US3857251A - Lng storage tank vapor recovery by nitrogen cycle refrigeration with refrigeration make-up provided by separation of same vapor - Google Patents

Lng storage tank vapor recovery by nitrogen cycle refrigeration with refrigeration make-up provided by separation of same vapor Download PDF

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US3857251A
US3857251A US00315931A US31593172A US3857251A US 3857251 A US3857251 A US 3857251A US 00315931 A US00315931 A US 00315931A US 31593172 A US31593172 A US 31593172A US 3857251 A US3857251 A US 3857251A
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nitrogen
gas
liquid
gaseous nitrogen
outlet
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J Alleaume
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Technigaz
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Technigaz
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0257—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of nitrogen
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    • 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
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    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • F25J1/0025—Boil-off gases "BOG" from storages
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    • 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
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    • F25J1/0204—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 single flow SCR cycle
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    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
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    • 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
    • F17C2265/01—Purifying the fluid
    • F17C2265/015—Purifying the fluid by separating
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/76—Refluxing the column with condensed overhead gas being cycled in a quasi-closed loop refrigeration cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/90—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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/04—Recovery of liquid products
    • 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
    • F25J2230/20—Integrated compressor and process expander; Gear box arrangement; Multiple compressors on a common shaft
    • 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
    • F25J2270/04—Internal refrigeration with work-producing gas expansion loop
    • F25J2270/06—Internal refrigeration with work-producing gas expansion loop with multiple gas expansion loops
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/14—External refrigeration with work-producing gas expansion loop
    • F25J2270/16—External refrigeration with work-producing gas expansion loop with mutliple gas expansion loops of the same refrigerant
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/42—Quasi-closed internal or closed external nitrogen refrigeration cycle

Definitions

  • ABSTRACT Method and device of treatment of natural gas contained in storage tanks, for producing liquid nitrogen by extraction of nitrogen from the vapours resulting from the evaporation of said liquefied natural gas in said tanks, liquefaction of a portion of said extracted nitrogen and storage thereof for forming a reserve of cold.
  • the present invention relates to a method of treatment of natural gas contained in a liquefied state in storage and/or transportation tanks, of the type consisting in producing liquid nitrogen by utilizing, to this end, the boil-off of the liquefied natural gas, the methane and higher-hydrocarbon fraction of which is simultaneously re-liquefied, as well as a device for carrying out said method, usable especially on board methane tankers or in land storage plants.
  • the invention aims at providing simple means for producing liquid nitrogen usable partly as a coldproducing fluid for the re-liquefaction of methane, and partly for sale.
  • the invention provides a method of treatment of natural gas contained in a liquefied state in storage and/or transportation tanks, of the type consisting in producing liquid nitrogen from the boil-off of the liquefied gas and characterized in that nitrogen is extracted from the vapours resulting from the evaporation of the liquefied natural gas contained in the said tanks, at least a portion of the extracted nitrogen is liquefied and the liquid nitrogen is stored as a reserve of cold.
  • the method of the present invention differs therefrom by the fact that the nitrogen used in an open circuit as a cold-producing fluid is extracted from the evaporations of the liquefied natural gas conveyed in the tanks of methane tankers or stored in land reservoirs.
  • the nitrogen extracted from the liquefied natural gas is free from interfering impurities such as steam, carbon dioxide, sulphur oxide, oxygen and so forth, which are present in the gases usually employed for the production of liquid nitrogen (atmospheric air or gases resulting from combustion).
  • Another advantage lies in the fact that the nitrogen extracted from the liquefied-natural-gas evaporations already has a temperature close to that of liquid methane, i.e. about l60C under the usual conditions of transportation and storage of the liquefied natural gases.
  • This low initial temperature of the nitrogen contained in the liquefied natural gas reduces the amount of cold necessary to liquefy the same and, in case of partial liquefaction of the available nitrogen, the nitrogen which is rejected to the atmosphere in a gaseous state supplies previously the frigories corresponding to its sensible heat, thus facilitating the reliquefaction of the nitrogen fraction entering the cycle.
  • the method of re-liquefaction of the methane vapours resulting from the evaporation of liquefied natural gas, with simultaneous extraction of nitrogen consists in treating the liquefied-natural-gas vapours by way of cryogenic distillation or fractioning by bringing them into contact with a reflux liquid rich in nitrogen, so as to obtain gaseous nitrogen, on the one hand, and a condensed hydrocarbon mixture practically free from nitrogen, on the other hand, the latter then being returned into the liquefied-natural-gas tanks.
  • the cold for the condenser of the distillation column is provided by the evaporation of the liquid nitrogen contained in a reservoir.
  • the liquid-nitrogen vapours of the reservoir are mixed with the gaseous nitrogen extracted from the natural gas in order to be introduced into a nitrogen re-liquefaction cycle.
