US3818714A - Process for the liquefaction and subcooling of natural gas - Google Patents

Process for the liquefaction and subcooling of natural gas Download PDF

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Publication number
US3818714A
US3818714A US00231984A US23198472A US3818714A US 3818714 A US3818714 A US 3818714A US 00231984 A US00231984 A US 00231984A US 23198472 A US23198472 A US 23198472A US 3818714 A US3818714 A US 3818714A
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cycle
gas
liquid
nitrogen
precooling
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US00231984A
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V Etzbach
W Forg
P Grimm
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Linde GmbH
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Linde GmbH
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    • 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0257—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation 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
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0035—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work
    • F25J1/0037—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work of a return stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0045—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by vaporising a liquid return stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—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
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    • 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
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
    • F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
    • F25J1/0055—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream originating from an incorporated cascade
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
    • F25J1/0214—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a dual level refrigeration cascade with at least one MCR cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
    • F25J1/0219—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle in combination with an internal quasi-closed refrigeration loop, e.g. using a deep flash recycle loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0244—Operation; Control and regulation; Instrumentation
    • F25J1/0245—Different modes, i.e. 'runs', of operation; Process control
    • F25J1/0249—Controlling refrigerant inventory, i.e. composition or quantity
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0244—Operation; Control and regulation; Instrumentation
    • F25J1/0245—Different modes, i.e. 'runs', of operation; Process control
    • F25J1/0249—Controlling refrigerant inventory, i.e. composition or quantity
    • F25J1/025—Details related to the refrigerant production or treatment, e.g. make-up supply from feed gas itself
    • 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.
    • F25J1/0285—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
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    • 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0209—Natural gas or substitute natural gas
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
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    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
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    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
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    • 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
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    • 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
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/10—Mathematical formulae, modeling, plot or curves; Design methods

Definitions

  • ABSTRACT A process for the liquefaction and subcooling of natural gas with a Claude closed refrigerating cycle comprising compressing gaseous cycle medium; cooling resultant compressed-gaseous cycle medium; dividing cooled compressed gas into two streams; engineexpanding one stream; and cooling the other stream with the engine-expanded stream to such an extent that said other stream becomes partially liquefied after a subsequent throttle expansion thereof; the improvement comprising employing as the cycle medium, a
  • This invention relates to a process for liquefaction and subcooling of natural gas by a Claude cycle.
  • This cycle comprises compressing cycle gas; cooling same; dividing cooled compressed gas into two streams; engine-expanding one stream; and cooling the other stream with the engine-expanded stream to such an extent that said other stream becomes partially liquefied after a subsequent throttle expansion thereof.
  • peak cold is made available, namely that amount of refrigeration required for subcooling the natural gas.
  • the natural gas Before subcooling, the natural gas has already been liquefied under a higher pressure by heat exchange with the cycle gas, but the subcooling ensures that the natural gas remains practically entirely in the liquid phase even after expansion to the pressure of the storage tank. If it is desired to avoid operation of the Claude cycle under a negative pressure, it is essential to employ as the cycle medium a gas having a lower boiling point than methane, nitrogen being conventionally employed.
  • FIG. 1 is a boiling point-composition diagram for N -CH at various pressures.
  • FIGS. 2 and 3 are schematic views of preferred embodiments of the process.
  • the methane in mixture with the nitrogen, is vaporized at its partial pressure, i.e., a pressure lower than the ambient evaporation pressure, it is possible to obtain, with methane, a specific low temperature at a relatively high pressure level.
  • the refrigerating capacity of the Claude cycle is likewise improved by the addition of methane to the nitrogen.
  • methane as a less than ideal gas, increases the Joule-Thomson effect in the peak cooler, so that the amount of cycle gas to be fed to the J-T valve can be smaller, and a larger proportion of the cycle gas can be fed to the engine expansion.
  • the enthalpy gradient in the turbine and thus the specific refrigerating capacity of the cycle, based on the unit quantity of circulated gas is larger in the case of methane than in the case of nitrogen. The same holds true for the isothermal Joule-Thomson effect at the warm end. Therefore, in total, the amount of cycle gas required to produce a specific amount of cold is reduced.
