EP0377117B1 - Procédé et dispositif de séparation de l'air - Google Patents

Procédé et dispositif de séparation de l'air Download PDF

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Publication number
EP0377117B1
EP0377117B1 EP89122047A EP89122047A EP0377117B1 EP 0377117 B1 EP0377117 B1 EP 0377117B1 EP 89122047 A EP89122047 A EP 89122047A EP 89122047 A EP89122047 A EP 89122047A EP 0377117 B1 EP0377117 B1 EP 0377117B1
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EP
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Prior art keywords
column
argon
rectification
oxygen
crude argon
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Expired - Lifetime
Application number
EP89122047A
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German (de)
English (en)
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EP0377117B2 (fr
EP0377117A1 (fr
Inventor
Wilhelm Rohde
Horst Dipl.-Ing. Corduan
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Linde GmbH
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Linde GmbH
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Classifications

    • 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
    • F25J3/04248—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
    • F25J3/04406—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
    • F25J3/04721—Producing pure argon, e.g. recovered from a crude argon column
    • F25J3/04727—Producing pure argon, e.g. recovered from a crude argon column using an auxiliary pure argon column for nitrogen rejection
    • 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
    • F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
    • 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
    • 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
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/42—One fluid being nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/58—One fluid being argon or crude argon
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/12—Particular process parameters like pressure, temperature, ratios
    • 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
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/923—Inert gas
    • Y10S62/924—Argon
    • 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
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/939—Partial feed stream expansion, air

