CN105705893A - Method and device for separation at sub-ambient temperature - Google Patents

Method and device for separation at sub-ambient temperature Download PDF

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Publication number
CN105705893A
CN105705893A CN201480061010.4A CN201480061010A CN105705893A CN 105705893 A CN105705893 A CN 105705893A CN 201480061010 A CN201480061010 A CN 201480061010A CN 105705893 A CN105705893 A CN 105705893A
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China
Prior art keywords
tower
heat pump
heat
district
fluid
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Pending
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CN201480061010.4A
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Chinese (zh)
Inventor
G·卡登
阿纳克莱托 A·科雷亚
A·科雷亚阿纳克莱托
B·达维迪安
C·历克斯
B·索尼耶
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Priority claimed from FR1358668A external-priority patent/FR3010511B1/en
Priority claimed from FR1358667A external-priority patent/FR3010510B1/en
Priority claimed from FR1358666A external-priority patent/FR3010509A1/en
Application filed by LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Publication of CN105705893A publication Critical patent/CN105705893A/en
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—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 for air
    • F25J3/04406—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 for air using a dual pressure main column system
    • F25J3/04412—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 for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • 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
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B30/00—Heat pumps
    • F25B30/06—Heat pumps characterised by the source of low potential heat
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—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 for air
    • F25J3/04636—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 for air using a hybrid air separation unit, e.g. combined process by cryogenic separation and non-cryogenic separation techniques
    • 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
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B21/00—Machines, plants or systems, using electric or magnetic effects
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—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 for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—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 for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04278—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using external refrigeration units, e.g. closed mechanical or regenerative refrigeration units
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—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 for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—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 for air
    • F25J3/044—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 for air using a single pressure main column system only
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—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 for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/0466—Producing crude argon in a crude argon column as a parallel working rectification column or auxiliary column system 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
    • 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
    • F25J3/04—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 for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
    • F25J3/04884—Arrangement of reboiler-condensers
    • 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
    • F25J2200/40—Features relating to the provision of boil-up in the bottom of a column
    • 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
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/908—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by regenerative chillers, i.e. oscillating or dynamic systems, e.g. Stirling refrigerator, thermoelectric ("Peltier") or magnetic refrigeration
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
    • Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

The invention provides a method and device for separation at sub-ambient temperature. In a method for separation at sub-ambient temperature, a mixture of fluid (A, B) at a sub-ambient temperature is sent to a system of separation columns comprising at least one separation column (3, 5), a fluid enriched in a lighter component of the mixture exits from a head of the column of the system and a fluid enriched in a heavier component is withdrawn from the vessel of a column of the system, the cold source of a heat pump (MC, MC1, MC2, MC3) using the magnetocaloric effect is thermally linked to a first area (1) of a column of the system and the hot source of the same heat pump is thermally linked to a second area (2) of the same or of another column of the system.

Description

For the method and apparatus separated at temperatures below ambient
