EP0611218B1 - Procédé et installation de production d'oxygene sous pression - Google Patents
Procédé et installation de production d'oxygene sous pression Download PDFInfo
- Publication number
- EP0611218B1 EP0611218B1 EP94400300A EP94400300A EP0611218B1 EP 0611218 B1 EP0611218 B1 EP 0611218B1 EP 94400300 A EP94400300 A EP 94400300A EP 94400300 A EP94400300 A EP 94400300A EP 0611218 B1 EP0611218 B1 EP 0611218B1
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- EP
- European Patent Office
- Prior art keywords
- pressure
- air
- component
- column
- high pressure
- 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.)
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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
- F25J3/04006—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
- F25J3/04084—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 nitrogen
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- 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
- F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
- F25J3/04018—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of main feed air
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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
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
- F25J3/04024—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of purified feed air, so-called boosted air
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- 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
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- 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
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- 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
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- F25J3/04109—Arrangements of compressors and /or their drivers
- F25J3/04145—Mechanically coupling of different compressors of the air fractionation process to the same driver(s)
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- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
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- F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
- F25J3/04175—Hot end purification of the feed air by adsorption of the impurities at a pressure of substantially more than the highest pressure column
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- 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
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- 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
- F25J3/04236—Integration of different exchangers in a single core, so-called integrated cores
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- 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
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- 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
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- 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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- 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
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- 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
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- 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
- F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
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- 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
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- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
- F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
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- F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
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- F25J2270/00—Refrigeration techniques used
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- 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
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- 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
- Y10S62/94—High pressure column
Definitions
- EP-A-0 504 029 describes a method of this type in which the fraction of air that is overpressed at the second high pressure is constituted by a very low air flow, the only function of which is to provide calories near intake temperature of the turbine which relaxes the fraction of air not overpressed.
- the object of the invention is to improve this known process in order to increase performance thermodynamics without increasing the corresponding investment.
- the subject of the invention is a process of the aforementioned type, characterized by the part Characterizing of claim 1.
- the air distillation system shown in Figure 1 essentially comprises: a air compressor 1; an air cleaning device 2 compressed into water and C02 by adsorption, this device comprising two adsorption bottles 2A, 2B, one of which works in adsorption while the other is in progress regeneration; a fan-blower assembly 3 comprising an expansion turbine 4 and a blower or blower 5 whose shafts are coupled, the blower possibly being equipped with a refrigerant (not represented); a heat exchanger 6 constituting the installation heat exchange line; a double distillation column 7 comprising a medium column pressure 8 surmounted by a low pressure column 9, with a vaporizer-condenser 10 putting the overhead vapor (nitrogen) from column 8 in heat exchange relationship with the tank liquid (oxygen) of column 9; a liquid oxygen tank 11, the bottom of which is connected to a liquid oxygen pump 12; and a nitrogen tank liquid 13, the bottom of which is connected to a nitrogen pump liquid 14.
- This facility is intended to provide, via a line 15, gaseous oxygen under a high predetermined pressure, which can be between a few bars and a few dozen bars (in the present brief, the pressures considered are absolute pressures).
- liquid oxygen drawn from the column 9 tank via line 16 and stored in the reservoir 11 is brought to high pressure by the pump 12 in the liquid state, then vaporized and reheated under this high pressure in passages 17 of the exchanger 6.
- the heat necessary for this vaporization and to this reheating, as well as to reheating and possibly vaporization of other fluids drawn from the double column, is supplied by the air to be distilled, in the following conditions.
- All of the air to be distilled is compressed by compressor 1 at a first high pressure significantly higher than the average column pressure 8, in practice greater than 9 bars. Then the air, precooled in 18 and cooled to around temperature room in 19, is purified in one, 2A for example, adsorption bottles, and divided into two fractions.
- the first fraction representing at least 70% of the treated air flow, is boosted a second time high pressure by the booster 5, which is driven by the turbine 4.
- the first fraction of air is then introduced at the hot end of the exchanger 6 and cooled in all up to an intermediate temperature. At this temperature, a fraction of the air continues to cool and is liquefied in passages 20 of the exchanger and then is relaxed at low pressure in an expansion valve 21 and introduced at a level intermediate in column 9. The rest of the air is expanded at medium pressure in turbine 4 then sent directly, via a line 22, to the base of the column 8.
- the second fraction is introduced under the first high pressure in exchange line 6, cooled and liquefied to the cold end of it in passages 20A, expanded in an expansion valve 21A and connected to the current from the expansion valve 21.