  • the use of a methane-nitrogen mixture as the cycle gas affords the further advantage that the leakage losses of the cycle medium can be compensated for at less cost by utilizing natural gas therefor. This is so because the separation of a gas rich in nitrogen prior to the liquefaction is in most cases absolutely necessary, even in case of gases of low nitrogen content, since too great a drop in the liquefaction temperature of the natural gas must be avoided.
  • the above-described advantage is especially noticeable in the processing of natural gases having a low nitrogen content, for otherwise rectification devices would have to be provided in this pro cedure wherein the nitrogen is separated from the natural gas not only in a high purity, but also in good yields.
  • the process according to the present invention offers advantages even if the natural gas contains no nitrogen at all, since only that proportion of the leakage losses associated with the nitrogen need be made up from a source externally of the plant, whereas the lost methane can readily be taken from the natural gas.
  • the nitrogen concentration of the cycle gas is, on a molar basis, at least 20 percent, preferably at least 40 percent, conversely, the maximum preferred nitrogen concentration is 80 percent, particularly 60 percent.
  • a nitrogen separation unit is incorporated in the natural gas liquefaction process. From the head of this unit there is withdrawn a fraction having a nitrogen concentration of at least the same level as that of the cycle gas, and this fraction is then fed into the cycle as makeup gas. If this fraction contains more nitrogen than the cycle gas, then supplemental methane from the purified natural gas (freed of CO H 0, and heavy hydrocarbons) can be added thereto.
  • One negative feature of the cycle of this invention is that the cycle gas must be precooled to a very low temperature prior to entering the expansion engine so that it can be cooled to a sufficiently low temperature during the expansion.
  • This precooling can be conducted conventionally with a multistage refrigerating machine operating with freon, ammonia, or propane, also including, in many cases, an essential third stage of vacuum.
  • These refrigerating machines exhibit the same disadvantage described above in connection with the Claude cycle, namely that the refrigeration is transferred at a constant temperature, to a stream having a sliding temperature.
  • there is employed a mixture of methane, propane, and optionally ethane as the cycle medium for the precooling cycle is employed.
  • a main advantage of this latter feature is that the refrigeration liberated during the evaporation is transferred at a decreasing temperature so that small temperature differences (ATs) can be employed in the heat exchangers, resalting in a thermodynamically more efficient process. Since the propane and any ethane present evaporate under a partial pressure lower than the total pressure ambient during the evaporation, the desired low temperature is obtained at a higher total pressure than would be the case when evaporating pure ethane or propane. In other words, because the transfer of peak cold involves a smaller pressure drop, the number of compressor stages and thus the number of evaporators is decreased, and the cost of control elements is also reduced.
  • leakage losses amounting to about 1 5 parts per thousand of the quantity of cycle medium can frequently be covered, in the case of methane and ethane, merely by simple separation from the natural gas proper, i.e., they need not be stored in additional tanks. Propane is always available in any case so that the BTU value of the gas can be adjusted or desired.
  • the proportion of each of methane, propane and optionally ethane in the total of the cycle gas is about 20-50 molar percent, respectively.
  • a cycle gas having a composition, of in moles percent 40 and 60 methane; 25 and 60 percent propane; and 0 and 15 ethane.
  • the precooling temperature attainable in this manner is generally sufficient, even in case of low natural gas pressures, to result in the condensation of the heavy hydrocarbons which, otherwise, could lead to obstructions in the low-temperature sections.
  • the plant can be rapidly brought to the required cold operating condition.
  • an even lower precooling temperature e.g. to 200 K
  • a fraction of the cycle medium remains in the gaseous phase downstream of the final cooler of the compressor, and the fraction containing lower boiling components is separated from the liquid fraction containing predominantly the higher-boiling hydrocarbons.
  • Both separated gas and liquid are then cooled by heat exchange with the liquid evaporating at the suction pressure of the compressor.
  • the gas rich in lower-boiling components is thus totally condensed, and is then in the liquid phase expanded (pressurereduced) to the suction pressure of the compressor.
  • the resultant liquid is then evaporated to effect said total condensation.
  • the natural gas to be processed (0.6,780 Nm /hr.), after having been freed of water, carbon dioxide, and hydrogen sulfide, and having approximately the following composition: 2 percent nitrogen, 94 percent methane, 3 percent ethane, l percent propane and higher hydrocarbons, is fed to the plant, via conduit 1, at 298 K and under 39 ata. and is then cooled in the heat exchanger 2 to 216 K. During this step, the C and higher hydrocarbons are substantially condensed, which would otherwise cause clogging in subsequent sections of the plant.
