• the second heat exchanger comprises means for circulating a secondary refrigerant fluid, the installation comprising a third refrigeration cycle successively comprising means for secondary compression of the secondary refrigerant fluid coming from the second heat exchanger, cooling means, and expansion of the secondary refrigerant fluid from the secondary compression means, and means for introducing the secondary refrigerant fluid from the expansion means (65) into the second heat exchanger;
• the secondary refrigerant fluid comprises propane; - the installation includes:
• a third heat exchanger for putting the subcooling stream from the separation means in heat exchange relation with the mixing stream
• the secondary turbine is coupled to a compressor of the compression apparatus;
• the plant comprises, upstream of the cold turbine, means for introducing the subcooling stream from the third heat exchanger into the first heat exchanger to put it in heat exchange relation with the refrigerant circulating in the heat exchanger; first heat exchanger at the outlet of the cold turbine; and
• the refrigerant fluid contains a C 2 hydrocarbon.
• FIG. 1 is a functional block diagram of a first installation according to the invention
• FIG. 2 is a graph showing the efficiency curves of the second refrigeration cycle of the installation of FIG. 1 and of a state-of-the-art installation, as a function of the pressure of the refrigerating fluid at the outlet compressor;
• Figure 3 is a diagram similar to that of Figure 1 of a first variant of the first installation according to the invention.
• FIG. 4 is a graph similar to that of Figure 2, for the installation of Figure 3;
• Figure 5 is a diagram similar to that of Figure 1 of a second variant of the first installation according to the invention.
• FIG. 6 is a diagram similar to that of Figure 1 of a second installation according to the invention
• - Figure 7 is a graph similar to that of Figure 2, for the second installation according to the invention
• FIG. 8 is a diagram similar to that of Figure 3 of a third installation according to the invention.
• FIG. 9 is a graph similar to that of Figure 2, for the third installation according to the invention.
• the sub-cooling plant 10 shown in FIG. 1, is intended for production, starting from a stream 11 of liquefied natural gas (LNG) starting at a temperature below -90 ° C. of a subcooled LNG stream 12, brought to a temperature below -140 ° C.
• LNG liquefied natural gas
• the starting LNG stream 11 is produced by a natural gas liquefaction unit 13 comprising a first refrigeration cycle 15.
• the first cycle 15 comprises, for example, a cycle comprising condensation and vaporization means. a mixture of hydrocarbons.
• the installation 10 comprises a first heat exchanger 19 and a second refrigeration cycle 21 closed, independent of the first cycle 15.
• the second refrigerant cycle 21 comprises a second heat exchanger 23, a stage compression apparatus comprising a plurality of compression stages 26, each stage 26 comprising a compressor 27 and a refrigerant 29.
• the second cycle 21 further comprises an expansion turbine 31 coupled to the compressor 27C of the last compression stage.
• the stage compressor 25 comprises three compressors 27.
• the first and second compressors 27A and 27B are driven by the same source 33 of external energy, whereas the third compressor 27C is driven by the expansion turbine 31.
• the source 33 is for example a gas turbine engine type.
• Refrigerants 29 are cooled by water and / or air.
• the starting LNG stream 11 from the liquefaction unit 13 is at a temperature below -90 ° C., for example at -110 ° C.
• This stream comprises, for example, substantially 5% of nitrogen, 90% of methane and 5% ethane, and its flow rate is 50,000 kmol / h.
• the LNG stream 11 at -1100 ° C. is introduced into the first heat exchanger 19, where it is subcooled to a temperature below -150 ° C. by heat exchange with a starting refrigerant flow.
• the stream 41 of the refrigerant starting fluid comprises a mixture of nitrogen and methane.
• the molar content of methane in the coolant 41 is between 5 and 15%.
• the coolant 41 may be derived from a mixture of nitrogen and methane from the denitrogenation of the LNG stream 12, implemented downstream of the installation 11.
• the current flow 41 is for example 73 336 kmol / h and its temperature is - 152 ° C at the inlet of the exchanger 19.
• the stream 42 of refrigerant from the heat exchanger 19 undergoes a second closed refrigeration cycle 21, independent of the first cycle 15.
• the stream 42 which has a low pressure substantially between 10 and 30 bars, is introduced into the second heat exchanger 23 and heated in this exchanger 23 to form a stream 43 of heated refrigerant.
• the stream 43 is then compressed successively in the three compression stages 26 to form a stream of compressed refrigerant 45.
• the stream 43 is compressed in the compressor 27, and then cooled to a temperature of 35.degree. refrigerant 29.
