US3343374A - Liquid nitrogen production - Google Patents

Liquid nitrogen production Download PDF

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Publication number
US3343374A
US3343374A US484604A US48460465A US3343374A US 3343374 A US3343374 A US 3343374A US 484604 A US484604 A US 484604A US 48460465 A US48460465 A US 48460465A US 3343374 A US3343374 A US 3343374A
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gas
pressure
recycle stream
nitrogen
natural gas
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US484604A
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English (en)
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Warren L Nelson
Kositsky Nathan
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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.
    • F25J1/0292—Refrigerant compression by cold or cryogenic suction of the refrigerant gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C9/00—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure
    • F17C9/02—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure with change of state, e.g. vaporisation
    • F17C9/04—Recovery of thermal energy
    • 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
    • F25J1/003—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
    • F25J1/02—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
    • F25J1/0224—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 in combination with an internal quasi-closed refrigeration loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2265/00—Effects achieved by gas storage or gas handling
    • F17C2265/05—Regasification
    • 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
    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • 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
    • F25J2205/84—Processes or apparatus using other separation and/or other processing means using filter
    • 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
    • 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
    • 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

Definitions

  • This invention relates to the liquefaction of a gas utilizing a liquid regrigerant of a type having a boiling point at some convenient pressure lower than the critical ternperature 4of said gas.
  • a liquid regrigerant of a type having a boiling point at some convenient pressure lower than the critical ternperature 4of said gas.
  • it concerns the production of liquid nitrogen while regasifying liquid natural gas thereby to recover a part of the refrigeration potential inherent in the liquid natural gas.
  • the invention comprises:
  • a method of liquefying a gas utilizing a liquid refrigerant of a type having a boiling point lower than the critical temperature of said gas comprising (a) introducing a main stream of said gas at a selected pressure,-
  • gaseous nitrogen from any convenient source enters the system via a conduit 2 andisfcompressed in a three-stage compressor 4 to a pressure of approximately 340 p.s.i.a. (pounds per square inch, absolute), after which the heat of compression is removed by a water aftercooler 6 and a Freon aftercooler ICC 8.
  • the cooled nitrogen gas then passes through an oil separator 10 and oil adsorbers 12 to remove any entrained oil and next passes through a series of three heat exchangers 14, 16 and 18 respectively.
  • heat exchanger 14 the nitrogen is cooled down to a temperature of approximately 44 C. by relatively high pressure natural gas vapor in coil 20.
  • heat exchanger 16 the nitrogen is further cooled to a temperature of approximately 104 C.
  • liquid natural gas vaporizing in coil 22 In heat exchanger 18 the nitrogen gas is cooled to a temperature of approximately 129 C. by liquid natural gas being warmed (but not vaporized in coil 24. The chilled gaseous nitrogen then passes from heat exchanger 18 through a conduit 26 to a heat exchanger 28 where it is cooled to its dew point (approximately 155 C. at this pressure of slightly below 340 p.s.i.a.) against low pressure liquid natural gas vaporizing in coil 30. The nitrogen then leaves heat exchanger 28 via a 4conduit 32, mixes at point 34 with a recycle stream (to be described presently) in a conduit 112 and passes through another heat exchanger 36 where it is liquefied against low pressure liquid natural gas vaporizing in coil 38.
  • a 4conduit 32 mixes at point 34 with a recycle stream (to be described presently) in a conduit 112 and passes through another heat exchanger 36 where it is liquefied against low pressure liquid natural gas vaporizing in coil 38.
  • the liquid nitrogen leaves heat exchanger 36, via conduit 40, at a temperature of 155 C. and a pressure of approximately 335 p.s.i.a.
  • the liquid nitrogen is conducted by conduit 40 to a cold exchanger 42 where it is sub-cooled by iirst, second, and third recycle streams in coils 44, 46, and 48 respectively.
  • the liquid nitrogen is next expanded through a valve 50 into a separator 52. Gaseous nitrogen ilashed olf in separator 52, at a temperature of approximately 172 C. and a pressure of about 123 p.s.i.a., becomes the irst recycle stream.
  • Liquid nitrogen from separator 52 also at a temperature of 172 C. and a pressure of 123 p.s.i.a., enters a second cold exchanger 54 where it is cooled against the second and third recycle streams in coils 56 and 58 respectively.
  • the liquid nitrogen after being cooled in cold exchanger 54 is expanded through a valve 60 into a separator 62, the gaseous nitrogen flashed off in separator 62 becoming the second recycle stream at a temperature of about 184 C. and a pressure of about 47 p.s.i.a.
  • the liquid nitrogen from separator 62 also at a temperature of 184 C. and a pressure of. 47 p.s.i.a., enters a third cold exchanger 64, where it is cooled against the third recycle stream in coil 66 and is then expanded through a valve 68 into a separator 70.
  • the gaseous nitrogen flashed olf in separator 70 now at a temperature of about 193 C. and a pressure of about 20 p.s.i.a., becomes the third recycle stream.
  • the liquid nitrogen from separator 70 also at a ternperature of 193 C. and a pressure 20 p.s.i.a. (i.e. just slightly above atmospheric) leaves the system via a conduit and liquid nitrogen lilters 82.
