EP0595673B1 - Verfahren und Anlage zur Herstellung von Stickstoff und Sauerstoff - Google Patents

Verfahren und Anlage zur Herstellung von Stickstoff und Sauerstoff Download PDF

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Publication number
EP0595673B1
EP0595673B1 EP93402421A EP93402421A EP0595673B1 EP 0595673 B1 EP0595673 B1 EP 0595673B1 EP 93402421 A EP93402421 A EP 93402421A EP 93402421 A EP93402421 A EP 93402421A EP 0595673 B1 EP0595673 B1 EP 0595673B1
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EP
European Patent Office
Prior art keywords
column
liquid
reboiler
condenser
nitrogen
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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
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EP93402421A
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English (en)
French (fr)
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EP0595673A1 (de
Inventor
Pascal Arriulou
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Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Publication of EP0595673A1 publication Critical patent/EP0595673A1/de
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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
    • F25J3/044—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a single pressure main column system only
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—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
    • F25J3/04296—Claude expansion, i.e. expanded into the main or 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
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
    • F25J3/04884—Arrangement of reboiler-condensers
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/72—Refluxing the column with at least a part of the totally condensed overhead gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/76—Refluxing the column with condensed overhead gas being cycled in a quasi-closed loop refrigeration cycle
    • 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams
    • 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

  • DE-A-30.35.844 describes a process for the production of nitrogen and impure oxygen.
  • the supply air is used to reboil the tank of the single column and a liquid is drawn off at an intermediate level of the column to be sent to the overhead condenser with the rich liquid.
  • the object of the invention is to improve this process so as to also allow a minority production of oxygen.
  • the installation represented in FIG. 1 essentially comprises an air compressor 1, an apparatus 2 for purifying the air of water and CO 2 by adsorption, a heat exchange line 3, a distillation column 4, an air expansion turbine 5, an auxiliary heat exchanger 6 and a nitrogen compressor 7.
  • Column 4 comprises an overhead condenser 8 and a tank reboiler 9. This column operates under a pressure known as medium pressure, typically of the order of 3 to 5 bars absolute.
  • the air to be treated compressed by the compressor 1 at a pressure markedly higher than the medium pressure and then purified in 2, is cooled to an intermediate temperature in the heat exchange line 3. A fraction of the air is then out of heat exchange line, expanded at medium pressure in turbine 5 and introduced at an intermediate level in column 4.
  • Production nitrogen gas is drawn off at the top of the column via a pipe 11, heated in 6 then in 3, and recovered as the first product (medium-pressure nitrogen gas) via a pipe 12.
  • An adjustable flow of medium pressure nitrogen is taken from line 12 and compressed to a high pressure by compressor 7. Part of the high pressure nitrogen can constitute a second product of the installation, recovered via line 13, and the rest is recycled via a pipe 14, cooled to the cold end of the exchange line 3 and sent to the reboiler 9, where it condenses.
  • the liquid nitrogen thus obtained, sub-cooled in 6, is expanded in an expansion valve 15 and injected under reflux at the top of the column 4, part of this liquid nitrogen being able to be recovered as a third product (liquid nitrogen under high pressure) via a 15A line.
  • a liquid, called “rich liquid” is withdrawn, via a line 16, at an intermediate level between the level of introduction of the turbined air and the reboiler, that is to say that there are a certain number of distillation plates 17 between line 16 and the introduction of the turbined air and a certain number of plates 18 below line 16.
  • This liquid is sub-cooled in 6, expanded at a low pressure slightly higher than the atmospheric pressure in an expansion valve 19 and introduced into the condenser 8, where it vaporizes.
  • the rich liquid vaporized, after heating in 6 and then in the heat exchange line 3, is discharged via a pipe 19 constituting the waste gas W of the installation.
  • the bottom liquid of the column which cools the reboiler 9, consists of oxygen at a desired content of impurities.
  • a relatively low flow rate of this liquid of the order of a few% of the incoming air flow rate, is vaporized by the reboiler 9 and withdrawn from the column in gaseous form immediately above it via a line 20, c that is to say that there is no distillation stage between the reboiler and this pipe 20.
  • this medium-pressure gaseous oxygen constitutes a fourth product of the installation, which is recovered via a line 21.
  • a pipe 22 for purging liquid oxygen from the bottom of the column is also shown in Figure 1, a pipe 22 for purging liquid oxygen from the bottom of the column.
  • the pipe 20 is deleted, and a pipe 23 is pitted on the pipe 22.
  • the liquid oxygen conveyed by this line 23 is sub-cooled at 6, expanded in an expansion valve 24 and introduced into an auxiliary condenser 25 mounted in the column 4 below the head condenser 8, to be vaporized there.
  • the expression "below” means that there are a number of distillation trays between the two condensers.
  • This variant makes it possible to increase the reflux in column 4, in return for the production of gaseous oxygen under low pressure.
  • the embodiment 3 differs from the previous one only in that the auxiliary condenser 25 is mounted in parallel with the head condenser 8 and therefore constitutes a second head condenser of the column.
  • the production of the column is thereby simplified, but, on the other hand, it is necessary to slightly increase the pressure of the rich liquid vaporized and therefore the pressure of the incoming air.

