EP0422974A1 - Process and installation for the production of gaseous oxygen in variable quantities by the distillation of air - Google Patents

Process and installation for the production of gaseous oxygen in variable quantities by the distillation of air Download PDF

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Publication number
EP0422974A1
EP0422974A1 EP90402596A EP90402596A EP0422974A1 EP 0422974 A1 EP0422974 A1 EP 0422974A1 EP 90402596 A EP90402596 A EP 90402596A EP 90402596 A EP90402596 A EP 90402596A EP 0422974 A1 EP0422974 A1 EP 0422974A1
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EP
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Prior art keywords
flow
air
oxygen
tank
variable
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EP90402596A
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German (de)
French (fr)
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EP0422974B1 (en
Inventor
Bernard Darredeau
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Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Application filed by Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
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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
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04472—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages
    • F25J3/04496—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist
    • F25J3/04503—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist by exchanging "cold" between at least two different cryogenic liquids, e.g. independently from the main heat exchange line of the air fractionation and/or by using external alternating storage systems
    • F25J3/04509—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist by exchanging "cold" between at least two different cryogenic liquids, e.g. independently from the main heat exchange line of the air fractionation and/or by using external alternating storage systems within the cold part of the air fractionation, i.e. exchanging "cold" within the fractionation and/or main heat exchange line
    • F25J3/04515—Simultaneously changing air feed and products output
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/40—One fluid being air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/50—One fluid being oxygen
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/939—Partial feed stream expansion, air