  • the third recycle stream (being gaseous nitrogen at a pressure of about 20 p.s.i.a.) passes as mentioned through coils 66, 58, and 48 in heat exchangers 64, 54, and 42 respectively to cool incoming liquid nitrogen.
  • the third recycle stream leaves cold exchanger 42, it has been warmed to a temperature of about C., i.e., the temperature of the incoming liquid nitrogen in conduit 40.
  • the second and first recycle streams after passing through coils 46 and 44 of cold exchanger 42, are also warmed to a temperature of about 155 C.
  • the third recycle stream after leaving coil 48, passes through a conduit 84 to a compressor 86 where it is compressed to a pressure of about 47 p.s.i.a., i.e., the pressure of the second recycle stream.
  • the heat imparted to the third recycle stream by this compression is removed by low pressure liquid natural gas vaporizing in a coil 88 of a heat exchanger 90.
  • the third recycle stream leaves heat exchanger 90 via conduit 92 at a temperature of about 155 C. (i.e. the temperature of the second recycle stream) and mixes at point 94 with the second recycle stream leaving cold exchanger 42.
  • the combined second and third recycle streams are then compressed in a compressor 96 to a temperature of approximately 123 p.s.i.a. (i.e. the pressure of the first recycle stream) and the heat of compression is removed in heat exchanger 98 by means of vaporizing low pressure liquid natural gas in coil 100.
  • the combined second and third recycle streams leave heat exchanger 98, via conduit 102, at a temperature of approximately 155 C. (i.e. the temperature of the first recycle stream) and mix at point 104 with the first recycle stream.
  • the three combined recycle streams are then compressed in compressor 106 to a pressure of approximately 340 p.s.i.a. and the heat of compression is removed in heat exchanger 108 by low pressure liquid natural gas vaporizing in coil 110.
  • Nitrogen gas leaves heat exchanger 108 at a temperature of about 155 C., this being its dew point at the pressure of 340 p.s.i.a., and is conducted via the conduit 112 to mix with the main feed stream at point 34 as previously mentioned.
  • conduit 2 the flow through conduit 2, heat exchangers 14, 16 and 18, conduit 26, heat exchangers 28 and 36, conduit 40, cold exchangers 42, 54 and 64, and output conduit 80, may be thought of as the main stream.
  • liquid natural gas is supplied, usually from low pressure storage, and at a temperature of 158 C., via conduits 114 and 116, to pumps 118 and 120 respectively.
  • pump 120 the liquid natural gas is pumped to a pressure of just a few p.s.i. above atmospheric pressure.
  • the liquid natural gas passes through a conduit 122 and divides into five streams, each stream passing through one of the coils 30, 38, 88, 100, and 110 of the five respective heat exchangers 28, 36, 90, 98, and 108.
  • the liquid natural gas vaporizes in each of these five coils to cool the nitrogen flowing through the associated heat exchangers.
  • a relatively low pressure is required in these coils (just high enough to .move the liquid natural gas through the five heat exchangers referred to and to prevent air leakage into the system) because, if the pressure were too high, the liquid natural gas would vaporize in the heat exchangers at too high a temperature, possibly above the critical temperature for nitrogen of 147.1 C. In such case, the ve heat exchangers referred to would not cool the gaseous nitrogen sufficiently for it to condense.
  • Natural gas in vapor form after leaving the five coils 30, 38, 88, 100 and 110, recombincs in conduit 124. The natural gas is then conducted to a compressor 126 where it is compressed to a higher pressure and then mixed with vhigh pressure natural gas vapor at point 128, as will be described shortly.
  • Liquid natural gas coming in from a storage via conduit 114 is pumped by pump 118 to a pressure of about 300 p.s.i. and leaves pump 118 at a temperature of 153 C.
  • This high pressure liquid natural gas then passes through coil 24 of heat exchanger 18, where it is warmed (but not vaporized) against nitrogen gas passing through heat exchanger 18.
  • This warmed liquid natural gas now at a temperature of 107 C. next passes through coil 22 of heat exchanger 16 where it is vaporized to cool nitrogen gas passing through heat exchanger 16.
  • Natural gas vapor still at a temperature of 107 C., leaves coil 22 and passes through 4coil 20 of heat exchanger 14 where it is warmed to a temperature of +2 C. against nitrogen gas passing through heat exchanger 14.
  • This warmed natural gas vapor now at a pressure of about 294 p.s.i.a., travels via a conduit to mix with gas from compressor 126 at point 128.
  • the combined natural gas vapor streams at point 128 may be passed through an output compressor 132 for further compression depending on customer requirements, and the natural gas vapor leaves the system via a conduit 134.
  • customer requirements demand that natural gas in vapor form leaving the system be at a relatively high pressure. Since considerably less power is required in pumping a liquid to a high pressure as opposed to compressing a gas to a high pressure, a considerable saving in input power to the system is achieved by pumping liquid natural gas in conduit 114 to a high pressure before vaporizing it against nitrogen gas in heat exchangers 14, 16 and 18.
  • the liquid natural gas vaporized in the five heat exchangers 28, 36, 90, 98 and 108 must of necessity remain at a low pressure for reasons as mentioned.
  • gasifying and vaporizing are used interchangeably.
  • a method of liquefying a gas from thegroup consisting of nitrogen and oxygen utilizing a liquid refrigerant of a type having a boiling point, at a convenient pressure, lower than the critical temperature of said gas comprising (a) introducing a main stream of said gas at a selected pressure,
  • a method according to claim 1 including (h) introducing a stream of said liquid refrigerant at a low pressure for use in said steps (b) and (e),
  • step (k) compressing the low pressure refrigerant vapor resulting from said steps (b) and (e) to said high pressure and combining it with high pressure refrigerant vapor resulting from said step (j).
  • a method according to claim 1 including (h) introducing a stream of said liquid refrigerant at a low pressure for use in said steps (b) and (e),