- this air pressure is the condensation pressure of the air by exchange of heat with oxygen being vaporized under the high pressure, i.e. the pressure for which the knee G of liquefaction of one of the two fractions of air, on the heat exchange diagram (temperatures on the abscissa, quantities of heat exchanged on the ordinate) is located slightly to the right of the vertical landing P of vaporization of oxygen under high pressure ( Figure 2).
- the temperature difference at the hot end of the exchange line is adjusted by means of turbine 4, of which the suction temperature is indicated in A.
- the diagram in Figure 2 corresponds to following numerical values: first high pressure : 24.5 bars; high oxygen pressure: 10 bars; second high pressure: 31 bars; second fraction of air: 28% incoming flow; fraction liquefied in 20: very low; liquid production: 40% of the amount of oxygen separate.
- the diagram in Figure 3 corresponds to following numerical values: first high pressure: 28.5 bars; purification temperature: + 12 ° C; second air fraction: 11% of the incoming flow; second high pressure: 36.4 bars; fraction relaxed in 4 to 5.7 bars: 77% of the incoming flow; liquefied fraction in 20: 12% of incoming air flow; high oxygen pressure: 40 bars; liquid production: 35% of the amount of oxygen separate.
- the air from of the turbine 4 is sent to a separator pot 35.
- the resulting liquid phase is sent directly to the column 8, while the gas phase is, after partial heating in the heat exchange line, expanded at low pressure in a second turbine 36 fitted with an appropriate brake 37, then blown into the column 9.
- This variant allows either to produce impure oxygen under good energy conditions thanks to the increased production of liquid which results from the presence of the second turbine, i.e. increase liquid production at the expense of amount of oxygen separated, or producing only liquid oxygen.
- an air flow can be taken between the precooler 38 and blower 5 and sent via a line 39 in other passages 20B of the line heat exchange, therefore at a pressure intermediate between the first and second highs pressures.
- the installation can generate gaseous oxygen and / or nitrogen gas under at least two different pressures, as explained in the aforementioned EP-A-0 504 029.
- blower 5 Possibly a small part of the air from blower 5 can be overpressed again by a second blower (not shown), for example coupled to the turbine 36 of Figure 5, before being cooled and liquefied in the heat exchange line, according to the teaching of the request FR 91 15 935.
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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)
Description
- la Figure 1 représente schématiquement une installation conforme à l'invention;
- la Figure 2 est un diagramme d'échange thermique, obtenu par calcul, correspondant à l'installation de la Figure 1, dans un premier mode de fonctionnement de cette installation; sur ce diagramme, on a porté en abscisses les températures, en degrés Celsius, et en ordonnées les quantités de chaleur échangées;
- la Figure 3 est un diagramme analogue à celui de la Figure 2 mais correspondant à un autre mode de fonctionnement de l'installation de la Figure 1; et
- les Figures 4 à 6 sont des vues analogues à la Figure 1 représentant respectivement trois variantes.
Claims (10)
- Procédé de production d'oxygène gazeux sous une haute pression d'oxygène par distillation d'air dans une installation à double colonne (7) comprenant une colonne moyenne pression (8) qui fonctionne sous une pression dite moyenne pression, et une colonne basse pression (9) qui fonctionne sous une pression dite basse pression, pompage (en 12) d'oxygène liquide soutiré en cuve de la colonne basse pression (9), et vaporisation (en 6) de l'oxygène liquide comprimé par échange de chaleur avec de l'air dans une ligne d'échange thermique (6) de l'installation, procédé dans lequel :on comprime la totalité de l'air à distiller, au moyen d'un compresseur d'air principal (1) de l'installation, jusqu'à une première haute pression nettement supérieure à la moyenne pression, et on la divise en une première et une seconde fractions;on surpresse ladite première fraction jusqu'à une seconde haute pression; eton refroidit au moins l'essentiel de ladite première fraction dans la ligne d'échange thermique jusqu'à une température intermédiaire, à laquelle une partie est détendue dans une première turbine (4) à la moyenne pression puis introduite dans la colonne moyenne pression (8), tandis que le reste poursuit son refroidissement et est liquéfié, détendu dans une vanne de détente (21) et introduit dans la double colonne (7);
- Procédé suivant la revendication 1, caractérisé en ce qu'on détend dans une seconde turbine (36), jusqu'à la basse pression, la fraction gazeuse de l'air issu de la première turbine (4), cette fraction gazeuse étant partiellement réchauffée avant sa détente dans la seconde turbine et l'échappement de cette dernière étant insufflé dans la colonne basse pression (9), éventuellement après refroidissement.
