US3271965A - Methane liquefaction process - Google Patents

Methane liquefaction process Download PDF

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US3271965A
US3271965A US336560A US33656064A US3271965A US 3271965 A US3271965 A US 3271965A US 336560 A US336560 A US 336560A US 33656064 A US33656064 A US 33656064A US 3271965 A US3271965 A US 3271965A
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methane
natural gas
gas
vessel
temperature
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James B Maher
Mair James
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Chicago Bridge and Iron Co
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Chicago Bridge and Iron Co
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Priority to NL133167D priority Critical patent/NL133167C/xx
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Priority to US336560A priority patent/US3271965A/en
Priority to NL6411998A priority patent/NL6411998A/xx
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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
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
    • F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—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
    • F25J1/0002—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
    • F25J1/0025—Boil-off gases "BOG" from storages
    • 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
    • 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
    • F25J1/0208—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 in combination with an internal quasi-closed refrigeration loop, e.g. with 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
    • F25J1/0221—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 the cold stored in an external cryogenic component in an open refrigeration 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
    • 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
    • F25J2210/62—Liquefied natural gas [LNG]; Natural gas liquids [NGL]; Liquefied petroleum gas [LPG]
    • 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
    • F25J2230/30—Compression of the feed stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/60—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being (a mixture of) hydrocarbons
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/90—Processes or apparatus involving steps for recycling of process streams the recycled stream being boil-off gas from storage
    • 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

