US20160223254A1 - Method and apparatus for separation of a gaseous mixture at sub-ambient temperature - Google Patents

Method and apparatus for separation of a gaseous mixture at sub-ambient temperature Download PDF

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Publication number
US20160223254A1
US20160223254A1 US15/021,037 US201415021037A US2016223254A1 US 20160223254 A1 US20160223254 A1 US 20160223254A1 US 201415021037 A US201415021037 A US 201415021037A US 2016223254 A1 US2016223254 A1 US 2016223254A1
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Prior art keywords
heat
liquid
pressure
gaseous mixture
separation
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US15/021,037
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English (en)
Inventor
Antony CORREIA ANACLETO
Benoit Davidian
Bernard SAULNER
Jean-Pierre Tranier
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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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Publication of US20160223254A1 publication Critical patent/US20160223254A1/en
Assigned to L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude reassignment L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: TRANIER, JEAN-PIERRE, SAULNIER, BERNARD, CORREIA ANACLETO, Antony, DAVIDIAN, BENOIT
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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
    • 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
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B2321/00—Details of machines, plants or systems, using electric or magnetic effects
    • F25B2321/002—Details of machines, plants or systems, using electric or magnetic effects by using magneto-caloric 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
    • 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

Definitions

  • the present invention relates to a method and to a device for separating a gaseous mixture, for example air, at sub-ambient, or even cryogenic, temperature.
  • pseudo-vaporization replaces vaporization.
  • the term “vaporization” also covers pseudo-vaporization.
  • the term “condensation” also covers pseudo-condensation.
  • Separation may take place in at least one distillation column and/or at least one absorption column and/or at least one separating pot and/or at least one membrane and/or by dephlegmation.
  • Magnetic refrigeration relies on the use of magnetic materials that exhibit a magnetocaloric effect. Reversibly, this effect is manifested by a variation in their temperature when they are subjected to the application of an external magnetic field.
  • the optimum ranges within which these materials are used lie in the vicinity of their Curie temperature (Tc). This is because the greater the variation in magnetization and, therefore, the changes in magnetic entropy, the greater the changes in temperature.
  • the magnetocaloric effect is said to be direct when the temperature of the material increases when placed in a magnetic field, and indirect when it cools when placed in a magnetic field. The remainder of the description will be given for the direct case, but it is obvious to a person skilled in the art how to reapply this to the indirect case.
  • thermodynamic cycles There are many thermodynamic cycles based on this principle.
  • a conventional magnetic refrigeration cycle consists i) in magnetizing the material in order to increase its temperature, ii) in cooling the material in a constant magnetic field in order to dissipate heat, iii) in demagnetizing the material in order to cool it, and iv) in heating the material in a constant (generally zero) magnetic field in order to absorb heat.
  • a magnetic refrigeration device employs elements made of magnetocaloric material, which generate heat when magnetized and absorb heat when demagnetized. They may employ a magnetocaloric material regenerator in order to amplify the temperature difference between the “hot source” and the “cold source”: the magnetic refrigeration is then said to be magnetic refrigeration employing active magnetic regeneration. This effect is described in the Lebouc 2005 Techniques de l'In deciur [Engineering techniques] article entitled “Réfrigération magn electronically [Magnetic refrigeration]”.
  • the present invention tackles the problem of how to vaporize a liquid derived from the separation while reducing the pressure ratio between the gas that is to be condensed and the liquid that is to be vaporized that is normally required for an exchange of heat through an exchanger.
  • At least part of the heat required for vaporizing a liquid from a separation comes from a heat pump using the magnetocaloric effect.
  • One subject of the invention is a method for separating a gaseous mixture by separation at sub-ambient, or even cryogenic, temperature, in which a gaseous mixture at a first pressure is cooled, then separated in a separation unit, for example a system of columns comprising at least one column.