  • the invention is also characterized by a device for the re-liquefactiort of liquefied-natural-gas vapours and simultaneous extraction of nitrogen, the said device comprising a column for the cryogenic distillation or fractioning of liquefied-natural-gas vapours, connected, on the one hand, to the liquefied-natural-gas tanks by a vapour supply conduit and by a re-boiler drum for the return of the said condensed hydrocarbon mixture to the said tanks, and, on the other hand, to a reflux drum placed in the said liquid-nitrogen reservoir, the said reflux drum comprising a return outlet to the said distillation column and a second outlet to the said nitrogen re-liquefaction cycle.
  • the invention therefore results in a highly profitable exploitation of, for instance, a methane tanker, for it makes it possible, by means of an insignificant energy make-up, to re-liquefy all the liquid-natural-gas evaporation while extracting simultaneously the nitrogen contained in the liquid-natural-gas vapours, and to thus form a liquid nitrogen reserve capable of providing high-potential cold which can be used on board the tanker for the pre-cooling of the tanks and the tank filling conduits, for preparing a further liquid-natural-gas cargo, or on land for all the known uses of liquid nitrogen.
  • the invention is applied to stationary landstorage tanks, it makes it possible not only to re-liquefy all the methane vapours resulting from the evaporation of the liquefied natural gas, to enrich the liquefied natural gas, but also to extract the nitrogen contained in the said natural gas and store the liquid nitrogen thus obtained.
  • the nitrogen extracted from the natural-gas vapours is practically pure and free from interfering impurities, and can be sold at interesting prices.
  • FIG. 1 is a general diagrammatic view of a plant according to the invention, applicable to a methane tanker or a stationary storage plant;
  • FIG. la is a simplified diagrammatic view of the same plant
  • FIG. 2 is a general diagrammatic view of an alternative of embodiment of the invention.
  • FIG. 3 is a diagrammatic view of one exemplary embodiment of a, compressor and a turbine used in the invention
  • FIG. 4 is a view of another embodiment of a compressor and a turbine according to the invention.
  • FIG. is a graphic representation of the nitrogen reliquefaction and refrigeration cycle according to the invention. 1
  • a liquefied-natural-gas tank is shown at 1 and a liquid nitrogen reservoir is designated by the reference numeral 2.
  • the liquid-natural-gas vapours are sucked by a blower 3 into a conduit 4 and are conveyed into a cryogenic distillation or fractioning column 5.
  • the column 5 is connected, on the one hand, to a re-boiler drum 6 through a supply conduit 7, a reliquefied natural-gas pump 8 and through a return conduit 9 for the liquefied-natural-gas vapours.
  • the column 5 is connected to a reflux drum 10 placed within the liquid nitrogen reservoir 2, through a nitrogen vapour supply conduit 11, and a conduit 12 with a pump 13 for the return of liquid nitrogen into the said column.
  • the gaseous nitrogen proceeding from the reflux drum 10 and resulting from the liquid-nitrogen evaporations obtained in the tank 2 is conveyed by the conduits 14 and 15 into the nitrogen liquefaction circuit.
  • This circuit comprises a conduit 16 connected, on the one hand, to the conduits 14 and 15 and, on the other hand, to a blower 47 delivering into a series of heat exchangers 17, 18, 19 which areintended to heat the gaseous nitrogen, a multi-stage compressor 20 driven by a motor 21, a heat exchanger 22, using for instance water or any other suitable cooling fluid such as air, propane, ammonia, freon and so forth, serving to cool the nitrogen compressed in the compressor 20.
  • the compressed nitrogen then re-passes through the coil 23 of the heat exchanger 19, the coil 24 of the heat exchanger 25, and then the coils 26, 27, 28 of, respectively, the heat exchanger 18, the reboiler drum 6 and the heat exchanger 17.
  • the nitrogen thus cooled passes through the coil 29 of a heat exchanger 30 before being introduced into cold separates 31 and 32.
  • the liquid nitrogen collected at the bottom of the cold separator 31 is conveyed through a conduit 33 into the cold separator 32, and the liquid nitrogen collected in this second cold separator 32 returns to the reservoir 2 through a conduit 34.
  • the gaseous nitrogen contained in the first cold separator 31 is conveyed through a conduit 35 into an expansion-with-work plant 36 which may be constituted by a two-stage turbine or a thermal separator of a known type, comprising a group of pipes closed at one end and in which the gas is subjected to expansion-with work, the corresponding energy being released in the form of heat, or still by a reciprocatingmotion expansion machine coupled for instance to a piston compressor.
  • an expansion-with-work plant 36 which may be constituted by a two-stage turbine or a thermal separator of a known type, comprising a group of pipes closed at one end and in which the gas is subjected to expansion-with work, the corresponding energy being released in the form of heat, or still by a reciprocatingmotion expansion machine coupled for instance to a piston compressor.