Definitions

  • the present invention relates to the production of a variable flow rate of gaseous oxygen by air distillation. It relates firstly to a process of the type in which a variable quantity of oxygen is stored in liquid form in a first tank from which a variable flow of oxygen is taken and vaporized with, correspondingly, storage of another fluid in liquid form in a second reservoir.
  • the object of the invention is to provide a method which can be implemented more simply.
  • the subject of the invention is a method of the aforementioned type, characterized in that said fluid consists of a fraction of the air to be treated, in that a constant flow of liquid oxygen is sent into said first tank and a constant flow of liquefied air from said second tank into the distillation apparatus, and in that it is drawn from the first tank, depending on the oxygen demand gaseous, a variable flow of liquid oxygen which is vaporized by condensation of a corresponding variable flow of air to be treated.
  • the flow rates of each fluid introduced into the distillation apparatus and of each fluid withdrawn from this apparatus are kept constant, and the total air flow to be treated in the same way as the air flow condensed by oxygen vaporization.
  • the invention also relates to an installation intended for the implementation of such a method.
  • This installation of the type comprising a main air compressor, a double column distillation apparatus supplied by this compressor, a first storage tank for a variable quantity of liquid oxygen, a second storage tank for a variable quantity of another fluid in liquid form, and means for taking a variable flow of liquid oxygen in the first tank and vaporizing it and, approximately at the same time, adding said fluid in liquid form in the second tank, is characterized in that said vaporization means comprise a heat exchanger connected on the one hand to the outlet of the main compressor and on the other hand to the second tank, the lower part of the latter being also connected to the distillation apparatus, and in that the installation comprises means for passing a constant flow of liquid oxygen into the first tank, means for taking a variable flow of oxy liquid gene in this tank, means for varying the air flow rate sent to the heat exchanger, and means for send a constant flow of liquefied air from the second tank to the distillation apparatus.
  • FIGS. 1 and 2 schematically represent two embodiments of the installation according to the invention.
  • the installation shown in FIG. 1 essentially comprises a main air compressor 1 with variable flow rate, for example of the centrifugal type with movable blades, an adsorption purification device 2, a heat exchange line 3, a turbine 4 for keeping cold, an apparatus 5 for air distillation consisting of a double column itself comprising a medium pressure column 6 surmounted by a low pressure column 7 and a vaporizer-condenser 8, an auxiliary heat exchanger 9, a liquid oxygen tank 10 and a liquefied air tank 11.
  • This installation is intended to produce a variable flow of gaseous oxygen via a line 12, at a pressure slightly higher than atmospheric pressure.
  • the nominal flow of air to be treated, compressed to 6 bars by the compressor 1, cooled to room temperature and purified in the device 2, is divided into two flows each having a constant flow: - A first flow is cooled in passages 13 of the exchange line; a part has left this exchange line after partial cooling, expanded to 1 bar in the turbine 4 and blown into the low pressure column 7 near its dew point; the rest continues to cool down to the vicinity of its dew point at 6 bars, then is injected at the bottom of the medium pressure column 6 via a pipe 14. - A second flow is cooled to the vicinity of its dew point in passages 15 of the exchange line and then condensed in the exchanger 9 and stored in liquid form in the tank 11.
  • a constant flow of liquefied air is withdrawn from the bottom of this tank and is divided into a first constant flow at 6 bars sent to the medium pressure column via a line 16, and a second constant relaxed flow to 1 bar in an expansion valve 17 then injected into the low pressure column 7.
  • the vaporizer-condenser 8 vaporizes a constant flow of liquid oxygen in the bottom of the low pressure column by condensing a roughly equal flow of nitrogen from the top of the medium pressure column.
  • "Rich liquid” oxygen-enriched air
  • "lean liquid” nitrogen almost pure taken from the top of the medium pressure column and expanded to around 1 bar in an expansion valve 19 is injected at the top of the low pressure column.
  • a constant flow of liquid oxygen corresponding to 20% of the incoming air flow, passes, via a line 20, into the tank 10.
  • a constant flow identical liquid oxygen is withdrawn from the bottom of this tank, vaporized in the exchanger 9, heated in passages 21 of the exchange line and supplied to the production line 12.
  • a constant flow of impure nitrogen drawn off from the top of the low pressure column, is heated in passages 22 of the exchange line and evacuated as waste via a pipe 23.
  • Fig. 2 The installation shown in Fig. 2 is intended to supply gaseous oxygen under pressure. it differs from the previous one only in that a variable flow pump 24 is mounted in the pipe which connects the bottom of the tank 10 to the exchanger 9, and that an air blower 25 with movable blades is mounted in the pipe which conveys the fraction of the compressed air flow to the passages 15 of the heat exchange line.
  • the nominal operation of the installation is the same as above, except that the liquid oxygen withdrawn from the tank 10 is brought by the pump 24 to the desired pressure, then is vaporized under this pressure in the exchanger 9. To be able to carry out this vaporization, the corresponding air flow is boosted to a pressure somewhat higher than the oxygen vaporization pressure by the booster 25, condensed in the exchanger 9, then expanded to 6 bars in an expansion valve 26 before being stored in the tank 11.
  • each variation in the demand for gaseous oxygen in the pipe 12 requires a corresponding variation in the flow rate of the pump 24, a variation of the same order in the flow rate of air boosted by the booster 25, and an identical variation in the flow of air compressed by the main compressor 1.
  • the invention is particularly suitable for imparting flexibility to oxygen production installations with oxygen demands which vary frequently and rapidly.
  • the invention also applies to the case where, the oxygen demand always being greater than a given minimum value, a constant flow of gaseous oxygen equal to this minimum value is withdrawn directly from the bottom of the column low pressure 7 via a line 27, as indicated in phantom in Figs. 1 and 2, then reheated in the exchange line.
  • This variant makes it possible to reduce the capacity of the tanks 10 and 11.
  • constant productions of liquid oxygen and / or nitrogen gas and / or liquid nitrogen can be ensured simultaneously by the double column, via pipes 28 and / or 29 and / or 30, also as shown in dashed lines in FIGS. 1 and 2.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Oxygen, Ozone, And Oxides In General (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

In order to satisfy a variable demand for oxygen gas, a constant flow of liquid oxygen is transferred from the double distillation column (5) into a storage vessel (10) and a variable flow of liquid oxygen is drawn therefrom and vaporised in a heat exchanger (9) by condensation of a corresponding flow of entering air. The liquefied air is stored in a second storage vessel (11) from which a constant flow of liquefied air is conveyed into the double column. <IMAGE>

Description

La présente invention est relative à la production d'un débit variable d'oxygène gazeux par distillation d'air. Elle concerne en premier lieu un procédé du type dans lequel une quantité variable d'oxygène est stockée sous forme liquide dans un premier réservoir d'où un débit variable d'oxygène est prélevé et vaporisé avec, de façon correspondante, stockage d'un autre fluide sous forme liquide dans un second réservoir.The present invention relates to the production of a variable flow rate of gaseous oxygen by air distillation. It relates firstly to a process of the type in which a variable quantity of oxygen is stored in liquid form in a first tank from which a variable flow of oxygen is taken and vaporized with, correspondingly, storage of another fluid in liquid form in a second reservoir.

