EP1106945A1 - Process and system for air separation by cryogenic distillation - Google Patents

Process and system for air separation by cryogenic distillation Download PDF

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Publication number
EP1106945A1
EP1106945A1 EP00403354A EP00403354A EP1106945A1 EP 1106945 A1 EP1106945 A1 EP 1106945A1 EP 00403354 A EP00403354 A EP 00403354A EP 00403354 A EP00403354 A EP 00403354A EP 1106945 A1 EP1106945 A1 EP 1106945A1
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EP
European Patent Office
Prior art keywords
column
liquid
low pressure
pressure column
mixing
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.)
Granted
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EP00403354A
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German (de)
French (fr)
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EP1106945B1 (en
Inventor
Jean Renaud Brugerolle
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04709—Producing crude argon in a crude argon column as an auxiliary column system in at least a dual pressure main column system
    • F25J3/04715—The auxiliary column system simultaneously produces 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
    • F25J3/0446—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 heat generated by mixing two different phases
    • 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
    • F25J3/0446—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 heat generated by mixing two different phases
    • F25J3/04466—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 heat generated by mixing two different phases for producing oxygen as a mixing column overhead gas by mixing gaseous air feed and liquid 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
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04969—Retrofitting or revamping of an existing air fractionation unit
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
    • F25J2200/06—Processes or apparatus using separation by rectification in a dual pressure main column system in a classical double column flow-sheet, 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams
    • 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
    • Y10S62/923—Inert gas
    • Y10S62/924—Argon

Definitions

  • the present invention relates to a separation process and installation air by cryogenic distillation.
  • it relates to a method of production of pure oxygen using a mixing column and optionally argon production using an argon column
  • EP-A-0269342 relates to the case in which the argon column is connected thermally with a mixing column so that the overhead gas from the argon column heats the mixing column.
  • US-A-5551258 describes a process in which a mixing column is fed at the head with a liquid containing 55% vol. oxygen, the overhead gas the mixing column then used to heat the tank condenser of the low pressure column.
  • An object of the present invention is to increase the amount of gaseous oxygen pure (containing more than 99.5 mol% of oxygen) which can be produced by a double air separation column.
  • the installation can include an argon column or simply a medium pressure column tank vaporizer by exchange of heat with a gas from the low pressure column.
  • it comprises means for withdrawing the second liquid at a level between the column tank and the withdrawal level of the argon column supply or the low pressure gas withdrawal level used to vaporize the medium pressure column tank liquid.
  • the mixing column can be supplied to the tank by any gas more volatile than liquid oxygen sent to the top of the column.
  • the head gas of the mixing column can be racked at the top of the mixing column or at most five theoretical plates below the top of the mixing column.
  • Figure 1 The installation of Figure 1 comprises a double column 1 comprising a medium pressure column 3 and a low pressure column 5 connected between them by a vaporizer 7.
  • the vaporizer includes liquid vaporization passages and two independent series of heating passages for two different heating gases.
  • the low pressure column operates at between 1.4 and 2.7 bar and the column medium pressure operates at between 5 and 8 bar.
  • the argon column 9 is supplied from a first level of the column low pressure 5. There is also a mixing column 11 which operates at a pressure between 1.9 bar and 3.7 bar.
  • An air flow 13 is sent to column 3 and a blown air flow 14 is sent to column 5.
  • a flow of liquid 15 containing 40 mol%. oxygen is drawn from the medium pressure column tank 3: part 17 of this liquid supplies the low pressure column 5 after expansion in a valve and part 19 of the liquid is expanded to between 1.7 and 2.2 bar absolute in a valve and sent to the overhead condenser 21 of the argon column 9 where it vaporizes at least partially.
  • the vaporized liquid 23 is sent to the tank of the mixing column.
  • the nitrogen at the top of the medium pressure column at least condenses partially in the tank vaporizer 7 and the condensate is sent to the column medium pressure and / or low pressure column.
  • a gas flow 41 containing at least 80 mol% of nitrogen is withdrawn at the head of the medium pressure column as product and constitutes 10 to 15% of supply air.
  • a flow rate of liquid 25 enriched in nitrogen and containing less than 2 mol% oxygen is sent from the medium pressure column to the head of the column low pressure.
  • a liquid flow 27 containing less than 5 mol% of nitrogen is withdrawn in low pressure column tank 5 below the gas withdrawal point 26 intended for the argon column 9.
  • the second liquid is withdrawn from the low pressure column at a level at least 5 theoretical plates below from the injection point of the low pressure column (or from the most bottom), possibly at least 10 theoretical plates below the point injection of the low pressure column (or of the lowest injection point) and / or at a level of around a third of theoretical plates of the low pressure column above the tank of the low pressure column.
  • This liquid is sent after pumping at between 1.9 and 3.7 bar at the top of the mixing column 11.
  • this flow 27 is mixed with the liquid of tank 29 of the argon column before being pressurized and sent to the column of mixed.
  • a gas flow 31 containing at most 5 mol% of nitrogen is sent from the head of the mixing column to the vaporizer 7 where it is condensed in separate passages from those in which the column nitrogen condenses medium pressure to increase the reflux in low pressure column tank.
  • air or another fluid can condense there. less volatile than medium pressure nitrogen, provided that it is condensed in another condenser in the system, normally above the vaporizer.
  • Part of the flow 31 can be used as an oxygen-enriched product.
  • An intermediate liquid 33 from the mixing column containing 80 mol%. oxygen is sent to the low pressure column 5.
  • the tank liquid 35 of the mixing column containing 65 mol%. oxygen is sent to the low pressure column 5.
  • a flow 37 containing beyond 99.5% mol. oxygen is drawn off in the tank of the low pressure column 5 either in gaseous form or under liquid form.
  • the low pressure column is supplied ranging from top to bottom with lean liquid 25 containing less than 1 mol% of oxygen, of the blowing air 14, the non-vaporized rich liquid 45 of the head condenser of the argon column, rich liquid 17, liquid from the tank of the mixing column 35, the intermediate liquid of the mixing column 33 and the recondensed mixture 31 of the vaporizer 7.
  • the low pressure column contains at least 80 theoretical plates and preferably at least 90 theoretical trays.
  • Figure 2 differs from that of Figure 1 in that the column mixing is supplied to the tank exclusively by a flow of air from possibly a turbine or a booster (not shown).
  • the vapor of condenser 21 from the argon column is sent to the low pressure column just below the injection point of the rich liquid 45.
  • the argon column can be deleted entirely or can be reduced to a simple vaporizer of rich liquid heated by a gas from the low pressure column (which amounts to a column argon without theoretical plates of distillation).
  • the argon column and / or the low pressure column can be constructed in two sections as described in EP-A-0628777.
  • the second liquid 27 is withdrawn from the low pressure column at a level at least 5 theoretical plates below the point of injection of the liquid rich 45 from the low pressure column, possibly at least 10 theoretical plates below the injection point of the low pressure column, and / or at a level of around a third of theoretical plates in the low pressure column above the tank of the low pressure column.
  • the second liquid 27 is preferably withdrawn at a level between the low pressure column tank 5 and supply level 26 of the argon column 9, in the case where there is an argon column.
  • medium pressure and low pressure columns can be built side by side.
  • the frigories necessary for the appliance can be supplied by at least an insufflation turbine and / or at least one Claude turbine and / or at least one nitrogen turbine.
  • the device can produce liquids and / or gases.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

An amount of product(s) (36, 38, 41, 42) produced by an air separation unit (X) is increased by integrating a single column cryogenic distillation unit (Y) such that the production of the air separation unit is boosted to A+B moles/h. A process for increasing the amount of product(s) produced by the air separation unit (X) comprises integrating the single column cryogenic distillation unit. The product has a different composition, and optionally a different state and/or a different pressure, from the fluid mixture(s). The air separation unit alone, before a single column cryogenic distillation unit is integrated to it, produces an A moles/h of a first product and the amount of the first product withdrawn from the air separation unit and optionally from the distillation unit is increased to C moles/h. C is greater than A, and comprises fluid steam(s) withdrawn from the air separation unit and optionally from the distillation unit. The integration comprises sending energy and/or fluid stream(s) from the air separation unit to the distillation unit and/or from the distillation unit to the air separation unit. The distillation unit treats fluid mixture(s) by process(es) such that the air separation unit produces an amount of first product A+B moles/h. The process(es) is/are pressurization, mixing, expansion, distillation, liquefaction, adsorption, and/or permeation. An Independent claim is also included for an air separation apparatus having an air separation unit comprising a high and/or a low pressure column (25, 27) and possibly an intermediate pressure column and/or mixing column, which are thermally linked; means for producing a stream containing more than 20 mol % oxygen from a single column cryogenic distillation unit; means for sending part(s) of the stream to the high and/or low pressure column and/or intermediate pressure column and/or mixing column; means for sending cooled and purified air to the high pressure and/or to the distillation unit; and means for removing an oxygen enriched product from the unit(s) of the apparatus.