The present invention relates to the method and apparatus for separating, described separation by temperatures below ambient or even under low temperature (cryogenictemperature) separate carry out。Separation can be by distilling and/or pass through fractional condensation and/or passing through absorption and separation。Facility for this separation will be referred to as " tower "。Therefore, tower can be such as distillation column and absorption tower。Tapering to its simplest expression, it can be phase separator。Or, tower can also be the device that fractional condensation occurs。
Magnetic refrigeration depends on and uses the magnetic material demonstrating magnetothermal effect。Reversible, when standing to apply external magnetic field, this effect is showed by variations in temperature。These materials optimum range in the inner is positioned near its Curie temperature (Tc)。This is because the change in magnetization is more big, and thus changing more big on magnetic entropy, the change in temperature is more big。When being placed in magnetic field by material, the temperature of material rises, then it is assumed that magnetothermal effect is direct, the material cooling when being placed in magnetic field by material, then it is assumed that magnetothermal effect is indirectly。Remainder in description will provide for direct situation, but to those skilled in the art, how be reapplied indirectly situation and be apparent from。There are many thermodynamic cycles based on this principle。
Conventional magnetic refrigeration cycle include i) Magnetized Material to increase its temperature, ii) for stationary magnetic field cool down described material dispel the heat, iii) by described material degaussing to be cooled to and iv) in constant magnetic field (being generally zero magnetic field) heating material to absorb heat。
Magnetic refrigeration apparatus adopts the element be made up of magneto-caloric material, and when being magnetized, it produces heat and it absorbs heat when by degaussing。They can adopt magneto-caloric material regenerator to amplify the temperature difference between " thermal source " and " low-temperature receiver ": magnetic freezes thus being considered as that the magnetic utilizing active regeneration freezes。
Use magnetothermal effect to provide cooling to be known way by the method for separating air by cryogenic distillation to being used for。
US-A-6502404 describes and uses magnetothermal effect to provide cooling (needing the freezing balance in order to provide method) to the low temperature method of the gas for separating air, separation energy usually by forced air supply allows to operate the vaporizer-condenser (when nitrogen gas generator, it is possible to lower pressure column is reduced to a simple vaporizer) of double tower。
This invention address that from device problem being considered as the position of low-temperature receiver and transferring heat to that another of described device is considered as the position of thermal source, described device is at temperatures below ambient by distilling and/or pass through fractional condensation and/or passing through absorption and separation。
It has long been known that use same circuit, with not only for the reboiler offer heat of distillation column but also condenser offer kcal/h (frigories) for this same tower。US-A-2916888 discloses an example of the distillation of hydrocarbon。
Heat pump is thermodynamics device, its allow by a certain amount of heat from be considered as " emitter " and the medium (being taken out heat) being referred to as " low-temperature receiver " to be sent to be considered as " receptor " the medium being referred to as " thermal source " (to its supply heat), low-temperature receiver is in the temperature colder than thermal source。
For this kind of application, the regular circulation used in the prior art is that cryogenic fluid compresses-cools down the thermodynamic cycle of (condensation)-expansion-reheating (evaporation)。
Figure 12 that title is the file of " TECHNIQUESDEL ' INGENIEUR-R é frig é rationmagn é tique [Engineeringtechniques Magneticrefrigeration] 2005 " shows, compared with regular circulation, the coefficient of performance of the refrigeration system of magnetic cycle is used to improve 2 times。
Ambient temperature is the temperature of the surrounding air at described method, or alternatively, the temperature of the chilled(cooling) water return (CWR) for being connected with air themperature。
" lower than ambient temperature " refers to lower at least 10 DEG C than ambient temperature。
US-A-4987744 describes cryogenic distillation method, and wherein heat is sent to another site (it is under low temperature similarly) of this tower by heat pump from a site (it is in low temperature) of a tower。Heat pump includes two refrigerating circuits closed being thermally connected to each other, and each loop includes the compression step and the cooling step that use fluid (air, water) at ambient temperature。