Definitions

  • the invention relates to a method and a device for air separation by low-temperature rectification of air, in which air is compressed, pre-cleaned, cooled, fed to a two-stage rectification and broken down into an oxygen-rich and a nitrogen-rich fraction, with another from the low-pressure stage of the rectification Argon-enriched oxygen fraction is removed and broken down into crude argon in a crude argon rectification and into a heavy-boiling residual fraction.
  • the main products of air separation, oxygen and nitrogen, can be taken directly from the two-stage rectification.
  • Argon on the other hand, whose boiling temperature is between the boiling temperatures of oxygen and nitrogen, accumulates in the middle region of the low-pressure stage of the rectification.
  • a fraction consisting essentially of oxygen is removed, with which a large part of the argon contained in the feed air is drawn off.
  • This fraction is broken down into crude argon and into a liquid residual fraction by rectification in a crude argon column. The remaining fraction is returned to the low pressure stage.
  • a method of the type mentioned is known from DE-OS-34 36 897.
  • gaseous crude argon is obtained, which consists of approximately 95% argon and is mainly contaminated by approximately 3% oxygen and 2% nitrogen (all percentages relate to the volume).
  • the oxygen can only be incompletely removed in the processes known hitherto during rectification in the crude argon column, which usually contains about 60 rectification trays, since the boiling points of argon and oxygen are extremely close to one another.
  • the difference in boiling temperatures is, for example, 2.9 K at a pressure of 1 bar.
  • the oxygen is separated from the raw argon in a so-called deoxo device by burning the oxygen with added hydrogen and separating the water formed in a dryer.
  • a deoxo device by burning the oxygen with added hydrogen and separating the water formed in a dryer.
  • Such a deoxo device is a complex apparatus and, above all, causes high operating costs due to the not inconsiderable consumption of hydrogen.
  • the provision of hydrogen is particularly complex if it does not occur in chemical processes that are carried out at the site of the air separation plant.
  • the invention has for its object to develop a method and an apparatus of the type mentioned, which are characterized by a low level of equipment and low operating costs.
  • the head of the rectification column in which such a separation is to be carried out must be cooled in order to produce reflux.
  • An indirect heat exchange with the bottom fraction from the pressure stage comes into question, as is usually also used in the crude argon rectification.
  • the bottom fraction is expanded in a top condenser and liquefied there. Indirect heat exchange absorbs heat from condensing gas in the top of the crude argon column.
  • the evaporated bottom fraction is introduced into the low pressure column.
  • a prerequisite for the fact that return can be generated in this way is, however, that the condensation temperature of the gas at the top of the column to be cooled is higher than the evaporation temperature of the evaporating bottom liquid. These temperatures are determined by the pressures of the respective fractions.
  • an exclusively rectifying separation of the oxygen is nevertheless maintained.
  • rectification trays are dispensed with in the device according to the invention and instead structured packings or fillers are used which bring about a substantially lower pressure drop within the rectification column. Since there was no empirical data on the effect of structured packings or packing elements in air rectification, it was only with the experience gained in a larger test facility that the possible implementation of packs in this area and especially in the crude argon column could be assessed. The tests showed that with a theoretical number of trays between 150 and 200, preferably about 180, an oxygen content of less than 1 ppm in the raw argon is possible with an economical argon yield.
  • the invention is explained in more detail below on the basis of an exemplary embodiment shown schematically in the drawing.
  • the figure shows in simplified form a method for air separation with subsequent argon extraction, which is carried out purely by rectification according to the invention.
  • Air is drawn in from the compressor 2 via line 1 and freed of water vapor and carbon dioxide in a cleaning stage 3.
  • the air is then cooled in a heat exchanger 4 in countercurrent to product gases and partly introduced via line 5 into the pressure column 10 of a two-stage rectification column 9.
  • Another part of the air is branched off in the heat exchanger 4 at an average temperature (line 6), expanded in a turbine 7 while performing work, and fed to the low-pressure column 11 via line 8.
  • a condenser-evaporator 12 gas is condensed from the top of the pressure column against evaporating bottom liquid of the low-pressure column, and is fed as a return to the pressure column.
  • Nitrogen gaseous (line 15) and liquid (line 14) are removed from the pressure column.
  • a portion of the liquid nitrogen is fed as a return liquid into the low pressure column via line 18.
  • Sump liquid is fed out of the pressure column via line 13 and partly fed via line 16 to the central region of the low pressure column.
  • Gaseous nitrogen (line 20) and gaseous oxygen (line 21) are taken from the low-pressure column as product streams and then warmed to almost ambient temperature in the heat exchanger4. Another fraction leaves the low-pressure column via line 22. This fraction contains 87-92%, preferably 90% oxygen, 8-13%, preferably 10% argon and also about 0.05% nitrogen and is fed into the lower region of a crude argon column 24.
  • the top condenser 26 of the crude argon column 24 is cooled by vaporizing liquid which is fed from the bottom of the pressure column 10 via line 17.
  • the bottom liquid in line 17 contains 35-40% oxygen and is expanded to approximately the pressure of the low pressure column before being introduced into the top condenser 26.
  • the evaporated portion is introduced via line 19 into the low pressure column.
  • the raw argon column 24 is equipped with structured packings which correspond to a theoretical number of plates from 170 to 200, preferably approximately 180, and is operated under the pressure of the low pressure column from 1.2 to 1.6, preferably approximately 1.3 bar.
  • packings with a similarly low pressure drop could also be used.
  • Raw argon is removed in gaseous form via line 25 and contains only about 1 ppm oxygen. A part of this raw argon is liquefied in the top condenser 26 and returned to the raw argon column as a return. The remaining raw argon is condensed in a raw argon liquefier 28 by heat exchange with evaporating nitrogen 29, which comes from the pressure column.
  • the nitrogen remaining in the crude argon is separated off.
  • the bottom of the column is heated by nitrogen gas which is brought out of the pressure column via line 15.
  • the condensed nitrogen 31 is used together with the liquid 32 removed from the pressure column to cool the head of the pure argon column.
  • gas is withdrawn via line 34 and partly liquefied in the top condenser 33 and returned to the pure argon column 30.
  • the remaining part is discharged via line 37 as residual gas, which consists essentially of nitrogen.
  • Liquid pure argon is removed via line 39 and still contains a total of 1-10 ppm, preferably 3 ppm, of impurities.

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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)
  • Removal Of Specific Substances (AREA)
  • Polysaccharides And Polysaccharide Derivatives (AREA)
  • Exhaust Gas Treatment By Means Of Catalyst (AREA)
  • Acyclic And Carbocyclic Compounds In Medicinal Compositions (AREA)
  • Motor Or Generator Cooling System (AREA)

Claims (3)

