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EP0611218B2 - Procédé et installation de production d'oxygene sous pression - Google Patents

Procédé et installation de production d'oxygene sous pression Download PDF

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Publication number
EP0611218B2
EP0611218B2 EP94400300A EP94400300A EP0611218B2 EP 0611218 B2 EP0611218 B2 EP 0611218B2 EP 94400300 A EP94400300 A EP 94400300A EP 94400300 A EP94400300 A EP 94400300A EP 0611218 B2 EP0611218 B2 EP 0611218B2
Authority
EP
European Patent Office
Prior art keywords
pressure
air
fraction
column
turbine
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
EP94400300A
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German (de)
English (en)
Other versions
EP0611218A1 (fr
EP0611218B1 (fr
Inventor
Maurice Grenier
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.)
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
Air Liquide SA
LAir Liquide SA a Directoire et Conseil de Surveillance pour lEtude et lExploitation des Procedes Georges Claude
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Application filed by Air Liquide SA, LAir Liquide SA a Directoire et Conseil de Surveillance pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Publication of EP0611218A1 publication Critical patent/EP0611218A1/fr
Publication of EP0611218B1 publication Critical patent/EP0611218B1/fr
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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
    • 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
    • F25J3/04018—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
    • 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
    • F25J3/04006—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
    • 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
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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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    • F25J3/04—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
    • F25J3/04163—Hot end purification of the feed air
    • 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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    • 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
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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
    • F25J3/04151—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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    • 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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    • F25J3/04284—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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    • 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
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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
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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

  • the present invention relates to a method of production of gaseous oxygen under high pressure oxygen.
  • EP-A-0 504 029 describes a process of this type in which the fraction of the air that is overpressed to the second high pressure is constituted by a very low air flow, the only function of which is to supply calories near the intake temperature of the turbine which expands the fraction of unpressurized air.
  • the invention aims to improve this process known in order to increase thermodynamic performance without increasing the corresponding investment.
  • the invention relates to a method of aforementioned type, according to claim 1.
  • the air distillation installation shown in Figure 1 essentially comprises: a compressor air 1; a device 2 for purifying compressed air in water and CO2 by adsorption, this device comprising two adsorption bottles 2A, 2B, one of which works in adsorption while the other is being regeneration; a turbine-blower assembly 3 comprising an expansion turbine 4 and a blower or booster 5 with shafts coupled, the blower possibly being fitted with a retrigrant (not shown); a heat exchanger 6 constituting the line heat exchange of the installation; a double distillation column 7 comprising a column medium pressure B surmounted by a low column pressure 9, with a vaporizer-condenser 10 putting the overhead vapor (azole) of column 8 in relation heat exchange with the tank liquid (oxygen) from column 9; a liquid oxygen tank 11 of which the bottom is connected to a liquid oxygen pump 12; and a liquid nitrogen tank 13, the bottom of which is connected to a liquid nitrogen pump 14.
  • This installation is intended to supply, via a pipe 15, gaseous oxygen under high pressure predetermined, which can be between a few bars and a few dozen bars (in this brief, the pressures considered are absolute pressures).
  • liquid oxygen drawn from the tank from column 9 via line 16 and stored in the tank 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 reheating, as well as reheating and possibly to the vaporization of other fluids drawn from the double column, is supplied by the air to be distilled, under the conditions following.
  • All of the air to be distilled is compressed by the compressor 1 at a first high pressure markedly higher than average column pressure 8, in practice greater than 9 bars. Then the air, precooled in 18 and cooled to around room temperature in 19, is purified in one, 2A for example, bottles adsorption, and divided into two fractions.
  • the first fraction representing at least 70% of the treated air flow, is boosted to a second high pressure by the booster 5, which is driven by the turbine 4.
  • the first fraction of air is then introduced at the end heat exchanger 6 and completely cooled to an intermediate temperature. At this temperature, a fraction of the air continues to cool and is liquefied in passages 20 of the exchanger, then is relaxed at low pressure in an expansion valve 21 and introduced at an intermediate level in the column 9. The rest of the air is relaxed to average pressure in turbine 4 then sent directly, via a pipe 22, at the base of column 8.