One theme of the present invention is to provide a kind of method for separating at low temperatures at temperatures below ambient or even, wherein the mixture of fluid at temperatures below ambient or even at low temperatures is sent in the system of separation columns comprising at least one knockout tower, the top of a tower of system is left rich in the fluid of the lighter component of mixture, fluid rich in heavier component takes out from the bottom of system tower, the low-temperature receiver wherein using the heat pump of magnetothermal effect is thermally coupled to the firstth district of the tower of system directly or indirectly, and the thermal source of identical heat pump is thermally coupled to the identical tower of system or the secondth district of another tower directly or indirectly, the minimum temperature in the firstth district is lower than the maximum temperature in the secondth district。
According to the theme that other are optional:
The gas in the-the first district condenses at least in part and is likely to be sent back to the firstth district；
The liquid in the-the second district is evaporated at least in part and is likely to be sent back to the secondth district；
-at least be positioned to directly contact with the magneto-caloric material of the heat pump using magnetothermal effect by the fluid from the first or second district；
-between fluid and the heat-transfer fluid from the first or second district, carrying out heat exchange at least in part, described heat-transfer fluid contacts with the magneto-caloric material of the heat pump using magnetothermal effect already by exchanger；
-between fluid and the heat-transfer fluid from the first or second district, carrying out heat exchange at least in part, described heat-transfer fluid contacts with the magneto-caloric material of the heat pump using magnetothermal effect already by intermediate heat transfer loop；
-heat-transfer fluid is liquid；
-heat-transfer fluid not phase transformation in the process of method；
-in the process of method, heat-transfer fluid keeps under a constant；
-heat-transfer fluid is not compressed machine compression；
-heat pump does not transfer heat to outside segregation apparatus；
Heat is only sent to low-temperature receiver from thermal source by-heat pump；
-the thermal source that is connected to the secondth district is operated under the maximum temperature of heat pump；
-heat pump is operated completely at low temperatures；
-system of heat pump Yu tower is arranged in identical ice chest；
-mixture is air；
-use the heat pump of magnetothermal effect condense the gas rich in nitrogen in the firstth district and evaporate rich oxygen containing liquid in the second region；
-use several heat pump, it is supplied to the heat of the several heat pump heat from the firstth district and/or from several heat pumps and is sent to the secondth district；
The key component of-mixture is carbon monoxide and/or carbon dioxide and/or hydrogen and/or methane and/or nitrogen；
-in order to produce the liquid of the bottom at tower of the oxygen comprised more than 97 moles of %, separate the intermediate gas rich in argon by the tower from distillation column and from the liquid taken out in the bottom of tower, take out argon, to produce more rich in the stream of argon。
-make use of the several heat pumps using magnetothermal effect, one of them intermediate gas released for the more top being condensate in tower, another is for evaporating the intermediate liquid further below from tower；
-in order to produce containing liquid at the bottom of the tower less than 96.5 moles of % oxygen, wherein use the heat pump of magnetothermal effect for from the evaporation intermediate liquid further below of tower。
Another theme of the present invention is a kind of device for separating at low temperatures at temperatures below ambient or even, described device includes the system of separation columns comprising at least one knockout tower, and the mixture of fluid at temperatures below ambient or even at low temperatures is sent into described system of separation columns；For taking out the pipeline of the fluid of the lighter component rich in mixture from the top of system tower and for taking out the pipeline of the fluid rich in heavier component from the bottom of a tower of system；The low-temperature receiver wherein using the heat pump of magnetothermal effect is thermally coupled to the firstth district of the tower of system directly or indirectly, and the thermal source of identical heat pump is thermally coupled to the identical tower of system or the secondth district of another tower directly or indirectly, in one or more towers, the minimum temperature being arranged so that the firstth district in the first and secondth district is lower than the maximum temperature in the secondth district。
According to the aspect that other are optional, described device includes:
-for carrying the facility of the gas extremely condensation from the firstth district；
-for condensed gas being delivered to the facility in the firstth district；
-for carrying from the liquid in the secondth district to the facility that evaporates at least in part；
-for the liquid through evaporation being delivered to the facility in the secondth district；
-at least the fluid from the first or second district being positioned to the facility directly contacted with the magneto-caloric material of the heat pump using magnetothermal effect；
-between fluid and the heat-transfer fluid from the first or second district, carrying out heat exchange at least in part, described heat-transfer fluid contacts with the magneto-caloric material of the heat pump using magnetothermal effect already by exchanger；
