EP0677713B1 - Verfahren und Vorrichtung zur Herstellung von Sauerstoff durch Rektifikation von Luft - Google Patents

Verfahren und Vorrichtung zur Herstellung von Sauerstoff durch Rektifikation von Luft Download PDF

Info

Publication number
EP0677713B1
EP0677713B1 EP95400752A EP95400752A EP0677713B1 EP 0677713 B1 EP0677713 B1 EP 0677713B1 EP 95400752 A EP95400752 A EP 95400752A EP 95400752 A EP95400752 A EP 95400752A EP 0677713 B1 EP0677713 B1 EP 0677713B1
Authority
EP
European Patent Office
Prior art keywords
column
pressure column
low
argon
air
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
EP95400752A
Other languages
English (en)
French (fr)
Other versions
EP0677713A1 (de
Inventor
Yves Koeberle
Philippe Fraysse
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.)
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
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Publication of EP0677713A1 publication Critical patent/EP0677713A1/de
Application granted granted Critical
Publication of EP0677713B1 publication Critical patent/EP0677713B1/de
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

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
    • F25J3/04006—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
    • F25J3/04103—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 using solely hydrostatic liquid head
    • 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
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
    • F25J2200/92—Details relating to the feed point
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/58—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
    • F25J2250/40—One fluid being 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
    • 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
    • F25J2250/50—One fluid being oxygen