Definitions

  • This invention relates to apparatus and methods for storing in liquid form materials which are normally gases at ambient temperatures and pressures. More particularly, this invention is concerned with novel processes and apparatus for liquefying methane, such as in the form of natural gas, and subsequently storing the gas in liquefied form at veryl low temperatures and about atmospheric pressure.
  • Natural gas is distributed by means of pipelines which are usually unable to provide sufficient gas to supply the demand at peak periods.
  • the liquefied gas can be stored in large double-walled insulated tanks at a low temperature commensurate with a vapor pressure only slightly above atmospheric pressure.
  • Natural gas liquefaction is .presently accomplished by a process involving at least three refrigeration loops followed by expansion, or ashing, into the insulated storage tank.
  • Each loop utilizes a refrigerant at a dilierent pressure-temperature level and, since methane, ethylene and propane are among those often employed, they introduce additional hazard and expense.
  • These loops are difficult to synchronize and control and, as there exists a temperature difference between the condensing vapor and cooling liquid between each loop, power inefficiency is inherent in the system.
  • novel processes and apparatus for liquefying methane such as inthe form of natural gas, which do not employ a "ice I determined vpressure followed by a substantial lowering of the temperature ofthe ⁇ incoming methane by-means of a closed-loop refrigeration system, vfurther lowering the ternperature of the socooled-incomingfmethane gas by heat exchange with liquid.
  • the incoming methane* ⁇ gas is maintained at the same substantiallyvincreased predetermined pressure during ythe cooling cycle and until immediately prior to liquefaction of the incoming methane.
  • the process of this invention more specifically comprises receiving methane from a transmission pipeline
  • the methane gas cooled by the closed-loop refrigeration system employing achlorofluoroalkane gas as-the refrigerant is passed subsequently through thetube side of two consecutive evaporator vessels cooled'4 by the use of liquid methane removed from-the Imain storage tank and pumped to said vessels by useof inexpensive liquid-conveying pumps.
  • v natur al gas is received such as from a cross country transmissionline 9 at a ypressure of -about 3y00 p.s.i.a. -The -gas is conveyed to compressor Vl() whichincreasesits pressure, ,such as to usually notbe above 200() p.s.i.a. 1 Pressures lower than cascade refrigeration syste-m and which, in addition, ren v 800 p.s.i.a. lead to a less etiicientoperation.
  • the pressurized gas is then passed through heat exchanger 14. It is cooled in this heat exchanger by passing therethrough natural gas vapor at low temperatures. The vapor is obtained from the main storage tank 40 as will be more clearly seen hereinafter.
  • the pressurized natural gas is cooled considerably, such as down to about 45 F. It then is conveyed by pipe 15 into the -tube side of vessel 16.
  • the gas is cooled in vessel 16 by means of a liquefied chlorofluoroalkane type refrigerant boiling therein.
  • the vessel 16 is part of a closed-loop refrigeration system, as shown in the drawing, which employs a chloroffuoroalkane as the refrigerant.
  • compressors 18 and 19 compress the gas and convey it through a water cooled heat exchanger 20 and then to compressor 21 from which it goes to cooled condenser 22 and then is piped to pressure tank receiver 23.
  • the liquefied gas is then conveyed from vessel 23, such as at a temperature of about 50 F., by pipe 24 through heat exchanger 2S where it is cooled.
  • the liquefied gas then passes through pipe 26, through expansion valve 27 and then into vessel 16 at a pressure where it boils at a low temperature of about 102 F.
  • the vapor from vessel 16 is conveyed from the shell side thereof through pipe 28 and into heat exchanger 25 from which it emerges at a temperature of about 50 F. and then passes to compressor 18. The cycle is then repeated in this closed-loop refrigeration system.
  • the closed-loop refrigeration system 17 advisably employs any suitable commercial refrigerant which can lower the temperature of the methane adequately such as to about 75 to 125 F. It is particularly advisable, however, to employ as the refrigerant a fluorochlorinated alkane having one or two carbons such as dichlorodiuoromethane ⁇ (Freon 12), dichlorotetrafiuoroethane (Freon 114), trichloromonoiluoromethane (Freon 11), dichloromonofluoromethane (Freon 21), and monochlorotriuoromethane (Freon 13), or mixtures of such gases.
  • a fluorochlorinated alkane having one or two carbons such as dichlorodiuoromethane ⁇ (Freon 12), dichlorotetrafiuoroethane (Freon 114), trichloromonoiluoromethane (Freon 11), dich
  • the purpose is to lower the temperature of the methane on the tube side of vessel 16 as far as practicable with efficiency.