1. Procédé de fractionnement de l'air par rectification de l'air à très basse température, procédé dans lequel l'air est comprimé , prépurifié, refroidi, soumis à rectification en deux étages puis divisé en une fraction riche en oxygène et en une fraction riche en azote, et dans lequel une autre fraction d'oxygène enrichie en argon est prélevée dans l'étage basse-pression de la rectification et est séparée dans une zone de fractionnement de l'argon brut en une fraction d'argon brut et en une fraction résiduelle dont l'évaporation est plus difficile, caractérisé en ce que la rectification d'argon brut est mise en oeuvre sur au moins 150 plateaux théoriques et en présence de garnitures ou corps de remplissage structurés.
2. Procédé selon la revendication 1, caractérisé en ce que l'argon brut provenant de la rectification d'argon brut est fractionné dans une zone de rectification d'argon pur, en une fraction d'argon pur et en une fraction résiduelle de point d'ébullition moins élevé.
3. Dispositif d'exécution du procédé selon la revendication 1, comportant une colonne de rectification à deux étages, comprenant un étage sous pression et un étage basse-pression, ainsi qu'une colonne d'argon brut, caractérisé en ce que la colonne d'argon brut est mise en oeuvre sur au moins 150 plateaux théoriques et en présence de garnitures structurées ou corps de remplissage.
EP89122047A 1988-12-01 1989-11-29 Procédé et dispositif de séparation de l'air Expired - Lifetime EP0377117B2 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3840506 1988-12-01
DE3840506A DE3840506A1 (de) 1988-12-01 1988-12-01 Verfahren und vorrichtung zur luftzerlegung

Publications (3)

Publication Number Publication Date
EP0377117A1 EP0377117A1 (fr) 1990-07-11
EP0377117B1 true EP0377117B1 (fr) 1992-03-25
EP0377117B2 EP0377117B2 (fr) 1995-05-17

Family

ID=6368245

Family Applications (1)

Application Number Title Priority Date Filing Date
EP89122047A Expired - Lifetime EP0377117B2 (fr) 1988-12-01 1989-11-29 Procédé et dispositif de séparation de l'air

Country Status (11)

Country Link
US (1) US5019145A (fr)
EP (1) EP0377117B2 (fr)
JP (1) JPH0781781B2 (fr)
KR (1) KR950014009B1 (fr)
CN (1) CN1019690B (fr)
AT (1) ATE74199T1 (fr)
AU (1) AU617226B2 (fr)
CA (1) CA2004263C (fr)
DE (2) DE3840506A1 (fr)
ES (1) ES2031677T5 (fr)
ZA (1) ZA899186B (fr)

Cited By (19)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0444422A1 (fr) * 1990-02-02 1991-09-04 Air Products And Chemicals, Inc. Production d'argon de pureté élevée
EP0446593A1 (fr) * 1990-02-02 1991-09-18 Air Products And Chemicals, Inc. Production d'argon de l'air à faible teneur d'oxygène
EP0669509A1 (fr) * 1994-02-24 1995-08-30 Linde Aktiengesellschaft Procédé et appareil permettant d'obtenir d l'argon pur
EP0684438A1 (fr) 1994-05-27 1995-11-29 The BOC Group plc Séparation de l'air
EP0722074A2 (fr) * 1995-01-11 1996-07-17 The BOC Group plc Séparation d'air
US5557951A (en) * 1995-03-24 1996-09-24 Praxair Technology, Inc. Process and apparatus for recovery and purification of argon from a cryogenic air separation unit
EP0733869A2 (fr) * 1995-03-21 1996-09-25 The BOC Group plc Séparation d'air
DE19543953C1 (de) * 1995-11-25 1996-12-19 Linde Ag Verfahren und Vorrichtung zur Gewinnung von Sauerstoff und Stickstoff unter überatmosphärischem Druck
EP0752565A2 (fr) * 1995-07-06 1997-01-08 The BOC Group plc Production d'argon
EP0768503A2 (fr) * 1995-10-11 1997-04-16 Linde Aktiengesellschaft Procédé de séparation d'air à triple colonne
EP0775880A2 (fr) 1995-11-21 1997-05-28 Linde Aktiengesellschaft Procédé et dispositif à double colonne pour la séparation cryogénique d'air
AU685930B2 (en) * 1994-06-17 1998-01-29 Boc Group Plc, The Air separation
US6612129B2 (en) 2001-10-31 2003-09-02 Linde Aktiengesellschaft Process and apparatus for producing krypton and/or xenon by low-temperature fractionation of air
EP2645033A1 (fr) 2012-03-29 2013-10-02 Linde Aktiengesellschaft Paquet transportable avec boîtier frigorifique et procédé de fabrication d'une installation de décomposition de l'air à basse température
EP2645031A1 (fr) 2012-03-29 2013-10-02 Linde Aktiengesellschaft Colonne de séparation pour une installation de décomposition de l'air à basse température, installation de décomposition de l'air à basse température et procédé de décomposition à basse température de l'air
WO2013159868A2 (fr) 2012-04-27 2013-10-31 Linde Aktiengesellschaft Paquet transportable comprenant une boîte froide, installation de décomposition de l'air à basse température et procédé de fabrication d'une installation de décomposition de l'air à basse température
WO2014135271A2 (fr) 2013-03-06 2014-09-12 Linde Aktiengesellschaft Installation de séparation d'air, procédé de récupération d'un produit contenant de l'argon et procédé pour créer une installation de séparation d'air
EP3040665A1 (fr) 2014-12-30 2016-07-06 Linde Aktiengesellschaft Système de colonne de distillation et installation pour la production d'oxygène par séparation cryogénique de l'air
EP3048401A1 (fr) 2015-01-20 2016-07-27 Linde Aktiengesellschaft Procédé et dispositif destinés à l'extraction variable d'argon par la séparation cryogénique de l'air