Definitions

  • the present invention relates to a method and an installation for oxygen and argon production by air distillation and more particularly to a process and an installation for the production of oxygen under pressure and argon.
  • EP-A-0422974 describes a process for producing oxygen under pressure by cryogenic air distillation in a double column.
  • Oxygen liquid is withdrawn from the tank of the low pressure column 7, as illustrated in Figure 1, and vaporizes in the auxiliary exchanger 9 by heat exchange with a fraction of the supply air.
  • the remaining part of the air feed is divided into two flow rates, one of which goes directly to the column medium pressure 6, via line 14, and the other of which is relaxed in a turbine 4 before being sent to the low pressure column 7.
  • EP-A-0580348 describes a process in which rich liquid is sent from a medium pressure column to a low pressure column in two fractions, one of which vaporizes at the head of an argon column before being injected into the low pressure column.
  • An object of this invention is to improve the argon yields if the installation also includes an argon column supplied by the low pressure column.
  • the subject of the invention is a process for the production of oxygen. gas and argon according to claim 1.
  • the rich medium pressure medium liquid first, second and a third fractions and we send the first and second fractions to different levels in the low pressure column after sub-cooling prior.
  • the third fraction is sent to the head condenser of the argon column. This notably makes it possible to significantly improve the extraction argon.
  • the first and second fractions can be sent to the low pressure column at different temperatures, in order to improve again the reflux in the low pressure column and the argon extraction in the case where the installation also includes an argon column.
  • part of the supply air is expanded before to be sent to the double column, the remaining part of the supply air being partially condensed in the auxiliary exchanger.
  • the temperature difference in the auxiliary exchanger can be reduced to an average value of 0.6 ° C.
  • the invention also relates to a production installation according to claim 6.
  • EP-A-422,974 send some of the condensed air to the medium pressure column, a few trays above the tank so that she can participate in the less weakly, on distillation in this column.
  • the installation represented in FIG. 1 essentially comprises a main air compressor 1 with variable flow, for example of the type centrifugal with movable blades, an air blower with movable blades 2, a heat exchange line 3, a turbine 4 for maintaining cold, a air distillation apparatus 5 consisting of a double column comprising itself a medium pressure column 6 surmounted by a low column pressure 7 and a minaret 7A, a vaporizer-condenser 8, a heat exchanger auxiliary heat 9 and a pump 10.
  • This installation is intended for produce a variable flow of gaseous oxygen via a line 12, under a pressure higher than atmospheric pressure.
  • the first overpressed fraction is cooled to the neighborhood from its dew point in passages of the exchange line then condensed in the auxiliary exchanger 9 and is divided into a first flow constant relaxed under 6 bar sent to the medium pressure column via a pipe 16, and a second constant relaxed flow towards 1 bar in a expansion valve 13 then injected into the low pressure column 7.
  • the vaporizer-condenser 8 vaporizes a constant flow of oxygen liquid in the low pressure column tank by condensation of a flow at about equal to nitrogen at the head of the medium pressure column.
  • Some cash rich "(oxygen-enriched air) taken from the bottom of the middle column pressure and expanded to around 1 bar in an expansion valve 18a is injected at an intermediate level of the low pressure column, and of the "lean liquid” (almost pure nitrogen) taken from the top of the medium pressure column and expanded to around 1 bar in an expansion valve 19 is injected at the top of the low pressure column.
  • Liquid nitrogen is injected at the top of the 7A minaret through the expansion valve 21. Pure nitrogen is withdrawn from the top of the minaret 7A and sent to exchange line 3 to be reheated there before exiting by the line 20. The impure nitrogen leaves via line 25 from the top of the column low pressure 7 and is sent outside via line 18.
  • Liquid oxygen withdrawn from the lower column tank pressure 7 is pumped to production pressure before being sprayed into the auxiliary exchanger 9 (constituted by a “film” type vaporizer) by heat exchange with partially condensed air. Oxygen vaporized comes out, after heating in the exchange line 3, by the driving 12.
  • argon a fraction rich in argon is drawn off from the lower part of the low pressure column 7 and is sent to the column of argon 16 for distillation.
  • This fraction includes mainly argon and oxygen.
  • the tank liquid resulting from the distillation in column 16 is returned to the bottom of the low pressure column 7.
  • the overhead condenser 29 of the argon column 16 is cooled by rich liquid from the medium column tank pressure 6, relieved by valve 23, vaporized and sent to the lower column pressure.
  • valve 18a The remaining part of the rich liquid from the column tank medium pressure 6 is relieved by the valve 18a at a pressure slightly above atmospheric pressure and sent to the bottom column pressure 7 by valve 18, substantially at the same level as the level injection of the air expanded by the turbine 4 (the blowing air).
  • the remaining part of rich liquid not vaporized in 29 is divided into two fractions: one first fraction is injected, as shown in Figure 1, after expansion by valve 18 in the low pressure column 7 at the air blast and the second fraction of rich liquid is sent to the low pressure column 7, after expansion to the pressure thereof by the valve 17, at an intermediate level between the injection level of the first fraction of rich liquid through valve 18a and the level of withdrawal of nitrogen through line 25.
  • the variant of Figure 3 has only one compressor air 1, all the compressed air being sent either to turbine 4 or to exchanger 9.
  • the partially condensed air in exchanger 9 passes entirely in the tank of the medium pressure column 6.
  • the difference in level between the level of liquid oxygen in the BP column tank and its inlet in the fixed vaporizer 9, in this case, the vaporization pressure of oxygen; the pump 10 in Figure 2 is therefore deleted.
  • the fractions of rich liquid can be sub-cooled so that the temperature of the fraction injected at the level of insufflation of air is lower than that of the fraction injected at the level intermediate.
  • This arrangement of the exchanger 9 allows a gain of approximately 6% on the compression of the air and therefore on the specific energy of oxygen product.

Landscapes

  • 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)
  • Oxygen, Ozone, And Oxides In General (AREA)

Claims (7)