Dans un procédé connu de ce type, mis en oeuvre dans des installations réelles et connu sous l'appellation "procédé à bascule" la vaporisation et la condensation d'oxygène correspondent à une conden­sation et à une vaporisation d'azote, les échanges de chaleur étant effectués dans la double colonne qui constitue l'appareil de distillation d'air. Par suite, chaque modification du débit d'oxygène gazeux produit s'accompagne d'une modification du régime de marche de la double colonne, et en particulier de ses taux de chauffage et de reflux. Il en résulte des périodes de pertes d'efficacité de la distillation, d'autant plus importantes que les variations de régime sont rapprochées et rapides. De plus, une régulation complexe de l'installation est nécessaire.In a known process of this type, implemented in real installations and known under the name "rocking process" the vaporization and condensation of oxygen correspond to a condensation and to a vaporization of nitrogen, the heat exchanges being carried out in the double column which constitutes the air distillation apparatus. Consequently, each modification of the flow rate of gaseous oxygen produced is accompanied by a modification of the operating regime of the double column, and in particular of its heating and reflux rates. This results in periods of loss of efficiency of the distillation, all the more important as the variations in speed are close and rapid. In addition, complex regulation of the installation is necessary.

L'invention a pour but de fournir un procédé pouvant être mis en oeuvre de manière plus simple.The object of the invention is to provide a method which can be implemented more simply.

A cet effet, l'invention a pour objet un procédé du type précité, caractérisé en ce que ledit fluide est constitué par une fraction de l'air à traiter, en ce qu'on envoie un débit constant d'oxy­gène liquide dans ledit premier réservoir et un débit constant d'air liquéfié dudit second réservoir dans l'appareil de distillation, et en ce qu on soutire du premier réservoir, en fonction de la demande d oxygène gazeux, un débit variable d'oxygène liquide que l'on vaporise par condensation d'un débit variable corres­pondant d'air à traiter.To this end, the subject of the invention is a method of the aforementioned type, characterized in that said fluid consists of a fraction of the air to be treated, in that a constant flow of liquid oxygen is sent into said first tank and a constant flow of liquefied air from said second tank into the distillation apparatus, and in that it is drawn from the first tank, depending on the oxygen demand gaseous, a variable flow of liquid oxygen which is vaporized by condensation of a corresponding variable flow of air to be treated.

Dans un mode de mise en oeuvre avantageux, lors d'une variation de la demande d'oxygène, on main­tient constants les débits de chaque fluide introduit dans l'appareil de distillation et de chaque fluide soutiré de cet appareil, et on fait varier le débit total d'air à traiter de la même façon que le débit d'air condensé par vaporisation d'oxygène.In an advantageous embodiment, when the oxygen demand varies, the flow rates of each fluid introduced into the distillation apparatus and of each fluid withdrawn from this apparatus are kept constant, and the total air flow to be treated in the same way as the air flow condensed by oxygen vaporization.

L'invention a également pour objet une ins­tallation destinée à la mise en oeuvre d'un tel pro­cédé. Cette installation, du type comprenant un com­presseur principal d'air, un appareil de distillation à double colonne alimenté par ce compresseur, un premier réservoir de stockage d'une quantité variable d'oxygène liquide, un second réservoir de stockage d une quantité variable d'un autre fluide sous forme liquide, et des moyens pour prélever un débit variable d'oxygène liquide dans le premier réservoir et le va­poriser et, à peu près en même temps, ajouter dudit fluide sous forme liquide dans le second réservoir, est caractérisée en ce que lesdits moyens de vaporisa­tion comprennent un échangeur de chaleur relié d'une part à la sortie du compresseur principal et d'autre part au second réservoir, la partie inférieure de ce dernier étant par ailleurs reliée à l'appareil de dis­tillation, et en ce que l'installation comprend des moyens pour faire passer un débit constant d'oxygène liquide dans le premier réservoir, des moyens pour prélever un débit variable d'oxygène liquide dans ce réservoir, des moyens pour faire varier le débit d'air envoyé à l'échangeur de chaleur, et des moyens pour envoyer un débit constant d'air liquéfié du second réservoir dans l'appareil de distillation.The invention also relates to an installation intended for the implementation of such a method. This installation, of the type comprising a main air compressor, a double column distillation apparatus supplied by this compressor, a first storage tank for a variable quantity of liquid oxygen, a second storage tank for a variable quantity of another fluid in liquid form, and means for taking a variable flow of liquid oxygen in the first tank and vaporizing it and, approximately at the same time, adding said fluid in liquid form in the second tank, is characterized in that said vaporization means comprise a heat exchanger connected on the one hand to the outlet of the main compressor and on the other hand to the second tank, the lower part of the latter being also connected to the distillation apparatus, and in that the installation comprises means for passing a constant flow of liquid oxygen into the first tank, means for taking a variable flow of oxy liquid gene in this tank, means for varying the air flow rate sent to the heat exchanger, and means for send a constant flow of liquefied air from the second tank to the distillation apparatus.