Description

La présente invention est relative à un procédé et installation de séparation d'air par distillation cryogénique. En particulier, elle concerne un procédé de production d'oxygène pur utilisant une colonne de mélange et éventuellement de production d'argon utilisant une colonne d'argonThe present invention relates to a separation process and installation air by cryogenic distillation. In particular, it relates to a method of production of pure oxygen using a mixing column and optionally argon production using an argon column

Dans EP-A-0229803 la colonne de mélange est alimentée en cuve par du liquide riche vaporisé provenant du condenseur de tête de la colonne d'argon.In EP-A-0229803 the mixing column is supplied to the tank with rich liquid vaporized from the head condenser of the argon column.

EP-A-0269342 concerne le cas dans lequel la colonne d'argon est reliée thermiquement avec une colonne de mélange de sorte que le gaz de tête de la colonne d'argon chauffe la colonne de mélange.EP-A-0269342 relates to the case in which the argon column is connected thermally with a mixing column so that the overhead gas from the argon column heats the mixing column.

US-A-5551258 décrit un procédé dans lequel une colonne de mélange est alimentée en tête par un liquide contenant 55 % vol. d'oxygène, le gaz de tête de la colonne de mélange servant ensuite à chauffer le condenseur de cuve de la colonne basse pression.US-A-5551258 describes a process in which a mixing column is fed at the head with a liquid containing 55% vol. oxygen, the overhead gas the mixing column then used to heat the tank condenser of the low pressure column.

Un but de la présente invention est d'augmenter la quantité d'oxygène gazeux pur (contenant plus que 99,5% molaires d'oxygène) qui peut être produit par une double colonne de séparation d'air.An object of the present invention is to increase the amount of gaseous oxygen pure (containing more than 99.5 mol% of oxygen) which can be produced by a double air separation column.

Selon un objet de l'invention, il est prévu une installation de séparation d'air pour produire un fluide riche en oxygène par distillation cryogénique comprenant ;

  • une double colonne comprenant au moins une colonne moyenne pression et une colonne basse pression comprenant un vaporiseur pour vaporiser le liquide de cuve de la colonne basse pression,
  • une colonne de mélange,
  • des moyens pour envoyer de l'air refroidi et comprimé à la colonne moyenne pression,
  • des moyens pour envoyer un liquide enrichi en oxygène de la colonne moyenne pression à un point d'injection de la colonne basse pression et un liquide enrichi en azote de la colonne moyenne pression à la colonne basse pression,
  • des moyens pour envoyer du gaz à la cuve de la colonne de mélange,
  • des moyens pour envoyer un deuxième liquide enrichi en oxygène de la colonne basse pression à la tête de la colonne de mélange, ce deuxième liquide étant moins volatil que le gaz alimentant la cuve de la colonne de mélange,
  • des moyens pour soutirer un fluide riche en oxygène de la colonne basse pression
  • des moyens pour envoyer au moins une partie d'un gaz, éventuellement le gaz de tête, de la colonne de mélange à des passages de chauffage du vaporiseur
   caractérisée en ce qu'elle comprend des moyens pour soutirer le deuxième liquide de la colonne basse pression à un niveau au moins 5 plateaux théoriques en dessous du point d'injection de la colonne basse pression, éventuellement au moins 10 plateaux théoriques en dessous du point d'injection de la colonne basse pression, et/ou à un niveau d'environ d'un tiers de plateaux théoriques de la colonne basse pression au-dessus de la cuve de la colonne basse pression.According to an object of the invention, an air separation installation is provided for producing an oxygen-rich fluid by cryogenic distillation comprising;
  • a double column comprising at least one medium pressure column and a low pressure column comprising a vaporizer for vaporizing the bottom liquid of the low pressure column,
  • a mixing column,
  • means for sending cooled and compressed air to the medium pressure column,
  • means for sending a liquid enriched in oxygen from the medium pressure column to an injection point of the low pressure column and a liquid enriched in nitrogen from the medium pressure column to the low pressure column,
  • means for sending gas to the tank of the mixing column,
  • means for sending a second oxygen-enriched liquid from the low-pressure column to the head of the mixing column, this second liquid being less volatile than the gas supplying the tank of the mixing column,
  • means for withdrawing an oxygen-rich fluid from the low pressure column
  • means for sending at least part of a gas, possibly the overhead gas, from the mixing column to heating passages of the vaporizer
characterized in that it comprises means for withdrawing the second liquid from the low pressure column at a level at least 5 theoretical plates below the point of injection of the low pressure column, possibly at least 10 theoretical plates below the point injection of the low pressure column, and / or at a level of approximately one third of theoretical plates of the low pressure column above the tank of the low pressure column.

L'installation peut comprendre une colonne d'argon ou tout simplement un vaporiseur de liquide de cuve de la colonne moyenne pression par échange de chaleur avec un gaz de la colonne basse pression.The installation can include an argon column or simply a medium pressure column tank vaporizer by exchange of heat with a gas from the low pressure column.

De préférence, elle comprend des moyens pour soutirer le deuxième liquide à un niveau entre le cuve de la colonne et le niveau de soutirage de l'alimentation de la colonne argon ou le niveau de soutirage du gaz basse pression utilisé pour vaporiser le liquide de cuve de la colonne moyenne pression.Preferably, it comprises means for withdrawing the second liquid at a level between the column tank and the withdrawal level of the argon column supply or the low pressure gas withdrawal level used to vaporize the medium pressure column tank liquid.

Dans ce cas, la colonne de mélange peut être alimentée en cuve par n'importe lequel gaz plus volatil que l'oxygène liquide envoyé en tête de colonne.In this case, the mixing column can be supplied to the tank by any gas more volatile than liquid oxygen sent to the top of the column.

Selon un autre objet de l'invention, il est prévu une installation de séparation d'air pour produire un fluide riche en oxygène et éventuellement de l'argon par distillation cryogénique comprenant ;

