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US3203191A - Energy derived from expansion of liquefied gas - Google Patents

Energy derived from expansion of liquefied gas Download PDF

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US3203191A
US3203191A US125398A US12539861A US3203191A US 3203191 A US3203191 A US 3203191A US 125398 A US125398 A US 125398A US 12539861 A US12539861 A US 12539861A US 3203191 A US3203191 A US 3203191A
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gas
pressure
expansion
liquefied
liquefied gas
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US125398A
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French Michael Joseph
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Conch International Methane Ltd
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Conch International Methane Ltd
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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
    • 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
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0005—Light or noble gases
    • F25J1/0007—Helium
    • 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
    • F25J1/0005—Light or noble gases
    • F25J1/001—Hydrogen
    • 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
    • F25J1/0012—Primary atmospheric gases, e.g. air
    • F25J1/0015—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
    • F25J1/0012—Primary atmospheric gases, e.g. air
    • F25J1/0017—Oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0042—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by liquid expansion with extraction of work
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
    • F25J1/005—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
    • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
    • F25J1/007—Primary atmospheric gases, mixtures thereof
    • F25J1/0072—Nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0203—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 single-component refrigerant [SCR] fluid in a closed vapor compression cycle
    • F25J1/0205—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 single-component refrigerant [SCR] fluid in a closed vapor compression cycle as a dual level SCR refrigeration cascade
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—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
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/62—Separating low boiling components, e.g. He, H2, N2, Air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/08—Cold compressor, i.e. suction of the gas at cryogenic temperature and generally without afterstage-cooler
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/60—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being hydrocarbons or a mixture of hydrocarbons
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • 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
    • F25J2290/62—Details of storing a fluid in a tank
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/902—Apparatus
    • Y10S62/91—Expander