  • the natural gas is cooled in vessel 16 to a substantially lower temperature than at which it entered.
  • vessel 16 can leave vessel 16 at a temperature of about 98 F. and be conveyed by pipe 29 to pipe 30 and from pipe 30 through pipe 31 into heat exchanger 32.
  • heat exchanger 32 the temperature of the natural gas is lowered such as to about 154 F. This lowering of the temperature is effected by means of natural gas being passed through the other side of the exchanger at a lower temperature.
  • This natural gas is obtained indirectly from the main storage tank 40 as will be shown hereinafter.
  • the cooled natural gas Upon leaving heat exchanger 32 the cooled natural gas, still at the same pressure as created by compressor 10, viz. 1000 p.s.i.a., is conveyed at a temperature such as about 154 F. by means of pipe 33 to the tube side of vessel 34.
  • Vessel 34 is cooled by means of liquid natural gas boiling therein on the shell side.
  • the liquid natural gas used for this cooling operation is removed Vfrom the main storage tank 40 by pipe 35 and by means of an inexpensive liquid pump 36 is conveyed by pipe 37 to the vessel 34.
  • the liquid methane in the main storage tank 40 is maintained at a temperature of 258 F. and at a pressure of about 15 p.s.i.a.
  • the liquid methane is advisably used in vessel 34 at a temperature which will permit it to vaporize lat a pressure such that it can be recirculated directly into a transmission or consumer pipeline.
  • the gas may be removed directly at that pressure by employing a suitable boiling temperature in vessel 34.
  • the temperature of the liquid methane in vessel 34 can be at 210 F. for the vapor to boil off at 90 p.s.i.a., which is a conventional pressure used in consumer lines delivering natural gas.
  • the vapor leaving vessel 34 can be conveyed by pipe 38 through heat exchanger 32 and then by pipe '75 into heat exchanger 14 for cooling incoming natural gas.
  • the outgoing gas, upon leaving heat exchanger 14, can be conveyed by conduit 39 at 90 p.s.i.a. directly to a consumer line 41 or it can be directed through line 42 to compressor 43 and the pressure thereof raised, such as to 300 p.s.i.a., for conveying by pipe 44 to pipe 9 for recirculation in the stream.
  • the methane which is recirculated completes a closed-loop cooling system which utilizes liquefied natural gas from the main storage tank 46 for cooling such as by vessel 34.
  • the very cold gas is removed from vessel 34 by pipe 44 and is sent through pressure control valve 45 into liquefied gas receiver 46 which is maintained at about p.s.i.a.
  • the liquid level in the vessel 46 is maintained at a predetermined position by means of control system 47 which is interconnected with control valve 48 in line 49. Vapor is removed from vessel 46 by line 4.
  • This vapor is generally very high in nitrogen but, nevertheless, is suitable for operating gas engines for furnishing power to operate various pumps and compressors in the system.
  • the liquefied natural gas or methane is then conveyed by pipe 50 into the main storage tank 40 where it is flashed to a temperature of about 258 F. for storage at approximately atmospheric pressure or slightly thereabove, such as at 15 p.s.i.a.
  • the vapors are then conducted by pipe 53 :through the tube side of evaporator-condenser vessel 60 where they are liquefied and then conveyed by pipe 54 into a receiver 55.
  • Pump 56 then conveys the liquefied gas from receiver 55 to pipe 57 and into the bottom of the main storage tank 40.
  • Vessel 60 is cooled by withdrawing liquefied natural gas from the main storage tank 40 by means of pipe 35 and then sending it to pump 58 by which the liquefied gas is pumped through pipe 59 into vessel 60.
  • the liquefied natural gas in evaporator-condenser 60 is at about 254 F. and the vapor at 18 p.s.i.a.
  • the gas leaves the shell side of vessel 60 and is conveyed by pipe 61 into heat exchanger 32 from which it leaves by pipe 62 which feeds to blower 63.
  • Blower 63 sends the gas through heat exchanger 14 and by means of pipe 64 it is conveyed to compressors 65 and 66 which increase its pressure, such as to 90 p.s.i.a., for delivery directly to a consumer line.
  • the 'process as illustrated therein utilizes a second evaporator .vessel 70 for lowering the temperature of the natural gas after it leaves the closed-loop refrigeration cycle.
  • the natural gas leaves vessel 16
  • it can be conveyed through pipe 29 into pipe 71 .and through the tube side of vessel 70.
  • the gas enters vessel 70 at about 98 F. and is cooled therein to a temperature of about 130 F.
  • the so-cool'ed natural gas is conveyed from vessel 70 by pipe 72 into previously described pipe 31 and would thereafter follow the previously described route for further cooling in vessel 34.
  • the coolant for evaporator-condenser 70 is liquefied natural gas removed from the main storage tank 40 and conveyed by pipe 35 to pump 80 from which it emerges to pipe 81 for conveyance to the shell side of vessel 70.