  • the second fraction is introduced under the first high pressure in exchange line 6, cooled and liquefied until cold end of it in passages 20A, relaxed in an expansion valve 21A and connected to the current from the expansion valve 21.
  • Low pressure nitrogen is heated in passages 28 of exchanger 6 then recovered via a pipe 29, while the waste gas, after heating in passages 30 of the exchanger, is used to regenerate an adsorption bottle, the bottle 2B in the example considered, before being evacuated via a pipe 31.
  • this air pressure is the pressure of air condensation by heat exchange with oxygen during vaporization under high pressure, i.e. the pressure at which the knee G liquefies of one of the two air fractions, on the diagram heat exchange (temperatures on the abscissa, amounts of heat exchanged on the ordinate) is located slightly to the right of the vertical spraying stage P oxygen under high pressure ( Figure 2).
  • the temperature difference at the hot end of the line is adjusted by means of the turbine 4, the suction temperature is indicated in A.
  • the diagram in Figure 2 corresponds to the values following digital: first high pressure: 24.5 bars; high oxygen pressure: 10 bars; second high pressure: 31 bars; second fraction of air: 28% of the incoming flow liquefied fraction in 20: very low; liquid production: 40% of the amount of oxygen separate.
  • the diagram in Figure 3 corresponds to the values following digital: 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 separated.
  • the air from the turbine 4 is sent to a separator pot 35.
  • the phase resulting liquid is sent directly to the column 8, while the gas phase is, after heating partial in the heat exchange line, relaxed 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 oxygen impure under good energy conditions thanks to the increased production of liquid which results from the presence of the second turbine, soil increase liquid production at the expense of amount of oxygen separated, or produce only liquid oxygen.
  • Figure 6 illustrates another variant in which the first high pressure is that of the penultimate main compressor stage 1.
  • the air is divided into two fractions as previously.
  • the first fraction is reintroduced at the suction of the last stage of compressor 1, and comes out at higher pressure.
  • this air is overpressed every second high pressure in 5 then is treated as explained more high.
  • the second fraction of air is directly introduced in the passages 20A of the heat exchange line.
  • the installation can produce, in addition to low pressure nitrogen gas coming directly from the head of column 9 and high pressure oxygen gas, nitrogen gas under pressure, obtained by spraying in the line heat exchange of a flow of liquid nitrogen sampled in line 33.
  • This nitrogen vaporization can in particular by condensation of the contained air in passages 20 or 20A.
  • the installation can produce gaseous oxygen and / or nitrogen gas under at least two pressures different, as explained in EP-A-0 504 029 cited above.
  • a small part of the air coming from the blower 5 can be overpressed again by a second blower (not shown), for example coupled to the turbine 36 of FIG. 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 présente invention est relative à un procédé de production d'oxygène gazeux sous une haute pression d'oxygène.
Dans ce qui suit, le terme "condensation" doit être entendue au sens large, c'est-à-dire recouvrant également la pseudo-condensation, aux pressions supercritiques.
Le EP-A-0 504 029 décrit un procédé de ce type dans lequel la fraction de l'air qui est surpressée à la seconde haute pression est constituée par un très faible débit d'air, dont la seule fonction est d'apporter des calories au voisinage de la température d'admission de la turbine qui détend la fraction de l'air non surpressé.
L'invention a pour but de perfectionner ce procédé connu de manière à en accroítre les performances thermodynamiques sans augmenter l'investissement correspondant.
A cet effet, l'invention a pour objet un procédé du type précité, selon la revendication 1.
D'autres modes particuliers de réalisation du procédé suivant l'invention sont décrits dans les revendications 2 à 5.
Des exemples de mise en oeuvre de l'invention vont maintenant être décrits en regard des dessins annexés, sur lesquels :
  • la Figure 1 représente schématiquement une installation capable d'opérer selon un procédé 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 5 sont des vues analogues à la Figure 1 représentant respectivement trois variantes.