-between fluid and the heat-transfer fluid from the first or second district, carrying out heat exchange at least in part, described heat-transfer fluid contacts with the magneto-caloric material of the heat pump using magnetothermal effect already by intermediate heat transfer loop；
-mixture is air；
-use the heat pump of magnetothermal effect can condense the gas rich in nitrogen in the firstth district and evaporate rich oxygen containing liquid in the second region；
-several heat pumps, for supplying heat to the facility of several heat pumps and/or for the facility from several heat pumps conveying heat to the secondth district from the firstth district；
-in order to produce liquid at the bottom of the tower comprising the oxygen more than 97 moles of %, for removing argon from the liquid taken out in the bottom of tower to produce more rich in the distillation column of the stream of argon by separating the intermediate gas rich in argon from tower；
Several heat pumps of-use magnetothermal effect, one of them intermediate gas released for the more top being condensate in tower, another is for evaporating the intermediate liquid further below from tower。
It is more fully described the present invention with reference to appended accompanying drawing。
In FIG, tower 3 separates the mixture at least contain component A, B being cooled to lower than ambient temperature or even low temperature, with the formation fluid (being likely gaseous state) rich in volatile component A with rich in the fluid (being likely liquid) of the less component B of volatility。It is it desired to heat from the second district 2 being transferred between the first and second solution-air contact portions in second and the 3rd the first district 1 between solution-air contact portion, this can be utilize the heat pump using magnetothermal effect MC to complete, the temperature in the first district 1 is significantly lower than the temperature in the second district 2, this means that the heat exchange between the two district by simple exchanger can not occur, or because temperature difference is for negative or too small because of temperature difference。First district 1 is thermally coupled to the low-temperature receiver of the heat pump MC using magnetothermal effect directly or indirectly, and the second district 2 is thermally connected to the thermal source of the identical heat pump MC using magnetothermal effect directly or indirectly。
In fig. 2, tower 3 separates the mixture at least contain component A, B being cooled to lower than ambient temperature or even low temperature, with the formation fluid (being likely gaseous state) rich in volatile component A with rich in the fluid (being likely liquid) of the less component B of volatility。Tower 5 separates the mixture at least contain C, D being cooled to lower than ambient temperature or even low temperature, with the formation fluid (being likely gaseous state) rich in volatile component C with rich in the fluid (being likely liquid) of the less component D of volatility。Being it desired to be transferred to heat from the first district 1 between the second and first solution-air contact portion of tower 3 second and the 3rd the second district 2 between solution-air contact portion at tower 5, this can be utilize the heat pump MC using magnetothermal effect to complete。First district 1 is thermally coupled to the low-temperature receiver of the heat pump MC using magnetothermal effect directly or indirectly, and the second district 2 is thermally connected to the thermal source of the identical heat pump MC using magnetothermal effect directly or indirectly。
In figure 3, compressor 7 compression stream A, the B stream of the air of the mixture of oxygen and nitrogen (be such as considered be mainly)。Compressed stream cools down in cooler 9 and is purified to remove impurity (if present) in purification unit 11。Purified stream is cooled to low temperature by heat exchanger 13, and is divided into two streams 23,25。Flow 23 by one and be transported to tower 3 in a gaseous form, in exchanger 27, remaining stream 25 is cooled down or liquefies at least in part。By this, stream that is cooled or that liquefy at least in part is transported to tower 3。Tower 3 has top condenser 15 and bottom reboiler 17。Condenser 15 is considered as the first district 1, and reboiler 17 is the second district 2, utilizes the heat pump MC1 using magnetothermal effect that from the first district 1, heat is sent to the second district 2。The cooling of stream 25 or at least partly liquefaction (electric energy that its heat pump MC1 partially compensating for being operated by using magnetothermal effect introduces or mechanical energy) can be passed through to use the heat pump MC4 of magnetothermal effect, use cooling fluid 51 (being typically surrounding air or cooling water) or any other refrigeration system (such as compression/expansion thermodynamic cycle) carry out directly or indirectly。