Definitions

  • Processes for the liquefaction of gases include those in which the gas is liquefied under high pressure, usually by mechanical refrigeration, and the pressure on the liquefied gas is then reduced to produce a cold liquid at a lower pressure.
  • Typical examples of such processes are described in U.S. Patent No. 2,896,414, and the copending application Ser. No. 698,667, filed November 25, 1957, now U.S. Patent No. 3,020,723, and the copending appli cation Ser. No. 114,199, filed lune l, 1961.
  • the reduction in pressure on the liquefied gas has been achieved by passing the liqueed gas through an expansion valve.
  • the present invention provides a process for the liquefaction of a gas in Which the gas is liquefied under a high pressure and the pressure of the liquefied gas is then reduced, the method of effecting such reduction in pressure comprising passing the liquefied gas at 4the high pressure through a hydraulic motor under such conditions that substantiallyno gas phase is formed in the motor and energy is produced.
  • the liquefied gas Will require further cooling after passing through the hydraulic motor and and this may be achieved by then passing the liquefied gas through an expansion means in which part of the liquid is converted to gas and the pressure and temperature of the liquid are reduced to the required level.
  • further cooling may be employed in suitable circumstances, e.g. further refrigeration by heat exchange.
  • hydraulic motor includes any motor driven by passage of a liquid through it. It thus includes hydraulic turbines of the impulse or Pelton type, of the reaction or Francis type or of the propeller or axial flow type, and also displacement machines.
  • This invention is applicable to the liquefaction of any gas, such as oxygen, nitrogen, helium or hydrogen, but is particularly useful in the liquefaction of hydrocarbon gases, such as natural gas or methane or ethane.
  • liquid methane at a pressure of 3000 pounds per square inch and a temperature of 245 F. is passed through a hydraulic turbine to let the pressure down to Cce 50 pounds per square inch, and then through an expansion valve to reduce its pressure to 15 pounds per square inch and its temperature to 258 F.
  • the amount of gaseous methane produced is about a third of the amount of gaseous methane produced when the liquefied methane at 3000 pounds per square inch and 245 F. is passed through an expansion valve only to reduce its pressure to 15 pounds per square inch and its temperature to 258 F. This means that there is a reduction of about two thirds in the energy required to reliquefy the gaseous methane.
  • the energy produced by the hydraulic turbine is the equivalent of 20 B.t.u./ pound methane which is a further saving.
  • the process of the present invention is applicable to all liquefaction processes in which the gas is liquefied under high pressure, and the pressure of the liquefied gas is then reduced, irrespective of the refrigeration system employed.
  • a gas expansion process of refrigeration or a vapour compression or two-phase process of refrigeration may be employed.
  • Natural gas at a pressure of 465 p.s.i.a. and a temperature of F. is fed through pipe 1 into a two-stage reciprocating compressor 2 in which it is compressed to 3000 p.s.i.a. Cooling between the two stages of the compressor is achieved by water in inter-cooler 3, and the compressed natural gas passes from the compressor by pipe 4 through a further water cooler 5 and then through two heat exchangers 6 and 7 in parallel. In these heat exchangers, the temperature of the compressed natural gas is reduced to 247 F. and the gas is liquefied. The liquefied gas then passes through a Peiton wheel S from which it issues still as a liquid at a temperature of 224 F. and a pressure of 55 p.s.i.a. The power output of the Felton wheel which, for a flow of 240,000 lbs. per hour of natural gas, will amount to about 1500 horsepower, may be used in any convenient manner, for example in driving one or more of the compressors in the system.
  • the liquefied natural gas leaves the Pelton wheel through line 9 and passes through expansion valve 10 into the fiashing vessel 11.
  • the pressure in the flashing vessel 11 is 16 p.s.i.a., and the temperature 264 F.