Claims (10)

  1. Verfahren zur Herstellung von mehrheitlich Stickstoff und minderheitlich Sauerstoff durch Destillation eines Gasgemischs, insbesondere Luft, bei dem
    - das Gasgemisch in einer Wärmeaustauschleitung (3) abgekühlt und sodann auf einer Zwischenhöhe einer Destillationskolonne (4) eingeleitet wird, die mit einem mittleren Druck arbeitet und mit einem Kopfkondensator (8) und einem im Sumpf angeordneten Aufkocher (9) versehen ist;
    - der Kolonne unterhalb des Einleitungspunkts des Gasgemischs entnommene Flüssigkeit nach Entspannung (bei 19) auf einen niedrigen Druck kleiner als der mittlere Druck in dem Kopfkondensator (8) verdampft wird;
    - gasförmiger Stickstoff (11) am Kopf der Kolonne entnommen, erwärmt, teilweise auf einen hohen Druck größer als der mittlere Druck verdichtet, abgekühlt und in den Aufkocher (9) eingeleitet wird, um dort kondensiert zu werden; und
    - zumindest ein Teil des so erhaltenen flüssigen Stickstoffs (bei 15) auf den mittleren Druck entspannt und, gegebenenfalls gereinigt, in den Kopf der Kolonne eingeleitet wird, dadurch gekennzeichnet, daß:
    - die Flüssigkeit (16) auf einer Zwischenhöhe zwischen der Luftzufuhrhöhe und dem Aufkocher entnommen und in der Austauschleitung (3) erwärmt wird, bevor sie als Restgas ausgeleitet wird, und
    - Flüssigkeit aus dem Sumpf der Kolonne verdampft und als aus im wesentlichen Sauerstoff bestehendes Nebenprodukt zurückgewonnen wird.
  2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß die Sumpfflüssigkeit, die das Nebenprodukt bilden soll, durch den Aufkocher (9) verdampft und unmittelbar oberhalb diesem in gasförmiger Form entnommen wird.
  3. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß die Sumpfflüssigkeit, die das Nebenprodukt bilden soll, entspannt (bei 24) und dann in einem im oberen Teil der Kolonne (4) angeordneten Hilfskondensator (25) verdampft wird.
  4. Verfahren nach Anspruch 3, dadurch gekennzeichnet, daß der Hilfskondensator (25) unterhalb des Kopfkondensators (8) angeordnet ist.
  5. Verfahren nach Anspruch 3, dadurch gekennzeichnet, daß der Hilfskondensator (25) parallel zu dem Kopfkondensator (8) angeordnet ist und die Sumpfflüssigkeit (bei 24) auf einen Druck kleiner als der niedrige Druck entspannt wird.
  6. Vorrichtung zur Herstellung von mehrheitlich Stickstoff und minderheitlich Sauerstoff durch Destillation eines Gasgemischs, insbesondere Luft, umfassend:
    - eine unter einem mittleren Druck arbeitende und mit einem Kopfkondensator (8) und einem im Sumpf angeordneten Aufkocher (9) versehene Destillationskolonne (4);
    - Mittel (1, 2, 3, 5) zum Verdichten, Reinigen und Abkühlen des Gasgemischs und zum Einleiten desselben auf einer Zwischenhöhe der Kolonne;
    - Mittel (16) zum Entnehmen einer Flüssigkeit auf einer Höhe der Kolonne unterhalb der Einleitungshöhe des Gasgemischs, Mittel (19) zum Entspannen dieser Flüssigkeit auf einen niedrigen Druck und Mittel zum Einleiten derselben in den Kopfkondensator (8), um sie zu verdampfen;
    - Mittel (11) zum Entnehmen von Stickstoff am Kopf der Kolonne und Mittel (6, 3, 7, 14) zum Erwärmen, Verdichten auf einen hohen Druck, Abkühlen und Einleiten eines Teils dieses Stickstoffs in den Aufkocher (9); und
    - Mittel (15) zum Entspannen zumindest eines Teils des durch den Aufkocher abgegebenen flüssigen Stickstoffs auf den mittleren Druck und zum Einleiten desselben in den Kopf der Kolonne; dadurch gekennzeichnet, daß
    - die Flüssigkeitsentnahmehöhe zwischen der Einleitungshöhe des Gasgemischs und dem Aufkocher (9) liegt; und
    - Mittel (9, 20, 21; 23 bis 26) vorgesehen sind zum Verdampfen der Sumpfflüssigkeit der Kolonne und zum Zurückgewinnen des im wesentlichen aus Sauerstoff bestehenden, resultierenden Gases als Nebenprodukt der Vorrichtung.
  7. Vorrichtung nach Anspruch 6, dadurch gekennzeichnet, daß die Kolonne (4) eine Leitung (20) zum Entnehmen des Nebenprodukts unmittelbar oberhalb des Aufkochers (9) umfaßt.
  8. Vorrichtung nach Anspruch 6, dadurch gekennzeichnet, daß die Kolonne (4) einen Hilfskondensator (25) umfaßt, der über eine mit einem Druckminderventil (24) versehene Leitung (23) durch die Sumpfflüssigkeit gespeist wird.
  9. Vorrichtung nach Anspruch 8, dadurch gekennzeichnet, daß der Hilfskondensator (25) auf einer Höhe niedriger als die des Kopfkondensators (25) angeordnet ist.
  10. Vorrichtung nach Anspruch 8, dadurch gekennzeichnet, daß der Hilfskondensator (25) parallel zu dem Kopfkondensator (8) angeordnet ist.
EP93402421A 1992-10-27 1993-10-04 Verfahren und Anlage zur Herstellung von Stickstoff und Sauerstoff Expired - Lifetime EP0595673B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR9212759 1992-10-27
FR9212759A FR2697325B1 (fr) 1992-10-27 1992-10-27 Procédé et installation de production d'azote et d'oxygène.