L'installation de distillation d'air représentée à la Figure 1 comprend essentiellement: un compresseur d'air 1; un appareil 2 d'épuration de l'air comprimé en eau et en CO2 par adsorption, cet appareil comprenant deux bouteilles d'adsorption 2A, 2B dont l'une fonctionne en adsorption pendant que l'autre est en cours de régénération; un ensemble turbine-soufflante 3 comprenant une turbine de détente 4 et une soufflante ou surpresseur 5 dont les arbres sont couplés, la soufflante étant éventuellement équipée d'un rétrigérant (non représenté); un échangaur de chaleur 6 constituant la ligne d'échange thermique de l'installation; une double colonne de distillation 7 comprenant une colonne moyenne pression B surmontée d'une colonne basse pression 9, avec un vaporiseur-condenseur 10 mettant la vapeur de tête (azole) de la colonne 8 en relation d'échange thermique avec le liquide de cuve (oxygène) de la colonne 9; un réservoir d'oxygène liquide 11 dont le fond est relié à une pompe d'oxygène liquide 12; et un réservoir d'azote liquide 13 dont le fond est relié à une pompe d'azote liquide 14.
Cette installation est destinée à fournir, via une conduite 15, de l'oxygène gazeux sous une haute pression prédéterminée, qui peut être comprise entre quelques bars et quelques dizaines de bars (dans la présent mémoire, les pressions considérées sont des pressions absolues).
Pour cela, de l'oxygène liquide soutiré de la cuve de la colonne 9 via une conduite 16 et stocké dans le réservoir 11, est amené à la haute pression par la pompe 12 à l'état liquide, puis vaporisé et réchauffé sous cette haute pression dans des passages 17 de l'échangeur 6.
La chaleur nécessaire à cette vaporisation et à ce réchauffage, ainsi qu'au réchauffage et éventuellement à la vaporisation d'autres fluides soutirés de la double colonne, est fournie par l'air à distiller, dans les conditions suivantes.
La totalité de l'air à distiller est comprimée par le compresseur 1 à une première haute pression nettement supérieure à la moyenne pression de la colonne 8, en pratique supérieure à 9 bars. Puis l'air, prérefroidi en 18 et refroidi au voisinage de la température ambiante en 19, est épuré dans l'une, 2A par exemple, des bouteilles d'adsorption, et divisé en deux fractions.
La première fraction, représentant au moins 70% du débit d'air traité, est surpressée à une deuxième haute pression par la surpresseur 5, lequel est entraíné par la turbine 4.
La première fraction d'air est alors introduite au bout chaud de l'échangeur 6 et refroidie en totalité jusqu'à une température intermédiaire. A cette température, une fraction de l'air poursuit son refroidissement et est liquéfiée dans des passages 20 de l'échangeur, puis est détendue à la basse pression dans une vanne de détente 21 et introduite à un niveau intermédiaire dans la colonne 9. Le reste de l'air est détendu à la moyenne pression dans la turbine 4 puis envoyé directement, via une conduite 22, à la base de la colonne 8.
La deuxième fraction, éventuellement prérefroidie vers -40°C par un groupe trigorifique 6A indiqué en traits mixtes, est introduite sous la première haute pression dans la ligne d'échange 6, refroidie et liquéfiée jusqu'au bout froid de celle-ci dans des passages 20A, détendue dans une vanne de détente 21A et réunie au courant issu de la vanne de détente 21.
On reconnaít par ailleurs sur la Figure 1 les conduites habituelles des installations à double colonne, celle représentée étant du type dit "à minaret", c'est-à-dire avec production d'azote sous la basse pression : les conduites 23 à 25 d'injection dans la colonne 9, à des niveaux croissants, de "liquide riche" (air enrichi en oxygène) détendu, de "liquide pauvre inférieur" (azote impur) détendu et de "liquide pauvre supérieur" (azote pratiquement pur) détendu, respectivement, ces trois fluides étant respectivement soutirés à la base, en un point intermédiaire et au sommet de la colonne 8; et les conduites 26 de soutirage d'azote gazeux partant du sommet de la colonne 9 et 27 d'évacuation du gaz résiduaire (azote impur) partant du niveau d'injection du liquide pauvre inférieur. L'azote basse pression est réchauffé dans des passages 28 de l'échangeur 6 puis récupéré via une conduite 29, tandis que le gaz résiduaire, après réchauffement dans des passages 30 de l'échangeur, est utilisé pour régénérer une bouteille d'adsorption, la bouteille 2B dans l'exemple considéré, avant d'être évacué via une conduite 31.