  • the gaseous nitrogen expanded in the plant 36 is mixed with the gaseous nitrogen resulting from the second cold separator 32 and then passes through the heat exchanger 30 where it cools the nitrogen passing through the coil 29 and is injected into the said nitrogen liquefaction circuit through the conduit 16 before the heat exchanger 17.
  • the distillation column 5, the re-boiler drum 6, the heat exchangers 17, 18, 30, the cold separators 31 and 32, the expansion-with-work plant 36 are placed in a chamber filled with, low-temperature gaseous nitrogen, the said chamber being shown in FIG. 1 by the dotted outline 40.
  • the liquefied-natural-gas vapours are conveyed from the tank 1 into the fractioning column 5 where they are cooled by contact with the liquid rich in nitrogen proceeding from the reflux drum 10.
  • the nitrogen contained in the natural-gas vapours remains in a gaseous state, whereas the tower bottom liquid, which is constituted by a mixture rich in hydrocarbons and poor in nitrogen, is then returned to the re-boiler drum 6.
  • the latter is at the boiling temperature of nitrogen-free liquid-natural-gas, so that the hydrocarbon mixture returned into the tank 1 contains practically no nitrogen.
  • the vapours from the top of the distillation column 5 are conveyed into the reflux drum 10 where they are partially liquefied.
  • the distillate consitituted by the remaining gaseous nitrogen is conveyed into the previously described nitrogen liquefaction circuit where it is first successively heated in the exchangers l7, l8 and 19 and then compressed in the compressor 20, cooled by passing through the coils of the exchangers 19, 20, 25, 18, 17, 30, and then either condensed in the cold separators 31 and 32 or expanded in the plant 36 and recycled into the liquefaction circuits.
  • the gaseous nitrogen may be made to escape to open air through the conduit 41 placed right before the compressor.
  • Use may also be made of the heat exchangers 22 and 25 to heat the liquefied natural gas contained in the tank 1 and intended for either the boiler of a tanker or a network for distribution to consumers.
  • the natural gas is delivered by a pump 42 into the coil 43 of a heat exchanger 44, and then into the coil 45 of a second heat exchanger 46, supplied, for instance, with high-temperature water from the heat exchanger 22.
  • the natural gas thus vaporized may either pass through the heat exchanger 25 where it takes heat from the compressed nitrogen, or be used directly.
  • a portion of the natural gas vaporized at the outlet of the exchanger 46 is conveyed into the exchanger 44 to vaporize the liquid natural gas.
  • FIG. 2 An alternative of embodiment of the invention is shown in FIG. 2, wherein, instead of arranging on one and the same shaft-line the motor 21, the multi-stage compressor 20 and the multi-stage expansion plant 36, the same function may be fulfilled by grouping on three different shaft-lines an electric motor (or a steam turbine), a single-stage or two-stage compressor and a'single-stage or two-stage expansion plant.
  • an electric motor or a steam turbine
  • a single-stage or two-stage compressor or a'single-stage or two-stage expansion plant.
  • the compression and expansion circuit for the gaseous nitrogen shown in FIG. 2, comprises three electric motors 51, 52, 53 which may also be replaced by steam turbines, three compressors 54, 55, S6 ensuring lowpressure, medium-pressure and high-pressure levels respectively. With each of these motor-compressor sets are respectively associated turbines 57, 58, 59 for the expansion of the compressed nitrogen.
  • the gaseous nitrogen after having passed through the exchangers 17, 18, 19, passed successively through the three compression stages 54, 55, 65 and is cooled after each compression in a heat exchanger 60 using for instance water or any other suitable refrigerating fluid, the circulation pumps and circuits of which are not shown. Thereafter, the nitrogen repasses, as in the first embodiment, through the heat exchangers 19, 18, the re-boiler drum 6 and the exchanger 17.
  • the compressed nitrogen then passes through the coils of three exchangers 61, 62, 63 and then arrives in a first cold separator 64 wherefrom the gaseous nitrogen is conveyed to the turbine 59 and the liquid nitrogen is conveyed to a second cold separator 65.
  • the gaseous nitrogen partially expanded in the turbine 59 passes through the cold separator 65 and then through the heat exchanger 63 and the second turbine 58.
  • the liquid nitrogen proceeding from the cold separator 65 is injected into a third separator 66 into which is also conveyed the expanded gaseous nitrogen proceeding from the turbine 58.
  • the gaseous nitrogen contained in the separator 66 is again conveyed into an exchanger 62 and then passes in the turbine 57 where it is expanded and then conveyed into a fourth cold separator 67.
  • the liquid nitrogen from the separator 66 is returned into the separator67.
  • the gaseous nitrogen from the latter separator then passes through the heat exchanger 61 and is injected at the beginning of the nitrogen liquefaction cycle, before the exchanger 17.
  • FIG. 3 illustrates an example of embodiment of a motor-compressor-turbine set corresponding to one of the sets used in the embodiment shown in FIG. 2.