  • the temperature of the liquefied natural gas in vessel 70 is raised to 160 F. which is commensurate with a pressure of 300 p.s.i.a.
  • the evaporated gas leaves vessel 70 by means of pipe 82 and passes through heat exchanger 14 for cooling incoming natural gas in line V12.
  • the gas from pipe 82 leaves heat exchanger 14 by pipe 83 and is then recirculated into the system by means of pipe 9.
  • the main storage tank contains a supply yof liquefied natural gas.
  • the closed-loop refrigeration system operating with a lchlorofluoroalkane refrigerant will cool the gas sufficiently in vessel 16 so that upon being ashed subsequently into the main storage tank 40 -it will lead to the production of some liquid methane although mostly vapor.
  • This vapor can be ared off by pipe 90 until there is sufficient liquid natural gas available in the main storage tank for Arecycling in the system.
  • the vapor from pipe 90 can be recirculatedback into the system. Since it is cool, however, various heat exchangers, not shown, could be yused to 4rernove refrigeration therefrom for cooling incoming natural gas.
  • the method of liquefying methane which comprises subjecting incoming methane gas to a substantially increased predetermined pressure, substantially lowering the temperature of the incoming methane vby means of ⁇ a closed-loop refrigeration system, further lowering the temperature of the so-cooled incoming methane gas by means of liquid methane removed from an insulated main storage tank for liquid met-haue to further reduce the temperature of the incoming methane, expanding the gaseous methane to liquefy and then flashing ⁇ the resulting liquefied methane into the main .storage tank to further lower the tempe-rature of the liquid methane for storage at a temperature at which the gas gives a vapor pressure close to but slightly above atmospheric pressure.
  • a method of liquefying natural gas and storing the same in an insulated storage tank at close to but slightly above atmospheric pressure which comprises subjecting incoming natural gas to a substantially increased predetermined pressure, cooling the so pressurized natural gas by means of a closed-loop refrigeration system which employs a chlorofluoroalkane gas as the refrigerant, further cooling the incoming natural gas by passing 'it through the tube side of a first vessel cooled on the shell side by liquefied natural gas pumped from the insulated storage tank, removing the incoming natural gas from the tube side of the first vessel at a much lower temperature than at which it enters, passing 'the lincoming natural gas through the tube side of a second vessel vcooled on the shell side by liquefied natural gas pumped from the insuilated storage tank to further lower the temperature of the incoming natural gas, said second vessel being at a much lower temperature than said first vessel, expanding the natural gas to liquefy and ashing the expanded liquefied natural gas into said storage tank for storage
  • step (9) recycling the vaporized methane liquid product from the first evaporator-cooler of step (7) back to the suction of the compressor in step (1) after the vaporized methane liquid has been heat exchanged in step (8),
  • step 10 passing the vaporized methane liquid product from the second evaporator of step (7) to a pipe line for use after the vaporized methane liquid has been heat exchanged in step (8),
  • step (12) passing the third vaporized liquid methane product stream in heat exchange with the inlet gas of step (2) before passing it to pipe line use of step (10).
  • a method of liquefying a compressed natural gas stream and storing liquefied methane product in an insulted storage tank at a low temperature wherein the pressure is only slightly above atmospheric comprising the steps of:
  • step (7) removing the second residual gas of step (7) from the storage tank, comprising said gas, liquefying said gas in a third evaporator-cooler by means of low temperature liquid methane product removed from the insulated storage tank, returning the now liquefied second residual gas to the storage tank and forming a third vaporized liquid methane product stream, and
  • step (11) passing the third vaporized liquid methane product stream in heat exchange with the inlet gas of step (2) before passing it to a pipe line or compressor as in step (9).
  • a method of liquefying a compressed natural gas stream and storing liquefied methane pnoduct in an insulated storage tank at a low temperature wherein the pressure is only slightly above atmospheric comprising the steps of (1) compressing a natural gas stream to a substantially increased predetermined pressure to form a main inlet natural gas stream,
  • step (9) passing the vaporized methane liquid product from the iirst and second evaporators of step (7 to a pipe line or back to the suction of the compressor in step (l).