• the compressed refrigerant fluid stream 45 has a high pressure greater than its critical pressure, or cricondenbar pressure. It is at a temperature substantially equal to 35 ° C.
• the high pressure is preferably greater than 70 bar and between 70 bar and 100 bar. This pressure is preferably as high as possible given the mechanical strength limits of the circuit.
• the compressed refrigerant fluid stream 45 is then introduced into the second heat exchanger 23, where it cools by heat exchange with the stream 42 from the first exchanger 19 and circulating in counter-current.
• a stream 47 of cooled compressed cooling fluid is thus formed.
• the stream 47 is expanded to the low pressure in the turbine 31 to form the flow 41 of refrigerant starting fluid.
• the stream 41 is substantially in gaseous form, that is to say it contains less than 10% by weight (or 1% by volume) of liquid.
• the current 41 is then introduced into the first heat exchanger 19 where it is heated by heat exchange with the flow of LNG 11 circulating against the current.
• the cooling fluid is kept in gaseous or supercritical form throughout the cycle 21.
• the exchanger 19 is in fact devoid of liquid dispensing device and steam.
• the refrigeration condensation of the stream 47 at the outlet of the second heat exchanger 23 is limited to less than 10% by weight, so that a simple expansion turbine 31 is used to relax the compressed refrigerant stream 47.
• the respective curves 50 and 51 of the respective efficiencies of the cycle 21 in the process according to the invention and in a method of the state of the art are represented as a function of the value of the high pressure.
• the refrigerant fluid consists solely of nitrogen.
• the addition of a quantity of methane of between 5 and 15 mol% in the coolant significantly increases the efficiency of the cycle 21 to sub-cool the LNG from -110 0 C to -15O 0 C.
• the efficiencies represented in FIG. 2 were calculated by considering the polytropic efficiency of the compressors 27A, 27B equal to 83%, the polytropic efficiency of the compressor 27C equal to 80%, and the adiabatic efficiency of the turbine 31 equal to 85%. Furthermore, the average temperature difference between the currents flowing in the first heat exchanger 19 is maintained at approximately 40 ° C. The average temperature difference between the currents flowing in the second heat exchanger 23 is also maintained at approximately 4 ° C. This result is obtained, surprisingly, without modification of the installation 10, and provides gains of about 1000 kW for high pressures between 70 and 85 bar.
• the installation 10 further comprises a third refrigeration cycle 59 closed, independent of the cycles 15 and 21.
• the third cycle 59 comprises a secondary compressor 61 driven by the external energy source 33, first and second secondary refrigerants 63A and 63B, and an expansion valve 65.
• This cycle is implemented using a stream 67 of secondary refrigerant fluid formed of liquid propane.
• the current 67 is introduced into the second heat exchanger 23 parallel to the stream 42 of refrigerant from the heat exchanger 19, and countercurrent of the compressed refrigerant fluid stream 45.
• the vaporization of the propane stream 67 in the second heat exchanger 23 cools the stream 45 by heat exchange and produces a stream of heated propane 69.
• This stream 69 is then compressed in the compressor 61, then cooled and condensed in the refrigerants 63A and 63B to form a stream 71 of liquid compressed propane.
• This stream 71 is expanded in the valve 65 to form the stream 67 of refrigerant propane.
• the power consumed by the compressor 61 represents approximately 5% of the total power supplied by the energy source 33.
• the curve 73 of the efficiency as a function of the high pressure for this first variant method shows that the efficiency of the ring 21 in the second process is increased by about 5% compared to the first method according to the invention in the high pressure range considered.
• the total power reduction consumed for a high pressure of 80 bar is greater than 12%, compared to a method of the state of the art.
• the second variant of the first installation illustrated in FIG. 5 differs from the first variant in the following features.
• the coolant used in the third cycle 59 comprises at least 30 mol% of ethane. In the illustrated example, this cycle comprises about 50 mol% of ethane and 50 mol% of propane.
• the secondary coolant stream 71 obtained at the outlet of the second secondary refrigerant 63B is introduced into the second heat exchanger 23 where it is subcooled, before being expanded in the valve 65, countercurrent to the expanded stream 67.
• the average efficiency of the cycle 21 increases by about 0.7% compared with the second variant shown in FIG. 3.
• the second installation 79 according to the invention shown in FIG. 6 differs from the first installation 10 in that it further comprises a third heat exchanger 81 interposed between the first heat exchanger 19 and the second heat exchanger 23.
• the compression apparatus 25 further comprises a fourth compression stage 26D interposed between the second compression stage 26B and the third compression stage 26C.
• the compressor 27D of the fourth stage 26D is coupled to a secondary turbine 83 of expansion.