  • une double colonne comprenant une colonne moyenne pression et une colonne basse pression comprenant un vaporiseur pour vaporiser le liquide de cuve de la colonne basse pression,
  • un condenseur, éventuellement prévu en tête d'une colonne argon de tête,
  • une colonne de mélange,
  • des moyens pour envoyer de l'air refroidi et comprimé à la colonne moyenne pression,
  • des moyens pour envoyer un premier liquide enrichi en oxygène de la colonne moyenne pression au condenseur,
  • des moyens pour soutirer un gaz enrichi en argon à un premier niveau de la colonne basse pression et des moyens pour l'envoyer au condenseur, éventuellement après être enrichi en argon,
  • des moyens pour envoyer un liquide enrichi en oxygène de la colonne moyenne pression à un ou plusieurs points d'injection de la colonne basse pression ,directement et/ou indirectement et un liquide enrichi en azote de la colonne moyenne pression à la colonne basse pression,
  • des moyens pour vaporiser du liquide enrichi en oxygène dans le condenseur de tête et d'en envoyer au moins une partie de la vapeur ou de l'air à la cuve de la colonne de mélange,
  • des moyens pour envoyer un deuxième liquide enrichi en oxygène de la colonne basse pression à la tête de la colonne de mélange, ce deuxième liquide étant moins volatil que le gaz alimentant la cuve de la colonne de mélange
  • éventuellement des moyens pour soutirer un fluide enrichi en argon en tête de la colonne argon,
  • des moyens pour soutirer un fluide riche en oxygène de la colonne basse pression et
  • des moyens pour envoyer au moins une partie d'un gaz, éventuellement le gaz de tête, de la colonne de mélange à des passages de chauffage du vaporiseur.
According to another object of the invention, an air separation installation is provided for producing a fluid rich in oxygen and optionally argon by cryogenic distillation comprising;
  • a double column comprising a medium pressure column and a low pressure column comprising a vaporizer for vaporizing the bottom liquid of the low pressure column,
  • a condenser, possibly provided at the head of an argon column at the top,
  • a mixing column,
  • means for sending cooled and compressed air to the medium pressure column,
  • means for sending a first oxygen-enriched liquid from the medium pressure column to the condenser,
  • means for withdrawing a gas enriched in argon at a first level of the low pressure column and means for sending it to the condenser, possibly after being enriched in argon,
  • means for sending a liquid enriched in oxygen from the medium pressure column to one or more injection points of the low pressure column, directly and / or indirectly and a liquid enriched in nitrogen from the medium pressure column to the low pressure column,
  • means for vaporizing oxygen-enriched liquid in the overhead condenser and for sending at least part of the vapor or air to the tank of the mixing column,
  • means for sending a second liquid enriched in oxygen from the low pressure column to the head of the mixing column, this second liquid being less volatile than the gas supplying the tank of the mixing column
  • possibly means for withdrawing a fluid enriched in argon at the top of the argon column,
  • means for withdrawing an oxygen-rich fluid from the low pressure column and
  • means for sending at least part of a gas, possibly the overhead gas, from the mixing column to heating passages of the vaporizer.

Selon d'autres aspects facultatifs :

  • l'installation comprend des moyens pour soutirer le deuxième liquide de la colonne basse pression à un niveau au moins 5 plateaux théoriques en dessous du point d'injection de la colonne basse pression (ou du point d'injection le plus bas), éventuellement au moins 10 plateaux théoriques en dessous du point d'injection de la colonne basse pression (ou du point d'injection le plus bas) et/ou à un niveau d'environ d'un tiers de plateaux théoriques de la colonne basse pression au-dessus de la cuve de la colonne basse pression.
  • le gaz de tête de la colonne de mélange se condense au moins partiellement dans le vaporiseur et le condensat est envoyé à un niveau de la colonne basse pression, éventuellement au-dessus du premier niveau.
  • il y a des moyens pour envoyer le liquide de cuve de la colonne argon en tête de la colonne de mélange.
  • il y a des moyens pour envoyer un liquide de cuve et un liquide intermédiaire de la colonne de mélange à la double colonne.
  • il y a au moins 80 plateaux théoriques, de préférence au moins 90, dans la colonne basse pression.
  • il y a des moyens pour envoyer de l'air ou un gaz de la colonne moyenne pression à d'autres passages de chauffage du vaporiseur.
  • l'appareil comprend une turbine d'insufflation pour envoyer de l'air à la colonne basse pression ou à la colonne de mélange.
  • l'appareil comprend des moyens pour soutirer de l'azote gazeux de la colonne moyenne pression.
According to other optional aspects:
  • the installation comprises means for withdrawing the second liquid from the low pressure column at a level at least 5 theoretical plates below the injection point of the low pressure column (or the lowest injection point), possibly at minus 10 theoretical plates below the injection point of the low pressure column (or the lowest injection point) and / or at a level of approximately one third of theoretical plates of the low pressure column at- above the tank of the low pressure column.
  • the overhead gas from the mixing column at least partially condenses in the vaporizer and the condensate is sent to a level in the low pressure column, possibly above the first level.
  • there are means for sending the liquid from the bottom of the argon column to the top of the mixing column.
  • there are means for sending a tank liquid and an intermediate liquid from the mixing column to the double column.
  • there are at least 80 theoretical plates, preferably at least 90, in the low pressure column.
  • there are means for sending air or gas from the medium pressure column to other heating passages of the vaporizer.
  • the apparatus includes an insufflation turbine for sending air to the low pressure column or to the mixing column.
  • the apparatus comprises means for withdrawing nitrogen gas from the medium pressure column.

Selon un autre objet de l'invention, il est prévu un procédé de séparation d'air par distillation cryogénique pour produire de l'oxygène avec une double colonne comprenant une colonne moyenne pression
   et une colonne basse pression comprenant un vaporiseur pour vaporiser le liquide de cuve de la colonne basse pression,
   comprenant les étapes de :

  • envoyer de l'air refroidi et comprimé à la colonne moyenne pression,
  • envoyer un liquide enrichi en oxygène et un liquide enrichi en azote de la colonne moyenne pression à la colonne basse pression,
  • envoyer du gaz à la cuve de la colonne de mélange,
  • envoyer un deuxième liquide enrichi en oxygène de la colonne basse pression à la tête de la colonne de mélange, ce deuxième liquide étant moins volatil que le gaz alimentant la cuve de la colonne de mélange,
  • soutirer un fluide riche en oxygène de la colonne basse pression
  • envoyer au moins une partie d'un gaz, éventuellement le gaz de tête, de la colonne de mélange à des passages de chauffage du vaporiseur
   caractérisé en ce quele deuxième liquide contient moins de 5 % mol. d'azote et/ou le gaz envoyé de la colonne de mélange aux passages de chauffage contient moins de 15 % mol. d'azote.According to another object of the invention, there is provided a method of air separation by cryogenic distillation to produce oxygen with a double column comprising a medium pressure column
and a low pressure column comprising a vaporizer for vaporizing the bottom liquid of the low pressure column,
including the steps of:
  • send cooled and compressed air to the medium pressure column,
  • send a liquid enriched in oxygen and a liquid enriched in nitrogen from the medium pressure column to the low pressure column,
  • send gas to the tank of the mixing column,
  • send a second liquid enriched with oxygen from the low pressure column to the head of the mixing column, this second liquid being less volatile than the gas supplying the tank of the mixing column,
  • withdraw an oxygen-rich fluid from the low pressure column
  • send at least part of a gas, possibly the overhead gas, from the mixing column to heating passages of the vaporizer
characterized in that the second liquid contains less than 5% mol. of nitrogen and / or the gas sent from the mixing column to the heating passages contains less than 15 mol%. nitrogen.

Selon un autre objet de l'invention, il est prévu un procédé de séparation d'air par distillation cryogénique pour produire de l'oxygène et éventuellement de l'argon avec une double colonne comprenant