  • phase separator 3 evaporated and warmed in heat exchanger 2
  • discharged from the plant via conduit 4 The portion remaining in the gaseous phase is further cooled in heat exchanger 5 to about 190 K; during this step, a liquid is obtained consisting of about 85 percent methane, percent ethane, and 5 percent propane.
  • This liquid after being passed in separator-collector 6, is branched into two streams, and the amount necessary to make up for leakage losses of the precooling cycle is introduced into the latter via conduit 7.
  • the remainder is evaporated and warmed in heat exchangers 5 and 2, and then discharged from the plant via conduit 4.
  • a portion of the gas withdrawn from the separator 6 overhead is now further cooled in the heat exchanger 8 to 163 K and expanded into the nitrogen separation column 9 operating at 22 ata.
  • the remaining gas is conducted through a heating coil located in the sump of the column 9 and is then expanded into the midsection of column 9.
  • a temperature of about 150 K is maintained; the gaseous head product consists of 50 percent of a methane and 50% of nitrogen.
  • This head product is discharged from the plant via conduit 4, except for that amount of gas required for providing makeup due to the leakage losses of the Claude refrigerating cycle and which is fed into said cycle via conduit 10. From the sump of the column 9, 5,820 Nm /h.
  • liquid natural gas is withdrawn having a temperature of 167 K and approximately the following composition: 97 percent methane, 1 percent nitrogen, and 2 percent ethane.
  • This liquid is passed to the heat exchangers l1 and 12 and cooled therein to l 1 1 K so that, during the subsequent expansion in the valve 13 to the pressure of the storage tank (slightly above 1 ata.), only a minimum amount of liquid is evaporated (about 40 Nm lh).
  • the refrigeration required for the liquefaction is provided by a Claude cycle with precooling by a one-stage cycle based on a mixture of gases.
  • This mixture comprises 50 percent methane and 50 percent nitrogen and is employed as the cycle medium.
  • This gas (37,900 Nm lhr) is compressed, in compressor 14, to 25.5 ata., and after being cooled, is further compressed to 35.5 ata. in compressor 15.
  • the gas enters the heat exchanger 2 at a temperature of 298 K and is precoolcd therein and also in the heat exchanger 5 to 197 K.
  • cycle gas 35,600 Nm /h. of cycle gas is then expanded in the expansion turbine 16 to 8 ata. and, during this step, is cooled to 138 K.
  • a portion of this gas is branched off via conduit 17 and serves for cooling the head of column 9; the main quantity is fed, via conduit 18, to the cold end of the heat exchanger 11, heated therein and in heat exchangers 8, 5, and 2, to ambient temperature and thereafter recompressed in the compressor 14.
  • the proportion of the cycle medium not subjected to engine expansion i.e., 2,300 Nm /h., is cooled in conduit 19 under its pressure of 35.5 ata. in heat exchangers 8, l1, and 12, to 111 K.
  • the temperature drops to 109 K, so that the liquid natural gas can be subcooled to l 1 1 K by heat exchange with the boiling cycle liquid, before it is expanded in valve 13.
  • the throttle-expanded cycle medium is combined with the engine-expanded cycle medium, and is warmed and recompressed together therewith.
  • the cycle medium of the precooling cycle consists of 45 percent methane, 5 percent ethane, and 50 percent propane. 4,200 Nm lh. of this gas is compressed in compressor 22 from 10 ata. to 50 ata., cooled and simultaneously liquefied in heat exchanger 2, and then expanded to 10 ata. in valve 23.
  • the precooling temperature attainable in this manner i.e., the temperature at which the gaseous streams to be cooled leave the cold end of the heat exchanger 2, is 216 K.
  • the evaporated and warmed cycle medium is then recompressed in the compressor 22.
  • the leakage losses of the cycle as mentioned above, are, in part, compensated for by the liquid withdrawn from separator 6 via conduit 7.
  • this liquid contains less propane than the cycle medium, pure propane or a gas more enriched therewith must be added. This can be done by conducting the gaseous stream returning to the compressor 22 via conduit 30 through the tank 28 filled with liquid propane, rather than via conduit 29.