  • a liquid is withdrawn from the separation unit and vaporized to form a pressurized gaseous product, possibly following pressurization to a higher pressure or following depressurization to a pressure lower than the pressure at which it is withdrawn, characterized in that at least part of the heat of vaporization of the liquid is supplied by a heat pump using the magnetocaloric effect of which the hot source exchanges heat, indirectly or directly, with the liquid which vaporizes.
  • Another subject of the invention is a device for separating a gaseous mixture by separation at sub-ambient, or even cryogenic, temperature, comprising cooling means for cooling a gaseous mixture at a first pressure, a separation unit, for example a system of columns comprising at least one column, which is connected to the cooling means, and a pipe for withdrawing a liquid from the separation unit, means for vaporizing the liquid to form a pressurized gaseous product, possibly downstream of means of pressurizing to a pressure that is higher or of depressurizing to a pressure that is lower than the pressure at which it is withdrawn, characterized in that it comprises using a heat pump using the magnetocaloric effect capable of supplying at least part of the heat of vaporization of the liquid and means allowing the hot source of the heat pump to exchange heat, directly or indirectly, with the liquid which vaporizes.
  • the device may comprise
  • a heat pump is a thermodynamic device that allows a quantity of heat to be transferred from a medium considered to be the “emitter” and referred to as the “cold source” from which heat is extracted, to a medium considered to be the “receiver” and referred to as the “hot source” to which the heat is supplied, the cold source being at a colder temperature than the hot source.
  • thermodynamic cycle of compressing—cooling (condensing)—expanding—reheating (vaporizing) a refrigerating fluid.
  • FIG. 12 of the document entitled “TECHNIQUES DE L'INGENIEUR—Réfrigération magnically” [Engineering techniques—Magnetic refrigeration] 2005” shows a twofold improvement in the coefficient of performance of a refrigeration system using a magnetic cycle as compared with the conventional cycle.
  • An ambient temperature is the temperature of the ambient air in which the method is situated or, alternatively, a temperature of a cooling water circuit connected with the air temperature.
  • a sub-ambient temperature is at least 10° C. below the ambient temperature.
  • a cryogenic temperature is below ⁇ 50° C.
  • FIG. 1 represents a process flow diagram in accordance with an embodiment of the present invention.
  • FIG. 2 represents a process flow diagram in accordance with an embodiment of the present invention.
  • FIG. 3 represents a process flow diagram in accordance with an embodiment of the present invention.
  • FIG. 4 represents a process flow diagram in accordance with an embodiment of the present invention.
  • FIG. 5 represents a process flow diagram in accordance with an embodiment of the present invention.
  • FIG. 6 represents a process flow diagram in accordance with an embodiment of the present invention.
  • FIG. 7 represents a generic figure illustrating the at least partial vaporization of liquid in accordance with an embodiment of the present invention.
  • FIG. 8 represents a process flow diagram in accordance with an embodiment of the present invention.
  • FIG. 1 shows a device for separating air by cryogenic distillation.
  • the device comprises a heat exchange line 17 and a double air separation column comprising a medium-pressure column 23 and a low-pressure column 25 which are thermally connected by means of a vaporizer-condenser 27 .
  • Air 1 is compressed in a compressor 3 to a pressure of 5.5 bara.
  • the compressed air is cooled in the cooler 5 to form a cooled flow 7 which is purified to remove the water and carbon dioxide and other impurities in an adsorption unit 9 .
  • the purified air is split into two.
  • One part 8 is cooled as it passes completely through the exchange line 17 down to a temperature of around ⁇ 170° C. It is then split into two.
  • One part 19 acts as a cold source for the heat pump 31 using the magnetocaloric effect.
  • the rest 21 is sent to separate in gaseous form in the bottom of the medium-pressure column 23 .
  • the part 19 cools and liquefies through exchange of heat in the heat pump 31 to form the flow 37 .
  • the flow 37 is split into a part 39 which is sent to the medium-pressure column 23 and a part 41 which is cooled in the subcooler 43 , expanded then sent to the low-pressure column 25 .
  • An oxygen-enriched liquid 33 is withdrawn from the bottom of the medium-pressure column 23 , cooled in the subcooler 43 and sent to the low-pressure column 25 .
  • a nitrogen-enriched liquid 35 is withdrawn from the top of the medium-pressure column 23 , cooled in the subcooler 43 and sent to the top of the low-pressure column 25 .
  • Air 11 is pressure-boosted in a pressure booster 13 , cooled partially in the exchange line 17 , expanded in the inlet turbine 15 and sent to the low-pressure column 25 .
  • a nitrogen-rich gas 45 is withdrawn from the top of the low-pressure column 25 , heated in the subcooler 43 and in the exchange line 17 to serve at least in part as gas for regenerating the adsorption unit 9 .