In figures 4 and 5, heat is sent to from the top of the medium pressure column of double air separation the bottom of its lower pressure column。In the diagram, compressor 7 compression stream A, the B air of the mixture of oxygen and nitrogen (be such as considered be mainly)。Compressed stream cools down in cooler 9 and is purified to remove impurity (if present) in purification unit 11。Purified stream is divided into two streams。The part 23 being cooled to low temperature in heat exchanger 13 is delivered to the bottom of medium pressure column 3。Remainder 123 is boosted in supercharger 41, partly cools down in heat exchanger 13, and then expand in entrance turbine 43, drive supercharger 41。Expanded air is delivered to lower pressure column 5, and described lower pressure column 5 is thermally connected to medium pressure column 3 directly or indirectly by using the heat pump MC of magnetothermal effect。Other facilities producing cooling except air inlet turbine can be considered。
Will be enriched in the liquid stream 61 of B (oxygen) and the liquid stream 63 rich in A (nitrogen) takes out and be delivered to lower pressure column 5 from medium pressure column 3。
In the diagram, tower 3 does not have top condenser in tower, and tower 5 does not have bottom reboiler in tower。Gaseous nitrogen 47 is taken out from tower 3 and is divided into two。One part 49 is heated in the exchanger 13。Remainder 51 is delivered to the heat pump MC using magnetothermal effect, is condensed (being likely to partly condensation) at this, condensed nitrogen is delivered to the top of tower 3。The liquid oxygen of the bottom from tower 5 is also delivered to the heat pump MC using magnetothermal effect, and it evaporated (being likely to partly evaporation) before being sent back to tower 5 at this。Therefore, the heat pump MC of magnetothermal effect is used to instead of both evaporator overhead condenser and bottom reboiler so that likely to reduce the total height of the system of tower 3,5 especially。Gaseous oxygen 53 is taken out from tower 5 in the way of product, heats in the exchanger 13, and compress in compressor 55。By liquid oxygen by the way of product liquid or make its mode that can be pumped take out from tower, and then contrary with boost air can evaporate in switched line 13, will be readily apparent to one having ordinary skill。
Nitrogen 57 is taken out from the top of lower pressure column 5, heated in subcooler 45 and exchanger 13 before being used at least partially for the regeneration of unit 11。
Fig. 5 illustrate more conventional can preferred form of this, wherein, tower 3 has top condenser 15, and tower 5 has bottom reboiler 17。Heat between the two passes through the heat pump MC of use magnetothermal effect, supply occurs to the heat transfer fluid (such as from the liquid of the heat pump MC using magnetothermal effect) of condenser, supply indirectly to the heat transfer fluid (such as from the liquid of the heat pump MC using magnetothermal effect) of vaporizer, and two of which heat-transfer fluid can be identical。
Compared with traditional Double-Tower Structure, use as at Fig. 3,4 and the heat pump adopting magnetothermal effect shown in 5 carry out distilling the energy making it possible to save about 20%, separate the required pressure flowing A, B in compressor 7 especially by reducing。
Fig. 6 is shown similar to the device described in Fig. 3, is different in that it includes producing tower 103 from the argon of tower 3 supply。Argon produces tower 103 and actually can produce the fluid rich in argon or can produce the fluid rich in argon alternatively in residual stream。Supplying from the liquid of tower 3 to the condenser of argon column 103, " distillation Equivalent Plate " near the import of liquid air, above the import 23 of air is upper to be taken out。Described liquid is evaporated (at least in part) so that argon column 103 to be freezed by the condenser of argon column 103, and then it is re-introduced in tower 3 below air supply 23。Under being re-introduced into of the described liquid evaporated, argon column 103 is connected to tower 3。In this case, the oxygen 29 taken out from the bottom of tower 3 can have the purity more than 97 moles of %。
Fig. 7 is shown similar to the device described in Fig. 6, wherein uses heat pump MC2, the MC3 of magnetothermal effect to replace argon and produces tower 103 and its evaporator overhead condenser。Some heats exchanged by condenser 15 at tower 3 are sent to the low-temperature receiver of the heat pump MC3 using magnetothermal effect directly or indirectly。The heat pump MC3 using magnetothermal effect has the liquid that (by the mode of thermal source) takes out between liquid air entrance and gaseous state air intake 23, and it is evaporated at least in part and is reintroduced into tower 3 in the lower section of gaseous air supply 23。The heat pump MC2 using magnetothermal effect has the gas taken out under the described level being re-introduced into as its low-temperature receiver, and the gas of described taking-up is condensed at least in part and is reintroduced in the described level being re-introduced into。Some heats exchanged at the vaporizer 17 of tower 3 are directly or indirectly from the thermal source of the heat pump MC2 using magnetothermal effect。The after-heat exchanged by condenser 15 at tower 3 is sent to the low-temperature receiver of the heat pump MC1 using magnetothermal effect directly or indirectly。The after-heat exchanged at the vaporizer 17 of tower 3 is directly or indirectly from the thermal source of the heat pump MC1 using magnetothermal effect。Heat pump MC1, MC2 and/or MC3 of using magnetothermal effect can completely or partially be combined into same device。