  • the liquefied natural gas collecting in flashing vessel 11 is finally pumped to storage tank 12 via pump 13.
  • the gas phase at 264 F. formed in flashing vessel 11 is led by line 14 through heat exchanger 6 to condense some of the high pressure natural gas and is then recompressed to 50 p.s.i.a. in compressor 15 for use as fuel.
  • the boil-off from the storage tank 12 is led through line 16 and compressors 17 and 15 for subsequent use as fuel.
  • the refrigerating means in heat exchanger 7 which effects the refrigeration of the bulk of the pressurized natural gas is pipe 18 which carries gaseous nitrogen at 118 p.s.i.a. and 250 F.
  • the temperature of the nitrogen is 89 F. and its pressure 103 p.s.i.a.
  • the nitrogen is then compressed in compressor 19 to 2312 p.s.i.a., cooled to 33 F. in heat exchanger 20 against liquid ammonia in line 22 and expanded back to 118 p.s.i.a. and a temperature of 250 F. in expander 21 to complete the refrigeration cycle.
  • Expander 21 provides some o the power for driving the compressor 19.
  • the ammonia refrigeration cycle for cooling in heat exchanger 20 may be of any conventional type and is not shown in the drawing.
  • Another particularly useful application of the present invention is in connection with the invention described in the aforementioned copending application Serial No. 114,199 and can be applied, for example, by passing the liquefied natural gas leaving heat exchanger 4 through a hydraulic turbine before it passes through expansion valve 6 as shown in the drawing accompanying that application.
  • That invention provides a method of liquefying natural gas comprising inter alia the steps of supplying the gas in a process stream at an elevated temperature and pressure, removing heat from the process stream to reduce the natural gas to a temperature at which it is condensed to a liqueed state at the pressure conditions existing, and expanding the liqueed gas to lower pressure for storage and transportation.
  • Heat is removed from the process stream by heat exchange with a plurality of separate refrigerants, each of said refrigerants passing though a compession and expansion cycle, the expansion step being subdivided into a higher pressure section and a lower pressure section, the refrigerant owing from the higher pressure section to the lower pressure section and the process stream passing in heat exchange relationship first with the higher pressure section and then with the lower pressure section.
  • the pressure reduction step in that method may be accomplished in accordance with the present invention.
  • the liqueed natural gas stream leaving heat exchanger 144 may be passed through a Pelton wheel before it passes through throttling valve 146 as shown in FIG URE 1 of the drawings accompanying said copending application Serial No. 698,667.
  • the pressure reducing valve 156 in the said FIGURE 1 could be preceded by a Pelton wheel.
  • the expanion means through which the liquefied gas is passed after leaving the hydraulic motor may be an expansion valve or throttle valve or an expansion engine which may be of the reciprocating piston type or a turbine.
  • the work developed by the hydraulic motor and also Iby the expansion engine if used may of course be used for any suitable purpose such as driving the compressors required in the liquefaction cycle or for generating electricity.
  • the liqueed gas stream has to be subjected to pressure reduction in a number of stages, and the method of the present invention may be used in any one or more of these stages as may be found convenient.
  • a process as claimed in claim 2 in which the expansion means in which part of the liquid is converted to gas is an expansion valve.
  • a process for the liquefaction of a gas in which the gas is liqueed under high pressure and the liquefied gas is then passed at the high pressure through a hydraulic turbine while maintaining the back pressure on the motor in excess of the saturation pressure of the liquid whereby substantially no gas phase is formed in the turbine and energy is produced and then passed through an expansion valve in which part of the liquid is converted to gas and the pressure and temperature of the liquid are reduced to the required level.