  • the dome 31 serves as an entrainment separator for the separation of droplets of liquid propane.
  • the cycle medium consists of about percent methane, 5 percent ethane, and 25 propane.
  • the liquid formed in the secondary cooler of the compressor denoted by 24 is separated from the gaseous phase in the separator 25, cooled in heat exchanger 2, expanded in valve 23' from 35 to 8 ata., and reevaporated and warmed in heat exchanger 2.
  • the gaseous phase enriched in the lower-boiling components of the cycle medium is withdrawn from separator 25, conducted, via conduit 26, through the heat exchangers 2 and 5, being cooled and liquefied during this step, and then expanded in valve 27 from 35 to 8 ata.
  • a precooling temperature of about K is attacined at the cold end of the heat exchanger 5.
  • the cycle medium evaporated and warmed in heat exchanger 5 is recombined with the cycle medium expanded in valve 23', and the combined stream is then recycled to the suction side of compressor 22.
  • B in FIG. 3 denotes the sum total of the remaining gaseous streams to be cooled, i.e., the natural gas to be liquefied and the compressed cycle medium of the Claude cycle; and C denotes the sum total of the other gaseous streams to be warmed, i.e., the fractions obtained during the natural gas liquefaction and to be discharged from the plant in the gaseous phase, and the expanded cycle medium of the Claude cycle.
  • the improvement comprising employing as the cycle medium, a mixture of nitrogen and methane.
  • a process according to claim 1, wherein the nitrogen molar concentration in the cycle medium is at least 40 percent.
  • a process according to claim 1 further comprising separating the natural gas from CO H and heavy hydrocarbons; separating a nitrogen enriched stream from resultant purified natural gas, the nitrogen content of said enriched stream being at least as large as that of said cycle medium and feeding said nitrogen enriched stream into the Claude cycle in sufficient amounts to provide makeup cycle medium.
  • a process according to claim 1 further comprising precooling said one stream prior to engine expanding thereof with a refrigeration precooling cycle based on a cycle medium comprising a mixture of methane and propane ethane.
  • said precooling refrigeration cycle comprising a precooling compressor and a cooler downstream of the precooling compressor, and further comprising with drawing a mixture of gas and liquid from said cooler, said liquid containing predominantly higher-boiling hydrocarbons and said gas being rich in lower-boiling components; separating the gas and the liquid; said separated gas and liquid streams in heat exchange with liquid evaporating at the suction pressure of the compressor, totally condensing said gas rich in lower-boiling components, the resultant liquid being expanded to the suction pressure of the compressor, whereby the total condensation is effected by the evaporation of the thus-formed, expanded liquid.
  • said precooling refrigeration cycle comprising a precooling compressor and a cooler downstream of the precooling compressor, and further comprising with drawing a mixture of gas and liquid from said cooler, said liquid containing predominantly higher-boiling hydrocarbons and said gas being rich in lower-boiling components; separating the gas and the liquid; said separated gas and liquid streams in heat exchange with liquid evaporating at the suction pressure of the compressor, totally condensing said gas rich in lower-boiling components, the resultant liquid being expanded to the suctionpressure of the compressor, whereby the total condensation is effected by the evaporation of the thus-formed, expanded liquid.
  • precooling cycle medium further comprises ethane.
  • a process as defined by claim 2 wherein the maximum molar concentration in the medium is 60 percent nitrogen.

