EP1031804B1 - Procédé de séparation des gaz de l'air avec recyclage d'azote - Google Patents

Procédé de séparation des gaz de l'air avec recyclage d'azote Download PDF

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Publication number
EP1031804B1
EP1031804B1 EP20000102977 EP00102977A EP1031804B1 EP 1031804 B1 EP1031804 B1 EP 1031804B1 EP 20000102977 EP20000102977 EP 20000102977 EP 00102977 A EP00102977 A EP 00102977A EP 1031804 B1 EP1031804 B1 EP 1031804B1
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EP
European Patent Office
Prior art keywords
pressure column
nitrogen
low
feed air
fraction
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
EP20000102977
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German (de)
English (en)
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EP1031804A1 (fr
Inventor
Herbert Grad.-Ing. Schoenecker
Jürgen Dipl.-Ing. Voit
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
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Linde GmbH
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Filing date
Publication date
Priority claimed from DE19908451A external-priority patent/DE19908451A1/de
Application filed by Linde GmbH filed Critical Linde GmbH
Priority to EP20000102977 priority Critical patent/EP1031804B1/fr
Publication of EP1031804A1 publication Critical patent/EP1031804A1/fr
Application granted granted Critical
Publication of EP1031804B1 publication Critical patent/EP1031804B1/fr
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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
    • 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
    • F25J3/04284—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
    • F25J3/04309—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 nitrogen
    • F25J3/04315—Lowest pressure or impure nitrogen, so-called waste nitrogen expansion
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/20—Processes or apparatus using separation by rectification in an elevated pressure multiple column system wherein the lowest pressure column is at a pressure well above the minimum pressure needed to overcome pressure drop to reject the products to atmosphere
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/04—Mixing or blending of fluids with the feed stream
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being nitrogen