- Procédé suivant la revendication 1 ou 2, caractérisé en ce qu'on amène l'air à la première haute pression au moyen d'une partie seulement des étages du compresseur d'air (1), on épure l'air en eau et en anhydrique carbonique (en 2) à cette première haute pression, puis on comprime ladite première fraction au moyen du ou des derniers étages de ce compresseur.
- Procédé suivant la revendication 3, caractérisé en ce qu'on surpresse au moins une partie de l'air sortant du dernier étage du compresseur (1) au moyen d'une soufflante (5) couplée à la première turbine (4).
- Procédé suivant l'une quelconque des revendications 1 à 4, caractérisé en ce qu'on prérefroidit ladite seconde fraction au moyen d'un groupe frigorifique (6A) avant de l'introduire dans la ligne d'échange thermique (6).
- Installation de production d'oxygène gazeux sous une haute pression d'oxygène , du type comprenant un compresseur d'air principal (1), une double colonne de distillation d'air (7) comprenant une colonne moyenne pression (8) qui fonctionne sous une pression dite moyenne pression, et une colonne basse pression (9) qui fonctionne sous une pression dite basse pression (7), une pompe (12) de compression d'oxygène liquide soutiré en cuve de la colonne basse pression (9), des moyens (1, 5) pour amener une fraction de l'air à distiller à une haute pression d'air, et une ligne d'échange thermique (6), caractérisée en ce que :lesdits moyens sont agencés pour amener la totalité de l'air à distiller à une première haute pression nettement supérieure à la moyenne pression, et comprennent des moyens (5) pour surpresser une première fraction de cet air, représentant au moins 70% du débit d'air traité, jusqu'à une seconde haute pression;la ligne d'échange thermique (6) comprend des moyens pour refroidir ladite première fraction jusqu'à une température intermédiaire et pour refroidir plus avant et liquéfier une partie de cette première fraction, et des moyens (20A, 20B) pour refroidir et liquéfier l'air non surpressé à la seconde haute pression, en un ou plusieurs flux à ladite première haute pression ou à une ou plusieurs pressions comprises entre ladite première haute pression et ladite seconde haute pression; etl'installation comprend une turbine (4) de détente dont l'aspiration est reliée aux passages de refroidissement d'air sous la seconde haute pression, en un point intermédiaire de la ligne d'échange thermique (6), et dont l'échappement est relié à la colonne moyenne pression (8).
- Installation suivant la revendication 6, caractérisée en ce qu'elle comprend une seconde turbine (36) de détente à la basse pression d'une partie au moins de l'air issu de la première turbine (4).
- Installation suivant la revendication 6 ou 7, caractérisée en ce que ladite seconde fraction est issue d'un étage intermédiaire du compresseur d'air principal (1), la première fraction étant, après épuration en eau et en anhydrique carbonique (en 2), réintroduite dans ce compresseur.
- Installation suivant la revendication 8, caractérisée en ce qu'elle comprend une soufflante (5) couplée à la première turbine (4) et dont l'aspiration est reliée au refoulement du dernier étage du compresseur d'air principal (1).
- Installation suivant l'une quelconque des revendications 6 à 9, caractérisée en ce qu'elle comprend un groupe frigorifique (6A) de prérefroidissement de ladite seconde fraction d'air en amont de la ligne d'échange thermique (6).