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Description

M. J. FRENCH Aug. 31, 1965 ENERGY DERIVED FROM EXPANSION OF LIQUEFIED GAS Filed July 20. 1961 y Inventor /f/'Cbae/ JUSQU/7 f/eC/? B 7/2 Mide# (VAGSSQW m out loog .E .mmmev me@ FS M- J. FRENCH Aug. 31, 1965 ENERGY DERIVED FROM EXPANSION 0F LIQUEFIED GAS Filed July 20. 1961 mmL OWN..
. Inventor /V//Cbcze/ L/Ogep f/e/)C M;
OW, w 4%* A Horne y VUnited States Patent O 3,203,191 ENERGY DERIVED FROM EXPANSION F LIQUEFIED GAS Michael Joseph French, New Malden, England, assiguor to Couch International Methane Limited, Nassau, Bahamas, a company of the Bahamas Filed July 20, 1961, Ser. No. 125,398 Claims priority, application Great Britain, Sept. 2, 1960, 30,348/ 60 11 Claims. (Cl. 62-9) This invention relates to improvements in processes for the liquefaction of gases.
Processes for the liquefaction of gases include those in which the gas is liquefied under high pressure, usually by mechanical refrigeration, and the pressure on the liquefied gas is then reduced to produce a cold liquid at a lower pressure. Typical examples of such processes are described in U.S. Patent No. 2,896,414, and the copending application Ser. No. 698,667, filed November 25, 1957, now U.S. Patent No. 3,020,723, and the copending appli cation Ser. No. 114,199, filed lune l, 1961. Heretofore, the reduction in pressure on the liquefied gas has been achieved by passing the liqueed gas through an expansion valve. This method involves the conversion of a considerable proportion of the liquefied gas into a gas phase, and the gas phase so produced has to be recycled and reliquefied. It is clear that any method of reducing the amount of gas formed during this pressure reduction step will result in a saving in the horse power required to operate the liquefaction plant.
I have now found that, if the liquefied gas be passed through a hydraulic motor under such conditions that substantially no gas is produced in the motor before being passed through a conventional expansion valve, then the amount of vapour produced for a given pressure reduc- 'tion is far less than if the expansion valve were used on its own.
Accordingly, the present invention provides a process for the liquefaction of a gas in Which the gas is liquefied under a high pressure and the pressure of the liquefied gas is then reduced, the method of effecting such reduction in pressure comprising passing the liquefied gas at 4the high pressure through a hydraulic motor under such conditions that substantiallyno gas phase is formed in the motor and energy is produced.
The conditions necessary to ensure that no gas phase is formed in the hydraulic motor are achieved by maintaining the back pressure on the motor in excess of the saturation pressure of the liquid.
Generally, the liquefied gas Will require further cooling after passing through the hydraulic motor and and this may be achieved by then passing the liquefied gas through an expansion means in which part of the liquid is converted to gas and the pressure and temperature of the liquid are reduced to the required level. However, other means of further cooling may be employed in suitable circumstances, e.g. further refrigeration by heat exchange.
In this specification, the term hydraulic motor includes any motor driven by passage of a liquid through it. It thus includes hydraulic turbines of the impulse or Pelton type, of the reaction or Francis type or of the propeller or axial flow type, and also displacement machines.
This invention is applicable to the liquefaction of any gas, such as oxygen, nitrogen, helium or hydrogen, but is particularly useful in the liquefaction of hydrocarbon gases, such as natural gas or methane or ethane.
The following shows the savings that can be achieved by the present invention.
If liquid methane at a pressure of 3000 pounds per square inch and a temperature of 245 F. is passed through a hydraulic turbine to let the pressure down to Cce 50 pounds per square inch, and then through an expansion valve to reduce its pressure to 15 pounds per square inch and its temperature to 258 F., the amount of gaseous methane produced is about a third of the amount of gaseous methane produced when the liquefied methane at 3000 pounds per square inch and 245 F. is passed through an expansion valve only to reduce its pressure to 15 pounds per square inch and its temperature to 258 F. This means that there is a reduction of about two thirds in the energy required to reliquefy the gaseous methane. In addition, the energy produced by the hydraulic turbine is the equivalent of 20 B.t.u./ pound methane which is a further saving.
The process of the present invention is applicable to all liquefaction processes in which the gas is liquefied under high pressure, and the pressure of the liquefied gas is then reduced, irrespective of the refrigeration system employed. Thus, for example, a gas expansion process of refrigeration or a vapour compression or two-phase process of refrigeration may be employed.
The invention will now be illustrated by reference to the accompanying drawing which represents a ow sheet for the liquefaction of natural gas using a gas expansion process ot refrigeration.
Natural gas at a pressure of 465 p.s.i.a. and a temperature of F. is fed through pipe 1 into a two-stage reciprocating compressor 2 in which it is compressed to 3000 p.s.i.a. Cooling between the two stages of the compressor is achieved by water in inter-cooler 3, and the compressed natural gas passes from the compressor by pipe 4 through a further water cooler 5 and then through two heat exchangers 6 and 7 in parallel. In these heat exchangers, the temperature of the compressed natural gas is reduced to 247 F. and the gas is liquefied. The liquefied gas then passes through a Peiton wheel S from which it issues still as a liquid at a temperature of 224 F. and a pressure of 55 p.s.i.a. The power output of the Felton wheel which, for a flow of 240,000 lbs. per hour of natural gas, will amount to about 1500 horsepower, may be used in any convenient manner, for example in driving one or more of the compressors in the system.
The liquefied natural gas leaves the Pelton wheel through line 9 and passes through expansion valve 10 into the fiashing vessel 11. The pressure in the flashing vessel 11 is 16 p.s.i.a., and the temperature 264 F. The liquefied natural gas collecting in flashing vessel 11 is finally pumped to storage tank 12 via pump 13.