Families Citing this family (41)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5133790A (en) * 1991-06-24 1992-07-28 Union Carbide Industrial Gases Technology Corporation Cryogenic rectification method for producing refined argon
US5161380A (en) * 1991-08-12 1992-11-10 Union Carbide Industrial Gases Technology Corporation Cryogenic rectification system for enhanced argon production
US5235816A (en) * 1991-10-10 1993-08-17 Praxair Technology, Inc. Cryogenic rectification system for producing high purity oxygen
US5207066A (en) * 1991-10-22 1993-05-04 Bova Vitaly I Method of air separation
US5237823A (en) * 1992-03-31 1993-08-24 Praxair Technology, Inc. Cryogenic air separation using random packing
JP2966999B2 (ja) * 1992-04-13 1999-10-25 日本エア・リキード株式会社 超高純度窒素・酸素製造装置
US5230217A (en) * 1992-05-19 1993-07-27 Air Products And Chemicals, Inc. Inter-column heat integration for multi-column distillation system
US5305611A (en) * 1992-10-23 1994-04-26 Praxair Technology, Inc. Cryogenic rectification system with thermally integrated argon column
US5311744A (en) * 1992-12-16 1994-05-17 The Boc Group, Inc. Cryogenic air separation process and apparatus
DE4317916A1 (de) * 1993-05-28 1994-12-01 Linde Ag Verfahren und Vorrichtung zur Gewinnung von Argon
DE4332870C2 (de) * 1993-09-27 2003-02-20 Linde Ag Verfahren und Vorrichtung zur Gewinnung eines Krypton-/Xenon-Konzentrats durch Tieftemperaturzerlegung von Luft
DE4406069A1 (de) * 1994-02-24 1995-09-07 Linde Ag Verfahren und Vorrichtung zur Gewinnung von reinem Argon
DE4406049A1 (de) * 1994-02-24 1995-09-07 Linde Ag Verfahren und Vorrichtung zur Gewinnung von reinem Argon
DE4406051A1 (de) * 1994-02-24 1995-08-31 Linde Ag Verfahren und Vorrichtung zur Gewinnung von reinem Argon
CA2142317A1 (fr) * 1994-02-24 1995-08-25 Anton Moll Methode et appareil pour la recuperation d'argon pur
US5396772A (en) * 1994-03-11 1995-03-14 The Boc Group, Inc. Atmospheric gas separation method
US5440884A (en) * 1994-07-14 1995-08-15 Praxair Technology, Inc. Cryogenic air separation system with liquid air stripping
GB9423955D0 (en) 1994-11-24 1995-01-11 Boc Group Plc Air seperation
DE4443190A1 (de) * 1994-12-05 1996-06-13 Linde Ag Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
US5784899A (en) * 1995-06-20 1998-07-28 Nippon Sanso Corporation Argon separation method and apparatus therefor
US5799508A (en) * 1996-03-21 1998-09-01 Praxair Technology, Inc. Cryogenic air separation system with split kettle liquid
FR2757421B1 (fr) * 1996-12-24 1999-01-15 Air Liquide Procede d'epuration d'un fluide cryogenique par filtration et/ou adsorption
US5768914A (en) * 1997-07-28 1998-06-23 Air Products And Chemicals, Inc. Process to produce oxygen and argon using divided argon column
US5916261A (en) * 1998-04-02 1999-06-29 Praxair Technology, Inc. Cryogenic argon production system with thermally integrated stripping column
US6276170B1 (en) * 1999-05-25 2001-08-21 Air Liquide Process And Construction Cryogenic distillation system for air separation
US6347534B1 (en) * 1999-05-25 2002-02-19 Air Liquide Process And Construction Cryogenic distillation system for air separation
DE19957017A1 (de) * 1999-11-26 2001-05-31 Linde Ag Vorrichtung zur Gewinnung von Argon
US6321567B1 (en) 2000-10-06 2001-11-27 Praxair Technology, Inc. Structured packing system for reduced distillation column height
US7087804B2 (en) * 2003-06-19 2006-08-08 Chevron U.S.A. Inc. Use of waste nitrogen from air separation units for blanketing cargo and ballast tanks
EP2026024A1 (fr) 2007-07-30 2009-02-18 Linde Aktiengesellschaft Procédé et dispositif pour la production d'argon par séparation cryogénique d'air
DE102007035619A1 (de) * 2007-07-30 2009-02-05 Linde Ag Verfahren und Vorrichtung zur Gewinnung von Argon durch Tieftemperaturzerlegung von Luft
JP5642923B2 (ja) * 2008-06-10 2014-12-17 エア・ウォーター株式会社 空気分離方法
EP2211131A1 (fr) 2009-01-21 2010-07-28 Linde AG Procédé destiné au fonctionnement d'une installation de séparation de l'air
DE102009016043A1 (de) 2009-04-02 2010-10-07 Linde Ag Verfahren zum Betreiben einer Reinargonsäule und Vorrichtung zur Reinargongewinnung
US8899075B2 (en) 2010-11-18 2014-12-02 Praxair Technology, Inc. Air separation method and apparatus
DE102012006479A1 (de) 2012-03-29 2013-10-02 Linde Ag Transportables Paket mit einer Coldbox und Verfahren zum Herstellen einer Tieftemperatur-Luftzerlegungsanlage
CN103267403B (zh) * 2013-05-15 2015-09-16 兖矿集团有限公司 一种提高液氩产量的***及方法
CN103256081B (zh) * 2013-05-22 2015-04-22 南京飓能电控自动化设备制造有限公司 基于超临界空气的能源综合利用方法
DE102013018664A1 (de) 2013-10-25 2015-04-30 Linde Aktiengesellschaft Verfahren zur Tieftemperaturzerlegung von Luft und Tieftemperatur-Luftzerlegungsanlage
US10663222B2 (en) * 2018-04-25 2020-05-26 Praxair Technology, Inc. System and method for enhanced recovery of argon and oxygen from a nitrogen producing cryogenic air separation unit
US11828532B2 (en) * 2020-12-31 2023-11-28 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and apparatus for transfer of liquid