Des exemples de mise en oeuvre de l'inven­tion vont maintenant être décrits en regard du dessin annexé, sur lequel les Fig. 1 et 2 représentent sché­matiquement deux modes de réalisation de l'instal­lation conforme à l'invention.Examples of implementation of the invention will now be described with reference to the attached drawing, in which FIGS. 1 and 2 schematically represent two embodiments of the installation according to the invention.

L'installation représentée à la Fig. 1 comprend essentiellement un compresseur d'air prin­cipal 1 à débit variable, par exemple du type cen­trifuge à aubages mobiles, un appareil d'épuration par adsorption 2, une ligne d'échange thermique 3, une turbine 4 de maintien en froid, un appareil 5 de dis­tillation d'air constitué par une double colonne comprenant elle-même une colonne moyenne pression 6 surmontée d'une colonne basse pression 7 et un vapo­riseur-condenseur 8, un échangeur de chaleur auxi­liaire 9, un réservoir d'oxygène liquide 10 et un réservoir d'air liquéfié 11 . Cette installation est destinée à produire un débit variable d'oxygène gazeux via une conduite 12, sous une pression légèrement supérieure à la pression atmosphérique.The installation shown in FIG. 1 essentially comprises a main air compressor 1 with variable flow rate, for example of the centrifugal type with movable blades, an adsorption purification device 2, a heat exchange line 3, a turbine 4 for keeping cold, an apparatus 5 for air distillation consisting of a double column itself comprising a medium pressure column 6 surmounted by a low pressure column 7 and a vaporizer-condenser 8, an auxiliary heat exchanger 9, a liquid oxygen tank 10 and a liquefied air tank 11. This installation is intended to produce a variable flow of gaseous oxygen via a line 12, at a pressure slightly higher than atmospheric pressure.

Pour décrire le fonctionnement de cette installation, on supposera tout d'abord que la demande d'oxygène gazeux dans la conduite 12 est constante et égale à la production nominale, soit 20 % du débit d'air nominal comprimé par le compresseur 1. Dans tout le présent mémoire, des pressions indiquées sont des pressions absolues approximatives, et les débits sont des débits molaires.To describe the operation of this installation, it will first be assumed that the demand for gaseous oxygen in line 12 is constant and equal to the nominal production, ie 20% of the nominal air flow compressed by the compressor 1. In throughout this specification, indicated pressures are approximate absolute pressures, and flow rates are molar flow rates.

Le débit nominal d'air à traiter, comprimé à 6 bars par le compresseur 1, refroidi à la température ambiante et épuré dans l'appareil 2, est divisé en deux flux ayant chacun un débit constant :
- Un premier flux est refroidi dans des passages 13 de la ligne d'échange ; une partie est sortie de cette ligne d'échange après un refroidisse­ment partiel, détendue vers 1 bar dans la turbine 4 et insufflée dans la colonne basse pression 7 au voisinage de son point de rosée ; le reste poursuit son refroidissement jusqu'au voisinage de son point de rosée sous 6 bars, puis est injecté au bas de la colonne moyenne pression 6 via une conduite 14.
- Un second flux est refroidi jusqu'au voisinage de son point de rosée dans des passages 15 de la ligne d'échange puis condensé dans l'échangeur 9 et stocké sous forme liquide dans le réservoir 11. Un débit constant d'air liquéfié est soutiré du fond de ce réservoir et est divisé en un premier débit cons­tant sous 6 bars envoyé dans la colonne moyenne pres­sion via une conduite 16, et un second débit constant détendu vers 1 bar dans une vanne de détente 17 puis injecté dans la colonne basse pression 7.The nominal flow of air to be treated, compressed to 6 bars by the compressor 1, cooled to room temperature and purified in the device 2, is divided into two flows each having a constant flow:
- A first flow is cooled in passages 13 of the exchange line; a part has left this exchange line after partial cooling, expanded to 1 bar in the turbine 4 and blown into the low pressure column 7 near its dew point; the rest continues to cool down to the vicinity of its dew point at 6 bars, then is injected at the bottom of the medium pressure column 6 via a pipe 14.
- A second flow is cooled to the vicinity of its dew point in passages 15 of the exchange line and then condensed in the exchanger 9 and stored in liquid form in the tank 11. A constant flow of liquefied air is withdrawn from the bottom of this tank and is divided into a first constant flow at 6 bars sent to the medium pressure column via a line 16, and a second constant relaxed flow to 1 bar in an expansion valve 17 then injected into the low pressure column 7.