  • une colonne moyenne pression
  • une colonne basse pression comprenant un vaporiseur pour vaporiser le liquide de cuve de la colonne basse pression,
  • un condenseur éventuellement en tête d'une colonne d'argon
  • et une colonne de mélange,
   comprenant les étapes de :
  • envoyer de l'air refroidi et comprimé à la colonne moyenne pression,
  • envoyer un premier liquide enrichi en oxygène de la colonne moyenne pression au condenseur de tête,
  • soutirer un gaz enrichi en argon à un premier niveau de la colonne basse pression et l'envoyer au condenseur ou à la colonne d'argon,
  • envoyer un liquide enrichi en oxygène et un liquide enrichi en azote de la colonne moyenne pression à la colonne basse pression,
  • vaporiser au moins partiellement du liquide enrichi en oxygène du condenseur de tête et envoyer au moins une partie de la vapeur ou de l'air à la cuve de la colonne de mélange,
  • envoyer un deuxième liquide enrichi en oxygène de la colonne basse pression à la tête de la colonne de mélange, ce deuxième liquide étant moins volatil que le gaz alimentant la cuve de la colonne de mélange
  • éventuellement soutirer un fluide enrichi en argon en tête de la colonne argon,
  • soutirer un fluide riche en oxygène de la colonne basse pression et
  • envoyer au moins une partie d'un gaz, éventuellement le gaz de tête, de la colonne de mélange à des passages de chauffage du vaporiseur.
According to another object of the invention, there is provided a method of air separation by cryogenic distillation to produce oxygen and possibly argon with a double column comprising
  • a medium pressure column
  • a low pressure column comprising a vaporizer for vaporizing the bottom liquid of the low pressure column,
  • a condenser possibly at the head of an argon column
  • and a mixing column,
including the steps of:
  • send cooled and compressed air to the medium pressure column,
  • send a first liquid enriched in oxygen from the medium pressure column to the head condenser,
  • withdraw a gas enriched in argon at a first level from the low pressure column and send it to the condenser or to the argon column,
  • send a liquid enriched in oxygen and a liquid enriched in nitrogen from the medium pressure column to the low pressure column,
  • at least partially vaporize oxygen-enriched liquid from the head condenser and send at least some of the vapor or air to the tank of the mixing column,
  • send a second liquid enriched with oxygen from the low pressure column to the head of the mixing column, this second liquid being less volatile than the gas supplying the tank of the mixing column
  • possibly withdrawing a fluid enriched in argon at the top of the argon column,
  • withdraw an oxygen-rich fluid from the low pressure column and
  • send at least part of a gas, possibly the overhead gas, from the mixing column to the vaporizer heating passages.

Selon d'autres aspects facultatifs :

  • le deuxième liquide contient moins de 5 % mol. d'azote et/ou le gaz envoyé de la colonne de mélange aux passages de chauffage contient moins de 15 % mol. d'azote.
  • le gaz de tête de la colonne de mélange se condense au moins partiellement dans le vaporiseur et le condensat est envoyé à un niveau de la colonne basse pression, éventuellement au-dessus du premier niveau.
  • on envoie le liquide de cuve de la colonne argon en tête de la colonne de mélange.
  • on envoie un liquide de cuve et un liquide intermédiaire de la colonne de mélange à la double colonne.
  • un gaz de la colonne moyenne pression ou de l'air se condense au moins partiellement dans d'autres passages de chauffage du vaporiseur.
  • le gaz de tête de la colonne de mélange comprend 3 à 5% mol. d'azote.
  • le gaz de tête de la colonne de mélange comprend au moins 93%mol., éventuellement au moins 95% mol. d'oxygène.
  • le liquide envoyé en tête de la colonne de mélange contient au moins 98% mol. d'oxygène.
  • la colonne de mélange fonctionne à une pression entre 0,5 et 1 bar au dessus de la pression de la colonne basse pression.
According to other optional aspects:
  • the second liquid contains less than 5% mol. of nitrogen and / or the gas sent from the mixing column to the heating passages contains less than 15 mol%. nitrogen.
  • the overhead gas from the mixing column at least partially condenses in the vaporizer and the condensate is sent to a level in the low pressure column, possibly above the first level.
  • the liquid from the argon column is sent to the top of the mixing column.
  • a tank liquid and an intermediate liquid are sent from the mixing column to the double column.
  • gas from the medium pressure column or air at least partially condenses in other heating passages of the vaporizer.
  • the top gas of the mixing column comprises 3 to 5 mol%. nitrogen.
  • the top gas of the mixing column comprises at least 93% mol., optionally at least 95% mol. oxygen.
  • the liquid sent to the head of the mixing column contains at least 98% mol. oxygen.
  • the mixing column operates at a pressure between 0.5 and 1 bar above the pressure of the low pressure column.

Il sera compris que le gaz de tête de la colonne de mélange peut être soutiré au sommet de la colonne de mélange ou au plus cinq plateaux théoriques en dessous du sommet de la colonne de mélange.It will be understood that the head gas of the mixing column can be racked at the top of the mixing column or at most five theoretical plates below the top of the mixing column.

L'invention sera maintenant décrite en plus de détail en se référant aux figures qui illustre schématiquement des installations selon l'invention.The invention will now be described in more detail with reference to the figures. which schematically illustrates installations according to the invention.

L'installation de la Figure 1 comprend une double colonne 1 comprenant une colonne moyenne pression 3 et une colonne basse pression 5 reliées entre elles par un vaporiseur 7.The installation of Figure 1 comprises a double column 1 comprising a medium pressure column 3 and a low pressure column 5 connected between them by a vaporizer 7.

Le vaporiseur comprend des passages de vaporisation de liquide et deux séries indépendantes de passages de chauffage pour deux gaz de chauffage différents.The vaporizer includes liquid vaporization passages and two independent series of heating passages for two different heating gases.

La colonne basse pression opère à entre 1,4 et 2,7 bar et la colonne moyenne pression opère à entre 5 et 8 bar. The low pressure column operates at between 1.4 and 2.7 bar and the column medium pressure operates at between 5 and 8 bar.

La colonne argon 9 est alimentée à partir d'un premier niveau de la colonne basse pression 5. Il y a également une colonne de mélange 11 qui opère à une pression entre 1,9 bar et 3,7 bar.The argon column 9 is supplied from a first level of the column low pressure 5. There is also a mixing column 11 which operates at a pressure between 1.9 bar and 3.7 bar.

Un débit d'air 13 est envoyé à la colonne 3 et un débit d'air insufflé 14 est envoyé à la colonne 5.An air flow 13 is sent to column 3 and a blown air flow 14 is sent to column 5.

Un débit de liquide 15 contenant 40% mol. d'oxygène est soutiré de la cuve de la colonne moyenne pression 3 : une partie 17 de ce liquide alimente la colonne basse pression 5 après détente dans une vanne et une partie 19 du liquide est détendu à entre 1,7 et 2,2 bar absolus dans une vanne et envoyé au condenseur de tête 21 de la colonne argon 9 où il se vaporise au moins partiellement. Le liquide vaporisé 23 est envoyé en cuve de la colonne de mélange.A flow of liquid 15 containing 40 mol%. oxygen is drawn from the medium pressure column tank 3: part 17 of this liquid supplies the low pressure column 5 after expansion in a valve and part 19 of the liquid is expanded to between 1.7 and 2.2 bar absolute in a valve and sent to the overhead condenser 21 of the argon column 9 where it vaporizes at least partially. The vaporized liquid 23 is sent to the tank of the mixing column.

L'azote de tête de la colonne moyenne pression se condense au moins partiellement dans le vaporiseur de cuve 7 et le condensat est envoyé à la colonne moyenne pression et/ou la colonne basse pression.The nitrogen at the top of the medium pressure column at least condenses partially in the tank vaporizer 7 and the condensate is sent to the column medium pressure and / or low pressure column.

Un débit gazeux 41 contenant au moins 80% molaires d'azote est soutiré en tête de la colonne moyenne pression comme produit et constitue 10 à 15% de l'air d'alimentation.A gas flow 41 containing at least 80 mol% of nitrogen is withdrawn at the head of the medium pressure column as product and constitutes 10 to 15% of supply air.

Un débit de liquide 25 enrichi en azote et contenant moins de 2% molaires d'oxygène est envoyé de la colonne moyenne pression à la tête de la colonne basse pression.A flow rate of liquid 25 enriched in nitrogen and containing less than 2 mol% oxygen is sent from the medium pressure column to the head of the column low pressure.