Definitions

  • the invention relates to a method for the low temperature decomposition of air with a Rectification system that has at least one pressure column and one low pressure column having feed air in a first compressor to a first pressure compressed, cleaned in a cleaning stage, cooled and at least partially in the pressure column is introduced, at least one liquid fraction from the pressure column in the low pressure column is fed and a nitrogen-rich fraction from the Low pressure column warmed up and with feed air downstream of the cleaning stage of the Air is mixed.
  • a process of this type and a corresponding device are known from EP 810412 A, known. There, the nitrogen-rich fraction is mixed before using a Compressor recompressed.
  • the invention has for its object a method of the type mentioned as well as specify a corresponding device that is particularly economical economically are and in particular need relatively low investment costs.
  • This object is achieved in that the mixture of feed air and nitrogen-rich fraction is further compressed in a second compressor to a second pressure p 2 , which is greater than the first pressure p 1 .
  • the first and the second compressor can be designed in one or more stages. They can be driven independently of one another or can be coupled to one another via a common shaft or a gear.
  • the first pressure p 1 is preferably in the vicinity of the operating pressure of the low-pressure column, that is to say the difference between the two pressures mentioned is not more than about 0.5 bar.
  • Preferred ranges of values for the outlet pressures of the two compressors are: first compressor (p 1 ) 2 to 12 bar, preferably 3 to 4 bar second compressor (p 2 ) 6 to 40 bar, preferably 9 to 13 bar
  • the specific values depend in individual cases on the desired delivery pressure of or one of the products (for example nitrogen) in one of the columns are generated in gaseous form, or after the pressure of one or more Product flows (oxygen and / or nitrogen) flowing out of one of the columns removed and after pressure increase in the liquid state under delivery pressure be evaporated.
  • the "nitrogen-rich fraction” can be made up of pure nitrogen or a mixture Air gases are formed, the nitrogen content for example greater than about Is 50 mol%. It can be from the head or from an intermediate point of the low pressure column subtracted from.
  • Cold can further relax in the process by work-relieving nitrogen-rich fraction are generated from the low pressure column. This can for example from the upper area, preferably from the top of the low pressure column subtracted from. It is beneficial if the returnable and the work-performing too relaxing nitrogen-rich fraction together from the low pressure column deducted and warmed if necessary.
  • the more nitrogen-rich Fraction can, for example, at an intermediate temperature of the main heat exchanger be separated from the stream to be recirculated for cooling feed air.
  • an oxygen-containing fraction from the lower one Work area can be relaxed in the low pressure column, especially in the same relaxation machine.
  • an oxygen-containing fraction is used Example from the bottom of the low pressure column or from the evaporation chamber of the Bottom evaporator of the low pressure column (main condenser) deducted in Main heat exchanger warmed to an intermediate temperature and one Relaxation machine fed. Will add another nitrogen-rich Relaxed fraction while working, this is preferably immediately upstream the work-related relaxation mixed with the oxygen-containing fraction and the two factions to be relaxed are together in the same Relaxation machine (preferably expansion turbine) initiated.
  • the invention also relates to a device for the low-temperature separation of air according to claim 6.
  • the method according to the invention is particularly suitable for methods in which the Operating pressure at the top of the pressure column at 5.7 to 29.7 bar, preferably at 8.7 to 12.7 bar, the operating pressure at the top of the low pressure column at 1.8 to 11.8 bar, is preferably 2.8 to 3.8 bar.
  • Process cold can be caused by work-related relaxation of the process Process stream are generated. It is beneficial to relax one Residual gas flow from the low pressure column, for example together with the nitrogen-rich fraction taken from the low pressure column, onto a The intermediate temperature is warmed up and fed to a relaxation machine.
  • Atmospheric air 1 is drawn in through a filter 2 by a first compressor 3 and compressed to a pressure p 1 of 3 bar.
  • the air 5 is led to a cleaning stage 6, which in the example is formed by a pair of switchable molecular sieve adsorbers.
  • carbon dioxide and water are removed from the feed air.
  • the cleaned feed air flows via lines 7 and 8 to a second compressor 9, which brings it to a pressure p 2 of 9 bar.
  • the heat of compression is removed again in an aftercooler 10.
  • the highly compressed feed air 11 is cooled in a main heat exchanger 12 to approximately dew point and partially liquefied and finally completely fed via line 13 to the pressure column 14 of a two-column rectification system, which also has a low pressure column 15.
  • Pressure column 14 and low pressure column 15 are in a heat-exchanging connection via a common condenser-evaporator (main condenser) 16.
  • the operating pressures (each at the head) in the example are 8.7 bar in the pressure column 14 and 2.8 bar in the low pressure column 15.
  • a first part 18 of the top nitrogen 17 of the pressure column 14 is the line 18 Main condenser 16 supplied and there against evaporating bottom liquid Low pressure column 15 at least partially, preferably essentially completely condensed.
  • the condensate 19 produced in this way is at least partly via line 20 abandoned as a return to the pressure column 14.
  • a subset can be one Internal compression can be supplied by increasing to a liquid state Pressure and then evaporated against feed air; this variant is not shown in the drawing.
  • part of the condensate 18 as Liquid nitrogen product 21 can be obtained.
  • Another part is connected via line 22 of the gaseous pressure column nitrogen 17 to the main heat exchanger 12, there warmed to about ambient temperature and finally as a pressure nitrogen product 23 deducted.
  • the low pressure column 15 becomes more liquid as the main product Oxygen 28 removed from the sump by means of a pump 29 to an increased pressure brought from for example 30 bar and evaporated against feed air 11 and warmed up.
  • oxygen evaporation takes place in the main heat exchanger 12 instead.
  • the oxygen is finally discharged via line 31 as a printed product.
  • impure nitrogen 32 becomes nitrogen-rich Fraction removed and in the counterflow 25 and in the main heat exchanger 12th warmed up.
  • the nitrogen-rich fraction warmed to around ambient temperature 33 is mixed with the cleaned feed air 7, together with this via line 8 the second compressor 9 and further via the lines 11 and 13 of the pressure column 14 fed.
  • the practical unpressurized residual gas is transferred Line 37 from the warm end of the main heat exchanger 12.
  • a first part 38 of the heated unpressurized residual gas 37 can in the cleaning stage 6 as Regeneration gas are used, while the rest 39 in the example in the Atmosphere is blown off.
  • the embodiment can be easily modified, for example Generation of a more enriched nitrogen product in the low pressure column 15.
  • at least one further must be above the feed 27 of the raw oxygen Rectification section may be provided, at the head of which the nitrogen-rich fraction 32 is subtracted.
  • this Impure nitrogen discharge can also be pure nitrogen at the top of the low pressure column 15 be won. In both cases, part of the liquid nitrogen 19 from Main condenser 16 of the low pressure column 15 is supplied as the return liquid become.