  1. Verfahren zur Herstellung von unter Druck stehendem gasförmigem Sauerstoff und von Argon durch Tieftemperaturdestillation von Luft in einer Doppelsäule (5) mit einer Mitteldrucksäule (6) und einer Niederdrucksäule (7), bei dem man die aus dem Sumpf der Mitteldrucksäule stammende angereicherte Flüssigkeit in eine erste und eine zweite flüssige Fraktion aufteilt und diese in unterschiedlichen Höhen der Niederdrucksäule (7) zuführt, aus der Niederdrucksäule (7) ein mit Argon angereichertes Fluid abzieht, dieses in einer Argonsäule (16) destilliert und Argon am Kopf der Argonsäule abzieht, aus einem unteren Teil der Niederdrucksäule eine mit Sauerstoff angereicherte Flüssigkeit abzieht, diese verdichtet und durch Wärmeaustausch mit der der Doppelsäule (5) zuströmenden Luft zur Erzeugung von unter Druck stehendem gasförmigem Sauerstoff verdampft, und dem Kondensator am Kopf der Argonsäule eine dritte Fraktion der angereicherten Flüssigkeit zuführt, wo sie vor der Zuführung zur Niederdrucksäule (7) in einer dritten Höhe verdampft, wobei die unterschiedlichen Höhen unter einer Abzugshöhe von unreinem Stickstoff aus der Niederdrucksäule (7) liegen.
  2. Verfahren nach Anspruch 1, bei dem man die erste und die zweite Fraktion vor der Zuführung zur Niederdrucksäule (7) auf unterschiedliche Temperaturen abkühlt.
  3. Verfahren nach Anspruch 1 oder 2, bei dem man einen Teil der zugeführten Luft in einer mittleren Höhe der Niederdrucksäule (7) einspeist und die Einspeisungshöhen der ersten und der zweiten Fraktion der angereicherten Flüssigkeit nicht unter dieser mittleren Höhe liegen.
  4. Verfahren nach Anspruch 3, bei dem man der Niederdrucksäule (7) eine Fraktion der angereicherten Flüssigkeit etwa in der gleichen Höhe wie die eingespeiste Luft zuführt.
  5. Anlage zur Herstellung von unter Druck stehendem gasförmigem Sauerstoff und von Argon durch Tieftemperaturdestillation von Luft, mit einer Doppelsäule (5) aus mindestens einer Mitteldrucksäule (6), einer darüber angeordneten Niederdrucksäule (7) und einer Argondestillationssäule, Mitteln (25) zum Abziehen von unreinem Stickstoff aus der Niederdrucksäule, Mitteln (12) zum Abziehen einer mit Sauerstoff angereicherten Flüssigkeit aus dem unteren Teil der Niederdrucksäule (7), zu deren Verdichtung (10) und zu deren Verdampfung (9) gegen der Doppelsäule zuströmende Luft zur Erzeugung von unter Druck stehendem gasförmigem Sauerstoff, und Mitteln zum Abziehen von Argon am Kopf der Argondestillationssäule, Mitteln zum Abziehen der angereicherten Flüssigkeit aus dem Sumpf der Mitteldrucksäule (6) und zur Zuführung der angereicherten Flüssigkeit zur Niederdrucksäule (7) in drei unterschiedlichen Höhen, die unterhalb der Abzugshöhe von unreinem Stickstoff liegen, und Leitungen zur Zuführung der angereicherten Flüssigkeit in zwei unterschiedlichen Höhen ohne Durchgang durch den Kondensator am Kopf der Argondestillationssäule und zur Zuführung einer dritten Fraktion der angereicherten Flüssigkeit zum Kondensator am Kopf der Argondestillationssäule, zu deren Verdampfung und zu deren Zuführung in der dritten Höhe der Niederdrucksäule.
  6. Anlage nach Anspruch 5 mit Mitteln zur Zuführung der angereicherten Flüssigkeit zur Niederdrucksäule (7) bei zwei unterschiedlichen Temperaturen.
  7. Anlage nach Anspruch 5 oder 6 mit Mitteln (4) zur Zuführung von Luft zur Niederdrucksäule (7) in einer mittleren Höhe und Mitteln zur Zuführung der beiden Fraktionen der angereicherten Flüssigkeit in Höhen in der Nähe der mittleren Höhe oder darüber.
EP95400752A 1994-04-12 1995-04-04 Verfahren und Vorrichtung zur Herstellung von Sauerstoff durch Rektifikation von Luft Expired - Lifetime EP0677713B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR9404298A FR2718518B1 (fr) 1994-04-12 1994-04-12 Procédé et installation pour la production de l'oxygène par distillation de l'air.
FR9404298 1994-04-12

Publications (2)

Publication Number Publication Date
EP0677713A1 EP0677713A1 (de) 1995-10-18
EP0677713B1 true EP0677713B1 (de) 1999-10-20

