EP2510294B1 - Process and unit for the separation of air by cryogenic distillation - Google Patents

Process and unit for the separation of air by cryogenic distillation Download PDF

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Publication number
EP2510294B1
EP2510294B1 EP10776785.7A EP10776785A EP2510294B1 EP 2510294 B1 EP2510294 B1 EP 2510294B1 EP 10776785 A EP10776785 A EP 10776785A EP 2510294 B1 EP2510294 B1 EP 2510294B1
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Prior art keywords
pressure column
chamber
low
flow
pressure
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EP10776785.7A
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German (de)
French (fr)
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EP2510294A1 (en
Inventor
Benoit Davidian
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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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    • 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
    • F25J3/04436—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 at least a triple pressure main column system
    • F25J3/04454—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 at least a triple pressure main column system a main column system not otherwise provided, e.g. serially coupling of columns or more than three pressure levels
    • 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
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • F25J3/04066—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams 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
    • F25J3/04163—Hot end purification of the feed air
    • F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
    • F25J3/04181—Regenerating the adsorbents
    • 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
    • F25J3/04309—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 nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/04—Mixing or blending of fluids with the feed 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/42—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
    • F25J2240/46—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval 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
    • F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
    • 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

Definitions

  • the present invention relates to a method and apparatus for air separation by cryogenic distillation.
  • An object of the invention is to reduce the separation energy to produce impure oxygen, especially in the case where there is no co-production of nitrogen.
  • Another object of the invention is to reduce the cost of at least some elements of the apparatus.
  • the invention involves the use of a cold compressor for compressing an oxygen-rich gas from an enclosure operating at a pressure below that of the low pressure column, the gas being intended for the tank of a column low pressure. This makes it possible to decouple the medium pressure column vessel pressure with the top of the low pressure column.
  • the invention is particularly interesting for the case where air partially condenses in the condenser of the chamber operating at lower pressure than the low pressure column.
  • an air separation apparatus comprising a medium pressure column, a low pressure column, an enclosure, an exchanger, a condenser of the low pressure column and a condenser placed in the enclosure, a pipe for supplying compressed, purified and cooled air from the exchanger to the medium pressure column, a pipe for sending a heat-transfer gas to the condenser placed in the enclosure, a pipe for sending a gas enriched in nitrogen from the medium pressure column at the condenser of the low pressure column, a pipe for sending an oxygen enriched flow from the tank of the medium pressure column to the low pressure column, a pipe for sending oxygen-rich liquid from the column vessel low pressure to the enclosure, a pipe for withdrawing from the enclosure a fluid richer in oxygen than that sent to the enclosure, a pipe for returning a gas from the enclosure to the column low pressure, a pipe for withdrawing a gas at the top of the low pressure column, characterized in that it comprises an expansion means for expanding the oxygen-rich liquid downstream of the
  • the air 1 is compressed between 3 and 5 bar in a compressor 3, purified in a purification unit 5 and divided into two.
  • a part 9 cools in the exchanger 13 and is sent to the tank condenser 15 of a chamber 141 where it partially condenses before being sent to the medium pressure column 39 of a double column.
  • the double column comprises the medium pressure column 39 and a low pressure column 41 which overcomes it, the thermal link between the two columns being provided by a condenser 25 in the tank of the low pressure column 41.
  • the other part of the air 7 is compressed in a compressor 11, cooled in the exchanger 13 and used to vaporize liquid oxygen under pressure. As the oxygen is vaporized at a low pressure, the vaporization takes place in an external vaporizer 27, distinct from the exchanger 13.
  • the liquefied air thus formed is sent to the medium pressure column 39 after expansion in a valve 19. Liquid air can also be sent to the low pressure column.
  • An oxygen enriched liquid 17 is withdrawn in the vat from the medium pressure column 39, cooled in the exchanger 43, expanded in a valve and sent to the low pressure column 41.
  • a liquid 49 having substantially the composition of the air is drawn off. at an intermediate level of the medium pressure column 39, cooled in the exchanger 43, expanded in a valve and sent to the low pressure column 41.
  • a nitrogen-enriched liquid 47 is withdrawn at the top of the medium pressure column 39, cooled in the exchanger 43, expanded in a valve and sent to the top of the low pressure column 41.
  • a gas 45 rich in nitrogen is withdrawn at the top of the low pressure column, heated in the exchanger 43 and then in the exchanger 13. Part of this gas can be compressed in the compressor 35 to form the flow 37 which participates in the regeneration of the purification unit 5.
  • a medium pressure nitrogen flow 33 is withdrawn at the top of the medium pressure column 39, heated in the exchanger 13, expanded in the turbine 23 and again heated in the exchanger 13 before serving for the regeneration of the purification unit 5.
  • a flow rich in oxygen 53 containing between 45 and 75% of oxygen is withdrawn from the tank of the low pressure column 41, expanded in a valve 51 and sent to the top of the chamber 141 which in this variant is a distillation column With a tank condenser 15. Above the condenser there are means for heat and mass exchange 143, for example packings, structured or not, or trays.
  • the valve 51 only lowers the liquid pressure by about 0.15 bar.
  • the liquid 53 is separated in the chamber to form a richer oxygen-rich liquid 29 in the tank. It is this liquid 29 which is sent to the vaporizer 27 after pressurization in the pump 63.
  • a purge liquid 61 is withdrawn from the vaporizer 27.
  • an oxygen-rich gas can be withdrawn from the chamber 141.
  • a top gas 145 is withdrawn from the chamber, compressed at the withdrawal temperature in a compressor 21 which increases its pressure by at most 0.15 bar.
  • the product gas is reinjected into the vessel of the low pressure column at the outlet pressure of the compressor 21.
  • the apparatus of the figure 2 differs from that of the figure 1 in that the enclosure 141 does not contain packings or trays. There is also the ascending partial condensation in the vaporizer 15. Thus the difference in composition between the liquid 53 sent to the chamber and the liquid 29 withdrawn from the chamber is very small even if the liquid 29 is still richer.
  • the gas 145 is the gas produced by partial vaporization of the liquid 53 in the chamber 141 by heat exchange with the air 9.

