EP1052465B1 - Procédé et appareil pour la séparation cryogénique de l'air - Google Patents

Procédé et appareil pour la séparation cryogénique de l'air Download PDF

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Publication number
EP1052465B1
EP1052465B1 EP99112289A EP99112289A EP1052465B1 EP 1052465 B1 EP1052465 B1 EP 1052465B1 EP 99112289 A EP99112289 A EP 99112289A EP 99112289 A EP99112289 A EP 99112289A EP 1052465 B1 EP1052465 B1 EP 1052465B1
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European Patent Office
Prior art keywords
liquid
transfer fraction
level
expansion
transfer
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Expired - Lifetime
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EP99112289A
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German (de)
English (en)
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EP1052465A1 (fr
Inventor
Thomas Dipl.-Ing. Nohlen
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Linde GmbH
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Linde GmbH
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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
    • 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.
    • 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
    • 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
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
    • 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
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • F25J3/04703—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser being arranged in more than one vessel
    • 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
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04793—Rectification, e.g. columns; Reboiler-condenser
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/06—Lifting of liquids by gas lift, e.g. "Mammutpumpe"
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/58—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being argon or crude argon

Definitions

  • the invention relates to a method for the cryogenic separation of air according to the The preamble of claim 1.
  • the invention particularly relates to two-pillar systems with a Pressure column and with a arranged above the pressure column low pressure column and / or multi-column systems with further separation columns for nitrogen-oxygen separation.
  • the pressure column in this case represents the "first rectification column” in the sense of Invention; the rectification in the low pressure column and / or the evaporation in the Top condenser of the crude argon column is the "further process step".
  • the "Transfer fraction” is here by the bottoms liquid or a Intermediate liquid of the pressure column formed in the low pressure column or in the Evaporation space of the top condenser of the crude argon column is initiated.
  • the invention relates in particular to double-column methods, as shown in FIGS. 4.23, 4.26, 4.28 and 4.34 are presented in Chapter 4.5 of Hausen / Linde. Notwithstanding the examples in Hausen / Linde is in the invention of Mass transfer preferably in at least one separation column (e.g. Low pressure and / or crude argon column) at least partially by packing or ordered Pack causes.
  • at least one separation column e.g. Low pressure and / or crude argon column
  • the transfer fraction collects within the first rectification column in one Reservoir that through the bottom of this column or a cup located in the column is formed.
  • the liquid level in this reservoir sets the "first level” h1 within the meaning of the invention.
  • the transfer fraction in directed a container in which a further process step is carried out, for example, the low-pressure column or the evaporation chamber of a condenser-evaporator (e.g., top condenser of the crude argon column).
  • a further process step for example, the low-pressure column or the evaporation chamber of a condenser-evaporator (e.g., top condenser of the crude argon column).
  • the place of supply to This further process step defines the "second, higher level" in the sense of Invention.
  • Air separation plants in which packages in the low-pressure part of a double column are used, for example, in EP 321163 A, WO 9319335, WO 9319336 or EP 628777A.
  • a disadvantage of the use of packages is that the height noticeably increased in comparison with tray columns.
  • the inequality stated that is, the pressure difference between pressure and pressure Low pressure column or between pressure column and evaporation chamber of the Top condenser of the crude argon column is no longer sufficient to the corresponding hydrostatic pressure of a liquid column of the transfer fraction to overcome. While this situation in some systems in normal operation under full load often appears particularly in special operating cases, especially when operating under load, so with a lower product and Amount used as at full load.
  • the invention is based on the object, the aforementioned method and the appropriate device to be further improved.
  • the expansion valve is at a suitable intermediate level between the first and the second level.
  • the concrete determination of this intermediate level is different for each specific embodiment of the invention, but can be easily determined by means of the calculation tools available to the person skilled in the art, if one specifies the height of the intermediate level as a degree of freedom.
  • the transfer fraction is subcooled before relaxing by indirect heat exchange. This will the formation of a two-phase mixture upstream of the relaxation all or partially avoided, so that only when relaxing the inventive targeted Steam bubble formation takes place.
  • the subcooling usually takes place near the first levels.
  • the degree of supercooling of the transfer fraction becomes usually determined independently of the liquid transport process and is of other criteria, such as the desire to have relatively little flash gas when feeding into the second container to produce.
  • the relaxation process in particular, the arrangement of the expansion valve, is then so determines that at the given supercooling the transfer fraction immediately before relaxing just in the single-phase liquid state and neither a significant hypothermia still steam bubbles in appreciable extent available.
  • the invention also relates to a device for the cryogenic separation of air according to claims 3 and 4.
  • purified air 1 is under a Pressure of 4 to 20 bar, preferably 5 to 12 bar in a heat exchanger 2 against Product streams cooled to about dew point and in the pressure column 3 a two-stage Rectifier fed.
  • the pressure column 3 is connected via a common Condenser-evaporator 4 in heat exchange relationship with a low pressure column 5th
  • Bottom liquid 6 and nitrogen 7 are withdrawn from the pressure column 3, in one Countercurrent 8 undercooled and at least partially in the low pressure column. 5 throttled. From the low pressure column are oxygen 9, nitrogen 10 and impure nitrogen 11 removed in gaseous form. The products can also be at least are partially removed liquid (oxygen 9a, nitrogen 10a).
  • the inventive method of transferring a liquid may as well the liquid nitrogen 7 from the head of the pressure column as (further) "transfer fraction" be applied.
  • the "first level” is thereby by the liquid level formed within the cup 16, in which coming from main capacitor 4 Liquid is collected. Undercooling is again in the counterstroller 8.
  • the supercooled nitrogen 17 flows to a relief valve 18, which on a Intermediate level hz 'is arranged and finally on to the feed point 19 ("second level" h2 ') at the top of the low pressure column.
  • the Invention also to the transport of a liquid transfer fraction in the Evaporation space of the top condenser of a crude argon column can be applied.
  • the crude argon column is formed in the example by two sections 20a, 20b, their function in European patent EP 628777 B1 and in the corresponding US Patent US 5426946 is described in detail.
  • the invention can be applied to anyone known type of Rohargon notung be used, in which an argon-containing Oxygen fraction 21 introduced from the low pressure column 5 in a crude argon column is, wherein in the upper part of the crude argon column depleted of oxygen Argon product 22a, 22b obtained in gaseous and / or liquid state.
  • the further transfer fraction is in the example shown in the drawing through a part 13a of the supercooled bottoms liquid 6 from the pressure column 5 educated. She is relaxed in a relaxation valve 14a, which on a Intermediate level is arranged. This intermediate level is in the example the same or about the same height as the intermediate level hz.
  • the in 14a relaxed transfer fraction 15a of sump 12 of the pressure column 3 is on a "second level" h2 "in the evaporation space 23 of the top condenser Introduced crude argon column.