  • Nitrogen-rich gas 49 is withdrawn from the top of the medium-pressure column 23 , heated in the exchange line 17 and serves as product.
  • Liquid oxygen 47 is withdrawn from the low-pressure column 25 , pressurized by a pump 29 and partially heated in the exchange line 17 .
  • the heated liquid is discharged from the exchange line 17 , vaporized at least partially in the heat pump using the magnetocaloric effect 31 where it acts as a hot source and sent back to the exchange line 17 , either to complete vaporization and warm up or only to warm up.
  • the oxygen thus obtained serves as product.
  • FIG. 2 unlike in FIG. 1 , all of the air 8 is cooled in the exchange line 17 to form the flow 19 which condenses partially in the heat pump using the magnetocaloric effect 31 to form the flow 37 . All of the flow 37 is sent to the bottom of the medium-pressure column 23 .
  • the purified air is split into three parts.
  • One part 11 is sent to the pressure booster 13 as in FIGS. 1 and 2 .
  • Another part 8 is cooled as it passes completely through the exchange line 17 and is then sent to the bottom of the column 23 .
  • the rest of the air 12 has its pressure boosted in a pressure booster 14 and is sent to the exchange line 17 where it cools to an intermediate level.
  • the partially cooled air 12 is condensed at least partly in the heat pump using the magnetocaloric effect 31 where it acts as a cold source.
  • the at least partially condensed air is reintroduced into the exchange line 17 where it cools further.
  • the air cooled further in the exchange line leaves the cold end thereof and is split into two parts.
  • the first part 16 is expanded and sent to the bottom of the medium-pressure column 23 .
  • the second part 18 is cooled in the subcooler 43 , expanded and sent to the low-pressure column.
  • liquid oxygen 51 is also withdrawn from the low-pressure column 25 , cooled in the subcooler 43 and serves as liquid product.
  • the proportion of oxygen produced in liquid form may represent up to half of the gaseous oxygen produced under pressure.
  • the liquid 47 vaporizes through exchange of heat with nitrogen 53 from the low-pressure column 23 with the aid of the heat pump using the magnetocaloric effect 31 .
  • the gaseous nitrogen 53 which acts as a cold source liquefies and is sent to the top of the column 23 to provide reflux. In that case, all the purified air is either sent to the pressure booster 13 , cooled and expanded, or cooled and sent for distillation.
  • FIG. 6 can be likened to FIG. 3 .
  • the fluid 12 , or, respectively, 47 which is indirectly thermally connected with the cold source or, respectively, the hot source, of the heat pump using the magnetocaloric effect 31 does not leave the exchange line 17 .
  • a heat-transfer fluid A transfers heat from the air 12 coming from the pressure booster 14 (at an intermediate level of the exchange line 17 near the point at which the air 12 at least partially condenses), is cooled in the heat pump using the magnetocaloric effect 31 at the level of the cold source and is returned to the exchange line 17 , in closed circuit.
  • a heat-transfer fluid B transfers heat to the oxygen 47 (at an intermediate level in the exchange line 17 near the point at which the oxygen 47 at least partially vaporizes), heats up in the heat pump using the magnetocaloric effect 31 at the level of the hot source and is returned to the exchange line 17 , in closed circuit.
  • the heat-transfer fluids A and B may be the same or different.
  • the invention could also be applied to methods for separating other mixtures.
  • the air could be replaced by a mixture containing methane and/or nitrogen and/or carbon dioxide and/or carbon monoxide and/or hydrogen as its main components.
  • FIG. 7 is a generic figure illustrating the at least partial vaporization of liquid 47 according to the invention.
  • the liquid 47 may come from a separation unit, for example a distillation or absorption column, from a phase separator, a dephlegmator or a membrane. It may be vaporized in the exchanger 17 following a pressurizing (for example in a pump or using hydrostatic head) or depressurizing (for example in a valve or a turbine). It may for example contain at least 70% oxygen, at least 80% nitrogen, at least 60% carbon dioxide or at least 60% methane or at least 60% carbon monoxide.
  • the fluid 12 which supplies the heat directly or indirectly to the cold source may be the fluid that is to be separated in the separation unit, a fluid separated in the separation unit or some other fluid. This fluid 12 at least partially condenses.
  • the exchanger 17 may also be used to heat and/or cool at least one other fluid 8 , 45 .
  • the heat pump using the magnetocaloric effect 31 allows the exchange of heat between the fluid 12 (for example air) which acts as a cold source and the liquid 47 (for example a liquid containing at least 70% oxygen), which acts as a hot source.
  • the fluid 12 for example air
  • the liquid 47 for example a liquid containing at least 70% oxygen