Family

ID=9461989

Family Applications (1)

Application Number Title Priority Date Filing Date
EP95400752A Expired - Lifetime EP0677713B1 (de) 1994-04-12 1995-04-04 Verfahren und Vorrichtung zur Herstellung von Sauerstoff durch Rektifikation von Luft

Country Status (7)

Country Link
US (1) US5586451A (de)
EP (1) EP0677713B1 (de)
JP (1) JPH0854181A (de)
CN (1) CN1121172A (de)
CA (1) CA2146831A1 (de)
DE (1) DE69512821T2 (de)
FR (1) FR2718518B1 (de)

Families Citing this family (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB9807833D0 (en) 1998-04-09 1998-06-10 Boc Group Plc Separation of air
US6178775B1 (en) * 1998-10-30 2001-01-30 The Boc Group, Inc. Method and apparatus for separating air to produce an oxygen product
GB9910701D0 (en) 1999-05-07 1999-07-07 Boc Group Plc Separation of air
GB9925097D0 (en) * 1999-10-22 1999-12-22 Boc Group Plc Air separation
US6253576B1 (en) * 1999-11-09 2001-07-03 Air Products And Chemicals, Inc. Process for the production of intermediate pressure oxygen
EP1338856A3 (de) * 2002-01-31 2003-09-10 L'AIR LIQUIDE, Société Anonyme à Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Verfahren und Vorrichtung zur Zerlegung von Luft durch Tieftemperaturdestillation
FR2854232A1 (fr) * 2003-04-23 2004-10-29 Air Liquide Procede de distillation d'air pour produire de l'argon
FR2864214B1 (fr) * 2003-12-22 2017-04-21 Air Liquide Appareil de separation d'air, appareil integre de separation d'air et de production d'un metal et procede de demarrage d'un tel appareil de separation d'air
US20070095100A1 (en) * 2005-11-03 2007-05-03 Rankin Peter J Cryogenic air separation process with excess turbine refrigeration
US9279613B2 (en) 2010-03-19 2016-03-08 Praxair Technology, Inc. Air separation method and apparatus
CN105115244B (zh) * 2015-08-10 2017-06-27 开封空分集团有限公司 一种低纯度氧空气分离的装置及方法

Family Cites Families (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR1253717A (fr) * 1960-04-08 1961-02-10 Union Carbide Corp Séparation à basse température de l'air en oxygène, azote et argon
DE1112997B (de) * 1960-08-13 1961-08-24 Linde Eismasch Ag Verfahren und Einrichtung zur Gaszerlegung durch Rektifikation bei tiefer Temperatur
US4737177A (en) * 1986-08-01 1988-04-12 Erickson Donald C Air distillation improvements for high purity oxygen
GB8820582D0 (en) * 1988-08-31 1988-09-28 Boc Group Plc Air separation
FR2655137B1 (fr) * 1989-11-28 1992-10-16 Air Liquide Procede et installation de distillation d'air avec production d'argon.
US4994098A (en) * 1990-02-02 1991-02-19 Air Products And Chemicals, Inc. Production of oxygen-lean argon from air
US5076823A (en) * 1990-03-20 1991-12-31 Air Products And Chemicals, Inc. Process for cryogenic air separation
GB9008752D0 (en) * 1990-04-18 1990-06-13 Boc Group Plc Air separation
US5228296A (en) * 1992-02-27 1993-07-20 Praxair Technology, Inc. Cryogenic rectification system with argon heat pump
US5275003A (en) * 1992-07-20 1994-01-04 Air Products And Chemicals, Inc. Hybrid air and nitrogen recycle liquefier

Also Published As

Publication number Publication date
EP0677713A1 (de) 1995-10-18
CA2146831A1 (fr) 1995-10-13
DE69512821T2 (de) 2000-05-25
JPH0854181A (ja) 1996-02-27
US5586451A (en) 1996-12-24
CN1121172A (zh) 1996-04-24
DE69512821D1 (de) 1999-11-25
FR2718518B1 (fr) 1996-05-03
FR2718518A1 (fr) 1995-10-13