Family Cites Families (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE821951C (de) * 1949-06-20 1951-11-22 Linde Eismasch Ag Verfahren zur Gewinnung von Argon
NL111405C (fr) * 1953-11-12
IT1034544B (it) * 1975-03-26 1979-10-10 Siad Procedimento ed impianto per il frazionamento dell aria con colon na a semplice rettifica
IT1034545B (it) * 1975-03-26 1979-10-10 Siad Processo ed impianto per l otte nimento dell argon a partire da un processo di frazionamento dell aria
CH617357A5 (fr) * 1977-05-12 1980-05-30 Sulzer Ag
DE3428968A1 (de) * 1984-08-06 1986-02-13 Linde Ag, 6200 Wiesbaden Verfahren und vorrichtung zur zerlegung von rohargon
DE3436897A1 (de) * 1984-10-08 1986-04-10 Linde Ag, 6200 Wiesbaden Verfahren und vorrichtung zum betreiben einer luftzerlegungsanlage
LU86284A1 (fr) * 1986-01-30 1987-09-03 Belge Etat Procede d'obtention d'ethylene a partir d'ethanol
US4871382A (en) * 1987-12-14 1989-10-03 Air Products And Chemicals, Inc. Air separation process using packed columns for oxygen and argon recovery
US4836836A (en) * 1987-12-14 1989-06-06 Air Products And Chemicals, Inc. Separating argon/oxygen mixtures using a structured packing
US4838913A (en) * 1988-02-10 1989-06-13 Union Carbide Corporation Double column air separation process with hybrid upper column