  • the motor for instance 51
  • the compressor 54 is provided with a tangential outlet and an axial inlet.
  • the motor-compressor-turbine sets by using a steam turbine instead of the motor, a centrifugal compressor and a centripetal expansion turbine as shown in FIG. 4.
  • the steam turbine 80, the compressor 81 and the expansion turbine 82 are mounted in one and the same body.
  • the latter, as well as the volutes and diffusers of the expansion turbine, are made from cyrogenic metal.
  • the various elements are assembled within the common body through the medium of heatinsulating members arranged to avoid any heatconducting bridges between the said elements.
  • the pressure of the steam used in the turbine 81 is slightly lower than the nitrogen pressure in order to avoid any pollution of the nitrogen by the steam at the rotary joints.
  • the main advantage of the arrangement just described consists in the use of a modular construction system and in that the power used in each module is only a fraction of the total power, thus facilitating the supply of energy by the networks on board a ship. Moreover, it is possible to achieve various dimensions and rotational speeds in each of the modules.
  • the nitrogen cooling cycle according to the invention is illustrated in FIG. 5, where the entropy values S are plotted in abscissae against enthalpy values H plotted in ordinates.
  • the line A B shows the heating of the gaseous nitrogen in the heat exchangers 17, 18, 19, whereas the line B C corresponds to the compression of the nitrogen in a four-stage compressor 20.
  • the curve C D corresponds to the cooling of the nitrogen compressed in the exchangers 22, 19, 25, 18, 27, 17, 29 and the cold separators 31 and 32.
  • the line D E corresponds to the expansion of the gaseous nitrogen in the plant 36, whereas the dotted line E A represents the vaporization of the liquid nitrogen and the compression of the vapour in the blower 3.
  • the production of nitrogen on board a methane tanker is always much higher than the quantity of liquid nitrogen consumed by the ship, either to compensate for the regrigerant fluid losses in the natural-gas vapour reliquefaction unit, or to pre-cool and to fill the tanks with an inert atmosphere.
  • the tank 1 is, of course, full of liquefied natural gas. So is the reservoir 2, the liquid nitrogen contained in the latter having been produced mainly during the empty return trip of the methane tanker. Since the tank 1 is practically full, the distillation column 5 operates at its full working rate since, the amount of methane to be re-liquefied being at a maximum.
  • Part of the necessary cold may be obtained by slowly vaporizing the liquid nitrogen of reservoir 2.
  • the volume of gas conveyed to the distillation tower is greatly reduced. Indeed, the boil-off in the liquefied-natural-gas tanks is reduced when the latter contain only a small amount of liquid.
  • the refrigerating capacity necessary to reliquefy the methane is therefore reduced and the plant may be used to condensate a larger fraction of the nitrogen contained in these evaporations.
  • the liquid nitrogen thus produced accumulates in the reservoir 2 which progressively fills during the return trip.
  • the volume of nitrogen conveyed to the compressor therefore differs very little from that conveyed to the compressor during the outward trip, in the course of which the tanks 1 are practically full and the reservoir 2 empties.
  • the time difference in phase of the variations of the levels in the liquefied-natural-gas tanks 1 and in the liquid nitrogen reservoir results in a regulation of the rate of flow from the compressor and from the expansion plant 36.
  • the relatively regular use of these machines emables them to be better dimensioned.
  • the heat exchanger 25 enables the cold of the natural gas to be recovered and used to produce an additional amount of liquid nitrogen, which is stored in the reservoir 2.
  • the volume of nitrogen sucked by the nitrogen compressor remains substantially constant in time.
