EP0611218B1 - Process and installation for producing oxygen under pressure - Google Patents

Process and installation for producing oxygen under pressure Download PDF

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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.)
Expired - Lifetime
Application number
EP94400300A
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German (de)
French (fr)
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EP0611218A1 (en
EP0611218B2 (en
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 pour lEtude et lExploitation des Procedes Georges Claude
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Application filed by Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Publication of EP0611218A1 publication Critical patent/EP0611218A1/en
Publication of EP0611218B1 publication Critical patent/EP0611218B1/en
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Publication of EP0611218B2 publication Critical patent/EP0611218B2/en
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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
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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
    • F25J3/04018—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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    • 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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    • F25J3/04012—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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    • 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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    • F25J3/04163—Hot end purification of the feed air
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    • 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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    • F25J3/04236—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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    • 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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    • 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)
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Description

La présente invention est relative à un procédé de production d'oxygène gazeux sous une haute pression d'oxygène, suivant le préambule de la revendication 1.The present invention relates to a process for producing gaseous oxygen under high oxygen pressure according to the preamble of claim 1.

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.In what follows, the term "condensation" must be understood in the broad sense, that is to say covering also pseudo-condensation, at supercritical pressures.

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.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.

L'invention a pour but de perfectionner ce procédé connu de manière à en accroítre les performances thermodynamiques sans augmenter l'investissement correspondant.The object of the invention is to improve this known process in order to increase performance thermodynamics without increasing the corresponding investment.

A cet effet, l'invention a pour objet un procédé du type précité, caractérisé par la partie caractérisante de la revendication 1.To this end, the subject of the invention is a process of the aforementioned type, characterized by the part Characterizing of claim 1.

D'autres modes particuliers de réalisation du procédé suivant l'invention sont décrits dans les revendications 2 à 5.Other particular embodiments of the following method the invention are described in claims 2 to 5.

L'invention a également pour objet une installation destinée à la mise en oeuvre d'un tel procédé. Cette installation est décrite dans la revendication 6.The subject of the invention is also a installation intended for the implementation of such process. This installation is described in the claim 6.

Des modes de réalisation de cette installation sont décrits dans les revendications 7 à 10.Embodiments of this installation are described in claims 7 to 10.

Des exemples de mise en oeuvre de l'invention vont maintenant être décrit en regard des dessins annexés, sur lesquels :

  • 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.
Examples of implementation of the invention will now be described with reference to the accompanying drawings, in which:
  • Figure 1 schematically shows an installation according to the invention;
  • Figure 2 is a heat exchange diagram, obtained by calculation, corresponding to the installation of Figure 1, in a first mode of operation of this installation; on this diagram, the temperatures are plotted on the abscissa, in degrees Celsius, and the quantities of heat exchanged on the ordinate;
  • Figure 3 is a diagram similar to that of Figure 2 but corresponding to another mode of operation of the installation of Figure 1; and
  • Figures 4 to 6 are views similar to Figure 1 respectively representing three variants.

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 C02 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 réfrigérant (non représenté); un échangeur de chaleur 6 constituant la ligne d'échange thermique de l'installation; une double colonne de distillation 7 comprenant une colonne moyenne pression 8 surmontée d'une colonne basse pression 9, avec un vaporiseur-condenseur 10 mettant la vapeur de tête (azote) 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. 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.

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 le présent mémoire, les pressions considérées sont des pressions absolues).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).

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.For this, 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.

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.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.

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.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.

La première fraction, représentant au moins 70% du débit d'air traité, est surpressée à une deuxième haute pression par le surpresseur 5, lequel est entraíné par la turbine 4.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.

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.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.

La deuxième fraction, éventuellement prérefroidie vers -40°C par un groupe frigorifique 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.The second fraction, possibly pre-cooled around -40 ° C by a 6A refrigeration unit indicated in dashed lines, 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.