Un débit liquide 27 contenant moins de 5% molaires d'azote est soutiré en cuve de la colonne basse pression 5 en dessous du point de soutirage du gaz 26 destiné à la colonne argon 9 . de préférence, le deuxième liquide est soutiré de la colonne basse pression à un niveau au moins 5 plateaux théoriques en dessous du point d'injection de la colonne basse pression (ou du point d'injection le plus bas), éventuellement au moins 10 plateaux théoriques en dessous du point d'injection de la colonne basse pression (ou du point d'injection le plus bas) et/ou à un niveau d'environ d'un tiers de plateaux théoriques de la colonne basse pression au-dessus de la cuve de la colonne basse pression.A liquid flow 27 containing less than 5 mol% of nitrogen is withdrawn in low pressure column tank 5 below the gas withdrawal point 26 intended for the argon column 9. preferably the second liquid is withdrawn from the low pressure column at a level at least 5 theoretical plates below from the injection point of the low pressure column (or from the most bottom), possibly at least 10 theoretical plates below the point injection of the low pressure column (or of the lowest injection point) and / or at a level of around a third of theoretical plates of the low pressure column above the tank of the low pressure column.

Ce liquide est envoyé après pompage à entre 1,9 et 3,7 bar en tête de la colonne de mélange 11. De préférence ce débit 27 est mélangé avec le liquide de cuve 29 de la colonne argon avant d'être pressurisé et envoyé à la colonne de mélange. This liquid is sent after pumping at between 1.9 and 3.7 bar at the top of the mixing column 11. Preferably this flow 27 is mixed with the liquid of tank 29 of the argon column before being pressurized and sent to the column of mixed.

Un débit gazeux 31 contenant au plus 5% molaires d'azote est envoyé de la tête de la colonne de mélange au vaporiseur 7 où il est condensé dans des passages séparés de ceux dans lesquels se condensent l'azote de la colonne moyenne pression afin d'augmenter le reflux en cuve de colonne basse pression. Eventuellement au lieu de cet azote on peut y condenser de l'air ou un autre fluide moins volatil que l'azote moyenne pression, à condition de condenser celui-ci dans un autre condenseur du système, normalement au-dessus du vaporiseur. Une partie du débit 31 peut servir de produit enrichi en oxygène.A gas flow 31 containing at most 5 mol% of nitrogen is sent from the head of the mixing column to the vaporizer 7 where it is condensed in separate passages from those in which the column nitrogen condenses medium pressure to increase the reflux in low pressure column tank. Optionally, instead of this nitrogen, air or another fluid can condense there. less volatile than medium pressure nitrogen, provided that it is condensed in another condenser in the system, normally above the vaporizer. Part of the flow 31 can be used as an oxygen-enriched product.

Ensuite le liquide contenant 5% mol. d'azote est envoyé à la colonne basse pression à un niveau au-dessus du point de soutirage du débit 26.Then the liquid containing 5% mol. nitrogen is sent to the column low pressure at a level above the flow draw point 26.

Un liquide intermédiaire 33 de la colonne de mélange contenant 80% mol. d'oxygène est envoyé à la colonne basse pression 5.An intermediate liquid 33 from the mixing column containing 80 mol%. oxygen is sent to the low pressure column 5.

Le liquide de cuve 35 de la colonne de mélange contenant 65% mol. d'oxygène est envoyé à la colonne basse pression 5.The tank liquid 35 of the mixing column containing 65 mol%. oxygen is sent to the low pressure column 5.

Un débit 37 contenant au-delà de 99,5 % mol. d'oxygène est soutiré dans la cuve de la colonne basse pression 5 soit sous forme gazeuse soit sous forme liquide.A flow 37 containing beyond 99.5% mol. oxygen is drawn off in the tank of the low pressure column 5 either in gaseous form or under liquid form.

Ainsi on peut voit que la colonne basse pression est alimentée allant de haut en bas par du liquide pauvre 25 contenant moins de 1% mol.d"oxygène, de l'air d'insufflation 14,le liquide riche non-vaporisé 45 du condenseur de tête de la colonne argon, le liquide riche 17,le liquide de la cuve de la colonne de mélange 35,le liquide intermédiaire de la colonne de mélange 33 et le mélange recondensé 31 du vaporiseur 7.So we can see that the low pressure column is supplied ranging from top to bottom with lean liquid 25 containing less than 1 mol% of oxygen, of the blowing air 14, the non-vaporized rich liquid 45 of the head condenser of the argon column, rich liquid 17, liquid from the tank of the mixing column 35, the intermediate liquid of the mixing column 33 and the recondensed mixture 31 of the vaporizer 7.

Afin d'améliorer encore le schéma, plusieurs liquides intermédiaires de la colonne de mélange pourraient être envoyés à la colonne basse pression.In order to further improve the scheme, several intermediate liquids of the mixing column could be sent to the low pressure column.

La colonne basse pression contient au moins 80 plateaux théoriques et de préférence au mois 90 plateaux théoriques.The low pressure column contains at least 80 theoretical plates and preferably at least 90 theoretical trays.

L'installation de la Figure 2 diffère de celle de la Figure 1 en ce que la colonne de mélange est alimentée en cuve exclusivement par un débit d'air provenant éventuellement d'une turbine ou un surpresseur (non-illustrés). La vapeur de condenseur 21 de la colonne argon est envoyée à la colonne basse pression juste en dessous du point d'injection du liquide riche 45. The installation of Figure 2 differs from that of Figure 1 in that the column mixing is supplied to the tank exclusively by a flow of air from possibly a turbine or a booster (not shown). The vapor of condenser 21 from the argon column is sent to the low pressure column just below the injection point of the rich liquid 45.

On pourrait envisager de combiner les concepts des Figures 1 et 2 et alimenter la colonne de mélange en air et en liquide riche vaporisé en même temps.We could consider combining the concepts of Figures 1 and 2 and feed the column mixing with air and rich liquid vaporized at the same time.

Evidemment dans le cas de la Figure 2, la colonne argon peut être supprimée entièrement ou bien peut être réduite à un simple vaporiseur de liquide riche chauffé par un gaz de la colonne basse pression (ce qui revient à une colonne d'argon sans plateaux théoriques de distillation).Obviously in the case of Figure 2, the argon column can be deleted entirely or can be reduced to a simple vaporizer of rich liquid heated by a gas from the low pressure column (which amounts to a column argon without theoretical plates of distillation).

Au besoin la colonne argon et/ou la colonne basse pression peuvent être construites en deux sections de la manière décrite en EP-A-0628777.If necessary, the argon column and / or the low pressure column can be constructed in two sections as described in EP-A-0628777.

Le deuxième liquide 27 est soutiré de la colonne basse pression à un niveau au moins 5 plateaux théoriques en dessous du point d'injection du liquide riche 45 de la colonne basse pression, éventuellement au moins 10 plateaux théoriques en dessous du point d'injection de la colonne basse pression, et/ou à un niveau d'environ d'un tiers de plateaux théoriques de la colonne basse pression au-dessus de la cuve de la colonne basse pression.The second liquid 27 is withdrawn from the low pressure column at a level at least 5 theoretical plates below the point of injection of the liquid rich 45 from the low pressure column, possibly at least 10 theoretical plates below the injection point of the low pressure column, and / or at a level of around a third of theoretical plates in the low pressure column above the tank of the low pressure column.

Le deuxième liquide 27 est soutiré, de préférence, à un niveau entre la cuve de la colonne basse pression 5 et le niveau de soutirage de l'alimentation 26 de la colonne argon 9, dans le cas où il y a une colonne argon.The second liquid 27 is preferably withdrawn at a level between the low pressure column tank 5 and supply level 26 of the argon column 9, in the case where there is an argon column.

De même les colonnes moyenne pression et basse pression peuvent être construites cote à cote.Likewise the medium pressure and low pressure columns can be built side by side.

Ces diverses alimentations étagées permettent d'obtenir une distillation basse pression quasi-parfaite. Ceci permet d'augmenter la production d'oxygène en maintenant ou même en augmentant la production d'argon lorsque l'on soutire plus de 10 à 15% de l'air comme azote moyenne pression ou on envoie 10 à 15% de l'air comme air d'insufflation.These various stepped feeds allow distillation to be obtained almost perfect low pressure. This increases the production of oxygen by maintaining or even increasing the production of argon when withdrawing more than 10 to 15% of the air as medium pressure nitrogen or we send 10 to 15% air as blowing air.