  • a device for treatment of natural gas stored in liquefred state comprising: tank means containing said liquefied natural gas and including a stop vapor space filled with the gaseous phase consisting of the vapors resulting from the boil-off of said liquefied-natural-gas; fractional distillating column means comprising 9 bottom collecting sump portion for holding reliquefiednatural-gas, an overhead vapor space collecting top portion for confining separated gaseous nitrogen and intermediate upper and lower portions and a sump portion; first vapor conveying duct means connecting said top vapor space of said tank means to said intermediate lower portion of said fractional distillating column means; first vapor pump means inserted in said first duct means and having its suction side communicating with said top vapor space and its discharge side communicating with said fractional distillating column means; reboiler vessel means including a lower liquid phase holding portion for containing reboiling liquefied-natural-gas and an upper gaseous phase holding portion for confining vapors of liquefied-natural-gas
  • a method of progressively cryogenically purifying a stored stationary body of liquefied-natural-gas containing at least a major portion of methane and a substantial amount of nitrogen mixed therewith by continuous cyclic process comprising the steps ofzproviding a stored stationary body of liquid nitrogen; collecting the boil-off forming the gaseous phase built up on the top of said body of liquefled-natural-gas; effecting a fractional distillation of said boil-off through heat exchange with a boiling refrigerant by using a cold reflux liquid previously separated and reliquefied-nitrogen whereby the nitrogen contained in said boil-off is separated as a gas therefrom and the so purified remaining boil-off is reliquefled; collecting the purified hydrocarbon-enriched reliquefied natural gas resulting as the bottoms from said fractional distillation and returning it to said body of liquefied-natural-gas which is thus also gradually enriched; collecting the separated overhead gaseous nitrogen and the gaseous nitrogen resulting from evaporation of said reflux liquid and conveying
  • a method of progressively cryogenically purifying a stored stationary body of liquefied natural gas containing at least a major portion of methane and a substantial amount of nitrogen mixed therewith by a continuous cyclic process comprising the steps of: providing a stored stationary body of liquid-nitrogen; collecting the boil-off forming the gaseous phase built up on the top of said body of liquefied-natural-gas; effecting a fractional distillation of said boil-off through heat exchange with a boiling refrigerant by using a cold reflux liquid previously separated and reliquefied nitrogen whereby the nitrogen contained in said boil-off is separated as a gas therefrom and the sopurified remaining boil-off is reliquefied; collecting the purified hydrocarbon-enriched reliquefied natural gas resulting as the bottoms from said fractional distillation and returning it to said body of liquefied-natural-gas which is thus also gradually enriched; collecting the separated overhead gaseous nitrogen and the gaseous nitrogen resulting from evaporation of said reflux liquid and conveying same in
  • a device comprising aftercooling means inserted in series between the outlet of each stage of said compressor means and the inlet of the heating medium flow path of said main heat exchanger means and extraneous coolant circulating means, said aftercooler means being cooled by the circulation of extraneous coolant of said extraneous coolant circulating means.
  • a device comprising workproducing gas expansion means having its inlet connected to another outlet of the vapor holding portion of said cold phase separator means and its outlet connected to an inlet of the refrigerating medium flow path of said main heat exchanger means.
  • said workproducing gas expansion means comprises a tubular thermal separator.
  • said workproducing gas expansion means comprising at least one reciprocating piston engine coupled to at least one piston compressor forming compressor means and motor means, said compressor means also being operatively connected to motor means.
  • said workproducing gas expansion means comprises turbine means having at least one stage, compressor means which comprise multiple stages, interstage cooler means separating said multiple stages and extraneous coolant means for said stages said turbine means and said compression means being directly coupled and operatively connected to said motor means.
  • main heat exchanger means comprise first and second heat exchangers whose said pipe coil means are interconnected.
  • a device comprising further gas flow heat exchanger means having a heating medium flow path connected in series between the outlet of the heating medium flow path of said main heat exchanger means and said inlet of the vapor holding portion of said cold phase separator means and a refrigerating medium flow path connected in series between said inlet of the refrigerating medium flow path of said main heat exchanger means and on the other hand said one outlet'of the vapor holding portion of said cold phase separator means and said outlet of said workproducing gas expansion means.
  • said cold phase separator means consist of first and second cold phase separators, the outlet of the condensate holding portion of said first cold phase separator being connected to the inlet of the vapor holding portion of said second cold phase separator whereas the outlet of the heating medium flow path of said further heat exchanger means is connected to an inlet of the vapor holding portion of said first cold phase separator and the outlet of said first cold phase separator is connected to the inlet of said work-producing gas expansion means, the outlet of the vapor holding portion of said second cold phase separator being connected to the inlet of the refrigerating medium flow path of said further heat exchanger means.
  • a device including a conduit connecting the outlet of the refrigerating medium flow path of said main exchanger means to the inlet of said compressor means and controllable vent pipe 'means branched off said conduit.
  • a device including third liquid pump means at least the suction side of which is immersed in the liquefied-natural-gas contained in said tank means; pipe line means leading from the discharge side of said third liquid pump means to the outside of said tank means towards a consumer station and auxiliary heat exchanger means comprising a heating medium flow path connected to the coolant outlet of said aftercooling means and a refrigerating medium flow path inserted in series in said pipe line means.
  • a device including additional'heat exchanger means comprising a heating medium flow path having an inlet connected through branch duct means to said pipe line means downstream of said auxiliary heat exchanger means and an outlet connected to the top vapor space of said tank means, and a refrigerating medium flow path inserted in series into said pipe line means upstream of said auxiliary heat exchanger means.
  • said power driven compressor means comprise a plurality of separate, respectively low intermediate and high pressure turbine-motor-compressor sets having each one a workproducing gas expansion turbine, a motor and a compressor, and drive shaft means, said drive shaft means operatively and mechanically coupling each set, the gas flow path of said compressors being interconnected in series and inserted between the outlet of the refrigerating medium flow path entering the low pressure compressor and the inlet of the heating medium flow path fed by the final high pressure compressor to said main heat exchanger means, with interstage extraneous gas coolant supplied cooler means connected in series between any two successive compressors and gas aftercooler means cooled by said extraneous coolant connected in seriesbetween the outlet of said high pressure compressor and the inlet of the heating medium flow path of said main heat exchange means; said cold phase separator means comprising a primary cold phase separator whose vapor holding portion is connected through an outlet to the inlet of the turbine of the final high pressure turbine-motor-compressor set and a like plurality of secondary cold phase
  • each turbine-motor-compressor set comprises multiplying gear means with two output shafts operatively coupled to drive shafts of said turbine and said compressor, respectively, and with an input shaft operatively coupled to said motor, said compressor having an axially di-- rected gas inlet and a tangentially directed gas outlet.