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR9301622 | 1993-02-12 | ||
FR9301622A FR2701553B1 (fr) | 1993-02-12 | 1993-02-12 | Procédé et installation de production d'oxygène sous pression. |
Publications (3)
Publication Number | Publication Date |
---|---|
EP0611218A1 EP0611218A1 (fr) | 1994-08-17 |
EP0611218B1 true EP0611218B1 (fr) | 1998-11-04 |
EP0611218B2 EP0611218B2 (fr) | 2002-08-07 |
Family
ID=9444023
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP94400300A Expired - Lifetime EP0611218B2 (fr) | 1993-02-12 | 1994-02-11 | Procédé et installation de production d'oxygene sous pression |
Country Status (10)
Country | Link |
---|---|
US (1) | US5426947A (fr) |
EP (1) | EP0611218B2 (fr) |
JP (1) | JPH06241650A (fr) |
CN (1) | CN1101924C (fr) |
AU (1) | AU660385B2 (fr) |
CA (1) | CA2115399C (fr) |
DE (1) | DE69414282T3 (fr) |
ES (1) | ES2124856T5 (fr) |
FR (1) | FR2701553B1 (fr) |
ZA (1) | ZA94968B (fr) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE102012017488A1 (de) | 2012-09-04 | 2014-03-06 | Linde Aktiengesellschaft | Verfahren zur Erstellung einer Luftzerlegungsanlage, Luftzerlegungsanlage und zugehöriges Betriebsverfahren |
Families Citing this family (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE19815885A1 (de) * | 1998-04-08 | 1999-10-14 | Linde Ag | Verfahren und Vorrichtung zur Erzeugung von gasförmigem Druckprodukt bei der Tieftemperaturzerlegung von Luft |
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 |
FR2828273A1 (fr) * | 2001-07-31 | 2003-02-07 | Air Liquide | Procede d'alimentation en air epure d'une unite de distillation d'air cryogenique et installation de mise en oeuvre de ce procede |
US7437890B2 (en) * | 2006-01-12 | 2008-10-21 | Praxair Technology, Inc. | Cryogenic air separation system with multi-pressure air liquefaction |
US7487648B2 (en) * | 2006-03-10 | 2009-02-10 | Praxair Technology, Inc. | Cryogenic air separation method with temperature controlled condensed feed air |
FR2928446A1 (fr) * | 2008-03-10 | 2009-09-11 | Air Liquide | Procede de modification d'un appareil de separation d'air par distillation cryogenique |
DE102009048456A1 (de) * | 2009-09-21 | 2011-03-31 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft |
Family Cites Families (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
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 |
JPS62102074A (ja) * | 1985-10-30 | 1987-05-12 | 株式会社日立製作所 | ガス分離方法及び装置 |
FR2652409A1 (fr) † | 1989-09-25 | 1991-03-29 | Air Liquide | Procede de production frigorifique, cycle frigorifique correspondant et leur application a la distillation d'air. |
US5148680A (en) † | 1990-06-27 | 1992-09-22 | Union Carbide Industrial Gases Technology Corporation | Cryogenic air separation system with dual product side condenser |
FR2674011B1 (fr) * | 1991-03-11 | 1996-12-20 | Maurice Grenier | Procede et installation de production d'oxygene gazeux sous pression. |
JP2909678B2 (ja) * | 1991-03-11 | 1999-06-23 | レール・リキード・ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード | 圧力下のガス状酸素の製造方法及び製造装置 |
FR2695714B1 (fr) † | 1992-09-16 | 1994-10-28 | Maurice Grenier | Installation de traitement cryogénique, notamment de distillation d'air. |
-
1993
- 1993-02-12 FR FR9301622A patent/FR2701553B1/fr not_active Expired - Fee Related
-
1994
- 1994-01-27 US US08/186,844 patent/US5426947A/en not_active Expired - Lifetime
- 1994-02-07 JP JP6013677A patent/JPH06241650A/ja active Pending
- 1994-02-08 CN CN94101375A patent/CN1101924C/zh not_active Expired - Fee Related
- 1994-02-10 CA CA002115399A patent/CA2115399C/fr not_active Expired - Fee Related
- 1994-02-11 ZA ZA94968A patent/ZA94968B/xx unknown
- 1994-02-11 DE DE69414282T patent/DE69414282T3/de not_active Expired - Fee Related
- 1994-02-11 AU AU55060/94A patent/AU660385B2/en not_active Ceased
- 1994-02-11 EP EP94400300A patent/EP0611218B2/fr not_active Expired - Lifetime
- 1994-02-11 ES ES94400300T patent/ES2124856T5/es not_active Expired - Lifetime
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE102012017488A1 (de) | 2012-09-04 | 2014-03-06 | Linde Aktiengesellschaft | Verfahren zur Erstellung einer Luftzerlegungsanlage, Luftzerlegungsanlage und zugehöriges Betriebsverfahren |
Also Published As
Publication number | Publication date |
---|---|
FR2701553A1 (fr) | 1994-08-19 |
CA2115399A1 (fr) | 1994-08-13 |
EP0611218B2 (fr) | 2002-08-07 |
AU5506094A (en) | 1994-08-18 |
CN1100514A (zh) | 1995-03-22 |
DE69414282T3 (de) | 2003-03-20 |
DE69414282D1 (de) | 1998-12-10 |
AU660385B2 (en) | 1995-06-22 |
CA2115399C (fr) | 2005-04-26 |
DE69414282T2 (de) | 1999-06-17 |
ES2124856T3 (es) | 1999-02-16 |
FR2701553B1 (fr) | 1995-04-28 |
EP0611218A1 (fr) | 1994-08-17 |
CN1101924C (zh) | 2003-02-19 |
JPH06241650A (ja) | 1994-09-02 |
US5426947A (en) | 1995-06-27 |
ES2124856T5 (es) | 2003-03-01 |
ZA94968B (en) | 1994-08-24 |
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