The gas phase at 264 F. formed in flashing vessel 11 is led by line 14 through heat exchanger 6 to condense some of the high pressure natural gas and is then recompressed to 50 p.s.i.a. in compressor 15 for use as fuel. Similarly, the boil-off from the storage tank 12 is led through line 16 and compressors 17 and 15 for subsequent use as fuel.
The refrigerating means in heat exchanger 7 which effects the refrigeration of the bulk of the pressurized natural gas is pipe 18 which carries gaseous nitrogen at 118 p.s.i.a. and 250 F. At the heat exchanger exit, the temperature of the nitrogen is 89 F. and its pressure 103 p.s.i.a. The nitrogen is then compressed in compressor 19 to 2312 p.s.i.a., cooled to 33 F. in heat exchanger 20 against liquid ammonia in line 22 and expanded back to 118 p.s.i.a. and a temperature of 250 F. in expander 21 to complete the refrigeration cycle. Expander 21 provides some o the power for driving the compressor 19. The ammonia refrigeration cycle for cooling in heat exchanger 20 may be of any conventional type and is not shown in the drawing.
ln the above-described process, other refrigerants may be used if desired, for example methane can be used in place of nitrogen, and propane in place of ammonia.
Another particularly useful application of the present invention is in connection with the invention described in the aforementioned copending application Serial No. 114,199 and can be applied, for example, by passing the liquefied natural gas leaving heat exchanger 4 through a hydraulic turbine before it passes through expansion valve 6 as shown in the drawing accompanying that application.
Another useful application of the present invention is in connection with the invention described in the aforementioned copending application Serial No. 698,667, now Patent No. 3,020,723. That invention provides a method of liquefying natural gas comprising inter alia the steps of supplying the gas in a process stream at an elevated temperature and pressure, removing heat from the process stream to reduce the natural gas to a temperature at which it is condensed to a liqueed state at the pressure conditions existing, and expanding the liqueed gas to lower pressure for storage and transportation. Heat is removed from the process stream by heat exchange with a plurality of separate refrigerants, each of said refrigerants passing though a compession and expansion cycle, the expansion step being subdivided into a higher pressure section and a lower pressure section, the refrigerant owing from the higher pressure section to the lower pressure section and the process stream passing in heat exchange relationship first with the higher pressure section and then with the lower pressure section.
The pressure reduction step in that method may be accomplished in accordance with the present invention. Thus, the liqueed natural gas stream leaving heat exchanger 144 may be passed through a Pelton wheel before it passes through throttling valve 146 as shown in FIG URE 1 of the drawings accompanying said copending application Serial No. 698,667. Similarly, the pressure reducing valve 156 in the said FIGURE 1 could be preceded by a Pelton wheel.
The expanion means through which the liquefied gas is passed after leaving the hydraulic motor may be an expansion valve or throttle valve or an expansion engine which may be of the reciprocating piston type or a turbine.
The work developed by the hydraulic motor and also Iby the expansion engine if used may of course be used for any suitable purpose such as driving the compressors required in the liquefaction cycle or for generating electricity.
In many liquefaction processes, the liqueed gas stream has to be subjected to pressure reduction in a number of stages, and the method of the present invention may be used in any one or more of these stages as may be found convenient.
I claim:
1. A process for the liquefaction of a gas in which the gas is liqueiied under a high pressure and the pressure of the liquelied gas is then reduced, the method of effecting such reduction in pressure comprising passing the liqueed gas at the high pressure through a hydraulic motor while maintaining the back pressure on the motor in excess of the saturation pressure of the liquid whereby substantially no gas phase is formed in the motor and energy is produced.
2. A process as claimed in claim 1 in which, after passing through the hydraulic motor, the liqueed gas is then passed through an expansion means in which part of the liquid is converted to gas and the pressure and temperature of the liquid are reduced to the required level.
3. A process as claimed in claim 2 in which the expansion means in which part of the liquid is converted to gas is an expansion valve.
4. A process as claimed in claim. 1 in which the hydraulic motor is a hydraulic turbine.
5. A process as claimed in claim 4 in which the hydraulic turbine is a Pelton Wheel.
6. A process as claimed in claim 1 in which the gas is liquefied under high pressure by heat exchange against a refrigerant operating in a gas expansion process of refrigeration.
7. A process as claimed in claim 1 in which the gas is liqueed under high pressure by heat exchange against a refrigerant operating in a vapour compression process of refrigeration.
8. A process as claimed in claim 1 applied to the liquefaction of natural gas.
9. A process for the liquefaction of a gas in which the gas is liqueed under high pressure and the liquefied gas is then passed at the high pressure through a hydraulic turbine while maintaining the back pressure on the motor in excess of the saturation pressure of the liquid whereby substantially no gas phase is formed in the turbine and energy is produced and then passed through an expansion valve in which part of the liquid is converted to gas and the pressure and temperature of the liquid are reduced to the required level.
10. A process as claimed in claim 9 in which the hydraulic turbine is a Pelton wheel.
11. A process as claimed in claim 9 applied to the liquefaction of natural gas.
References Cited by the Examiner UNITED STATES PATENTS 2,495,549 1/50 Roberts 62-39 2,552,451 5/51 Patterson 62--29 2,7 60,35 6 8/ 5 6 Sixsmith 62-9 2,896,414 7/59 Tung 62-40 2,901,326 8/59 Kurata 62-38 3,066,492 12/ 62 Grunberg 62-40 FOREIGN PATENTS 351,391 6/31 Great Britan. 864,855 4/ 61 Great Britain.
NORMAN YUDKOFF, Primary Examiner.
ROBERT A. OLEARY, Examiner.