  • a device mounted on board a ship and wherein the turbine-motor and compressor of each turbine-motor-compressor set are housed in a same casing and said motor comprises'a steam turbine whose steam pressure is slightly lower than the gas pressure in said gas flow path.
  • said cold phase separation comprises a first separation producing liquid nitrogen which is subject to a second separation producing liquid nitrogen which is returned to said body of liquid nitrogen whereas the non-condensed gaseous nitrogen resulting from said first separation is expanded and mixed with the non-condensed gaseous nitrogen resulting from said second separation.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Chemical & Material Sciences (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Ocean & Marine Engineering (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
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US00315931A 1971-12-27 1972-12-18 Lng storage tank vapor recovery by nitrogen cycle refrigeration with refrigeration make-up provided by separation of same vapor Expired - Lifetime US3857251A (en)

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JP (1) JPS4873404A (xx)
DE (1) DE2263055A1 (xx)
ES (1) ES410088A1 (xx)
FR (1) FR2165729B1 (xx)
GB (1) GB1403999A (xx)
IT (1) IT972507B (xx)
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US4586942A (en) * 1983-02-08 1986-05-06 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and plant for the cooling of a fluid and in particular the liquefaction of natural gas
US4604115A (en) * 1984-03-23 1986-08-05 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and installation for treating a storage site
US4675037A (en) * 1986-02-18 1987-06-23 Air Products And Chemicals, Inc. Apparatus and method for recovering liquefied natural gas vapor boiloff by reliquefying during startup or turndown
US4689064A (en) * 1985-10-21 1987-08-25 Societe Francaise De Stockage Geologigue Geostock-Tour Aurore Method of maintaining constant the composition of a product stored in a low temperature liquefied gas store
US4846862A (en) * 1988-09-06 1989-07-11 Air Products And Chemicals, Inc. Reliquefaction of boil-off from liquefied natural gas
US5139547A (en) * 1991-04-26 1992-08-18 Air Products And Chemicals, Inc. Production of liquid nitrogen using liquefied natural gas as sole refrigerant
US5141543A (en) * 1991-04-26 1992-08-25 Air Products And Chemicals, Inc. Use of liquefied natural gas (LNG) coupled with a cold expander to produce liquid nitrogen
US5150576A (en) * 1990-11-16 1992-09-29 Liquid Carbonic Corporation Vapor collecting apparatus
US5220798A (en) * 1990-09-18 1993-06-22 Teisan Kabushiki Kaisha Air separating method using external cold source
WO1994013376A1 (en) 1992-12-07 1994-06-23 Edwards Engineering Corp. Vapor recovery apparatus and method
US5507146A (en) * 1994-10-12 1996-04-16 Consolidated Natural Gas Service Company, Inc. Method and apparatus for condensing fugitive methane vapors
EP0880000A3 (en) * 1997-05-19 1998-12-16 Praxair Technology, Inc. Turbine/motor (generator) driven booster compressor
WO2001057430A1 (en) * 2000-02-03 2001-08-09 Cabot Lng Llc Vapor recovery system using turboexpander-driven compressor
US6672104B2 (en) 2002-03-28 2004-01-06 Exxonmobil Upstream Research Company Reliquefaction of boil-off from liquefied natural gas
US20040068993A1 (en) * 1999-11-05 2004-04-15 Toshikazu Irie Device and method for pressure control of cargo tank of liquefied natural gas carrier
US20040231359A1 (en) * 2003-05-22 2004-11-25 Brostow Adam Adrian Nitrogen rejection from condensed natural gas
US20050217281A1 (en) * 2004-02-03 2005-10-06 Linde Aktiengesellschaft Method for the reliquefaction of gas
US20070068177A1 (en) * 2005-09-29 2007-03-29 Paul Higginbotham Storage vessel for cryogenic liquid
EP1892457A1 (de) * 2006-08-24 2008-02-27 Eberhard Otten Verfahren und Vorrichtung zur Speicherung von Brenngas, insbesondere von Erdgas
US20090100863A1 (en) * 2007-10-19 2009-04-23 Air Products And Chemicals, Inc. System to Cold Compress an Air Stream Using Natural Gas Refrigeration