Le vaporiseur-condenseur 8 vaporise un débit constant d'oxygène liquide en cuve de la colonne basse pression par condensation d'un débit à peu près égal d'azote de tête de la colonne moyenne pression. Du "liquide riche" (air enrichi en oxygène) prélevé en cuve de la colonne moyenne pression et détendu vers 1 bar dans une vanne de détente 18 est injecté à un niveau intermédiaire de la colonne basse pression, et du "liquide pauvre" (azote à peu près pur) prélevé en tête de la colonne moyenne pression et détendu vers 1 bar dans une vanne de détente 19 est injecté au sommet de la colonne basse pression.The vaporizer-condenser 8 vaporizes a constant flow of liquid oxygen in the bottom of the low pressure column by condensing a roughly equal flow of nitrogen from the top of the medium pressure column. "Rich liquid" (oxygen-enriched air) taken from the tank of the medium pressure column and expanded to around 1 bar in an expansion valve 18 is injected at an intermediate level of the low pressure column, and "lean liquid" (nitrogen almost pure) taken from the top of the medium pressure column and expanded to around 1 bar in an expansion valve 19 is injected at the top of the low pressure column.

Un débit constant d'oxygène liquide, corres­pondant à 20 % du débit d'air entrant, passe, via une conduite 20, dans le réservoir 10. Un débit constant identique d'oxygène liquide est soutiré du fond de ce réservoir, vaporisé dans l'échangeur 9, réchauffé dans des passages 21 de la ligne d'échange et fourni à la conduite 12 de production. En outre, un débit constant d azote impur, soutiré du sommet de la colonne basse pression, est réchauffé dans des passages 22 de la ligne d'échange et évacué en tant que résiduaire via une conduite 23.A constant flow of liquid oxygen, corresponding to 20% of the incoming air flow, passes, via a line 20, into the tank 10. A constant flow identical liquid oxygen is withdrawn from the bottom of this tank, vaporized in the exchanger 9, heated in passages 21 of the exchange line and supplied to the production line 12. In addition, a constant flow of impure nitrogen, drawn off from the top of the low pressure column, is heated in passages 22 of the exchange line and evacuated as waste via a pipe 23.

Toutes les conduites qui aboutissent à la double colonne 5 et toutes celles qui en partent sont équipées de moyens (non représentés) assurant un débit constant. Ainsi, lorsque la demande d'oxygène gazeux varie, le réglage de cette double colonne n'est pas modifié.All the pipes which lead to the double column 5 and all those which leave from it are equipped with means (not shown) ensuring a constant flow. Thus, when the demand for gaseous oxygen varies, the setting of this double column is not modified.

Par contre, dans ce cas, le débit d'air condensé dans l'échangeur 9 varie, et la position des aubages mobiles du compresseur 1 est modifiée de façon correspondante.By cons, in this case, the condensed air flow in the exchanger 9 varies, and the position of the movable blades of the compressor 1 is modified correspondingly.

Ainsi, si la demande en oxygène gazeux augmente, un plus grand débit d'oxygène est vaporisé dans l'échangeur 9. Ceci augmente le débit d'air condensé dans cet échangeur, ce qui crée un appel d'air supplémentaire vers cet échangeur, dans les passages 15 de cette ligne d'échange. Le réglage des aubages du compresseur 1 est alors modifié de façon à admettre ce débit d'air supplémentaire. Le niveau du liquide dans le réservoir 10 baisse, et il monte dans le réservoir 11.Thus, if the demand for gaseous oxygen increases, a greater flow of oxygen is vaporized in the exchanger 9. This increases the flow of air condensed in this exchanger, which creates an additional air call towards this exchanger, in passages 15 of this exchange line. The setting of the blades of compressor 1 is then modified so as to allow this additional air flow. The level of the liquid in the reservoir 10 drops, and it rises in the reservoir 11.

Inversement, si la demande en oxygène gazeux diminue, un débit réduit d'oxygène est vaporisé dans l'échangeur 9. Ceci réduit le débit d'air condensé dans cet échangeur, et donc également le débit d'air circulant dans les passages 15 de la ligne d'échange. Le réglage des aubages du compresseur 1 est alors modifié de manière à diminuer d'autant le débit d'air atmosphérique aspiré.Conversely, if the demand for gaseous oxygen decreases, a reduced flow of oxygen is vaporized in the exchanger 9. This reduces the flow of air condensed in this exchanger, and therefore also the flow of air circulating in the passages 15 the exchange line. The setting for the blades of compressor 1 is then modified so as to decrease by as much the flow of atmospheric air aspirated.