Claims (1)

1. A PROCESS FOR LIQUEFACTION OF A GAS IN WHICH THE GAS IS LIQUEFIED UNDER A HIGH PRESSURE AND THE PRESSURE OF THE LIQUEFIED GAS IS THEN REDUCED, THE METHOD OF EFFECTING SUCH REDUCTION IN PRESSURE COMPRISING PASSING THE LIQUEFIED GAS AT THE HIGH PRESSURE THROUGH A HYDRAULIC MOTOR WHILE MAINTAINING THE BACK PRESSURE ON THE MOTOR IN EXCESS OF THE SATURATION PRESSURE OF THE LIQUID WHEREBY SUBSTANTIALLY NO GAS PHASE IS FORMED IN THE MOTOR AND ENERGY IS PRODUCED.
US125398A 1960-09-02 1961-07-20 Energy derived from expansion of liquefied gas Expired - Lifetime US3203191A (en)

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Cited By (19)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3339370A (en) * 1963-11-12 1967-09-05 Conch Int Methane Ltd Process for the separation of nitrogen and oxygen from air by fractional distillation
US3362173A (en) * 1965-02-16 1968-01-09 Lummus Co Liquefaction process employing cascade refrigeration
US3383873A (en) * 1964-11-03 1968-05-21 Linde Ag Engine expansion of liquefied gas at below critical temperature and above critical pressure
US3413817A (en) * 1964-04-10 1968-12-03 Lummus Co Liquefaction of natural gas at supercritical pressure employing a single refrigeration cycle
US3420633A (en) * 1966-09-27 1969-01-07 Chemical Construction Corp Removal of impurities from hydrogen
US3433026A (en) * 1966-11-07 1969-03-18 Judson S Swearingen Staged isenthalpic-isentropic expansion of gas from a pressurized liquefied state to a terminal storage state
US3542673A (en) * 1967-05-22 1970-11-24 Exxon Research Engineering Co Recovery of c3-c5 constituents from natural gas by compressing cooling and adiabatic autorefrigerative flashing
US3690114A (en) * 1969-11-17 1972-09-12 Judson S Swearingen Refrigeration process for use in liquefication of gases
US4456459A (en) * 1983-01-07 1984-06-26 Mobil Oil Corporation Arrangement and method for the production of liquid natural gas
US4970867A (en) * 1989-08-21 1990-11-20 Air Products And Chemicals, Inc. Liquefaction of natural gas using process-loaded expanders
US5505049A (en) * 1995-05-09 1996-04-09 The M. W. Kellogg Company Process for removing nitrogen from LNG
US5659205A (en) * 1996-01-11 1997-08-19 Ebara International Corporation Hydraulic turbine power generator incorporating axial thrust equalization means
US6089028A (en) * 1998-03-27 2000-07-18 Exxonmobil Upstream Research Company Producing power from pressurized liquefied natural gas
US6116031A (en) * 1998-03-27 2000-09-12 Exxonmobil Upstream Research Company Producing power from liquefied natural gas
WO2003064946A1 (en) * 2002-01-30 2003-08-07 Exxonmobil Upstream Research Company Processes and systems for liquefying natural gas
US20050020434A1 (en) * 2001-10-25 2005-01-27 Joachi Ansorge Process for liquefying natural gas and producing hydrocarbons
US20080066492A1 (en) * 2004-07-12 2008-03-20 Cornelis Buijs Treating Liquefied Natural Gas
US20090095018A1 (en) * 2006-05-15 2009-04-16 Hillegonda Bakker Method for liquefying a hydrocarbon stream
US10539363B2 (en) 2008-02-14 2020-01-21 Shell Oil Company Method and apparatus for cooling a hydrocarbon stream

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FR2471567B1 (en) 1979-12-12 1986-11-28 Technip Cie METHOD AND SYSTEM FOR COOLING A LOW TEMPERATURE COOLING FLUID
FR2848650A1 (en) * 2002-12-13 2004-06-18 Air Liquide Cryogenic fluid expansion procedure and apparatus, for use in distillation separation process, uses two expansion units to produce liquid and diphasic flows

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GB351391A (en) * 1930-01-21 1931-06-22 Wigan Coal And Iron Company Lt Improvements in hydraulic power systems particularly applicable for use in mines
US2495549A (en) * 1949-03-15 1950-01-24 Elliott Co Separation of ternary gaseous mixtures containing hydrogen and methane
US2552451A (en) * 1947-07-03 1951-05-08 Standard Oil Dev Co Fractionation of low molecular weight component mixtures
US2760356A (en) * 1952-04-22 1956-08-28 Nat Res Dev Method of liquefying gases
US2896414A (en) * 1955-09-12 1959-07-28 Constock Liquid Methane Corp Methane liquefaction cycle
US2901326A (en) * 1955-12-22 1959-08-25 Kurata Fred Separation of hydrogen sulfide and methane
GB864855A (en) * 1958-05-19 1961-04-12 Air Prod Inc Improvements in and relating to methods and apparatus for fractionating gaseous mixtures
US3066492A (en) * 1959-05-15 1962-12-04 Air Liquide Process for the liquefaction of a gas

