EP0489617B1 - Lufttrennungsverfahren und Anlage zur variablen Herstellung von gasförmigem Sauerstoff - Google Patents

Lufttrennungsverfahren und Anlage zur variablen Herstellung von gasförmigem Sauerstoff Download PDF

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EP0489617B1
EP0489617B1 EP91403174A EP91403174A EP0489617B1 EP 0489617 B1 EP0489617 B1 EP 0489617B1 EP 91403174 A EP91403174 A EP 91403174A EP 91403174 A EP91403174 A EP 91403174A EP 0489617 B1 EP0489617 B1 EP 0489617B1
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Prior art keywords
oxygen
column
liquid
gaseous oxygen
plant
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French (fr)
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EP0489617A1 (de
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Bernard Darredeau
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Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • 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
    • F25J3/04151—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
    • F25J3/042—Division of the main heat exchange line in consecutive sections having different functions having an intermediate feed connection
    • 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
    • F25J3/04363—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 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
    • F25J3/04406—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
    • F25J3/04472—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 the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages
    • F25J3/04496—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 the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist
    • F25J3/04503—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 the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist by exchanging "cold" between at least two different cryogenic liquids, e.g. independently from the main heat exchange line of the air fractionation and/or by using external alternating storage systems
    • F25J3/04509—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 the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist by exchanging "cold" between at least two different cryogenic liquids, e.g. independently from the main heat exchange line of the air fractionation and/or by using external alternating storage systems within the cold part of the air fractionation, i.e. exchanging "cold" within the fractionation and/or main heat exchange line
    • 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/42—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen
    • 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
    • Y10S62/912—External refrigeration system
    • Y10S62/913—Liquified gas
    • 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 present invention relates to the technique of air distillation in a variable regime for the production of gaseous oxygen, by means of a double column installation. It relates firstly to a process of the type in which, when the demand for gaseous oxygen is less than an average value, liquid oxygen is passed from the low pressure column of the double column to a first storage tank for liquid oxygen and liquid nitrogen is sent to the double column from a second liquid nitrogen storage tank, while when the demand for gaseous oxygen is greater than the average value, it is introduced into the column low pressure of the liquid oxygen taken from the first tank and a corresponding quantity of liquid nitrogen is condensed simultaneously, which is sent to the second tank.
  • the object of the invention is to make it possible to improve the average yield of argon, and / or, as a variant, to increase the production of liquid in the installation, in a rocking process.
  • the subject of the invention is a method of the aforementioned type, characterized in that when the oxygen demand is less than the average value, additional liquid oxygen is produced by introducing compressed oxygen to the gaseous state in the heat exchange line of the installation, the flow of liquid nitrogen injected into the double column being correspondingly reduced.
  • the saved liquid nitrogen is sent to the double column when the oxygen demand is lower than the average value; - when the installation includes a main cold-keeping turbine, during periods when the demand for gaseous oxygen is higher (respectively lower) than the average value, the flow of the main turbine is reduced (respectively increased) relative at nominal flow.
  • the invention also relates to an air distillation installation intended for the implementation of the process defined above.
  • This installation of the type comprising a heat exchange line, a scale which comprises a first storage tank for liquid oxygen connected to the low pressure column and a second storage tank for an auxiliary liquid connected to the double column, and a use line delivering gaseous oxygen under high pressure, is characterized in that it comprises a return line in the heat exchange line of a variable flow of gaseous oxygen under high pressure taken from the use pipe, this return pipe being connected to said first tank.