US20100089072A1 (en) * 2006-12-18 2010-04-15 Samsung Heavy Ind. Co., Ltd. Fuel supply apparatus of liquefied gas carrier and fuel supply method thereof
US20120000242A1 (en) * 2010-04-22 2012-01-05 Baudat Ned P Method and apparatus for storing liquefied natural gas
US20120011860A1 (en) * 2009-06-30 2012-01-19 Hamworthy Oil & Gas Systems As Method and system for storage and transport of liquefied petroleum gases
US20180245740A1 (en) * 2017-02-24 2018-08-30 Robert D. Kaminsky Method of Purging a Dual Purpose LNG/LIN Storage Tank
US20180259250A1 (en) * 2017-03-13 2018-09-13 General Electric Company Hydrocarbon Distillation
CN109297256A (zh) * 2018-11-03 2019-02-01 中科瑞奥能源科技股份有限公司 液氮气化制液化天然气的工艺与系统
US20190358582A1 (en) * 2018-05-23 2019-11-28 James Khreibani System and process for separating gas components using membrane filtration technology
CN114270112A (zh) * 2019-08-05 2022-04-01 乔治洛德方法研究和开发液化空气有限公司 冷却和/或液化方法及系统
US20220316794A1 (en) * 2019-08-13 2022-10-06 Linde Gmbh Method and unit for processing a gas mixture containing nitrogen and methane
US11608937B2 (en) 2020-01-30 2023-03-21 Caterpillar Inc. Separation and venting cryogenic liquid from vapor on a mobile machine

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ITBO20030061A1 (it) * 2003-02-12 2004-08-13 G I & E Srl Stazione per l'alimentazione, con gas in pressione, di
DE102007022950A1 (de) * 2007-05-16 2008-11-20 Weiss, Dieter Verfahren zum Transport von Wärmeenergie und Vorrichtungen zur Durchführung eines solchen Verfahrens
FR2924205B1 (fr) * 2007-11-23 2013-08-16 Air Liquide Dispositif et procede de refrigeration cryogenique
WO2016151636A1 (ja) * 2015-03-26 2016-09-29 千代田化工建設株式会社 天然ガスの製造システム及び製造方法

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Cited By (47)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4586942A (en) * 1983-02-08 1986-05-06 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and plant for the cooling of a fluid and in particular the liquefaction of natural gas
US4604115A (en) * 1984-03-23 1986-08-05 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and installation for treating a storage site
US4689064A (en) * 1985-10-21 1987-08-25 Societe Francaise De Stockage Geologigue Geostock-Tour Aurore Method of maintaining constant the composition of a product stored in a low temperature liquefied gas store
US4675037A (en) * 1986-02-18 1987-06-23 Air Products And Chemicals, Inc. Apparatus and method for recovering liquefied natural gas vapor boiloff by reliquefying during startup or turndown
US4846862A (en) * 1988-09-06 1989-07-11 Air Products And Chemicals, Inc. Reliquefaction of boil-off from liquefied natural gas
US5220798A (en) * 1990-09-18 1993-06-22 Teisan Kabushiki Kaisha Air separating method using external cold source
US5150576A (en) * 1990-11-16 1992-09-29 Liquid Carbonic Corporation Vapor collecting apparatus
US5141543A (en) * 1991-04-26 1992-08-25 Air Products And Chemicals, Inc. Use of liquefied natural gas (LNG) coupled with a cold expander to produce liquid nitrogen
US5139547A (en) * 1991-04-26 1992-08-18 Air Products And Chemicals, Inc. Production of liquid nitrogen using liquefied natural gas as sole refrigerant
WO1994013376A1 (en) 1992-12-07 1994-06-23 Edwards Engineering Corp. Vapor recovery apparatus and method
US5507146A (en) * 1994-10-12 1996-04-16 Consolidated Natural Gas Service Company, Inc. Method and apparatus for condensing fugitive methane vapors
EP0880000A3 (en) * 1997-05-19 1998-12-16 Praxair Technology, Inc. Turbine/motor (generator) driven booster compressor
US20040068993A1 (en) * 1999-11-05 2004-04-15 Toshikazu Irie Device and method for pressure control of cargo tank of liquefied natural gas carrier
US6901762B2 (en) * 1999-11-05 2005-06-07 Osaka Gas Co., Ltd. Device and method for pressure control of cargo tank of liquefied natural gas carrier
WO2001057430A1 (en) * 2000-02-03 2001-08-09 Cabot Lng Llc Vapor recovery system using turboexpander-driven compressor
AU777111B2 (en) * 2000-02-03 2004-09-30 Tractebel Lng North America Llc Vapor recovery system using turboexpander-driven compressor
US6460350B2 (en) * 2000-02-03 2002-10-08 Tractebel Lng North America Llc Vapor recovery system using turboexpander-driven compressor