Similar Documents

Publication Publication Date Title
EP0689019B1 (de) Verfahren und Einrichtung zur Herstellung von gasförmigem Drucksauerstoff
EP0576314B2 (de) Verfahren und Apparat zur Herstelling von gasförmigem Sauerstoff unter Druck
EP0547946B2 (de) Verfahren zur Herstellung unreinen Sauerstoffs
EP0618415B1 (de) Verfahren und Vorrichtung zur Herstellung von gasförmigem Sauerstoff und/oder gasförmigem Stickstoff unter Druck durch Zerlegung von Luft
EP0677713B1 (de) Verfahren und Vorrichtung zur Herstellung von Sauerstoff durch Rektifikation von Luft
EP0694746B1 (de) Verfahren zur Herstellung von Druckgas mit variabelen Mengen
CA2056915C (fr) Procede et installation de distillation d'air en regime variable de production d'oxygene gazeux
EP0606027A1 (de) Lufttrennungsverfahren und Anlage zur Herstellung von wenigstens ein Druckgasprodukt und von wenigstens eine Flüssigkeit
EP0641983B1 (de) Verfahren und Einrichtung zur Herstellung von gasförmigem Sauerstoff und/oder Stickstoff unter Druck
EP0611218B2 (de) Verfahren und Anlage zur Herstellung von Drucksauerstoff
FR2688052A1 (fr) Procede et installation de production d'oxygene et/ou d'azote gazeux sous pression par distillation d'air.
FR2724011A1 (fr) Procede et installation de production d'oxygene par distillation cryogenique
EP0612967B1 (de) Verfahren zur Herstellung von Sauerstoff und/oder Stickstoff unter Druck
EP3058297A2 (de) Verfahren und vorrichtung zur trennung von luft durch kryogene destillation
EP1132700B1 (de) Verfahren und Vorrichtung zur kryogenischen Luftzerlegung
EP0641982A1 (de) Verfahren und Einrichtung zur Herstellung von wenigstens einem Gas aus Druckluft
CA2109148A1 (fr) Procede et installation de production d'azote et d'oxygene
FR2929697A1 (fr) Procede de production d'azote gazeux variable et d'oxygene gazeux variable par distillation d'air
EP1063485B1 (de) Vorrichtung und Verfahren zur Luftzerlegung durch Tieftemperaturrektifikation

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): DE FR GB IT

17P Request for examination filed

Effective date: 19960418

17Q First examination report despatched

Effective date: 19970818

GRAG Despatch of communication of intention to grant

Free format text: ORIGINAL CODE: EPIDOS AGRA

GRAG Despatch of communication of intention to grant

Free format text: ORIGINAL CODE: EPIDOS AGRA

GRAG Despatch of communication of intention to grant

Free format text: ORIGINAL CODE: EPIDOS AGRA

GRAH Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOS IGRA

GRAH Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOS IGRA

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): DE FR GB IT

REF Corresponds to:

Ref document number: 69512821

Country of ref document: DE

Date of ref document: 19991125

ITF It: translation for a ep patent filed
GBT Gb: translation of ep patent filed (gb section 77(6)(a)/1977)

Effective date: 19991222

PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

26N No opposition filed
PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: FR

Payment date: 20010312

Year of fee payment: 7

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: GB

Payment date: 20010319

Year of fee payment: 7

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DE

Payment date: 20010321

Year of fee payment: 7

REG Reference to a national code

Ref country code: GB

Ref legal event code: IF02

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GB

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20020404

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: DE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20021101

GBPC Gb: european patent ceased through non-payment of renewal fee

Effective date: 20020404

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: FR

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20021231

REG Reference to a national code

Ref country code: FR

Ref legal event code: ST

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: IT

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES;WARNING: LAPSES OF ITALIAN PATENTS WITH EFFECTIVE DATE BEFORE 2007 MAY HAVE OCCURRED AT ANY TIME BEFORE 2007. THE CORRECT EFFECTIVE DATE MAY BE DIFFERENT FROM THE ONE RECORDED.

Effective date: 20050404