  • the air distillation installation shown in the drawing is intended to supply a variable quantity of gaseous oxygen under high pressure (which can range, for example, up to approximately 15 bars), as well as argon. It is of the double column type with minaret and impure argon production column, with air expansion and with an oxygen / nitrogen rocker.
  • It essentially comprises a medium pressure column 1 surmounted by a low pressure column 2 itself provided at its top with a minaret 3, a column 4 for producing impure argon, a first reservoir 5 of liquid oxygen storage, a second liquid nitrogen storage tank 6, a heat exchange line 7 and an air expansion turbine 8 from medium pressure to low pressure.
  • the medium pressure is around 6 bar absolute and the low pressure slightly higher than atmospheric pressure.
  • the overhead vapor (nitrogen) from column 1 is brought into indirect heat exchange relationship with the tank liquid (oxygen) from column 2 by means of a main vaporizer-condenser 9.
  • Lower lean liquid withdrawn at an intermediate level from column 1 by a line 13, is sub-cooled in the aforementioned sub-cooler, expanded in an expansion valve 14 and sent back into reflux in column 2 at a level corresponding to the base of the minaret 3.
  • Rich liquid consisting of air enriched with oxygen and withdrawn from the tank of column 1 via a pipe 15, is sub-cooled in the aforementioned sub-cooler. Part of this liquid, expanded in an expansion valve 16, is sent under reflux in column 2, and the rest is expanded in an expansion valve 17 then sent to the overhead condenser 18 of column 4 to be vaporized there. , then returned to column 2 via a line 19.
  • the gaseous oxygen produced is drawn off at the base of column 2 via a line 20, heated from the cold end to the hot end of the exchange line 7 and compressed at the high pressure by a compressor 21 discharging into a pipe 20A of use delivering the requested high pressure oxygen.
  • This compressor has a pipe 22 for recycling its outlet to its suction fitted with an expansion valve 23, in order to allow very different flow rates of high pressure gaseous oxygen to be delivered despite the limited flexibility of the compressor.
  • Column 4 is supplied at its base with steam taken from an intermediate level of column 2 by means of a pipe 24 called argon tapping.
  • the tank liquid returns to column 2, at approximately the same level, via a pipe 25.
  • the impure argon produced is withdrawn from the top of column 4 via a pipe 25A.
  • FIG. 1 also shows a pipe 26 for discharging a waste gas W (impure nitrogen) starting from the lower lean liquid injection level of column 2, and a pipe 27 for discharging pure nitrogen low pressure starting from the top of the minaret 3, the pipes 26 and 27 passing through the aforementioned sub-cooler to ensure cooling, then crossing the exchange line 7 from the cold end to the hot end.
  • a waste gas W pure nitrogen
  • the resistance to cold of the installation is ensured by expansion at low pressure of a part of the incoming air, partially cooled, in the turbine 8, and insufflation of this expanded air in the column 2 via a pipe 28.
  • liquid nitrogen is sent from the tank 6, which is approximately at atmospheric pressure, to the top of the minaret 3 by means of a pump 31 and via a pipe 32, in an amount approximately 20% higher than the quantity of liquid oxygen sent to the reservoir 5.
  • This nitrogen is found in gaseous form at the head of the minaret 3, so that an excess of gaseous products is generally sent to the cold end of the exchange line 7 with respect to the nominal step.
  • This excess refrigerant is used to produce additional liquid, as follows.
  • the tank 5 receives the same amount of liquid oxygen as in a conventional scale, but with less draw-off from the tank of the column 2. A corresponding amount of liquid nitrogen from the tank 6 is thus saved during the operation OL .
  • the injection of additional hot gas (high pressure oxygen) into the exchange line has the effect of raising the suction temperature of the turbine 8, for example to its value corresponding to the nominal operation, and therefore to increase its specific cooling capacity.
  • This makes it possible to further increase the production of liquid notably, by simultaneously increasing the flow rate of turbinated air, the extraction yield of argon, in this step, being close to the asymptote and consequently insensitive to this turbine flow rate.
  • the refrigeration balance is balanced by sending liquid nitrogen from the top of the column 1 to the tank 6 via the pipe 11 and a pipe 37 fitted with an expansion valve 38.
  • step OL use is made of the liquid nitrogen reserve constituted in step OL by the liquefaction of high pressure oxygen, by sending a corresponding flow of liquid nitrogen to the top of the minaret 3, via line 32.
  • This additional refrigerating contribution makes it possible to reduce the flow of turbined air accordingly and also creates additional reflux in column 2, which constitutes two factors favorable to distillation at low pressure.
  • the argon extraction yield is increased in the NL market.
  • the energy gain obtained thanks to the invention can be used not only to increase the extraction yield of argon, but also to increase the production of liquid (liquid oxygen or liquid nitrogen) of the installation. .