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB351391A (en) * 1930-01-21 1931-06-22 Wigan Coal And Iron Company Lt Improvements in hydraulic power systems particularly applicable for use in mines
US2552451A (en) * 1947-07-03 1951-05-08 Standard Oil Dev Co Fractionation of low molecular weight component mixtures
US2495549A (en) * 1949-03-15 1950-01-24 Elliott Co Separation of ternary gaseous mixtures containing hydrogen and methane
US2760356A (en) * 1952-04-22 1956-08-28 Nat Res Dev Method of liquefying gases
US2896414A (en) * 1955-09-12 1959-07-28 Constock Liquid Methane Corp Methane liquefaction cycle
US2901326A (en) * 1955-12-22 1959-08-25 Kurata Fred Separation of hydrogen sulfide and methane
GB864855A (en) * 1958-05-19 1961-04-12 Air Prod Inc Improvements in and relating to methods and apparatus for fractionating gaseous mixtures
US3066492A (en) * 1959-05-15 1962-12-04 Air Liquide Process for the liquefaction of a gas

Cited By (24)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3339370A (en) * 1963-11-12 1967-09-05 Conch Int Methane Ltd Process for the separation of nitrogen and oxygen from air by fractional distillation
US3413817A (en) * 1964-04-10 1968-12-03 Lummus Co Liquefaction of natural gas at supercritical pressure employing a single refrigeration cycle
US3383873A (en) * 1964-11-03 1968-05-21 Linde Ag Engine expansion of liquefied gas at below critical temperature and above critical pressure
US3362173A (en) * 1965-02-16 1968-01-09 Lummus Co Liquefaction process employing cascade refrigeration
US3420633A (en) * 1966-09-27 1969-01-07 Chemical Construction Corp Removal of impurities from hydrogen
US3433026A (en) * 1966-11-07 1969-03-18 Judson S Swearingen Staged isenthalpic-isentropic expansion of gas from a pressurized liquefied state to a terminal storage state
US3542673A (en) * 1967-05-22 1970-11-24 Exxon Research Engineering Co Recovery of c3-c5 constituents from natural gas by compressing cooling and adiabatic autorefrigerative flashing
US3690114A (en) * 1969-11-17 1972-09-12 Judson S Swearingen Refrigeration process for use in liquefication of gases
US4456459A (en) * 1983-01-07 1984-06-26 Mobil Oil Corporation Arrangement and method for the production of liquid natural gas
US4970867A (en) * 1989-08-21 1990-11-20 Air Products And Chemicals, Inc. Liquefaction of natural gas using process-loaded expanders
US5505049A (en) * 1995-05-09 1996-04-09 The M. W. Kellogg Company Process for removing nitrogen from LNG
US5659205A (en) * 1996-01-11 1997-08-19 Ebara International Corporation Hydraulic turbine power generator incorporating axial thrust equalization means
US6089028A (en) * 1998-03-27 2000-07-18 Exxonmobil Upstream Research Company Producing power from pressurized liquefied natural gas
US6116031A (en) * 1998-03-27 2000-09-12 Exxonmobil Upstream Research Company Producing power from liquefied natural gas
US20050020434A1 (en) * 2001-10-25 2005-01-27 Joachi Ansorge Process for liquefying natural gas and producing hydrocarbons
US7451618B2 (en) 2001-10-25 2008-11-18 Shell Oil Company Process for liquefying natural gas and producing hydrocarbons
WO2003064946A1 (en) * 2002-01-30 2003-08-07 Exxonmobil Upstream Research Company Processes and systems for liquefying natural gas
US6658892B2 (en) 2002-01-30 2003-12-09 Exxonmobil Upstream Research Company Processes and systems for liquefying natural gas
US20080066492A1 (en) * 2004-07-12 2008-03-20 Cornelis Buijs Treating Liquefied Natural Gas
US20080066493A1 (en) * 2004-07-12 2008-03-20 Cornelis Buijs Treating Liquefied Natural Gas
US20090095018A1 (en) * 2006-05-15 2009-04-16 Hillegonda Bakker Method for liquefying a hydrocarbon stream
US20090095019A1 (en) * 2006-05-15 2009-04-16 Marco Dick Jager Method and apparatus for liquefying a hydrocarbon stream
US8578734B2 (en) 2006-05-15 2013-11-12 Shell Oil Company Method and apparatus for liquefying a hydrocarbon stream
US10539363B2 (en) 2008-02-14 2020-01-21 Shell Oil Company Method and apparatus for cooling a hydrocarbon stream

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