  • FIG. 7 may be modified to use at least one heat-transfer fluid in closed circuit which transfers heat to and/or from the heat pump using the magnetocaloric effect 31 .
  • FIG. 8 shows a device for the cryogenic separation of a mixture of methane and nitrogen (typically 85% methane).
  • the device comprises a heat exchange line 17 and a double separation column comprising a medium-pressure column 23 and a low-pressure column 25 which are thermally connected by means of a vaporizer-condenser 27 .
  • the high-pressure mixture of methane and nitrogen 8 is cooled and condenses partially in the exchange line 17 . It is then expanded to a medium-pressure distillation column 23 . This expansion contributes to keeping the device cold.
  • a methane-enriched liquid 33 is withdrawn from the bottom of the medium-pressure column 23 , cooled in the subcooler 43 and sent to the low-pressure column 25 .
  • a nitrogen-enriched liquid 35 is withdrawn from the top of the medium-pressure column 23 , cooled in the subcooler 43 A and sent to the top of the low-pressure column 25 .
  • a nitrogen-rich gas 45 is withdrawn from the top of the low-pressure column 25 and heated in the subcoolers 43 A, 43 and in the exchange line 17 .
  • Liquid methane 47 is withdrawn from the low-pressure column 25 , pressurized by a pump 29 then heated and then vaporized in the exchange line 17 , then the vaporized liquid methane continues to heat up in the exchange line 17 .
  • the gaseous methane may be used directly as a product without additional compression in a compressor.
  • a heat-transfer fluid A transfers heat from the mixture 12 (at an intermediate level of the exchange line 17 in the vicinity of the point at which the mixture 12 is at least partially condensed), cools in the heat pump using the magnetocaloric effect 31 at the level of the cold source and is returned to the exchange line 17 , in closed circuit.
  • a heat-transfer fluid B transfers heat to the methane 47 (at an intermediate level in the exchange line 17 near the point at which the methane 47 is at least partially vaporized), heats up in the heat pump using the magnetocaloric effect 31 at the level of the hot source and is returned to the exchange line 17 , in closed circuit.
  • the liquid that is to be vaporized is not necessarily heated up in the exchange line 17 beforehand before effecting an exchange of heat with the heat pump using the magnetocaloric effect.
  • “Comprising” in a claim is an open transitional term which means the subsequently identified claim elements are a nonexclusive listing (i.e., anything else may be additionally included and remain within the scope of “comprising”). “Comprising” as used herein may be replaced by the more limited transitional terms “consisting essentially of” and “consisting of” unless otherwise indicated herein.
  • Providing in a claim is defined to mean furnishing, supplying, making available, or preparing something. The step may be performed by any actor in the absence of express language in the claim to the contrary.
  • Optional or optionally means that the subsequently described event or circumstances may or may not occur.
  • the description includes instances where the event or circumstance occurs and instances where it does not occur.
  • Ranges may be expressed herein as from about one particular value, and/or to about another particular value. When such a range is expressed, it is to be understood that another embodiment is from the one particular value and/or to the other particular value, along with all combinations within said range.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)
US15/021,037 2013-09-10 2014-08-20 Method and apparatus for separation of a gaseous mixture at sub-ambient temperature Abandoned US20160223254A1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
FR1358668A FR3010511B1 (fr) 2013-09-10 2013-09-10 Procede et appareil de separation d'un melange gazeux a temperature subambiante
FR1358668 2013-09-10
PCT/FR2014/052103 WO2015036673A2 (fr) 2013-09-10 2014-08-20 Procédé et appareil de séparation d'un mélange gazeux à température subambiante

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US20160223254A1 true US20160223254A1 (en) 2016-08-04

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US (1) US20160223254A1 (fr)
EP (1) EP3044529A2 (fr)
CN (1) CN105705892A (fr)
FR (1) FR3010511B1 (fr)
WO (1) WO2015036673A2 (fr)

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US11709018B2 (en) * 2017-12-25 2023-07-25 L'air Liquide, Societe Anonyme Pour L'etude Et L'expoitation Des Procedes Georges Claude Single packaged air separation apparatus with reverse main heat exchanger

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FR3033257A1 (fr) 2015-03-05 2016-09-09 Air Liquide Procede et appareil de separation d’un melange gazeux a temperature subambiante
FR3033395A1 (fr) 2015-03-05 2016-09-09 Air Liquide Procede et appareil de compression d’un gaz

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WO2015036673A3 (fr) 2015-08-06
FR3010511A1 (fr) 2015-03-13
EP3044529A2 (fr) 2016-07-20
FR3010511B1 (fr) 2017-08-11
WO2015036673A2 (fr) 2015-03-19

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