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)
US336560A 1963-01-08 1964-01-08 Methane liquefaction process Expired - Lifetime US3271965A (en)

Priority Applications (3)

Application Number Priority Date Filing Date Title
NL133167D NL133167C (enrdf_load_stackoverflow) 1963-01-08
US336560A US3271965A (en) 1963-01-08 1964-01-08 Methane liquefaction process
NL6411998A NL6411998A (enrdf_load_stackoverflow) 1963-01-08 1964-10-15

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Cited By (20)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3323315A (en) * 1964-07-15 1967-06-06 Conch Int Methane Ltd Gas liquefaction employing an evaporating and gas expansion refrigerant cycles
US3347055A (en) * 1965-03-26 1967-10-17 Air Reduction Method for recuperating refrigeration
US3407052A (en) * 1966-08-17 1968-10-22 Conch Int Methane Ltd Natural gas liquefaction with controlled b.t.u. content
US3413817A (en) * 1964-04-10 1968-12-03 Lummus Co Liquefaction of natural gas at supercritical pressure employing a single refrigeration cycle
US3416324A (en) * 1967-06-12 1968-12-17 Judson S. Swearingen Liquefaction of a gaseous mixture employing work expanded gaseous mixture as refrigerant
US3508413A (en) * 1965-11-22 1970-04-28 Air Prod & Chem Low temperature separation process of normally gaseous materials by plural stage phase separations
US3792590A (en) * 1970-12-21 1974-02-19 Airco Inc Liquefaction of natural gas
US3798918A (en) * 1971-04-15 1974-03-26 Chicago Bridge & Iron Co Method and apparatus for purifying natural gas to be liquefied and stored
US3837821A (en) * 1969-06-30 1974-09-24 Air Liquide Elevating natural gas with reduced calorific value to distribution pressure
US3874185A (en) * 1972-12-18 1975-04-01 Linde Ag Process for a more efficient liquefaction of a low-boiling gaseous mixture by closely matching the refrigerant warming curve to the gaseous mixture cooling curve
US4083194A (en) * 1976-12-02 1978-04-11 Fluor Engineers And Constructors, Inc. Process for recovery of liquid hydrocarbons
US4295282A (en) * 1978-11-15 1981-10-20 Minnesota Mining And Manufacturing Company Heat and liquid recovery using open cycle heat pump system
US4637216A (en) * 1986-01-27 1987-01-20 Air Products And Chemicals, Inc. Method of reliquefying cryogenic gas boiloff from heat loss in storage or transfer system
US5325894A (en) * 1992-12-07 1994-07-05 Chicago Bridge & Iron Technical Services Company Method and apparatus for fueling vehicles with liquefied natural gas
US5590535A (en) * 1995-11-13 1997-01-07 Chicago Bridge & Iron Technical Services Company Process and apparatus for conditioning cryogenic fuel to establish a selected equilibrium pressure
US5687776A (en) * 1992-12-07 1997-11-18 Chicago Bridge & Iron Technical Services Company Method and apparatus for fueling vehicles with liquefied cryogenic fuel
US5771946A (en) * 1992-12-07 1998-06-30 Chicago Bridge & Iron Technical Services Company Method and apparatus for fueling vehicles with liquefied cryogenic fuel
US5860294A (en) * 1995-01-19 1999-01-19 Sinvent As Recondensation of gaseous hydrocarbons
WO2009006694A1 (en) 2007-07-09 2009-01-15 Lng Technology Pty Ltd Boil-off gas treatment process and system
US20100126186A1 (en) * 2006-08-29 2010-05-27 Shell Internationale Research Maatschappij B.V. Method and apparatus for generating a gaseous hydrocarbon stream from a liquefied hydrocarbon stream

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US2082189A (en) * 1934-05-09 1937-06-01 Lee S Twomey Method of liquefying and storing fuel gases
US2495549A (en) * 1949-03-15 1950-01-24 Elliott Co Separation of ternary gaseous mixtures containing hydrogen and methane
US2500129A (en) * 1944-08-29 1950-03-07 Clark Bros Co Inc Liquefaction system
US2503265A (en) * 1946-07-23 1950-04-11 Koppers Co Inc Separating constituents of coke oven gases
US2645104A (en) * 1951-02-17 1953-07-14 Lummus Co Fractional distillation
US2716332A (en) * 1950-04-20 1955-08-30 Koppers Co Inc Systems for separating nitrogen from natural gas
US2959020A (en) * 1958-01-29 1960-11-08 Conch Internat Mcthane Ltd Process for the liquefaction and reliquefaction of natural gas
US2960837A (en) * 1958-07-16 1960-11-22 Conch Int Methane Ltd Liquefying natural gas with low pressure refrigerants
US2973834A (en) * 1958-08-12 1961-03-07 Hydrocarbon Research Inc Hydrocarbon recovery from natural gas
US3020723A (en) * 1957-11-25 1962-02-13 Conch Int Methane Ltd Method and apparatus for liquefaction of natural gas

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2082189A (en) * 1934-05-09 1937-06-01 Lee S Twomey Method of liquefying and storing fuel gases
US2500129A (en) * 1944-08-29 1950-03-07 Clark Bros Co Inc Liquefaction system
US2503265A (en) * 1946-07-23 1950-04-11 Koppers Co Inc Separating constituents of coke oven gases
US2495549A (en) * 1949-03-15 1950-01-24 Elliott Co Separation of ternary gaseous mixtures containing hydrogen and methane
US2716332A (en) * 1950-04-20 1955-08-30 Koppers Co Inc Systems for separating nitrogen from natural gas
US2645104A (en) * 1951-02-17 1953-07-14 Lummus Co Fractional distillation
US3020723A (en) * 1957-11-25 1962-02-13 Conch Int Methane Ltd Method and apparatus for liquefaction of natural gas
US2959020A (en) * 1958-01-29 1960-11-08 Conch Internat Mcthane Ltd Process for the liquefaction and reliquefaction of natural gas
US2960837A (en) * 1958-07-16 1960-11-22 Conch Int Methane Ltd Liquefying natural gas with low pressure refrigerants
US2973834A (en) * 1958-08-12 1961-03-07 Hydrocarbon Research Inc Hydrocarbon recovery from natural gas