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Separation By Low-Temperature Treatments (AREA)
US484604A 1964-12-16 1965-09-02 Liquid nitrogen production Expired - Lifetime US3343374A (en)

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CA918917 1964-12-16

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FR (1) FR1453071A (fr)
GB (1) GB1045660A (fr)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3581510A (en) * 1968-07-08 1971-06-01 Phillips Petroleum Co Gas liquefaction by refrigeration with parallel expansion of the refrigerant
US3690114A (en) * 1969-11-17 1972-09-12 Judson S Swearingen Refrigeration process for use in liquefication of gases
US3962881A (en) * 1974-02-19 1976-06-15 Airco, Inc. Liquefaction of a vapor utilizing refrigeration of LNG
EP3320283B1 (fr) * 2015-07-10 2025-01-01 ExxonMobil Technology and Engineering Company Procédé destiné à la production d'azote gazeux liquéfié au moyen de gaz naturel liquéfié

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
ITBG20030027A1 (it) * 2003-04-08 2004-10-09 Siad Macchine Impianti Spa Procedimento di recupero delle frigorie derivanti dalla gassificazione del metano liquido.

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2896414A (en) * 1955-09-12 1959-07-28 Constock Liquid Methane Corp Methane liquefaction cycle
US3058314A (en) * 1957-08-12 1962-10-16 British Oxygen Co Ltd Process and apparatus for the low temperature separation of air
US3092976A (en) * 1960-08-03 1963-06-11 Conch Int Methane Ltd Refrigeration of one fluid by heat exchange with another
US3160489A (en) * 1961-02-06 1964-12-08 Fluor Corp Nitrogen removal from natural gas
US3257813A (en) * 1960-08-03 1966-06-28 Conch Int Methane Ltd Liquefaction of gases

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2896414A (en) * 1955-09-12 1959-07-28 Constock Liquid Methane Corp Methane liquefaction cycle
US3058314A (en) * 1957-08-12 1962-10-16 British Oxygen Co Ltd Process and apparatus for the low temperature separation of air
US3092976A (en) * 1960-08-03 1963-06-11 Conch Int Methane Ltd Refrigeration of one fluid by heat exchange with another
US3257813A (en) * 1960-08-03 1966-06-28 Conch Int Methane Ltd Liquefaction of gases
US3160489A (en) * 1961-02-06 1964-12-08 Fluor Corp Nitrogen removal from natural gas

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3581510A (en) * 1968-07-08 1971-06-01 Phillips Petroleum Co Gas liquefaction by refrigeration with parallel expansion of the refrigerant
US3690114A (en) * 1969-11-17 1972-09-12 Judson S Swearingen Refrigeration process for use in liquefication of gases
US3962881A (en) * 1974-02-19 1976-06-15 Airco, Inc. Liquefaction of a vapor utilizing refrigeration of LNG
EP3320283B1 (fr) * 2015-07-10 2025-01-01 ExxonMobil Technology and Engineering Company Procédé destiné à la production d'azote gazeux liquéfié au moyen de gaz naturel liquéfié

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Publication number Publication date
GB1045660A (en) 1966-10-12
FR1453071A (fr) 1966-04-15

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