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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)

Claims (4)

  1. Procédé pour la séparation cryogénique de l'air, dans lequel l'air de charge (1) est introduit dans une première colonne de rectification (3) et une fraction de transfert (6, 7) de densité ρ à l'état fluide est prélevée d'un réservoir (24, 26) à l'intérieur de la première colonne de rectification (3), est surrefroidie par échange thermique indirect (8), détendue (14, 14a, 18) et est acheminée à une autre étape de procédé (5, 23),
    le niveau de liquide dans le réservoir (24, 16) se trouvant à un premier niveau h1 et à une première pression p1,
    la fraction de transfert détendue étant acheminée à l'autre étape de procédé (5, 23) à un deuxième niveau plus élevé h2 (h2 > h1) et à une deuxième pression inférieure (p2 < p1),
    la différence entre les deux pressions Δp = p1 - p2 étant inférieure à la pression hydrostatique produite par une colonne de liquide de la fraction de transfert entre le premier et le deuxième niveau (phydr = ρ. g. [h2-h1]) :
    Δp = p1 - p2 < ρ. g. [h2 - h1] (g = accélération due à la pesanteur)    caractérisé en ce que la détente (14, 14a, 18) est effectuée de telle sorte que les bulles de gaz formées lors de la détente diminuent la densité de la fraction de transfert dans une mesure telle que la différence de pression Δp suffise pour acheminer la fraction de transfert à l'autre étape de procédé (5, 23), ni la fraction de transfert en aval de la détente (14, 14a, 18) ne recevant un courant gazeux ou liquide, ni la fraction de transfert entre le sous-refroidissement (8) et la détente (14, 14a, 18) ne recevant un écoulement liquide.
  2. Procédé selon la revendication 1, caractérisé en ce que le sous-refroidissement (8) est effectué de telle sorte que la fraction de transfert (13, 13a, 17) se présente sous forme complètement ou substantiellement complètement liquide directement en amont de la détente (14, 14a, 18).
  3. Dispositif pour la mise en oeuvre du procédé selon la revendication 1, qui est conçu pour au moins un cas de fonctionnement et qui présente une première colonne de rectification (3) avec un réservoir (24, 16) pour une fraction de transfert liquide et une conduite de liquide (6 - 13 - 15, 6 - 13a - 15a, 7 - 17 - 19), laquelle est connectée au réservoir (24, 16) dans la première colonne de rectification (3) et à un autre récipient (5, 23), présente entre ces connexions une soupape de détente (14, 14a, 18) et, en amont de la soupape de détente (14, 14a, 18), conduit à travers un échangeur de chaleur (8) à un refroidissement de la fraction de transfert par échange thermique indirect,
    en cas de fonctionnement, le niveau de liquide dans le réservoir (24, 16) se trouvant à un premier niveau h1 et à une première pression p1,
    dans l'autre récipient (5, 23), à l'endroit de la connexion entre la conduite de liquide (15, 15a, 19) et l'autre récipient (5, 23), régnant en cas de fonctionnement une deuxième pression (p2),
    l'endroit de la connexion entre la conduite de liquide (15, 15a, 19) et l'autre récipient (5, 23) étant disposé à un deuxième niveau plus élevé h2 (h2 > h1),
    la différence entre les deux pression Δp = p1 - p2 en cas de fonctionnement étant inférieure à la pression hydrostatique produite par une colonne de liquide de la fraction de transfert entre le premier et le deuxième niveau (phydr = ρ. g. [h2-h1]) :
    Δp = p1 - p2 < ρ. g. [h2 - h1] (g = accélération due à la pesanteur) caractérisé en ce que la soupape de détente (14, 14a, 18) est disposée de telle sorte qu'en cas de fonctionnement, les bulles de gaz formées lors de la détente diminuent la densité de la fraction de transfert dans une mesure telle que la différence de pression Δp suffise pour acheminer la fraction de transfert à l'autre récipient (5, 23), ni la fraction de transfert en aval de la soupape de détente (14, 14a, 18) ne recevant un courant gazeux ou en deux phases, ni la fraction de transfert entre l'échangeur de chaleur (8) et la soupape de détente (14, 14a, 18) ne recevant un écoulement liquide.
  4. Dispositif selon la revendication 3, caractérisé en ce que l'échangeur de chaleur (8) est disposé de telle sorte qu'en cas de fonctionnement, la fraction de transfert se présente sous forme complètement ou substantiellement complètement liquide directement en amont de la soupape de détente (14, 14a, 18).
EP99112289A 1999-05-12 1999-06-25 Procédé et appareil pour la séparation cryogénique de l'air Expired - Lifetime EP1052465B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19921949A DE19921949A1 (de) 1999-05-12 1999-05-12 Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
DE19921949 1999-05-12