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Cited By (35)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3970441A (en) * 1973-07-17 1976-07-20 Linde Aktiengesellschaft Cascaded refrigeration cycles for liquefying low-boiling gaseous mixtures
US4017283A (en) * 1971-11-17 1977-04-12 Sulzer Brothers Limited Method and plant for making up nitrogen vaporization losses in nitrogen-containing liquified natural gas carrying tankers
US4072485A (en) * 1976-01-30 1978-02-07 Compagnie Francaise D'etudes Et De Construction - Technip Method of and arrangement for processing through low temperature heat exchanges and in particular for treating natural gases and cracked gases
US4461634A (en) * 1980-10-16 1984-07-24 Petrocarbon Developments Limited Separation of gas mixtures by partial condensation
US4501600A (en) * 1983-07-15 1985-02-26 Union Carbide Corporation Process to separate nitrogen from natural gas
US4592767A (en) * 1985-05-29 1986-06-03 Union Carbide Corporation Process for separating methane and nitrogen
US4617037A (en) * 1984-11-02 1986-10-14 Nippon Sanso Kabushiki Kaisha Nitrogen production method
US5755114A (en) * 1997-01-06 1998-05-26 Abb Randall Corporation Use of a turboexpander cycle in liquefied natural gas process
US5768912A (en) * 1994-04-05 1998-06-23 Dubar; Christopher Alfred Liquefaction process
US6016665A (en) * 1997-06-20 2000-01-25 Exxon Production Research Company Cascade refrigeration process for liquefaction of natural gas
US6070429A (en) * 1999-03-30 2000-06-06 Phillips Petroleum Company Nitrogen rejection system for liquified natural gas
US6085547A (en) * 1998-09-18 2000-07-11 Johnston; Richard P. Simple method and apparatus for the partial conversion of natural gas to liquid natural gas
US6085545A (en) * 1998-09-18 2000-07-11 Johnston; Richard P. Liquid natural gas system with an integrated engine, compressor and expander assembly
US6085546A (en) * 1998-09-18 2000-07-11 Johnston; Richard P. Method and apparatus for the partial conversion of natural gas to liquid natural gas
US6269656B1 (en) 1998-09-18 2001-08-07 Richard P. Johnston Method and apparatus for producing liquified natural gas
WO2003019095A1 (en) * 2001-08-21 2003-03-06 Gasconsult Limited Method for liquefying methane-rich gas
US20040231359A1 (en) * 2003-05-22 2004-11-25 Brostow Adam Adrian Nitrogen rejection from condensed natural gas
US20050056051A1 (en) * 2003-09-17 2005-03-17 Roberts Mark Julian Hybrid gas liquefaction cycle with multiple expanders
US20060090508A1 (en) * 2004-10-28 2006-05-04 Howard Henry E Natural gas liquefaction system
WO2006094676A1 (de) * 2005-03-04 2006-09-14 Linde Aktiengesellschaft Helium-gewinnung bei lng-anlagen
US20060225461A1 (en) * 2005-04-11 2006-10-12 Henri Paradowski Process for sub-cooling an LNG stream obtained by cooling by means of a first refrigeration cycle, and associated installation
US20080184711A1 (en) * 2007-02-01 2008-08-07 Diehl Bgt Defence Gmbh & Co. Kg Method for Cooling a Detector
US20090084132A1 (en) * 2007-09-28 2009-04-02 Ramona Manuela Dragomir Method for producing liquefied natural gas
US20090113928A1 (en) * 2007-11-05 2009-05-07 David Vandor Method and System for the Small-scale Production of Liquified Natural Gas (LNG) from Low-pressure Gas
WO2009063092A2 (en) * 2007-11-16 2009-05-22 Shell Internationale Research Maatschappij B.V. Method and apparatus for liquefying a hydrocarbon stream and floating vessel or offshore platform comprising the same
US20090217701A1 (en) * 2005-08-09 2009-09-03 Moses Minta Natural Gas Liquefaction Process for Ling
FR2936864A1 (fr) * 2008-10-07 2010-04-09 Technip France Procede de production de courants d'azote liquide et gazeux, d'un courant gazeux riche en helium et d'un courant d'hydrocarbures deazote et installation associee.
US20100107684A1 (en) * 2007-05-03 2010-05-06 Moses Minta Natural Gas Liquefaction Process
WO2010055153A2 (en) * 2008-11-17 2010-05-20 Shell Internationale Research Maatschappij B.V. Method and apparatus for liquefying a hydrocarbon stream and floating vessel or offshore platform comprising the same
WO2010128467A2 (en) * 2009-05-08 2010-11-11 Corac Group Plc Production and distribution of natural gas
US20100293967A1 (en) * 2007-12-07 2010-11-25 Dresser-Rand Company Compressor system and method for gas liquefaction system
US20120227418A1 (en) * 2011-03-08 2012-09-13 Linde Aktiengesellschaft Cooling unit
WO2010109228A3 (en) * 2009-03-25 2013-04-04 Costain Oil, Gas & Process Limited Process and apparatus for separation of hydrocarbons and nitrogen
US20170356687A1 (en) * 2015-01-09 2017-12-14 Mitsubishi Heavy Industries, Ltd. Gas liquefaction apparatus and gas liquefaction method
US11549746B2 (en) 2018-03-27 2023-01-10 Taiyo Nippon Sanso Corporation Natural gas liquefaction device and natural gas liquefaction method

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2471567B1 (fr) * 1979-12-12 1986-11-28 Technip Cie Procede et systeme de refrigeration d'un fluide a refroidir a basse temperature
FR2681859B1 (fr) * 1991-09-30 1994-02-11 Technip Cie Fse Etudes Const Procede de liquefaction de gaz naturel.