On voit donc que l'on peut répondre à la variation de la demande d'oxygène gazeux par une simple modification du réglage des aubages du com­presseur 1, ce qui peut s'effectuer simplement et quasi-instantanément, sans perturber aucunement le fonctionnement de l'appareil de distillation 5. De plus, cette souplesse est obtenue sans qu'aucun produit de la séparation de l'air soit perdu lors des variations du débit d'oxygène gazeux produit.We therefore see that we can respond to the variation in the demand for gaseous oxygen by a simple modification of the setting of the blades of the compressor 1, which can be done simply and almost instantaneously, without in any way disturbing the operation of the distillation apparatus 5. In addition, this flexibility is obtained without any product of air separation being lost during variations in the flow rate of gaseous oxygen produced.

L'installation représentée à la Fig.2 est destinée à fournir l'oxygène gazeux sous pression. elle ne diffère de la précédente que par le fait qu'une pompe 24 à débit variable est montée dans la conduite qui relie le fond du réservoir 10 à l'échan­geur 9, et qu'un surpresseur d'air 25 à aubages mobi­les est monté dans la conduite qui véhicule la frac­tion du débit d'air comprimé jusqu'aux passages 15 de la ligne d'échange thermique.The installation shown in Fig. 2 is intended to supply gaseous oxygen under pressure. it differs from the previous one only in that a variable flow pump 24 is mounted in the pipe which connects the bottom of the tank 10 to the exchanger 9, and that an air blower 25 with movable blades is mounted in the pipe which conveys the fraction of the compressed air flow to the passages 15 of the heat exchange line.

Le fonctionnement nominal de l'installation est le même que précédemment, à ceci près que l'oxy­gène liquide soutiré du réservoir 10 est amené par la pompe 24 à la pression désirée, puis est vaporisé sous cette pression dans l'échangeur 9. Pour pouvoir effec­tuer cette vaporisation, le débit correspondant d'air est surpressé à une pression quelque peu supérieure à la pression de vaporisation de l'oxygène par le sur­presseur 25, condensé dans l'échangeur 9, puis détendu à 6 bars dans une vanne de détente 26 avant d'être stocké dans le réservoir 11.The nominal operation of the installation is the same as above, except that the liquid oxygen withdrawn from the tank 10 is brought by the pump 24 to the desired pressure, then is vaporized under this pressure in the exchanger 9. To be able to carry out this vaporization, the corresponding air flow is boosted to a pressure somewhat higher than the oxygen vaporization pressure by the booster 25, condensed in the exchanger 9, then expanded to 6 bars in an expansion valve 26 before being stored in the tank 11.

Dans ce cas, chaque variation de la demande d'oxygène gazeux dans la conduite 12 nécessite une variation correspondante du débit de la pompe 24, une variation du même ordre du débit d'air surpressé par le surpresseur 25, et une variation identique du débit d'air comprimé par le compresseur principal 1.In this case, each variation in the demand for gaseous oxygen in the pipe 12 requires a corresponding variation in the flow rate of the pump 24, a variation of the same order in the flow rate of air boosted by the booster 25, and an identical variation in the flow of air compressed by the main compressor 1.

Ces modifications du réglage des machines tournantes sont de nouveau simples à obtenir et quasi-­instantanées, et elles n'induisent aucune perturbation du fonctionnement de la double colonne ni aucune perte de produit.These modifications to the setting of the rotating machines are again simple to obtain and almost instantaneous, and they do not induce any disturbance in the operation of the double column nor any loss of product.

De par sa simplicité et son efficacité, l'invention convient particulièrement bien pour con­férer de la souplesse à des installations de produc­tion d'oxygène avec des demandes d'oxygène qui varient fréquemment et rapidement.Owing to its simplicity and efficiency, the invention is particularly suitable for imparting flexibility to oxygen production installations with oxygen demands which vary frequently and rapidly.