US6672104B2 (en) 2002-03-28 2004-01-06 Exxonmobil Upstream Research Company Reliquefaction of boil-off from liquefied natural gas
US20040231359A1 (en) * 2003-05-22 2004-11-25 Brostow Adam Adrian Nitrogen rejection from condensed natural gas
WO2004104143A1 (en) * 2003-05-22 2004-12-02 Air Products And Chemicals, Inc. Nitrogen rejection from condensed natural gas
US6978638B2 (en) 2003-05-22 2005-12-27 Air Products And Chemicals, Inc. Nitrogen rejection from condensed natural gas
AU2004241309B2 (en) * 2003-05-22 2009-02-26 Air Products And Chemicals, Inc. Nitrogen rejection from condensed natural gas
EP2275520A1 (en) * 2003-05-22 2011-01-19 Air Products and Chemicals, Inc. Nitrogen rejection from condensed natural gas
US20050217281A1 (en) * 2004-02-03 2005-10-06 Linde Aktiengesellschaft Method for the reliquefaction of gas
US20070068177A1 (en) * 2005-09-29 2007-03-29 Paul Higginbotham Storage vessel for cryogenic liquid
US7581405B2 (en) * 2005-09-29 2009-09-01 Air Products And Chemicals, Inc. Storage vessel for cryogenic liquid
EP1892457A1 (de) * 2006-08-24 2008-02-27 Eberhard Otten Verfahren und Vorrichtung zur Speicherung von Brenngas, insbesondere von Erdgas
US20100089072A1 (en) * 2006-12-18 2010-04-15 Samsung Heavy Ind. Co., Ltd. Fuel supply apparatus of liquefied gas carrier and fuel supply method thereof
US10450045B2 (en) * 2006-12-18 2019-10-22 Samsung Heavy Ind. Co., Ltd. Fuel supply apparatus of liquefied gas carrier and fuel supply method thereof
US8601833B2 (en) * 2007-10-19 2013-12-10 Air Products And Chemicals, Inc. System to cold compress an air stream using natural gas refrigeration
US20090100863A1 (en) * 2007-10-19 2009-04-23 Air Products And Chemicals, Inc. System to Cold Compress an Air Stream Using Natural Gas Refrigeration
US20120011860A1 (en) * 2009-06-30 2012-01-19 Hamworthy Oil & Gas Systems As Method and system for storage and transport of liquefied petroleum gases
US20160281930A1 (en) * 2009-06-30 2016-09-29 Wartsila Oil & Gas Systems As Method and system for storage and transport of liquefied petroleum gases
US9810376B2 (en) * 2009-06-30 2017-11-07 Wartsila Oil & Gas Systems As Method and system for storage and transport of liquefied petroleum gases
US9982844B2 (en) * 2009-06-30 2018-05-29 Wärtsilä Oil & Gas Systems As Method and system for storage and transport of liquefied petroleum gases
US10006589B2 (en) * 2009-06-30 2018-06-26 Wärtsilä Oil & Gas Systems As Method and system for storage and transport of liquefied petroleum gases
US20160281929A1 (en) * 2009-06-30 2016-09-29 Wärtsilä Oil & Gas Systems As Method and system for storage and transport of liquefied petroleum gases
US20120000242A1 (en) * 2010-04-22 2012-01-05 Baudat Ned P Method and apparatus for storing liquefied natural gas
US20180245740A1 (en) * 2017-02-24 2018-08-30 Robert D. Kaminsky Method of Purging a Dual Purpose LNG/LIN Storage Tank
US10663115B2 (en) * 2017-02-24 2020-05-26 Exxonmobil Upstream Research Company Method of purging a dual purpose LNG/LIN storage tank
US20180259250A1 (en) * 2017-03-13 2018-09-13 General Electric Company Hydrocarbon Distillation
US10539364B2 (en) * 2017-03-13 2020-01-21 General Electric Company Hydrocarbon distillation
US20190358582A1 (en) * 2018-05-23 2019-11-28 James Khreibani System and process for separating gas components using membrane filtration technology
CN109297256A (zh) * 2018-11-03 2019-02-01 中科瑞奥能源科技股份有限公司 液氮气化制液化天然气的工艺与系统
CN114270112A (zh) * 2019-08-05 2022-04-01 乔治洛德方法研究和开发液化空气有限公司 冷却和/或液化方法及系统
US20220316794A1 (en) * 2019-08-13 2022-10-06 Linde Gmbh Method and unit for processing a gas mixture containing nitrogen and methane
US11608937B2 (en) 2020-01-30 2023-03-21 Caterpillar Inc. Separation and venting cryogenic liquid from vapor on a mobile machine

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Publication number Publication date
JPS4873404A (xx) 1973-10-03
NO132849B (xx) 1975-10-06
NL7217632A (xx) 1973-06-29
FR2165729B1 (xx) 1976-02-13
FR2165729A1 (xx) 1973-08-10
IT972507B (it) 1974-05-31
NO132849C (xx) 1976-01-14
ES410088A1 (es) 1975-12-01
GB1403999A (en) 1975-08-28
DE2263055A1 (de) 1973-07-05

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