DE4440407C1 (de) * 1994-11-11 1996-04-04 Linde Ag Verfahren zum Gewinnen einer Ethan-reichen Fraktion zum Wiederauffüllen eines Ethan-enthaltenden Kältekreislaufs eines Verfahrens zum Verflüssigen einer kohlenwasserstoffreichen Fraktion

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2823523A (en) * 1956-03-26 1958-02-18 Inst Gas Technology Separation of nitrogen from methane
CA635337A (en) * 1962-01-23 L. Van Kleef Alfred Natural gas liquefaction
US3180709A (en) * 1961-06-29 1965-04-27 Union Carbide Corp Process for liquefaction of lowboiling gases
US3274787A (en) * 1961-06-01 1966-09-27 Air Liquide Method for cooling a gaseous mixture to a low temperature
US3342037A (en) * 1964-04-10 1967-09-19 Lummus Co Liquefaction of natural gas by cascade refrigeration and multiple expansion
US3596472A (en) * 1967-12-20 1971-08-03 Messer Griesheim Gmbh Process for liquefying natural gas containing nitrogen
US3616652A (en) * 1966-09-27 1971-11-02 Conch Int Methane Ltd Process and apparatus for liquefying natural gas containing nitrogen by using cooled expanded and flashed gas therefrom as a coolant therefor
US3677019A (en) * 1969-08-01 1972-07-18 Union Carbide Corp Gas liquefaction process and apparatus

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA635337A (en) * 1962-01-23 L. Van Kleef Alfred Natural gas liquefaction
US2823523A (en) * 1956-03-26 1958-02-18 Inst Gas Technology Separation of nitrogen from methane
US3274787A (en) * 1961-06-01 1966-09-27 Air Liquide Method for cooling a gaseous mixture to a low temperature
US3180709A (en) * 1961-06-29 1965-04-27 Union Carbide Corp Process for liquefaction of lowboiling gases
US3342037A (en) * 1964-04-10 1967-09-19 Lummus Co Liquefaction of natural gas by cascade refrigeration and multiple expansion
US3616652A (en) * 1966-09-27 1971-11-02 Conch Int Methane Ltd Process and apparatus for liquefying natural gas containing nitrogen by using cooled expanded and flashed gas therefrom as a coolant therefor
US3596472A (en) * 1967-12-20 1971-08-03 Messer Griesheim Gmbh Process for liquefying natural gas containing nitrogen
US3677019A (en) * 1969-08-01 1972-07-18 Union Carbide Corp Gas liquefaction process and apparatus

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
Kleemenko, One Flow Cascade Cycle, Progress in Refrigeration Science and Technology, Vol. 1 (1960). *

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* Cited by examiner, † Cited by third party
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US4017283A (en) * 1971-11-17 1977-04-12 Sulzer Brothers Limited Method and plant for making up nitrogen vaporization losses in nitrogen-containing liquified natural gas carrying tankers
US3970441A (en) * 1973-07-17 1976-07-20 Linde Aktiengesellschaft Cascaded refrigeration cycles for liquefying low-boiling gaseous mixtures
US4072485A (en) * 1976-01-30 1978-02-07 Compagnie Francaise D'etudes Et De Construction - Technip Method of and arrangement for processing through low temperature heat exchanges and in particular for treating natural gases and cracked gases
US4461634A (en) * 1980-10-16 1984-07-24 Petrocarbon Developments Limited Separation of gas mixtures by partial condensation
US4501600A (en) * 1983-07-15 1985-02-26 Union Carbide Corporation Process to separate nitrogen from natural gas
US4617037A (en) * 1984-11-02 1986-10-14 Nippon Sanso Kabushiki Kaisha Nitrogen production method
US4592767A (en) * 1985-05-29 1986-06-03 Union Carbide Corporation Process for separating methane and nitrogen
US5768912A (en) * 1994-04-05 1998-06-23 Dubar; Christopher Alfred Liquefaction process