On voit encore sur la Figure 1 qu'une partie de l'azote liquide moyenne pression est, après détente dans une vanne de détente 32, stockée dans le réservoir 13, et qu'une production d'azote liquide et/ou d'oxygène liquide est fournie via une conduite 33 (pour l'azote) et/ou 34 (pour l'oxygène).
De même que dans le procédé du EP-A-0 504 029 précité, pour le choix de la pression de l'air surpressé, on distingue deux cas.
Lorsque la haute pression d'oxygène est inférieure à 20 bars environ, cette pression d'air est la pression de condensation de l'air par échange de chaleur avec l'oxygène en cours de vaporisation sous la haute pression, c'est-à-dire la pression pour laquelle le genou G de liquéfaction de l'une des deux fractions d'air, sur le diagramme d'échange thermique (températures en abscisses, quantités de chaleur échangées en ordonnées) est situé légèrement à droite du palier vertical P de vaporisation de l'oxygène sous la haute pression (Figure 2). L'écart de température au bout chaud de la ligne d'échange est ajusté au moyen de la turbine 4, dont la température d'aspiration est indiquée en A. Cet écart est rendu minimal, c'est-à-dire de l'ordre de 2 à 3°C, vers une température de l'ordre de +10 à +15°C, comme indiqué en B sur la Figure 2, grâce à l'introduction à cette température de la seconde fraction d'air dans la ligne d'échange thermique. C'est cette caractéristique, combinée à la présence du second genou de liquéfaction G', correspondant à la liquéfaction de l'autre fraction d'air, qui permet de resserrer davantage le diagramme d'échange thermique que dans le cas du FR-A précité. Il est à noter que ce résultat peut s'obtenir sans machine supplémentaire. La présence du groupe frigorifique 6A accentue encore ce phénomène favorable.
Le diagramme de la Figure 2 correspond aux valeurs numériques suivantes : première haute pression : 24,5 bars; haute pression d'oxygène : 10 bars; deuxième haute pression : 31 bars; seconde fraction d'air : 28% du débit entrant fraction liquéfiée en 20 : très faible; production de liquide : 40% de la quantité d'oxygène séparé.
Lorsque la haute pression d'oxygène est supérieure à 20 bars environ, on choisit une pression d'air comprise entre 30 bars et la pression de condensation de l'air dans l'oxygène en cours de vaporisation. Dans ce cas (Figure 3), les genoux de liquéfaction des deux fractions d'air se décalent vers la gauche par rapport au palier P de vaporisation de l'oxygène, et la température d'aspiration de la turbine devient inférieure à celle du palier P. Par suite, une fraction importante de l'air turbiné se trouve en moyenne pression sous forme liquide, et le bilan frigorifique de l'installation est équilibré, avec un écart de température au bout chaud de la ligne d'échange thermique de l'ordre de 3°C, en soutirant de l'installation au moins un produit (oxygène et/ou azote) sous forme liquide via les conduites 33 et/ou 34. Lorsque la pression de l'air est de l'ordre de 30 bars, cet équilibre s'obtient pour un soutirage de liquide de l'ordre de 25% de la production d'oxygène gazeux sous haute pression, proportion qui est accrue si la pression de l'air est supérieure à 30 bars.
Le diagramme de la Figure 3 correspond aux valeurs numériques suivantes : première haute pression: 28,5 bars; température d'épuration : +12°C; seconde fraction d'air: 11% du débit entrant; deuxième haute pression : 36,4 bars; fraction détendue en 4 à 5,7 bars: 77% du débit entrant; fraction liquéfiée en 20 : 12% du débit d'air entrant; haute pression d'oxygène : 40 bars: production de liquide : 35% de la quantité d'oxygène séparé.