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

Claims (5)

  1. Lufttrennungsverfahren zur variablen Herstellung von gasförmigem Sauerstoff in einer Anlage mit einer Doppelkolonne (1, 2), bei dem Flüssigsauerstoff aus der Niederdruckkolonne (2) der Doppelkolonne in einen ersten Speicherbehälter (5) für Flüssigsauerstoff eingeleitet und Flüssigstickstoff aus einem zweiten Speicherbehälter (6) für Flüssigstickstoff in die Doppelkolonne (1, 2) eingeleitet wird, wenn der Sauerstoffgasbedarf unter einem Mittelwert liegt, während aus dem ersten Behälter (5) entnommener Flüssigsauerstoff in die Niederdruckkolonne eingeleitet und gleichzeitig eine entsprechende Stickstoffmenge kondensiert wird, die in den zweiten Behälter (6) eingeleitet wird, wenn der Sauerstoffgasbedarf über dem Mittelwert liegt, dadurch gekennzeichnet, daß zusätzlicher Flüssigsauerstoff erzeugt wird, indem gasförmiger komprimierter Sauerstoff in die Wärmetauschereinheit (7) der Anlage eingeleitet wird, wobei der in die Doppelkolonne eingeleitete Flüssigstickstoffstrom entsprechend verringert wird.
  2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß Flüssigstickstoff, der gespeichert wird, wenn der Sauerstoffbedarf kleiner als der Mittelwert ist, in die Doppelkolonne (1, 2) eingeleitet wird, wenn der Sauerstoffgasbedarf größer als der Mittelwert ist.
  3. Verfahren nach Anspruch 2, für eine Anlage mit einer Hauptkühlturbine (8), dadurch gekennzeichnet, daß der Durchfluß der Hauptturbine (8) unter den Nenndurchfluß verringert wird, wenn der Sauerstoffgasbedarf größer als der Mittelwert ist.
  4. Verfahren für eine Anlage mit einer Hauptkühlturbine (8), dadurch gekennzeichnet, daß der Durchfluß der Hauptturbine über den Nenndurchfluß erhöht wird, wenn der Sauerstoffgasbedarf kleiner als der Mittelwert ist.
  5. Lufttrennungsanlage mit einer Doppelkolonne (1, 2) für die Herstellung eines variablen Sauerstoffgasstroms, mit einer Wärmetauschereinheit (7), einem Zwischenspeicherkreis, der einen mit der Niederdruckkolonne (2) verbundenen ersten Speicherbehälter (5) für Flüssigsauerstoff und einen mit der Doppelkolonne verbundenen zweiten Speicherbehälter (6) für eine Hilfsflüssigkeit umfaßt, und einer Verbraucherleitung (20A), die den gasförmigen Sauerstoff unter hohem Druck liefert, dadurch gekennzeichnet, daß sie eine Leitung (33) zur Rückführung eines aus der Verbraucherleitung (20A) entnommenen variablen Sauerstoffgasstroms unter hohem Druck in die Wärmetauschereinheit aufweist, wobei diese Rückführleitung mit dem ersten Behälter (5) verbunden ist.
EP91403174A 1990-12-06 1991-11-25 Lufttrennungsverfahren und Anlage zur variablen Herstellung von gasförmigem Sauerstoff Expired - Lifetime EP0489617B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR9015294A FR2670278B1 (fr) 1990-12-06 1990-12-06 Procede et installation de distillation d'air en regime variable de production d'oxygene gazeux.
FR9015294 1990-12-06

Publications (2)

Publication Number Publication Date
EP0489617A1 EP0489617A1 (de) 1992-06-10
EP0489617B1 true EP0489617B1 (de) 1993-12-22

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EP91403174A Expired - Lifetime EP0489617B1 (de) 1990-12-06 1991-11-25 Lufttrennungsverfahren und Anlage zur variablen Herstellung von gasförmigem Sauerstoff

Country Status (9)

Country Link
US (1) US5209070A (de)
EP (1) EP0489617B1 (de)
JP (1) JP3256250B2 (de)
AU (1) AU643091B2 (de)
CA (1) CA2056915C (de)
DE (1) DE69100838T2 (de)
ES (1) ES2047389T3 (de)
FR (1) FR2670278B1 (de)
ZA (1) ZA919570B (de)

Families Citing this family (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2694383B1 (fr) * 1992-07-29 1994-09-16 Air Liquide Production et installation de production d'azote gazeux à plusieurs puretés différentes.
FR2696821B1 (fr) * 1992-10-09 1994-11-10 Air Liquide Procédé et installation de production d'azote ultra-pur sous pression.
FR2697620B1 (fr) * 1992-10-30 1994-12-23 Air Liquide Procédé et installation de production d'azote gazeux à débit variable.
FR2704632B1 (fr) * 1993-04-29 1995-06-23 Air Liquide Procede et installation pour la separation de l'air.
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US5209070A (en) 1993-05-11
ZA919570B (en) 1992-08-26
AU643091B2 (en) 1993-11-04
CA2056915A1 (fr) 1992-06-07
JPH04283390A (ja) 1992-10-08
JP3256250B2 (ja) 2002-02-12
FR2670278B1 (fr) 1993-01-22
FR2670278A1 (fr) 1992-06-12
CA2056915C (fr) 2002-05-07
DE69100838D1 (de) 1994-02-03
ES2047389T3 (es) 1994-02-16
AU8833691A (en) 1992-06-11
EP0489617A1 (de) 1992-06-10
DE69100838T2 (de) 1994-04-28

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