US5755114A (en) * 1997-01-06 1998-05-26 Abb Randall Corporation Use of a turboexpander cycle in liquefied natural gas process
US6016665A (en) * 1997-06-20 2000-01-25 Exxon Production Research Company Cascade refrigeration process for liquefaction of natural gas
US6085547A (en) * 1998-09-18 2000-07-11 Johnston; Richard P. Simple method and apparatus for the partial conversion of natural gas to liquid natural gas
US6085545A (en) * 1998-09-18 2000-07-11 Johnston; Richard P. Liquid natural gas system with an integrated engine, compressor and expander assembly
US6085546A (en) * 1998-09-18 2000-07-11 Johnston; Richard P. Method and apparatus for the partial conversion of natural gas to liquid natural gas
US6269656B1 (en) 1998-09-18 2001-08-07 Richard P. Johnston Method and apparatus for producing liquified natural gas
US6070429A (en) * 1999-03-30 2000-06-06 Phillips Petroleum Company Nitrogen rejection system for liquified natural gas
US20040255616A1 (en) * 2001-08-21 2004-12-23 Maunder Anthony D. Method for liquefying methane-rich gas
GB2393504B (en) * 2001-08-21 2005-05-18 Gasconsult Ltd Method for liquefying methane-rich gas
WO2003019095A1 (en) * 2001-08-21 2003-03-06 Gasconsult Limited Method for liquefying methane-rich gas
US7234321B2 (en) * 2001-08-21 2007-06-26 Gasconsult Limited Method for liquefying methane-rich gas
GB2393504A (en) * 2001-08-21 2004-03-31 Gasconsult Ltd Method for liquefying methane-rich gas
US6978638B2 (en) 2003-05-22 2005-12-27 Air Products And Chemicals, Inc. Nitrogen rejection from condensed natural gas
US20040231359A1 (en) * 2003-05-22 2004-11-25 Brostow Adam Adrian Nitrogen rejection from condensed natural gas
US7127914B2 (en) 2003-09-17 2006-10-31 Air Products And Chemicals, Inc. Hybrid gas liquefaction cycle with multiple expanders
US20050056051A1 (en) * 2003-09-17 2005-03-17 Roberts Mark Julian Hybrid gas liquefaction cycle with multiple expanders
WO2006049885A3 (en) * 2004-10-28 2006-12-14 Praxair Technology Inc Natural gas liquefaction system
US7228714B2 (en) * 2004-10-28 2007-06-12 Praxair Technology, Inc. Natural gas liquefaction system
US7469556B2 (en) * 2004-10-28 2008-12-30 Praxair Technology, Inc. Natural gas liquefaction system
US20060090508A1 (en) * 2004-10-28 2006-05-04 Howard Henry E Natural gas liquefaction system
US20070234755A1 (en) * 2004-10-28 2007-10-11 Howard Henry E Natural gas liquefaction system
WO2006049885A2 (en) * 2004-10-28 2006-05-11 Praxair Technology, Inc. Natural gas liquefaction system
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US20060225461A1 (en) * 2005-04-11 2006-10-12 Henri Paradowski Process for sub-cooling an LNG stream obtained by cooling by means of a first refrigeration cycle, and associated installation
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US20080184711A1 (en) * 2007-02-01 2008-08-07 Diehl Bgt Defence Gmbh & Co. Kg Method for Cooling a Detector
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US20090084132A1 (en) * 2007-09-28 2009-04-02 Ramona Manuela Dragomir Method for producing liquefied natural gas
US20090113928A1 (en) * 2007-11-05 2009-05-07 David Vandor Method and System for the Small-scale Production of Liquified Natural Gas (LNG) from Low-pressure Gas
US8020406B2 (en) 2007-11-05 2011-09-20 David Vandor Method and system for the small-scale production of liquified natural gas (LNG) from low-pressure gas
AU2008322798B2 (en) * 2007-11-16 2011-05-12 Shell Internationale Research Maatschappij B.V. Method and apparatus for liquefying a hydrocarbon stream and floating vessel or offshore platform comprising the same