Publications (2)

Publication Number Publication Date
EP1052465A1 EP1052465A1 (fr) 2000-11-15
EP1052465B1 true EP1052465B1 (fr) 2005-05-11

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EP99112289A Expired - Lifetime EP1052465B1 (fr) 1999-05-12 1999-06-25 Procédé et appareil pour la séparation cryogénique de l'air

Country Status (6)

Country Link
US (1) US6308533B1 (fr)
EP (1) EP1052465B1 (fr)
JP (1) JP2000356463A (fr)
KR (1) KR20010049347A (fr)
DE (2) DE19921949A1 (fr)
ES (1) ES2242331T3 (fr)

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1300640A1 (fr) * 2001-10-04 2003-04-09 Linde Aktiengesellschaft Procédé et dispositif de production d'azote ultra-pur par séparation cryogénique d'air
FR2853405A1 (fr) * 2003-04-01 2004-10-08 Air Liquide Procede et installation de separation d'air par distillation cryogenique
FR2853406A1 (fr) * 2003-04-01 2004-10-08 Air Liquide Procede et appareil de separation d'air par distillation cryogenique

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5071458A (en) * 1989-07-28 1991-12-10 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Vaporization-condensation apparatus for air distillation double column, and air distillation equipment including such apparatus

Family Cites Families (6)

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Publication number Priority date Publication date Assignee Title
DE4224068A1 (de) * 1992-03-20 1993-09-23 Linde Ag Verfahren zur tieftemperaturzerlegung von luft und luftzerlegungsanlage
FR2689223B1 (fr) * 1992-03-24 1994-05-06 Air Liquide Procede et installation de transfert de fluide en provenance d'une colonne de distillation, notamment d'air.
DE4317916A1 (de) * 1993-05-28 1994-12-01 Linde Ag Verfahren und Vorrichtung zur Gewinnung von Argon
US5406800A (en) * 1994-05-27 1995-04-18 Praxair Technology, Inc. Cryogenic rectification system capacity control method
DE19609490A1 (de) * 1995-03-10 1996-09-12 Linde Ag Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
GB9711258D0 (en) * 1997-05-30 1997-07-30 Boc Group Plc Air separation

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5071458A (en) * 1989-07-28 1991-12-10 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Vaporization-condensation apparatus for air distillation double column, and air distillation equipment including such apparatus

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
DIN ET AL: "Low temperature techniques", 1960, GEORGES NEWNES LTD., LONDON *
STER J.V.: "The production of liquid nitrogen from atmospherique air using a gas refrigerating machine (Thesis)", 1960, TECHNISCHE HOGESCHOOL, DELFT *

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Publication number Publication date
EP1052465A1 (fr) 2000-11-15
JP2000356463A (ja) 2000-12-26
KR20010049347A (ko) 2001-06-15
ES2242331T3 (es) 2005-11-01
DE19921949A1 (de) 2000-11-16
US6308533B1 (en) 2001-10-30
DE59912043D1 (de) 2005-06-16

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