Cited By (21)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3413817A (en) * 1964-04-10 1968-12-03 Lummus Co Liquefaction of natural gas at supercritical pressure employing a single refrigeration cycle
US3323315A (en) * 1964-07-15 1967-06-06 Conch Int Methane Ltd Gas liquefaction employing an evaporating and gas expansion refrigerant cycles
US3347055A (en) * 1965-03-26 1967-10-17 Air Reduction Method for recuperating refrigeration
US3508413A (en) * 1965-11-22 1970-04-28 Air Prod & Chem Low temperature separation process of normally gaseous materials by plural stage phase separations
US3407052A (en) * 1966-08-17 1968-10-22 Conch Int Methane Ltd Natural gas liquefaction with controlled b.t.u. content
US3416324A (en) * 1967-06-12 1968-12-17 Judson S. Swearingen Liquefaction of a gaseous mixture employing work expanded gaseous mixture as refrigerant
US3837821A (en) * 1969-06-30 1974-09-24 Air Liquide Elevating natural gas with reduced calorific value to distribution pressure
US3792590A (en) * 1970-12-21 1974-02-19 Airco Inc Liquefaction of natural gas
US3798918A (en) * 1971-04-15 1974-03-26 Chicago Bridge & Iron Co Method and apparatus for purifying natural gas to be liquefied and stored
US3874185A (en) * 1972-12-18 1975-04-01 Linde Ag Process for a more efficient liquefaction of a low-boiling gaseous mixture by closely matching the refrigerant warming curve to the gaseous mixture cooling curve
US4083194A (en) * 1976-12-02 1978-04-11 Fluor Engineers And Constructors, Inc. Process for recovery of liquid hydrocarbons
US4295282A (en) * 1978-11-15 1981-10-20 Minnesota Mining And Manufacturing Company Heat and liquid recovery using open cycle heat pump system
US4637216A (en) * 1986-01-27 1987-01-20 Air Products And Chemicals, Inc. Method of reliquefying cryogenic gas boiloff from heat loss in storage or transfer system
US5325894A (en) * 1992-12-07 1994-07-05 Chicago Bridge & Iron Technical Services Company Method and apparatus for fueling vehicles with liquefied natural gas
US5687776A (en) * 1992-12-07 1997-11-18 Chicago Bridge & Iron Technical Services Company Method and apparatus for fueling vehicles with liquefied cryogenic fuel
US5771946A (en) * 1992-12-07 1998-06-30 Chicago Bridge & Iron Technical Services Company Method and apparatus for fueling vehicles with liquefied cryogenic fuel
US5860294A (en) * 1995-01-19 1999-01-19 Sinvent As Recondensation of gaseous hydrocarbons
US5590535A (en) * 1995-11-13 1997-01-07 Chicago Bridge & Iron Technical Services Company Process and apparatus for conditioning cryogenic fuel to establish a selected equilibrium pressure
US20100126186A1 (en) * 2006-08-29 2010-05-27 Shell Internationale Research Maatschappij B.V. Method and apparatus for generating a gaseous hydrocarbon stream from a liquefied hydrocarbon stream
WO2009006694A1 (en) 2007-07-09 2009-01-15 Lng Technology Pty Ltd Boil-off gas treatment process and system
EP2171341A4 (en) * 2007-07-09 2017-12-13 LNG Technology Pty Ltd Boil-off gas treatment process and system

Also Published As

Publication number Publication date
NL133167C (enrdf_load_stackoverflow)
GB1066479A (en) 1967-04-26
NL6411998A (enrdf_load_stackoverflow) 1965-07-09
FR1419550A (fr) 1965-11-26

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