WO2009063092A2 (en) * 2007-11-16 2009-05-22 Shell Internationale Research Maatschappij B.V. Method and apparatus for liquefying a hydrocarbon stream and floating vessel or offshore platform comprising the same
GB2465952A (en) * 2007-11-16 2010-06-09 Shell Int Research Method and apparatus for liquefying a hydrocarbon stream and floating vessel or offshore platform comprising the same
US20100293996A1 (en) * 2007-11-16 2010-11-25 Michiel Gijsbert Van Aken Method and apparatus for liquefying a hydrocarbon stream and floating vessel or offshore platform comprising the same
WO2009063092A3 (en) * 2007-11-16 2009-10-01 Shell Internationale Research Maatschappij B.V. Method and apparatus for liquefying a hydrocarbon stream and floating vessel or offshore platform comprising the same
US20100293967A1 (en) * 2007-12-07 2010-11-25 Dresser-Rand Company Compressor system and method for gas liquefaction system
EA020215B1 (ru) * 2008-10-07 2014-09-30 Текнип Франс Способ получения потоков жидкого и газообразного азота, газового потока с высоким содержанием гелия и деазотированного потока углеводородов и установка для его осуществления
WO2010040935A3 (fr) * 2008-10-07 2011-06-03 Technip France Procede de production de courants d'azote liquide et gazeux, d'un courant gazeux riche en helium et d'un courant d'hydrocarbures deazote et installation associee
AU2009300946B2 (en) * 2008-10-07 2015-09-17 Technip France Method for producing liquid and gaseous nitrogen streams, a helium-rich gaseous stream, and a denitrogened hydrocarbon stream, and associated plant
CN102216711A (zh) * 2008-10-07 2011-10-12 泰克尼普法国公司 液态和气态氮物流、富氦气流，和脱氮的碳氢化合物物流的生产方法和相关的设备
CN102216711B (zh) * 2008-10-07 2015-05-27 泰克尼普法国公司 液态和气态氮物流、富氦气流,和脱氮的碳氢化合物物流的生产方法和相关的设备
FR2936864A1 (fr) * 2008-10-07 2010-04-09 Technip France Procede de production de courants d'azote liquide et gazeux, d'un courant gazeux riche en helium et d'un courant d'hydrocarbures deazote et installation associee.
WO2010040935A2 (fr) * 2008-10-07 2010-04-15 Technip France Procede de production de courants d'azote liquide et gazeux, d'un courant gazeux riche en helium et d'un courant d'hydrocarbures deazote et installation associee
WO2010055153A2 (en) * 2008-11-17 2010-05-20 Shell Internationale Research Maatschappij B.V. Method and apparatus for liquefying a hydrocarbon stream and floating vessel or offshore platform comprising the same
WO2010055153A3 (en) * 2008-11-17 2014-10-23 Shell Internationale Research Maatschappij B.V. Method and apparatus for liquefying a hydrocarbon stream and floating vessel or offshore platform comprising the same
WO2010109228A3 (en) * 2009-03-25 2013-04-04 Costain Oil, Gas & Process Limited Process and apparatus for separation of hydrocarbons and nitrogen
WO2010128467A3 (en) * 2009-05-08 2011-12-29 Corac Group Plc Production and distribution of natural gas
WO2010128467A2 (en) * 2009-05-08 2010-11-11 Corac Group Plc Production and distribution of natural gas
US20120227418A1 (en) * 2011-03-08 2012-09-13 Linde Aktiengesellschaft Cooling unit
US20170356687A1 (en) * 2015-01-09 2017-12-14 Mitsubishi Heavy Industries, Ltd. Gas liquefaction apparatus and gas liquefaction method
US10718564B2 (en) * 2015-01-09 2020-07-21 Mitsubishi Heavy Industries Engineering, Ltd. Gas liquefaction apparatus and gas liquefaction method
US11549746B2 (en) 2018-03-27 2023-01-10 Taiyo Nippon Sanso Corporation Natural gas liquefaction device and natural gas liquefaction method

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FR2128674A1 (es) 1972-10-20
FR2128674B1 (es) 1976-07-09

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