• the second method according to the invention differs from the first method in that the current 84 from second refrigerant 29B is introduced into the fourth compressor 27D and then cooled in the fourth refrigerant 29D before being introduced into the third compressor 27C.
• the stream 47 of compressed cooled refrigerant obtained at the outlet of the second heat exchanger 23 is separated into a subcooling stream 85 and a secondary cooling stream 87.
• the ratio of the flow rate of the subcooling stream 85 to the secondary cooling stream 87 is greater than 1.
• the subcooling stream 85 is introduced into the third heat exchanger 81, where it is cooled to form a cooled subcooling stream 89.
• This stream 89 is then introduced into the turbine 31, where it is expanded.
• the expanded subcooling stream 90 at the outlet of the turbine 31 is in gaseous form.
• the stream 90 is introduced into the first heat exchanger 19 where it subcooled the LNG stream 11 by heat exchange and formed a heated subcooling stream 93.
• the secondary cooling stream 87 is supplied to the secondary turbine 83, where it is expanded to form a expanded secondary cooling stream 91 in gaseous form.
• the stream 91 is mixed with the heated subcooling stream 93 from the first heat exchanger 19, at a point upstream of the third heat exchanger 81.
• the mixture thus obtained is introduced into the third heat exchanger 81 where it cools the current subcooling device 85 to form the stream 42.
• the second installation 79 has a third refrigeration cycle 59 with propane or with a mixture of ethane-propane that cools the second heat exchanger 23.
• the third cycle 59 is structurally identical to the third cycles 59 shown respectively in Figures 3 and 5.
• FIG. 7 illustrates the curve 95 of the efficiency of the cycle 21 as a function of the high pressure when the installation shown in FIG. 6 is devoid of a refrigerant cycle, while the curves 97 and 99 represent the efficiency of the cycle 21 in depending on the pressure when third refrigeration cycles respectively with propane or propane and ethane mixture are used. As illustrated in Figure 7, the efficiency of cycle 21 is increased with respect to a cycle comprising only nitrogen as a coolant (curve 51).
• the third installation 100 according to the invention, shown in FIG. 8, differs from the second installation 79 by the following characteristics.
• the compression apparatus 25 does not comprise a third stage
• the installation comprises a dynamic expansion turbine 99 which allows liquefaction of the expanded fluid.
• This turbine 99 is coupled to a current generator 99A.
• the third method according to the invention differs from the second method in the ratio of the flow rate of the subcooling current 85 to the flow rate of the secondary cooling stream 87, which ratio is less than 1.
• the cooled subcooling stream 89 is introduced into the first heat exchanger 19, where it is cooled again before it is introduced into the turbine 99.
• the expanded subcooling stream 101 from the turbine 99 is completely liquid.
• the liquid stream 101 is vaporized in the first heat exchanger 19, countercurrently, on the one hand, the LNG stream 11 to be sub-cooled and, on the other hand, the cooled subcooling stream 89 circulating in the first exchanger 19.
• the secondary cooling stream 91 is in gaseous form at the outlet of the secondary turbine 83.
• the refrigerant circulating in the first cycle 21 preferably comprises a mixture of nitrogen and methane, the molar percentage of nitrogen in this mixture being less than 50%.
• the refrigerant also comprises a C 2 hydrocarbon, for example ethylene, at a content of less than 10%.
• the efficiency of the process is further improved, as illustrated by the efficiency curve 103 of the cycle 21 as a function of the pressure in FIG. 9.
• a third cycle 59 of propane refrigeration, or based on a mixture ethane-propane, of the type described in FIGS. 3 and 5, is used for cooling the second heat exchanger 23.
• the curves 105 and 107 of efficiency of the cycle 21 as a function of the pressure for these two variants are shown in Figure 9, and also show an increase in cycle efficiency 21 over the considered high pressure range.
• the process according to the invention makes it possible to have a sub-cooling process that is flexible and easy to implement in an installation that produces LNG either as a main product, for example in an LNG production unit, or as secondary product, for example in a natural gas liquids extraction unit (NGL).
• LNG natural gas liquids extraction unit
• the use of a secondary cooling cycle to cool the coolant prior to its adiabatic compression significantly improves the efficiency of the installation.
• the efficiency values obtained were calculated with an average temperature difference in the first heat exchanger 19 greater than or equal to 4 ° C.
• the yield of the inverted Brayton cycle may exceed 50 ° C. %, which is comparable to the efficiency of a condensation and vaporization cycle using a hydrocarbon mixture conventionally used for the liquefaction and subcooling of LNG.

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