Il est à noter que l'invention s'applique également au cas où, la demande d'oxygène étant tou­jours supérieure à une valeur minimale donnée, un débit d'oxygène gazeux constant égal à cette valeur minimale est soutiré directement du bas de la colonne basse pression 7 via une conduite 27, comme indiqué en trait mixte sur les Fig. 1 et 2, puis réchauffé dans la ligne d'échange. Cette variante permet de réduire la capacité des réservoirs 10 et 11. De même, des produc­tions constantes d'oxygène liquide et/ou d'azote ga­zeux et/ou d'azote liquide peuvent être assurées si­multanément par la double colonne, via des conduites 28 et/ou 29 et/ou 30, également comme indiqué en trait mixte sur les Fig. 1 et 2.It should be noted that the invention also applies to the case where, the oxygen demand always being greater than a given minimum value, a constant flow of gaseous oxygen equal to this minimum value is withdrawn directly from the bottom of the column low pressure 7 via a line 27, as indicated in phantom in Figs. 1 and 2, then reheated in the exchange line. This variant makes it possible to reduce the capacity of the tanks 10 and 11. Likewise, constant productions of liquid oxygen and / or nitrogen gas and / or liquid nitrogen can be ensured simultaneously by the double column, via pipes 28 and / or 29 and / or 30, also as shown in dashed lines in FIGS. 1 and 2.

Claims (7)

1. Procédé de production d'oxygène gazeux à débit variable par distillation d'air, du type dans lequel une quantité variable d oxygène est stockée sous forme liquide dans un premier réservoir (10) d'où un débit variable d'oxygène est prélevé et vaporisé avec, de façon correspondante, stockage d'un autre fluide sous forme liquide dans un second réservoir (11), caractérisé en ce que ledit fluide est constitué par une fraction de l'air à traiter, en ce qu on en­voie un débit constant d oxygène liquide dans ledit premier réservoir (10) et un débit constant d'air li­quéfié dudit second réservoir (11) dans l'appareil de distillation (5), et en ce qu'on soutire du premier réservoir (10), en fonction de la demande d'oxygène gazeux, un débit variable d'oxygène liquide que l'on vaporise par condensation d'un débit variable correspondant d'air à traiter.1. Method for producing gaseous oxygen at variable flow rate by air distillation, of the type in which a variable quantity of oxygen is stored in liquid form in a first tank (10) from which a variable flow rate of oxygen is withdrawn and vaporized with, correspondingly, storage of another fluid in liquid form in a second reservoir (11), characterized in that said fluid consists of a fraction of the air to be treated, in that a flow is sent constant liquid oxygen in said first tank (10) and a constant flow of liquefied air from said second tank (11) in the distillation apparatus (5), and in that it is withdrawn from the first tank (10), depending on the demand for gaseous oxygen, a variable flow of liquid oxygen which is vaporized by condensation of a corresponding variable flow of air to be treated. 2. Procédé suivant la revendication 1, caractérisé en ce que, lors d'une variation de la de­mande d'oxygène, on maintient constants les débits de chaque fluide introduit dans l'appareil de distilla­tion (5) et de chaque fluide soutiré de cet appareil, et on fait varier le débit total d'air à traiter de la même façon que le débit d'air condensé par vaporisa­tion d'oxygène.2. Method according to claim 1, characterized in that, during a variation in the oxygen demand, the flow rates of each fluid introduced into the distillation apparatus (5) and of each fluid withdrawn from this are kept constant device, and the total flow of air to be treated is varied in the same way as the flow of air condensed by oxygen vaporization. 3. Procédé suivant l'une des revendications 1 et 2, pour la production d'oxygène gazeux sous pression, caractérisé en ce qu on amène par pompage (en 24) ledit débit variable d'oxygène liquide à la pression de production, et on surpresse (en 25) le débit d'air à liquéfier correspondant.3. Method according to one of claims 1 and 2, for the production of gaseous oxygen under pressure, characterized in that one brings by pumping (at 24) said variable flow of liquid oxygen to the production pressure, and pressurizes (at 25) the corresponding air flow to be liquefied. 4. Procédé suivant l'une quelconque des revendications 1 à 3, caractérisé en ce que ledit débit variable d'oxygène liquide correspond à la demande d'oxygène gazeux.4. Method according to any one of claims 1 to 3, characterized in that said variable flow of liquid oxygen corresponds to the demand for gaseous oxygen. 5. Installation de production d oxygène gazeux à débit variable par distillation d'air, du type comprenant un compresseur principal d'air (1) , un appareil de distillation (5) à double colonne alimenté par ce compresseur, un premier réservoir (10) de stockage d'une quantité variable d'oxygène liquide, un second réservoir (11) de stockage d'une quantité va­riable d'un autre fluide sous forme liquide, et des moyens (9, 12) pour prélever un débit variable d'oxygè­ne liquide dans le premier réservoir (10) et le vaporiser et, à peu près en même temps, ajouter dudit fluide sous forme liquide dans le second réservoir (11), caractérisée en ce que lesdits moyens de vaporisation (9) comprennent un échangeur de chaleur relié d'une part à la sortie du compresseur principal (1) et d'autre part au second réservoir (11), la par­tie inférieure de ce dernier étant par ailleurs reliée à l'appareil de distillation (5), et en ce que l'ins­tallation comprend des moyens pour faire passer un débit constant d'oxygène liquide dans le premier ré­servoir (10), des moyens pour prélever un débit varia­ble d oxygène liquide dans ce réservoir, des moyens pour faire varier le débit d'air envoyé à l'échangeur de chaleur (9), et des moyens pour envoyer un débit constant d'air liquéfié du second réservoir (11) dans l'appareil de distillation (5).5. Installation for producing gaseous oxygen at variable flow rate by air distillation, of the type comprising a main air compressor (1), a double column distillation apparatus (5) supplied by this compressor, a first tank (10 ) for storing a variable quantity of liquid oxygen, a second reservoir (11) for storing a variable quantity of another fluid in liquid form, and means (9, 12) for taking a variable flow of liquid oxygen in the first tank (10) and vaporize it and, roughly at the same time, add said fluid in liquid form to the second tank (11), characterized in that said vaporization means (9) comprise a heat exchanger heat connected on the one hand to the output of the main compressor (1) and on the other hand to the second tank (11), the lower part of the latter being also connected to the distillation apparatus (5), and in this that the installation includes means for passing a constant flow of liquid oxygen into the first tank (10), means for taking a variable flow of liquid oxygen in this tank, means for varying the flow of air sent to the heat exchanger (9 ), and means for sending a constant flow of liquefied air from the second tank (11) into the distillation apparatus (5). 6. Installation suivant la revendication 5, caractérisée en ce qu'elle comprend des moyens pour faire varier le débit total d'air à traiter de la même façon que le débit d'air envoyé à l'échangeur de cha­leur (9)6. Installation according to claim 5, characterized in that it comprises means for varying the total air flow to be treated by the same so that the air flow sent to the heat exchanger (9) 7. Installation suivant l'une des revendi­cations 5 et 6, caractérisée en ce qu'elle comprend un pompe à débit variable (24) montée entre la sortie du premier réservoir (10) et l'échangeur de chaleur (9), et un surpresseur d'air à débit variable (25) monté entre la sortie du compresseur d'air principal (1) et cet échangeur de chaleur.7. Installation according to one of claims 5 and 6, characterized in that it comprises a variable flow pump (24) mounted between the outlet of the first tank (10) and the heat exchanger (9), and a variable air blower (25) mounted between the outlet of the main air compressor (1) and this heat exchanger.
EP90402596A 1989-10-09 1990-09-20 Process and installation for the production of gaseous oxygen in variable quantities by the distillation of air Revoked EP0422974B1 (en)