Les frigories nécessaires à l'appareil peuvent être fournies par au moins une turbine d'insufflation et/ou au moins une turbine Claude et/ou au moins une turbine d'azote. L'appareil peut produire des liquides et/ou des gaz.The frigories necessary for the appliance can be supplied by at least an insufflation turbine and / or at least one Claude turbine and / or at least one nitrogen turbine. The device can produce liquids and / or gases.

Claims (29)

Installation de séparation d'air pour produire un fluide riche en oxygène par distillation cryogénique comprenant : une double colonne (1) comprenant au moins une colonne moyenne pression (3) et une colonne basse pression (5)comprenant un vaporiseur (7) pour vaporiser le liquide de cuve de la colonne basse pression, une colonne de mélange (11), des moyens (13) pour envoyer de l'air refroidi et comprimé au moins à la colonne moyenne pression, des moyens (19,25) pour envoyer un liquide enrichi en oxygène de la colonne moyenne pression à un point d'injection de la colonne basse pression et un liquide enrichi en azote de la colonne moyenne pression à la colonne basse pression, des moyens (23,43) pour envoyer du gaz à la cuve de la colonne de mélange, des moyens (27) pour envoyer un deuxième liquide enrichi en oxygène de la colonne basse pression à la tête de la colonne de mélange, ce deuxième liquide étant moins volatil que le gaz alimentant la cuve de la colonne de mélange, des moyens (37) pour soutirer un fluide riche en oxygène de la colonne basse pression    des moyens (31) pour envoyer au moins une partie d'un gaz, éventuellement le gaz de tête, de la colonne de mélange à des passages de chauffage du vaporiseur (7)
   caractérisée en ce que le deuxième liquide (27) est soutiré de la colonne basse pression à un niveau au moins 5 plateaux théoriques en dessous du point d'injection de la colonne basse pression, éventuellement au moins 10 plateaux théoriques en dessous du point d'injection de la colonne basse pression, et/ou à un niveau d'environ d'un tiers de plateaux théoriques de la colonne basse pression au-dessus de la cuve de la colonne basse pression.Air separation installation for producing an oxygen-rich fluid by cryogenic distillation comprising: a double column (1) comprising at least one medium pressure column (3) and a low pressure column (5) comprising a vaporizer (7) for vaporizing the bottom liquid of the low pressure column, a mixing column (11), means (13) for sending cooled and compressed air at least to the medium pressure column, means (19,25) for sending a liquid enriched in oxygen from the medium pressure column to an injection point of the low pressure column and a liquid enriched in nitrogen from the medium pressure column to the low pressure column, means (23,43) for sending gas to the tank of the mixing column, means (27) for sending a second liquid enriched with oxygen from the low pressure column to the head of the mixing column, this second liquid being less volatile than the gas supplying the tank of the mixing column, means (37) for withdrawing an oxygen-rich fluid from the low pressure column means (31) for sending at least part of a gas, possibly the overhead gas, from the mixing column to heating passages of the vaporizer (7)
characterized in that the second liquid (27) is withdrawn from the low pressure column at a level at least 5 theoretical plates below the injection point of the low pressure column, possibly at least 10 theoretical plates below the point of injection of the low pressure column, and / or at a level of approximately one third of theoretical plates of the low pressure column above the tank of the low pressure column. Installation selon la revendication 1 comprenant des moyens (21) pour vaporiser au moins une partie d'un liquide (19) provenant de la colonne moyenne pression (3) et des moyens pour envoyer au moins une partie du liquide vaporisé à la cuve de la colonne de mélange (11).Installation according to claim 1 comprising means (21) for spraying at least part of a liquid (19) from the middle column pressure (3) and means for sending at least part of the vaporized liquid to the tank of the mixing column (11). Installation selon la revendication 2 dans laquelle les moyens (21) pour vaporiser au moins une partie d'un liquide (19) provenant de la colonne moyenne pression (3) sont constitués par le condenseur de tête (21) d'une colonne argon (9).Installation according to claim 2 in which the means (21) for spraying at least part of a liquid (19) from the middle column pressure (3) consist of the head condenser (21) of an argon column (9). Installation selon la revendication 2 dans laquelle les moyens (21) pour vaporiser au moins une partie d'un liquide (19) provenant de la colonne moyenne pression (3) sont constitués par le condenseur chauffé par un gaz de la colonne basse pression (5).Installation according to claim 2 in which the means (21) for spraying at least part of a liquid (19) from the middle column pressure (3) consist of the condenser heated by a column gas low pressure (5). Installation de séparation d'air pour produire un fluide riche en oxygène et éventuellement de l'argon par distillation cryogénique comprenant : une double colonne (1) comprenant une colonne moyenne pression (3) et une colonne basse pression (5) comprenant un vaporiseur (7) pour vaporiser le liquide de cuve de la colonne basse pression, avec un condenseur (21), éventuellement prévu en tête (21)d'une colonne d'argon (9) une colonne de mélange (11), des moyens (13) pour envoyer de l'air refroidi et comprimé à la colonne moyenne pression, des moyens (19) pour envoyer un premier liquide enrichi en oxygène de la colonne moyenne pression au condenseur, des moyens (26) pour soutirer un gaz enrichi en argon à un premier niveau de la colonne basse pression et des moyens pour l'envoyer au condenseur, éventuellement après enrichissement dans la colonne argon, des moyens (17,25) pour envoyer un liquide enrichi en oxygène et un liquide enrichi en azote de la colonne moyenne pression à la colonne basse pression, des moyens pour vaporiser au moins partiellement du liquide enrichi en oxygène dans le condenseur et des moyens (23,43) pour envoyer au moins une partie de la vapeur et/ou de l'air à la cuve de la colonne de mélange, des moyens pour envoyer un deuxième liquide (27) enrichi en oxygène de la colonne basse pression à la tête de la colonne de mélange, ce deuxième liquide étant moins volatil que le gaz alimentant la cuve de la colonne de mélange éventuellement des moyens (47) pour soutirer un fluide enrichi en argon en tête de la colonne argon, des moyens (37) pour soutirer un fluide riche en oxygène de la colonne basse pression    des moyens (31) pour envoyer au moins une partie d'un gaz, éventuellement le gaz de tête, de la colonne de mélange à des passages de chauffage du vaporiseurAir separation installation to produce a fluid rich in oxygen and possibly argon by cryogenic distillation comprising: a double column (1) comprising a medium pressure column (3) and a low pressure column (5) comprising a vaporizer (7) for vaporizing the bottom liquid of the low pressure column, with a condenser (21), optionally provided at the head (21) of an argon column (9) a mixing column (11), means (13) for sending cooled and compressed air to the medium pressure column, means (19) for sending a first liquid enriched in oxygen from the medium pressure column to the condenser, means (26) for withdrawing a gas enriched in argon at a first level of the low pressure column and means for sending it to the condenser, possibly after enrichment in the argon column, means (17,25) for sending a liquid enriched in oxygen and a liquid enriched in nitrogen from the medium pressure column to the low pressure column, means for at least partially vaporizing oxygen-enriched liquid in the condenser and means (23,43) for sending at least part of the steam and / or air to the tank of the mixing column, means for sending a second liquid (27) enriched with oxygen from the low pressure column to the head of the mixing column, this second liquid being less volatile than the gas supplying the tank of the mixing column possibly means (47) for withdrawing a fluid enriched in argon at the top of the argon column, means (37) for withdrawing an oxygen-rich fluid from the low pressure column means (31) for sending at least part of a gas, possibly the overhead gas, from the mixing column to heating passages of the vaporizer Installation selon l'une des revendications 3,4 ou 5 comprenant des moyens pour soutirer le deuxième liquide à un niveau en dessous le point de soutirage du gaz chauffant le condenseur ou du gaz (26) alimentant la colonne argon.Installation according to one of claims 3,4 or 5 comprising means for withdrawing the second liquid at a level below the withdrawal point gas heating the condenser or gas (26) feeding the argon column. Installation selon la revendication 5 dans laquelle le deuxième liquide est soutiré à un niveau entre la cuve de la colonne basse pression (5) et le premier niveau.Installation according to claim 5 in which the second liquid is drawn off at a level between the tank of the low pressure column (5) and the first level. Installation selon la revendication 3 ,5,6 ou 7 dans laquelle le gaz de tête de la colonne de mélange (11) se condense au moins partiellement dans le vaporiseur (7) et au moins une partie du condensat est envoyé à un niveau au-dessus du premier niveau.Installation according to claim 3, 5,6 or 7 in which the head of the mixing column (11) at least partially condenses in the vaporizer (7) and at least part of the condensate is sent to a level above of the first level. Installation selon la revendication 3,5,6,7 ou 8 comprenant des moyens pour envoyer au moins une partie du liquide de cuve de la colonne argon (9) en tête de la colonne de mélange (11).Installation according to claim 3,5,6,7 or 8 comprising means for sending at least part of the liquid from the bottom of the argon column (9) at the head of the mixing column (11). Installation selon l'une des revendications précédentes comprenant des moyens pour envoyer un liquide de cuve et/ou un liquide intermédiaire de la colonne de mélange (11) à la double colonne (1).Installation according to one of the preceding claims comprising means for sending a tank liquid and / or an intermediate liquid from the mixing column (11) to the double column (1). Installation selon l'une des revendications précédentes comprenant au moins 80 plateaux théoriques, de préférence au moins 90, dans la colonne basse pression.Installation according to one of the preceding claims comprising at least 80 theoretical plates, preferably at least 90, in the column low