When discharging in residual stream rich in the fluid of argon wherein, the method in Fig. 7 has the energy characteristics identical with described in Fig. 6。Compared with Fig. 3, it allows the energy saving of about 7%。In this case, the oxygen 29 taken out in the bottom of tower 3 can have the purity more than 97 moles of %。
Fig. 8 describe be similar to Fig. 3's but include the device of intermediate reboiler。In this case, by two heat pump MC1, MC2 using magnetothermal effect, indirectly heat is sent to both two reboilers 17,71 from condenser 15。The a part of heat exchanged by condenser 15 at tower 3 is sent to the low-temperature receiver of the heat pump MC2 using magnetothermal effect directly or indirectly。Be positioned at below gaseous air entrance 23 intermediate reboiler 71 exchange heat directly or indirectly from use magnetothermal effect heat pump MC2 thermal source。The after-heat exchanged by condenser 15 at tower 3 is sent to the low-temperature receiver of the heat pump MC1 using magnetothermal effect directly or indirectly。The heat exchanged at the vaporizer 17 of tower 3 is directly or indirectly from the heat pump MC1 using magnetothermal effect。In this case, the oxygen 29 taken out from the bottom of tower 3 can have the purity less than 96.5 moles of %。Heat pump MC1 and the MC2 using magnetothermal effect can completely or partially be combined into same device。
Compared with the traditional Double-Tower Structure in lower pressure column with double evaporators, the heat pump using magnetothermal effect as shown in Figure 8 is used to carry out distilling and allow the energy of at most about 20% to save。

Claims (15)

1. the method for separating at low temperatures at temperatures below ambient or even, wherein by fluid (A at temperatures below ambient or even at low temperatures, B) mixture is sent into and is comprised at least one knockout tower (3, 5) in system of separation columns, the top of a tower of system is left rich in the fluid of the lighter component of mixture, fluid rich in heavier component takes out from the bottom of system tower, wherein use the heat pump (MC of magnetothermal effect, MC1, MC2, the thermal source in the firstth district (1) and identical heat pump that low-temperature receiver MC3) is thermally coupled to the tower of system directly or indirectly is thermally coupled to the identical tower of system or secondth district (2) of another tower directly or indirectly, the minimum temperature in the firstth district is lower than the maximum temperature in the secondth district。
2. method according to claim 1, wherein the gas in the firstth district condenses at least in part and is likely to be sent back to the firstth district (1)。
3. method according to claim 1 and 2, wherein the liquid in the secondth district is evaporated at least in part and is likely to be sent back to the secondth district (2)。
4. the method according to claim 1,2 or 3, at least a part of which will be positioned to directly contact with the magneto-caloric material of the heat pump (MC, MC1, MC2, MC3) using magnetothermal effect from the fluid in the first or second district (1,2)。
5. the method according to claim 1,2 or 3, at least a part of which is partly from the first or second district (1,2) heat exchange is carried out between fluid and heat-transfer fluid, described heat-transfer fluid is already by exchanger and the heat pump (MC using magnetothermal effect, MC1, MC2, MC3) magneto-caloric material contact。
6. the method according to claim 1,2 or 3, at least a part of which is partly from the first or second district (1,2) heat exchange is carried out between fluid and heat-transfer fluid, described heat-transfer fluid is already by intermediate heat transfer loop and the heat pump (MC using magnetothermal effect, MC1, MC2, MC3) magneto-caloric material contact。
7., according to method in any one of the preceding claims wherein, wherein mixture is air。
8. method according to claim 7, wherein uses the heat pump of magnetothermal effect condense the gas rich in nitrogen in the firstth district and evaporate rich oxygen containing liquid in the second region。
9. according to method in any one of the preceding claims wherein, wherein use several heat pump (MC, MC1, MC2, MC3), be supplied to the heat of the several heat pump heat from the firstth district and/or from several heat pumps and be sent to the secondth district。
10. according to method in any one of the preceding claims wherein, wherein, the key component of described mixture is carbon monoxide and/or carbon dioxide and/or hydrogen and/or methane and/or nitrogen。
11. according to the method according to any one of aforementioned claim 1 to 9, wherein, in order to produce the liquid of the bottom at tower of the oxygen comprised more than 97 moles of %, separate the intermediate gas rich in argon by the tower from distillation column and from the liquid taken out in the bottom of tower, take out argon, to produce more rich in the stream of argon。