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FR8913159A FR2652887B1 (en) 1989-10-09 1989-10-09 PROCESS AND PLANT FOR THE PRODUCTION OF VARIABLE FLOW GAS OXYGEN BY AIR DISTILLATION.
FR8913159 1989-10-09

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EP0556861A1 (en) * 1992-02-21 1993-08-25 Praxair Technology, Inc. Cryogenic air separation system for producing gaseous oxygen
FR2751737A1 (en) * 1996-07-25 1998-01-30 Air Liquide METHOD AND INSTALLATION FOR PRODUCING A VARIABLE FLOW AIR GAS
WO1998004877A1 (en) * 1996-07-25 1998-02-05 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and plant for producing an air gas with a variable flow rate
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EP0952417A2 (en) * 1998-04-09 1999-10-27 The BOC Group plc Separation of air
EP0952417A3 (en) * 1998-04-09 2000-04-12 The BOC Group plc Separation of air
US6170291B1 (en) 1998-04-09 2001-01-09 The Boc Group Plc Separation of air
FR2929697A1 (en) * 2008-04-07 2009-10-09 Air Liquide PROCESS FOR PRODUCING VARIABLE GASEOUS NITROGEN AND VARIABLE GAS OXYGEN BY AIR DISTILLATION

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DE69000903D1 (en) 1993-03-25
US5082482A (en) 1992-01-21
ES2037535T3 (en) 1993-06-16
AU625950B2 (en) 1992-07-16
FR2652887B1 (en) 1993-12-24
ZA908000B (en) 1991-08-28
ATE85696T1 (en) 1993-02-15
EP0422974B1 (en) 1993-02-10
JPH03134481A (en) 1991-06-07
AU6388290A (en) 1991-04-11
CA2027071A1 (en) 1991-04-10
CA2027071C (en) 2000-07-18
FR2652887A1 (en) 1991-04-12
DE69000903T2 (en) 1993-07-01
JP3117702B2 (en) 2000-12-18

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