Publications (2)

Publication Number Publication Date
EP0595673A1 EP0595673A1 (de) 1994-05-04
EP0595673B1 true EP0595673B1 (de) 1996-12-04

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EP93402421A Expired - Lifetime EP0595673B1 (de) 1992-10-27 1993-10-04 Verfahren und Anlage zur Herstellung von Stickstoff und Sauerstoff

Country Status (7)

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US (1) US5404725A (de)
EP (1) EP0595673B1 (de)
JP (1) JP3436398B2 (de)
CA (1) CA2109148A1 (de)
DE (1) DE69306362T2 (de)
ES (1) ES2095019T3 (de)
FR (1) FR2697325B1 (de)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE10157544A1 (de) * 2001-11-23 2003-06-12 Messer Ags Gmbh Verfahren und Vorrichtung zur Erzeugung von Stickstoff aus Luft

Families Citing this family (7)

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Publication number Priority date Publication date Assignee Title
US5706675A (en) * 1995-08-18 1998-01-13 G & A Associates High efficiency oxygen/air separation system
US5832748A (en) * 1996-03-19 1998-11-10 Praxair Technology, Inc. Single column cryogenic rectification system for lower purity oxygen production
US5761927A (en) * 1997-04-29 1998-06-09 Air Products And Chemicals, Inc. Process to produce nitrogen using a double column and three reboiler/condensers
FR2767317B1 (fr) * 1997-08-14 1999-09-10 Air Liquide Procede de conversion d'un debit contenant des hydrocarbures par oxydation partielle
US6000239A (en) * 1998-07-10 1999-12-14 Praxair Technology, Inc. Cryogenic air separation system with high ratio turboexpansion
FR2782544B1 (fr) * 1998-08-19 2005-07-08 Air Liquide Pompe pour un liquide cryogenique ainsi que groupe de pompage et colonne de distillation equipes d'une telle pompe
CN113686099B (zh) * 2021-08-09 2022-08-09 北京科技大学 一种基于内压缩空分储能装置的物质回收方法

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Publication number Priority date Publication date Assignee Title
BE680216A (de) * 1965-05-07 1966-10-28
FR2461906A1 (fr) * 1979-07-20 1981-02-06 Air Liquide Procede et installation cryogeniques de separation d'air avec production d'oxygene sous haute pression
DE3035844A1 (de) * 1980-09-23 1982-05-06 Linde Ag, 6200 Wiesbaden Verfahren und vorrichtung zur gewinnung von sauerstoff mittlerer reinheit
DE3738559A1 (de) * 1987-11-13 1989-05-24 Linde Ag Verfahren zur luftzerlegung durch tieftemperaturrektifikation
FR2651035A1 (fr) * 1989-08-18 1991-02-22 Air Liquide Procede de production d'azote par distillation
US5049173A (en) * 1990-03-06 1991-09-17 Air Products And Chemicals, Inc. Production of ultra-high purity oxygen from cryogenic air separation plants

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE10157544A1 (de) * 2001-11-23 2003-06-12 Messer Ags Gmbh Verfahren und Vorrichtung zur Erzeugung von Stickstoff aus Luft

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JP3436398B2 (ja) 2003-08-11
CA2109148A1 (fr) 1994-04-28
EP0595673A1 (de) 1994-05-04
DE69306362D1 (de) 1997-01-16
FR2697325B1 (fr) 1994-12-23
US5404725A (en) 1995-04-11
DE69306362T2 (de) 1997-06-26
JPH06207776A (ja) 1994-07-26
ES2095019T3 (es) 1997-02-01
FR2697325A1 (fr) 1994-04-29

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