pressure. Installation selon l'une des revendications précédentes comprenant des moyens pour envoyer de l'air ou un gaz contenant plus d'azote que l'air de la colonne moyenne pression à d'autres passages de chauffage du vaporiseur (7). Installation according to one of the preceding claims comprising means for sending air or a gas containing more nitrogen than the air of the medium pressure column to other heating passages of the vaporizer (7). Procédé de séparation d'air par distillation cryogénique pour produire de l'oxygène avec une double colonne (1) comprenant : une colonne moyenne pression (3) une colonne basse pression (5) comprenant un vaporiseur (7) pour vaporiser le liquide de cuve de la colonne basse pression,    comprenant les étapes de : envoyer de l'air refroidi et comprimé à la colonne moyenne pression, envoyer un liquide enrichi en oxygène et un liquide enrichi en azote de la colonne moyenne pression à la colonne basse pression, envoyer du gaz à la cuve de la colonne de mélange, envoyer un deuxième liquide enrichi en oxygène de la colonne basse pression à la tête de la colonne de mélange, ce deuxième liquide étant moins volatil que le gaz alimentant la cuve de la colonne de mélange, soutirer un fluide riche en oxygène de la colonne basse pression envoyer au moins une partie d'un gaz, éventuellement le gaz de tête, de la colonne de mélange à des passages de chauffage du vaporiseur    caractérisé en ce que le deuxième liquide contient moins de 5 % mol. d'azote et/ou le gaz envoyé de la colonne de mélange aux passages de chauffage contient moins de 15 % mol. d'azote.Process for the separation of air by cryogenic distillation to produce oxygen with a double column (1) comprising: a medium pressure column (3) a low pressure column (5) comprising a vaporizer (7) for vaporizing the bottom liquid of the low pressure column, including the steps of: send cooled and compressed air to the medium pressure column, send a liquid enriched in oxygen and a liquid enriched in nitrogen from the medium pressure column to the low pressure column, send gas to the tank of the mixing column, send a second liquid enriched with oxygen from the low pressure column to the head of the mixing column, this second liquid being less volatile than the gas supplying the tank of the mixing column, withdraw an oxygen-rich fluid from the low pressure column send at least part of a gas, possibly the overhead gas, from the mixing column to heating passages of the vaporizer characterized in that the second liquid contains less than 5% mol. of nitrogen and / or the gas sent from the mixing column to the heating passages contains less than 15 mol%. nitrogen. Procédé selon la revendication 13 dans lequel le gaz (23) envoyé en cuve de la colonne de mélange est un liquide vaporisé enrichi en oxygène, soutiré sous forme liquide (19) de la colonne moyenne pression et ensuite vaporisé.The method of claim 13 wherein the gas (23) sent in mixing column tank is a vaporized liquid enriched with oxygen, withdrawn in liquid form (19) from the medium pressure column and then vaporized. Procédé selon la revendication 14 dans lequel le liquide est vaporisé dans un condenseur de tete (21) d'une colonne argon (9).The method of claim 14 in which the liquid is vaporized in a head condenser (21) of an argon column (9). Procédé selon la revendication 14 dans lequel le liquide est vaporisé dans un condenseur chauffé par un gaz provenant de la colonne basse pression (5).The method of claim 14 in which the liquid is vaporized in a condenser heated by a gas from the low pressure column (5). Procédé de séparation d'air par distillation cryogénique pour produire de l'oxygène et éventuellement de l'argon avec une double colonne (1) comprenant une colonne moyenne pression (3) une colonne basse pression (5) comprenant un vaporiseur (7) pour vaporiser le liquide de cuve de la colonne basse pression, un condenseur (21) éventuellement en tête d'une colonne d'argon (9) et une colonne de mélange (11),    comprenant les étapes de : envoyer de l'air refroidi et comprimé à la colonne moyenne pression, envoyer un premier liquide enrichi en oxygène de la colonne moyenne pression au condenseur, soutirer un gaz enrichi en argon à un premier niveau de la colonne basse pression et l'envoyer au condenseur, éventuellement après enrichissement dans la colonne argon, envoyer un liquide enrichi en oxygène et un liquide enrichi en azote de la colonne moyenne pression à la colonne basse pression, vaporiser au moins partiellement du liquide enrichi en oxygène dans le condenseur et envoyer au moins une partie de la vapeur et/ou de l'air à la cuve de la colonne de mélange, envoyer un deuxième liquide enrichi en oxygène de la colonne basse pression à la tête de la colonne de mélange, ce deuxième liquide étant moins volatil que le gaz alimentant la cuve de la colonne de mélange soutirer un fluide enrichi en argon en tête de la colonne argon, soutirer un fluide riche en oxygène de la colonne basse pression envoyer au moins une partie d'un gaz, éventuellement le gaz de tête, de la colonne de mélange à des passages de chauffage du vaporiseur (7). Process for the separation of air by cryogenic distillation to produce oxygen and possibly argon with a double column (1) comprising a medium pressure column (3) a low pressure column (5) comprising a vaporizer (7) for vaporizing the bottom liquid of the low pressure column, a condenser (21) optionally at the head of an argon column (9) and a mixing column (11), including the steps of: send cooled and compressed air to the medium pressure column, send a first liquid enriched in oxygen from the medium pressure column to the condenser, withdraw a gas enriched in argon at a first level of the low pressure column and send it to the condenser, possibly after enrichment in the argon column, send a liquid enriched in oxygen and a liquid enriched in nitrogen from the medium pressure column to the low pressure column, at least partially vaporize oxygen-enriched liquid in the condenser and send at least part of the vapor and / or air to the tank of the mixing column, send a second liquid enriched with oxygen from the low pressure column to the head of the mixing column, this second liquid being less volatile than the gas supplying the tank of the mixing column withdrawing a fluid enriched in argon at the top of the argon column, withdraw an oxygen-rich fluid from the low pressure column send at least part of a gas, possibly the overhead gas, from the mixing column to heating passages of the vaporizer (7). Procédé selon la revendication 17 dans lequel le deuxième liquide contient moins de 5 % mol. d'azote et/ou le gaz envoyé de la colonne de mélange aux passages de chauffage contient moins de 15 % mol. d'azote.The method of claim 17 wherein the second liquid contains less than 5% mol. nitrogen and / or gas sent from the mixing column at the heating passages contains less than 15% mol. nitrogen. Procédé selon l'une des revendications 134 à 18 dans lequel le gaz de tête de la colonne de mélange (11) se condense au moins partiellement dans le vaporiseur (7) et le condensat est éventuellement envoyé à un niveau au-dessus du premier niveau.Method according to one of claims 134 to 18 wherein the gas at the top of the mixing column (11) at least partially condenses in the vaporizer (7) and the condensate is optionally sent to a level above of the first level. Procédé selon la revendication 15,17 ou 18 comprenant l'étape d'envoyer le liquide de cuve de la colonne argon (9) en tête de la colonne de mélange (11). The method of claim 15,17 or 18 comprising the step send the liquid from the argon column (9) to the top of the mixing column (11). Procédé selon l'une des revendications 13 à 20 comprenant l'étape d'envoyer un liquide de cuve et/ou un liquide intermédiaire de la colonne de mélange (11) à la double colonne (1).Method according to one of claims 13 to 20 comprising the step to send a tank liquid and / or an intermediate liquid from the mixing column (11) in the double column (1). Procédé selon l'une des revendications 13 à 21 dans lequel un gaz de la colonne moyenne pression ou de l'air se condense au moins partiellement dans d'autres passages de chauffage du vaporiseur.Method according to one of claims 13 to 21 in which a gas of the medium pressure column or air at least partially condenses in other heating passages of the vaporizer. Procédé selon l'une des revendications 13 à 22 dans lequel le gaz de tête de la colonne de mélange(11) comprend 0,1 à 5 % mol.d'azote, de préférence entre 1 et 3 % mol.d'azote.Method according to one of claims 13 to 22 wherein the gas at the top of the mixing column (11) comprises 0.1 to 5 mol% of nitrogen, preferably between 1 and 3 mol% of nitrogen. Procédé selon l'une des revendications 13 à 23 dans lequel le gaz de tête de la colonne de mélange (11) comprend au moins 93 %, mol. éventuellement au moins 95% mol. d'oxygène.Method according to one of claims 13 to 23 wherein the gas at the top of the mixing column (11) comprises at least 93%, mol. eventually at least 95 mol%. oxygen. Procédé selon l'une des revendications 13 à 24 dans lequel le liquide envoyé en tête de la colonne de mélange (11) contient au moins 99% mol. d'oxygène.Method according to one of claims 13 to 24 wherein the liquid sent at the head of the mixing column (11) contains at least 99% mol. oxygen. Procédé selon l'une des revendications 13 à 25 dans lequel on envoie de l'air à une turbine d'insufflation qui envoie de l'air à la colonne basse pression ou à la colonne de mélange (11).Method according to one of claims 13 to 25 in which we send air to an insufflation turbine which sends air to the lower column pressure or to the mixing column (11). Procédé selon l'une des revendications 13 à 26 dans lequel on soutire du gaz en tête de la colonne moyenne pression comme produit.Method according to one of claims 13 to 26 wherein it is withdrawn gas at the top of the medium pressure column as product. Procédé selon l'une des revendications 13 à 27 dans lequel le gaz envoyé à la cuve de la colonne de mélange est enrichi en oxygène par rapport à de l'air.Method according to one of claims 13 to 27 wherein the gas sent to the mixing column tank is enriched with oxygen compared to air. Procédé selon l'une des revendications 13 à 28 dans lequel la colonne de mélange opère à une pression entre 0 ,5 et 1 bar au-dessus de la pression de la colonne basse pression.Method according to one of claims 13 to 28 wherein the column mixing operates at a pressure between 0, 5 and 1 bar above the pressure of the low pressure column.
EP00403354A 1999-12-02 2000-11-30 Process for air separation by cryogenic distillation Expired - Lifetime EP1106945B1 (en)