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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)

Claims (6)

  1. Procédé de séparation d'air à basse température avec un système de rectification qui présente au moins une colonne de pression (14) et une colonne de basse pression (15), l'air d'alimentation (1) étant comprimé (3) dans un premier compresseur (3) à une première pression p1, purifié dans un étage de purification (6), refroidi (12) et introduit (13) au moins partiellement dans la colonne de pression (14), au moins une fraction de liquide (24) provenant de la colonne de pression (14) étant introduite (26, 27) dans la colonne de basse pression (15) et une fraction riche en azote (32) provenant de la colonne de basse pression (15) étant chauffée (25, 12) et mélangée à l'air d'alimentation (7) en aval de l'étage de purification (6) de l'air d'alimentation, caractérisé en ce que le mélange (8) d'air d'alimentation et de fraction riche en azote est surpressé dans un deuxième compresseur (9) à une deuxième pression p2 qui est supérieure à la première pression p1.
  2. Procédé selon la revendication 1, caractérisé en ce que le chauffage de la fraction riche en azote (32) est réalisé au moins partiellement par échange thermique indirect (12) avec l'air d'alimentation (11).
  3. Procédé selon l'une quelconque des revendications 1 ou 2, caractérisé en ce qu' une fraction d' azote (17, 22) est prélevée dans la zone supérieure de la colonne de pression (14), chauffée (12) et extraite sous forme de produit d'azote sous pression (23).
  4. Procédé selon l'une quelconque des revendications 1 à 3, caractérisé en ce qu'une autre fraction riche en azote (32, 34) provenant de la colonne de basse pression (15) est détendue en fournissant du travail (35).
  5. Procédé selon l'une quelconque des revendications 1 à 4, caractérisé en ce que la fraction contenant de l'oxygène provenant de la zone inférieure de la colonne de basse pression est détendue en fournissant du travail.
  6. Dispositif de séparation d'air à basse température avec un système de rectification qui présente au moins une colonne de pression (14) et une colonne de basse pression (15), et avec une conduite d'air d'alimentation (1, 5, 7, 8, 11, 13) qui conduit par l'intermédiaire d'un premier compresseur (3), d'un étage de purification (6) et d'un échangeur de chaleur principal (12) dans la colonne de pression (14), avec une conduite de liquide (24, 27) pour introduire une fraction liquide provenant de la colonne de pression (14) dans la colonne de basse pression (15) et avec une conduite de recirculation (32, 33) pour une fraction riche en azote provenant de la colonne de basse pression (15), qui passe à travers l'échangeur de chaleur principal (12) et débouche en aval de l'étage de purification (6) dans la conduite d'air d'alimentation (7), caractérisé en ce qu'un deuxième compresseur est disposé dans la conduite d'air d'alimentation (8, 11) en aval de l'embouchure de la conduite de recirculation (33).
EP20000102977 1999-02-26 2000-02-14 Procédé de séparation des gaz de l'air avec recyclage d'azote Expired - Lifetime EP1031804B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP20000102977 EP1031804B1 (fr) 1999-02-26 2000-02-14 Procédé de séparation des gaz de l'air avec recyclage d'azote

Applications Claiming Priority (5)

Application Number Priority Date Filing Date Title
DE19908451 1999-02-26
DE19908451A DE19908451A1 (de) 1999-02-26 1999-02-26 Zweisäulensystem zur Tieftemperaturzerlegung von Luft
EP99114706 1999-07-27
EP99114706 1999-07-27
EP20000102977 EP1031804B1 (fr) 1999-02-26 2000-02-14 Procédé de séparation des gaz de l'air avec recyclage d'azote

Publications (2)

Publication Number Publication Date
EP1031804A1 EP1031804A1 (fr) 2000-08-30
EP1031804B1 true EP1031804B1 (fr) 2004-02-04