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.We also recognize in Figure 1 the normal pipes in double column installations, that represented being of the type known as "minaret", that is to say with nitrogen production under low pressure: the injection lines 23 to 25 in column 9, to increasing levels of "rich liquid" (enriched air in oxygen) relaxed, of "lower lean liquid" (nitrogen impure) relaxed and "superior poor liquid" (nitrogen practically pure) relaxed, respectively, these three fluids being respectively drawn off at the base, in a intermediate point and at the top of column 8; and the pipes 26 for withdrawing nitrogen gas leaving from top of column 9 and 27 for discharging the residual gas (impure nitrogen) from the injection level of the lower poor liquid. 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, bottle 2B in the example considered, before to be evacuated via a pipe 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).We can still see in Figure 1 that part medium pressure liquid nitrogen is, after expansion in an expansion valve 32, stored in the tank 13, and that a production of liquid nitrogen and / or oxygen liquid is supplied via line 33 (for nitrogen) and / or 34 (for oxygen).

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.As in the process of EP-A-0 504 029 above, for the choice of the pressure of the compressed air, there are two cases.

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.When the high oxygen pressure is less than about 20 bars, 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. This difference is made minimal, that is to say of the order of 2 to 3 ° C, towards a temperature of the order of +10 to + 15 ° C, as indicated in B in Figure 2, thanks to the introduction to this temperature of the second fraction of air in the heat exchange line. It is this characteristic, combined with the presence of the second liquefaction knee G ', corresponding to the liquefaction of the other fraction air, which allows to tighten the diagram further heat exchange than in the case of the aforementioned FR-A. he it should be noted that this result can be obtained without a machine additional. The presence of the refrigeration unit 6A further accentuates this favorable phenomenon.

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.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.

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.When the high oxygen pressure is greater than about 20 bars, a pressure is chosen of air between 30 bar and the condensing pressure air in oxygen during vaporization. In this case (Figure 3), the knees for liquefaction two fractions of air shift to the left by oxygen vaporization level P, and the turbine suction temperature becomes lower to that of bearing P. As a result, a large fraction turbinated air is found at medium pressure in the form liquid, and the refrigeration balance of the installation is balanced, with a temperature difference at the hot end of the heat exchange line of the order of 3 ° C, drawing at least one product from the installation (oxygen and / or nitrogen) in liquid form via lines 33 and / or 34. When the air pressure is around 30 bars, this balance is obtained for a racking of liquid of the order of 25% of oxygen production gaseous under high pressure, a proportion which is increased if the air pressure is greater than 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.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.

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, soit d'augmenter la production de liquide aux dépens de la quantité d'oxygène séparé, ou de produire uniquement de l'oxygène liquide.In the variant of Figure 4, 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.

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.As shown in Figure 5, it can then it would be preferable, in the same context, to warm up the gas phase from separator 35 to a temperature higher than the intake temperature of the main turbine 4, before introducing this gas phase at the inlet of turbine 36. In this case, it may be necessary, as shown, to introduce in the heat exchange line the air which escapes from turbine 36 and cools it down to cold end of this exchange line, before introducing it in column 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.Figure 6 illustrates another variant in which the first high pressure is that of the penultimate main compressor stage 1. After purification in 2 at this pressure, the air is divided into two fractions like before. The first fraction is reintroduced at the suction of the last stage of compressor 1, and comes out at higher pressure. Then, after precooling in 38, 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 passages 20A of the exchange line thermal.

Eventuellement, comme indiqué en traits mixtes, un flux d'air peut être prélevé entre le prérefroidisseur 38 et la soufflante 5 et envoyé via une conduite 39 dans d'autres passages 20B de la ligne d'échange thermique, par conséquent à une pression intermédiaire entre les première et seconde hautes pressions.Possibly, as indicated in lines mixed, 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.

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, 20A ou 20B.We have also shown in Figure 6 that the installation can produce, in addition to low nitrogen gas pressure coming directly from the column head 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 especially by condensation of the air contained in passages 20, 20A or 20B.

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.In addition, 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.

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.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.