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FR9915208 1999-12-02
FR9915208A FR2801963B1 (en) 1999-12-02 1999-12-02 METHOD AND PLANT FOR AIR SEPARATION BY CRYOGENIC DISTILLATION

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102620520A (en) * 2012-04-09 2012-08-01 开封黄河空分集团有限公司 Process for preparing pressure oxygen and pressure nitrogen as well as by-product liquid argon through air separation
CN103162512A (en) * 2013-01-27 2013-06-19 南京瑞柯徕姆环保科技有限公司 Air separation plant used for preparing oxygen and nitrogen in identical-pressure separation mode

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2854232A1 (en) * 2003-04-23 2004-10-29 Air Liquide Air separation procedure to produce argon uses cryogenic distillation with additional liquid flow containing 18-30 mol percent oxygen fed to low pressure column
JP5655104B2 (en) 2013-02-26 2015-01-14 大陽日酸株式会社 Air separation method and air separation device
EP3557166A1 (en) 2018-04-19 2019-10-23 Linde Aktiengesellschaft Method for the low-temperature decomposition of air and air separation plant

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2169561A6 (en) * 1971-02-01 1973-09-07 Air Liquide
US4818262A (en) * 1985-07-15 1989-04-04 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Air distillation process and plant
EP0430803A1 (en) * 1989-11-28 1991-06-05 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and installation for air distillation with argon production
US5291737A (en) * 1991-08-07 1994-03-08 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process or apparatus for distilling air and application in feeding gas to a steel mill
US5379599A (en) * 1993-08-23 1995-01-10 The Boc Group, Inc. Pumped liquid oxygen method and apparatus
US5551258A (en) * 1994-12-15 1996-09-03 The Boc Group Plc Air separation
US5865041A (en) * 1998-05-01 1999-02-02 Air Products And Chemicals, Inc. Distillation process using a mixing column to produce at least two oxygen-rich gaseous streams having different oxygen purities

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE69419675T2 (en) * 1993-04-30 2000-04-06 Boc Group Plc Air separation
US5490391A (en) * 1994-08-25 1996-02-13 The Boc Group, Inc. Method and apparatus for producing oxygen
FR2774159B1 (en) * 1998-01-23 2000-03-17 Air Liquide COMBINED INSTALLATION OF AN OVEN AND AN AIR DISTILLATION APPARATUS AND METHOD OF IMPLEMENTING IT
GB9902101D0 (en) * 1999-01-29 1999-03-24 Boc Group Plc Separation of air

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2169561A6 (en) * 1971-02-01 1973-09-07 Air Liquide
US4818262A (en) * 1985-07-15 1989-04-04 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Air distillation process and plant
EP0430803A1 (en) * 1989-11-28 1991-06-05 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and installation for air distillation with argon production
US5291737A (en) * 1991-08-07 1994-03-08 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process or apparatus for distilling air and application in feeding gas to a steel mill
US5379599A (en) * 1993-08-23 1995-01-10 The Boc Group, Inc. Pumped liquid oxygen method and apparatus
US5551258A (en) * 1994-12-15 1996-09-03 The Boc Group Plc Air separation
US5865041A (en) * 1998-05-01 1999-02-02 Air Products And Chemicals, Inc. Distillation process using a mixing column to produce at least two oxygen-rich gaseous streams having different oxygen purities

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102620520A (en) * 2012-04-09 2012-08-01 开封黄河空分集团有限公司 Process for preparing pressure oxygen and pressure nitrogen as well as by-product liquid argon through air separation
CN102620520B (en) * 2012-04-09 2014-09-17 开封黄河空分集团有限公司 Process for preparing pressure oxygen and pressure nitrogen as well as by-product liquid argon through air separation
CN103162512A (en) * 2013-01-27 2013-06-19 南京瑞柯徕姆环保科技有限公司 Air separation plant used for preparing oxygen and nitrogen in identical-pressure separation mode
CN103162512B (en) * 2013-01-27 2015-06-10 南京瑞柯徕姆环保科技有限公司 Air separation plant used for preparing oxygen and nitrogen in identical-pressure separation mode

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DE60020500D1 (en) 2005-07-07
ATE297001T1 (en) 2005-06-15
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FR2801963A1 (en) 2001-06-08
US6385996B2 (en) 2002-05-14
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EP1106945B1 (en) 2005-06-01
US20010003909A1 (en) 2001-06-21

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