12. according to method in any one of the preceding claims wherein, wherein make use of several heat pump (MC, the MC1 that use magnetothermal effect, MC2, MC3), one of them intermediate gas released for the more top being condensate in tower, another is used for the evaporation intermediate liquid further below from tower。
13. according to aforementioned claim 1 to 9, method according to any one of 11 or 12, in order to produce containing liquid at the bottom of the tower less than 96.5 moles of % oxygen, wherein use heat pump (MC, the MC1 of magnetothermal effect, MC2, MC3) it is used for the evaporation intermediate liquid further below from tower。
14. according to method in any one of the preceding claims wherein, wherein, thermal source operates under the maximum temperature of heat pump。
15. the device for separating at low temperatures at temperatures below ambient or even, described device includes comprising at least one knockout tower (3,5) system of separation columns, the mixture of fluid (A, B) at temperatures below ambient or even at low temperatures is sent into described system of separation columns；For taking out the pipeline of the fluid of the lighter component rich in mixture from the top of system tower and for taking out the pipeline of the fluid rich in heavier component from the bottom of a tower of system；Wherein use the heat pump (MC of magnetothermal effect, MC1, MC2, the thermal source in the firstth district (1) and identical heat pump that low-temperature receiver MC3) is thermally coupled to the tower of system directly or indirectly is thermally coupled to the identical tower of system or secondth district (2) of another tower directly or indirectly, and in one or more towers, the minimum temperature being arranged so that the firstth district in the first and secondth district is lower than the maximum temperature in the secondth district。
CN201480061010.4A 2013-09-10 2014-09-10 Method and device for separation at sub-ambient temperature Pending CN105705893A (en)

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FR1358668A FR3010511B1 (en) 2013-09-10 2013-09-10 METHOD AND APPARATUS FOR SEPARATING A GAS MIXTURE WITH SUBAMBIAN TEMPERATURE
FR1358667A FR3010510B1 (en) 2013-09-10 2013-09-10 METHOD AND APPARATUS FOR SUBAMBIAN TEMPERATURE SEPARATION
FR1358667 2013-09-10
FR1358666A FR3010509A1 (en) 2013-09-10 2013-09-10 METHOD AND APPARATUS FOR SUBAMBIAN TEMPERATURE SEPARATION
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Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4987744A (en) * 1990-01-26 1991-01-29 Union Carbide Industrial Gases Technology Corporation Cryogenic distillation with unbalanced heat pump
US6336331B1 (en) * 2000-08-01 2002-01-08 Praxair Technology, Inc. System for operating cryogenic liquid tankage
US6502404B1 (en) * 2001-07-31 2003-01-07 Praxair Technology, Inc. Cryogenic rectification system using magnetic refrigeration
CN1501044A (en) * 2002-11-01 2004-06-02 液体空气乔治洛德方法利用和研究的具 Combined air separation natural gas liquefaction plant
US20080016907A1 (en) * 2006-07-18 2008-01-24 John Arthur Barclay Active gas regenerative liquefier system and method

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2627731A (en) * 1949-06-18 1953-02-10 Hydrocarbon Research Inc Rectification of gaseous mixtures
US4345925A (en) * 1980-11-26 1982-08-24 Union Carbide Corporation Process for the production of high pressure oxygen gas
DE19529681C2 (en) * 1995-08-11 1997-05-28 Linde Ag Method and device for air separation by low-temperature rectification
US6082135A (en) * 1999-01-29 2000-07-04 The Boc Group, Inc. Air separation method and apparatus to produce an oxygen product
CH695836A5 (en) * 2002-12-24 2006-09-15 Ecole D Ingenieurs Du Canton D Method and device for continuously generating cold and heat by magnetic effect.
DE102005029274A1 (en) * 2004-08-17 2006-02-23 Linde Ag Obtaining gaseous pressure product, by cryogenic separation of air implementing normal operation, emergency operation, and bypass operation
FR2946417A1 (en) * 2009-06-03 2010-12-10 Air Liquide METHOD AND APPARATUS FOR PRODUCING AT LEAST ONE ARGON-ENRICHED FLUID AND / OR AT LEAST ONE OXYGEN-ENRICHED FLUID FROM A RESIDUAL FLUID

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4987744A (en) * 1990-01-26 1991-01-29 Union Carbide Industrial Gases Technology Corporation Cryogenic distillation with unbalanced heat pump
US6336331B1 (en) * 2000-08-01 2002-01-08 Praxair Technology, Inc. System for operating cryogenic liquid tankage
US6502404B1 (en) * 2001-07-31 2003-01-07 Praxair Technology, Inc. Cryogenic rectification system using magnetic refrigeration
CN1501044A (en) * 2002-11-01 2004-06-02 液体空气乔治洛德方法利用和研究的具 Combined air separation natural gas liquefaction plant
US20080016907A1 (en) * 2006-07-18 2008-01-24 John Arthur Barclay Active gas regenerative liquefier system and method

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
RAKESH AGRAWAL: "Heat pumps for thermally linked distillation columns:an exercise or argon production from air"", 《INDUSTRY &ENGINEERING CHEMISTRY RESEARCH》 *

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