Claims (10)

  1. Process for the production of gaseous oxygen under a high oxygen pressure by distilling air in a twin column system (7) comprising a medium pressure column (8), which operates at a pressure referred to as medium pressure, and a low pressure column (9), which operates at a pressure referred to as low pressure, pumping (at 12) liquid oxygen drawn off from the tank of the low pressure column (9), and vaporising (at 6) the compressed liquid oxygen by heat exchange with the air in a heat exchange section (6) of the system, in said process:
    all the air to be distilled is compressed by means of a main air compressor (1) of the system to a first high pressure clearly higher than the medium pressure, and this is divided into a first and a second component;
    said first component is subjected to overpressure to a second high pressure; and
    at least the essential part of said first component is cooled in the heat exchange section to an intermediate temperature, at which a portion is expanded in a first turbine (4) at the medium pressure, is then fed into the medium pressure column (8), while the remainder continues to be cooled and is liquified, is expanded in a pressure relief valve (21) and fed into the twin column (7);
    characterised in that said first component constitutes at least 70% of the flow of treated air, and that said second component is cooled and liquified in one or more fluxes at said first high pressure or at one or more pressures within the range between said first high pressure and said second high pressure, and after expanding in a pressure relief valve (21A) it is fed into the twin column.
  2. Process according to Claim 1, characterised in that the gaseous component of the air from the first turbine (4) is expanded in a second turbine (36) to the low pressure, said gaseous component being partially reheated prior to its expansion in the second turbine and the output therefrom being aspirated into the low pressure column (9), if necessary after cooling.
  3. Process according to Claim 1 or 2, characterised in that the air is brought to the first high pressure by means of only one part of the stages of the air compressor (1), the air is purified in water and in carbonic anhydride (at 2) at this first high pressure, said first component is then compressed by means of the last stage or stages of this compressor.
  4. Process according to Claim 3, characterised in that at least one part of the air exiting from the last stage of the compressor (1) is subjected to overpressure by means of a blower (5) coupled to the first turbine (4).
  5. Process according to any one of Claims 1 to 4,
    characterised in that said second component is pre-cooled by means of a cooling assembly (6A) before being fed into the heat exchange section (6).
  6. System for producing gaseous oxygen under a high oxygen pressure of the type comprising a main air compressor (1), a twin air distillation column (7) comprising a medium pressure column (8), which operates at a pressure referred to as medium pressure, and a low pressure column (9), which operates at a pressure referred to as low pressure, a pump (12) for compressing liquid oxygen drawn off from the tank of the low pressure column (9), means (1, 5) for bringing a component of the air to be distilled to a high air pressure, and a heat exchange section (6), characterised in that:
    said means are designed to bring all the air to be distilled to a first high pressure clearly higher than the medium pressure, and comprising means to subject a first component of this air constituting at least 70% of the flow of treated air to overpressure to a second high pressure;
    the heat exchange section (6) comprises means to cool said first component to an intermediate temperature and to further cool beforehand and liquify a portion of this first component, and means (20A, 20B) to cool the air which has not been subjected to overpressure to a second high pressure in one or more fluxes at said first high pressure or at one or more pressures within the range between said first high pressure and said second high pressure; and
    the system comprises an expansion turbine (4), the intake of which is connected to the air cooling ducts under the second high pressure at an intermediate point in the heat exchange section (6), and the output of which is connected to the medium pressure column (8).
  7. System according to Claim 6, characterised in that it comprises a second turbine (36) for expansion at low pressure of at least a portion of the air from the first turbine (4).
  8. System according to Claim 6, characterised in that said second component is taken from an intermediate stage of the main air compressor (1), the first component being fed back into this compressor after purification in water and carbonic anhydride (at 2).
  9. System according to Claim 8, characterised in that it comprises a blower (5) coupled to the first turbine (4), the intake of said blower being connected to the output of the last stage of the main air compressor (1).
  10. System according to any one of Claims 6 to 9, characterised in that it comprises a cooling assembly (6A) for precooling said second component of air upstream of the heat exchange section (6).
EP94400300A 1993-02-12 1994-02-11 Process and installation for producing oxygen under pressure Expired - Lifetime EP0611218B2 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR9301622 1993-02-12
FR9301622A FR2701553B1 (en) 1993-02-12 1993-02-12 Method and installation for producing oxygen under pressure.