Cited By (24)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0446593A1 (fr) * 1990-02-02 1991-09-18 Air Products And Chemicals, Inc. Production d'argon de l'air à faible teneur d'oxygène
EP0444422A1 (fr) * 1990-02-02 1991-09-04 Air Products And Chemicals, Inc. Production d'argon de pureté élevée
EP0669509A1 (fr) * 1994-02-24 1995-08-30 Linde Aktiengesellschaft Procédé et appareil permettant d'obtenir d l'argon pur
EP0684438A1 (fr) 1994-05-27 1995-11-29 The BOC Group plc Séparation de l'air
AU685930B2 (en) * 1994-06-17 1998-01-29 Boc Group Plc, The Air separation
AU706679B2 (en) * 1995-01-11 1999-06-24 Boc Group Plc, The Air separation
EP0722074A2 (fr) * 1995-01-11 1996-07-17 The BOC Group plc Séparation d'air
EP0733869A2 (fr) * 1995-03-21 1996-09-25 The BOC Group plc Séparation d'air
EP0733589A2 (fr) * 1995-03-24 1996-09-25 Praxair Technology, Inc. Procédé et l'appareil pour la récupération et purification d'argon issu d'une unité de séparation d'air cryogénique
US5557951A (en) * 1995-03-24 1996-09-24 Praxair Technology, Inc. Process and apparatus for recovery and purification of argon from a cryogenic air separation unit
EP0752565A2 (fr) * 1995-07-06 1997-01-08 The BOC Group plc Production d'argon
EP0768503A2 (fr) * 1995-10-11 1997-04-16 Linde Aktiengesellschaft Procédé de séparation d'air à triple colonne
DE19537913A1 (de) * 1995-10-11 1997-04-17 Linde Ag Dreifachsäulenverfahren zur Tieftemperaturzerlegung von Luft
EP0775880A2 (fr) 1995-11-21 1997-05-28 Linde Aktiengesellschaft Procédé et dispositif à double colonne pour la séparation cryogénique d'air
EP0775881A2 (fr) 1995-11-25 1997-05-28 Linde Aktiengesellschaft Procédé et dispositif pour la récupération d'oxygène et d'azote à pression superatmosphérique
DE19543953C1 (de) * 1995-11-25 1996-12-19 Linde Ag Verfahren und Vorrichtung zur Gewinnung von Sauerstoff und Stickstoff unter überatmosphärischem Druck
US6612129B2 (en) 2001-10-31 2003-09-02 Linde Aktiengesellschaft Process and apparatus for producing krypton and/or xenon by low-temperature fractionation of air
EP2645033A1 (fr) 2012-03-29 2013-10-02 Linde Aktiengesellschaft Paquet transportable avec boîtier frigorifique et procédé de fabrication d'une installation de décomposition de l'air à basse température
EP2645031A1 (fr) 2012-03-29 2013-10-02 Linde Aktiengesellschaft Colonne de séparation pour une installation de décomposition de l'air à basse température, installation de décomposition de l'air à basse température et procédé de décomposition à basse température de l'air
WO2013143646A2 (fr) 2012-03-29 2013-10-03 Linde Aktiengesellschaft Pack transportable comportant une boîte cryogénique et procédé pour fabriquer une installation de fractionnement de l'air à basse température
WO2013159868A2 (fr) 2012-04-27 2013-10-31 Linde Aktiengesellschaft Paquet transportable comprenant une boîte froide, installation de décomposition de l'air à basse température et procédé de fabrication d'une installation de décomposition de l'air à basse température
WO2014135271A2 (fr) 2013-03-06 2014-09-12 Linde Aktiengesellschaft Installation de séparation d'air, procédé de récupération d'un produit contenant de l'argon et procédé pour créer une installation de séparation d'air
EP3040665A1 (fr) 2014-12-30 2016-07-06 Linde Aktiengesellschaft Système de colonne de distillation et installation pour la production d'oxygène par séparation cryogénique de l'air
EP3048401A1 (fr) 2015-01-20 2016-07-27 Linde Aktiengesellschaft Procédé et dispositif destinés à l'extraction variable d'argon par la séparation cryogénique de l'air

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KR900009433A (ko) 1990-07-04
DE58901041D1 (de) 1992-04-30
ES2031677T5 (es) 1995-09-16
US5019145A (en) 1991-05-28
AU4582189A (en) 1990-06-07
CN1019690B (zh) 1992-12-30
DE3840506A1 (de) 1990-06-07
CA2004263C (fr) 1994-02-01
DE3840506C2 (fr) 1992-01-16
AU617226B2 (en) 1991-11-21
EP0377117B2 (fr) 1995-05-17
ATE74199T1 (de) 1992-04-15
KR950014009B1 (ko) 1995-11-20
EP0377117A1 (fr) 1990-07-11
CA2004263A1 (fr) 1990-06-01
JPH02247484A (ja) 1990-10-03
JPH0781781B2 (ja) 1995-09-06
CN1043196A (zh) 1990-06-20
ES2031677T3 (es) 1992-12-16
ZA899186B (en) 1990-08-29

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