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Families Citing this family (23)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE10111428A1 (de) * 2001-03-09 2002-09-12 Linde Ag Verfahren und Vorrichtung zur Zerlegung eines Gasgemischs mit Notbetrieb
DE102007031759A1 (de) 2007-07-07 2009-01-08 Linde Ag Verfahren und Vorrichtung zur Erzeugung von gasförmigem Druckprodukt durch Tieftemperaturzerlegung von Luft
DE102007031765A1 (de) 2007-07-07 2009-01-08 Linde Ag Verfahren zur Tieftemperaturzerlegung von Luft
US9714789B2 (en) * 2008-09-10 2017-07-25 Praxair Technology, Inc. Air separation refrigeration supply method
DE102009034979A1 (de) 2009-04-28 2010-11-04 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Erzeugung von gasförmigem Drucksauerstoff
EP2312248A1 (fr) 2009-10-07 2011-04-20 Linde Aktiengesellschaft Procédé et dispositif de production d'oxygène sous pression et de crypton/xénon
DE102010052544A1 (de) 2010-11-25 2012-05-31 Linde Ag Verfahren zur Gewinnung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft
DE102010052545A1 (de) 2010-11-25 2012-05-31 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Gewinnung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft
EP2520886A1 (fr) 2011-05-05 2012-11-07 Linde AG Procédé et dispositif de production d'un produit comprimé à oxygène gazeux par décomposition à basse température d'air
DE102011112909A1 (de) 2011-09-08 2013-03-14 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Gewinnung von Stahl
EP2600090B1 (fr) 2011-12-01 2014-07-16 Linde Aktiengesellschaft Procédé et dispositif destinés à la production d'oxygène sous pression par décomposition à basse température de l'air
DE102011121314A1 (de) 2011-12-16 2013-06-20 Linde Aktiengesellschaft Verfahren zur Erzeugung eines gasförmigen Sauerstoff-Druckprodukts durch Tieftemperaturzerlegung von Luft
DE102012017488A1 (de) 2012-09-04 2014-03-06 Linde Aktiengesellschaft Verfahren zur Erstellung einer Luftzerlegungsanlage, Luftzerlegungsanlage und zugehöriges Betriebsverfahren
EP2784420A1 (fr) 2013-03-26 2014-10-01 Linde Aktiengesellschaft Procédé de séparation de l'air et installation de séparation de l'air
WO2014154339A2 (fr) 2013-03-26 2014-10-02 Linde Aktiengesellschaft Procédé de séparation d'air et installation de séparation d'air
EP2801777A1 (fr) 2013-05-08 2014-11-12 Linde Aktiengesellschaft Installation de décomposition de l'air dotée d'un entraînement de compresseur principal
DE102013017590A1 (de) 2013-10-22 2014-01-02 Linde Aktiengesellschaft Verfahren zur Gewinnung eines Krypton und Xenon enthaltenden Fluids und hierfür eingerichtete Luftzerlegungsanlage
PL2963369T3 (pl) 2014-07-05 2018-10-31 Linde Aktiengesellschaft Sposób i urządzenie do niskotemperaturowej separacji powietrza
EP2963371B1 (fr) 2014-07-05 2018-05-02 Linde Aktiengesellschaft Procede et dispositif de production d'un produit de gaz sous pression par decomposition a basse temperature d'air
PL2963370T3 (pl) 2014-07-05 2018-11-30 Linde Aktiengesellschaft Sposób i urządzenie do kriogenicznego rozdziału powietrza
EP2963367A1 (fr) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Procédé et dispositif cryogéniques de séparation d'air avec consommation d'énergie variable
CN113996139A (zh) * 2021-12-10 2022-02-01 开封黄河空分集团有限公司 一种节能型低压气液制取空分设备
DE202022101052U1 (de) 2022-02-24 2022-06-02 Linde Gmbh Luftzerlegungsanlage

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3367023D1 (en) * 1982-05-03 1986-11-20 Linde Ag Process and apparatus for obtaining gaseous oxygen at elevated pressure
DE3814187C2 (de) * 1988-04-27 1994-03-10 Linde Ag Verfahren zur Luftzerlegung durch Tieftemperaturrektifikation
US5049173A (en) * 1990-03-06 1991-09-17 Air Products And Chemicals, Inc. Production of ultra-high purity oxygen from cryogenic air separation plants
JP2875206B2 (ja) * 1996-05-29 1999-03-31 日本エア・リキード株式会社 高純度窒素製造装置及び方法

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