Publications (3)

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EP0611218A1 EP0611218A1 (en) 1994-08-17
EP0611218B1 true EP0611218B1 (en) 1998-11-04
EP0611218B2 EP0611218B2 (en) 2002-08-07

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Application Number Title Priority Date Filing Date
EP94400300A Expired - Lifetime EP0611218B2 (en) 1993-02-12 1994-02-11 Process and installation for producing oxygen under pressure

Country Status (10)

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US (1) US5426947A (en)
EP (1) EP0611218B2 (en)
JP (1) JPH06241650A (en)
CN (1) CN1101924C (en)
AU (1) AU660385B2 (en)
CA (1) CA2115399C (en)
DE (1) DE69414282T3 (en)
ES (1) ES2124856T5 (en)
FR (1) FR2701553B1 (en)
ZA (1) ZA94968B (en)

Cited By (1)

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DE102012017488A1 (en) 2012-09-04 2014-03-06 Linde Aktiengesellschaft Method for building air separation plant, involves selecting air separation modules on basis of product specification of module set with different air pressure requirements

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DE19815885A1 (en) * 1998-04-08 1999-10-14 Linde Ag Air separation method producing gas, or gas and liquid e.g. for steel plant
FR2782544B1 (en) * 1998-08-19 2005-07-08 Air Liquide PUMP FOR A CRYOGENIC LIQUID AND PUMP GROUP AND DISTILLATION COLUMN EQUIPPED WITH SUCH A PUMP
FR2828273A1 (en) * 2001-07-31 2003-02-07 Air Liquide Air distillation method uses two adsorbers to purify air in operating cycle with adsorption and regeneration phases
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 (en) * 2008-03-10 2009-09-11 Air Liquide METHOD FOR MODIFYING AN AIR SEPARATION APPARATUS BY CRYOGENIC DISTILLATION
DE102009048456A1 (en) * 2009-09-21 2011-03-31 Linde Aktiengesellschaft Method and apparatus for the cryogenic separation of air

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FR2461906A1 (en) * 1979-07-20 1981-02-06 Air Liquide CRYOGENIC AIR SEPARATION METHOD AND INSTALLATION WITH OXYGEN PRODUCTION AT HIGH PRESSURE
JPS62102074A (en) * 1985-10-30 1987-05-12 株式会社日立製作所 Method of separating gas
FR2652409A1 (en) † 1989-09-25 1991-03-29 Air Liquide REFRIGERANT PRODUCTION PROCESS, CORRESPONDING REFRIGERANT CYCLE AND THEIR APPLICATION TO AIR DISTILLATION.
US5148680A (en) † 1990-06-27 1992-09-22 Union Carbide Industrial Gases Technology Corporation Cryogenic air separation system with dual product side condenser
FR2674011B1 (en) * 1991-03-11 1996-12-20 Maurice Grenier PROCESS AND PLANT FOR PRODUCING PRESSURE GAS OXYGEN.
JP2909678B2 (en) * 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 Method and apparatus for producing gaseous oxygen under pressure
FR2695714B1 (en) † 1992-09-16 1994-10-28 Maurice Grenier Installation of cryogenic treatment, in particular of air distillation.

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102012017488A1 (en) 2012-09-04 2014-03-06 Linde Aktiengesellschaft Method for building air separation plant, involves selecting air separation modules on basis of product specification of module set with different air pressure requirements

Also Published As

Publication number Publication date
EP0611218A1 (en) 1994-08-17
CN1101924C (en) 2003-02-19
FR2701553B1 (en) 1995-04-28
CA2115399C (en) 2005-04-26
AU660385B2 (en) 1995-06-22
ES2124856T5 (en) 2003-03-01
DE69414282T2 (en) 1999-06-17
CN1100514A (en) 1995-03-22
ES2124856T3 (en) 1999-02-16
DE69414282D1 (en) 1998-12-10
US5426947A (en) 1995-06-27
CA2115399A1 (en) 1994-08-13
FR2701553A1 (en) 1994-08-19
AU5506094A (en) 1994-08-18
DE69414282T3 (en) 2003-03-20
ZA94968B (en) 1994-08-24
JPH06241650A (en) 1994-09-02
EP0611218B2 (en) 2002-08-07

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