Dans la variante de la Figure 4, l'air issu de la turbine 4 est envoyé dans un pot séparateur 35. La phase liquide résultante est directement envoyée à la colonne 8, tandis que la phase gazeuse est, après réchauffement partiel dans la ligne d'échange thermique, détendue à la basse pression dans une seconde turbine 36 munie d'un frein approprié 37, puis insufflée dans la colonne 9. Cette variante permet soit de produire de l'oxygène impur dans de bonnes conditions énergétiques grâce à l'augmentation de la production de liquide qui résulte de la présence de la deuxième turbine, soil d'augmenter la production de liquide aux dépens de la quantité d'oxygène séparé, ou de produire uniquement de l'oxygène liquide.
Comme représenté sur la Figure 5, il peut être alors préférable, dans le même contexte, de réchauffer la phase gazeuse issue du séparateur 35 jusqu'à une température supérieure à la température d'admission de la turbine principale 4, avant d'introduire cette phase gazeuse à l'admission de la turbine 36. Dans ce cas, il peut être nécessaire, comme représenté, d'introduire dans la ligne d'échange thermique l'air qui s'échappe de la turbine 36 et de le refroidir jusqu'au bout froid de cette ligne d'échange, avant de l'introduire dans la colonne 8.
La Figure 6 illustre une autre variante dans laquelle la première haute pression est celle de l'avant-dernier étage du compresseur principal 1. Après épuration en 2 à cette pression, l'air est divisé en deux fractions comme précédemment. La première fraction est réintroduite à l'aspiration du dernier étage du compresseur 1, et en ressort à une pression plus élevée. Puis, après prérefroidissement en 38, cet air est surpressé à la seconde haute pression en 5 puis est traité comme expliqué plus haut. La seconde fraction d'air est directement introduite dans les passages 20A de la ligne d'échange thermique.
On a également montré sur la Figure 6 que l'installation peut produire, outre l'azote gazeux basse pression provenant directement de la tête de la colonne 9 et l'oxygène gazeux haute pression, de l'azote gazeux sous pression, obtenu par vaporisation dans la ligne d'échange thermique d'un débit d'azote liquide prélevé dans la conduite 33. Cette vaporisation d'azote peut notamment s'effectuer par condensation de l'air contenu dans les passages 20 ou 20A.
De plus, l'installation peut produire de l'oxygène gazeux et/ou de l'azote gazeux sous au moins deux pressions différentes, de la manière expliquée dans le EP-A-0 504 029 précité.
Eventuellement, une faible partie de l'air issu de la soufflante 5 peut être de nouveau surpressée par une seconde soufflante (non représentée), par exemple couplée à la turbine 36 de la Figure 5, avant d'être refroidie et liquéfiée dans la ligne d'échange thermique, suivant l'enseignement de la demande FR 91 15 935.

Claims (5)

  1. 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; et
    on refroidit toute la 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);
    ladite pramière fraction représentant au moins 70% du débit d'air traité, et dans lequel on refroidit et on liquéfie ladite seconde fraction, en un seul flux à ladite première haute pression et, après détente dans une vanne de détente (21A), on l'introduit dans la double colonne.
  2. Procédé suivant la revendication 1, caractérisé en ce qu'en 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.
  3. 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.
  4. 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).
  5. Procédé suivant l'une quelconque des revendicalions 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).
EP94400300A 1993-02-12 1994-02-11 Procédé et installation de production d'oxygene sous pression Expired - Lifetime EP0611218B2 (fr)

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FR9301622A FR2701553B1 (fr) 1993-02-12 1993-02-12 Procédé et installation de production d'oxygène sous pression.
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ES2124856T3 (es) 1999-02-16
ES2124856T5 (es) 2003-03-01
CN1101924C (zh) 2003-02-19
EP0611218A1 (fr) 1994-08-17
JPH06241650A (ja) 1994-09-02
DE69414282T3 (de) 2003-03-20
EP0611218B1 (fr) 1998-11-04
AU660385B2 (en) 1995-06-22
CA2115399A1 (fr) 1994-08-13
CN1100514A (zh) 1995-03-22
FR2701553A1 (fr) 1994-08-19
AU5506094A (en) 1994-08-18
US5426947A (en) 1995-06-27
CA2115399C (fr) 2005-04-26
DE69414282T2 (de) 1999-06-17
FR2701553B1 (fr) 1995-04-28
ZA94968B (en) 1994-08-24
DE69414282D1 (de) 1998-12-10

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