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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)

Description

La présente invention est relative à un procédé et à un appareil de séparation d'air par distillation cryogénique.The present invention relates to a method and apparatus for air separation by cryogenic distillation.

Il est connu de séparer l'air dans un appareil comprenant une colonne moyenne pression et deux colonnes basse pression opérant à la même pression, une des colonnes basse pression étant alimentée en tête par le liquide de cuve de l'autre et chaque colonne basse pression ayant un condenseur de cuve.It is known to separate the air in an apparatus comprising a medium pressure column and two low pressure columns operating at the same pressure, one of the low pressure columns being fed at the top by the vessel liquid of the other and each low pressure column. having a tank condenser.

Un but de l'invention est de réduire l'énergie de séparation pour produire de l'oxygène impur, en particulier dans le cas où il n'y a pas de co-production d'azote.An object of the invention is to reduce the separation energy to produce impure oxygen, especially in the case where there is no co-production of nitrogen.

Un autre but de l'invention est de réduire le coût d'au moins certains éléments de l'appareil.Another object of the invention is to reduce the cost of at least some elements of the apparatus.

Tous les pourcentages relatifs à des puretés sont des pourcentages molaires.All percentages for purities are molar percentages.

L'invention implique l'utilisation d'un compresseur froid pour comprimer un gaz riche en oxygène, provenant d'une enceinte opérant à une pression en dessous de celle de la colonne basse pression, le gaz étant destiné à la cuve d'une colonne basse pression. Ceci permet de découpler la pression en cuve de colonne moyenne pression avec le haut de la colonne basse pression.The invention involves the use of a cold compressor for compressing an oxygen-rich gas from an enclosure operating at a pressure below that of the low pressure column, the gas being intended for the tank of a column low pressure. This makes it possible to decouple the medium pressure column vessel pressure with the top of the low pressure column.

L'invention est particulièrement intéressante pour le cas où de l'air se condense partiellement dans le condenseur de l'enceinte opérant à plus basse pression que la colonne basse pression.The invention is particularly interesting for the case where air partially condenses in the condenser of the chamber operating at lower pressure than the low pressure column.

Selon un objet de l'invention, il est prévu un procédé de séparation d'air par distillation cryogénique dans lequel :

  1. i) un débit d'air comprimé et épuré est refroidi dans un échangeur et envoyé à une colonne opérant à une moyenne pression
  2. ii) le débit d'air se sépare en un débit enrichi en azote et un débit enrichi en oxygène
  3. iii) une partie du débit enrichi en azote est envoyé à une colonne basse pression
  4. iv) au moins une partie du débit enrichi en oxygène est envoyée à la colonne basse pression
  5. v) un débit riche en azote est soutiré de la tête de la colonne basse pression
  6. vi) un débit riche en oxygène est soutiré de la cuve de la colonne basse pression et envoyé à une enceinte contenant au moins un condenseur-vaporiseur
  7. vii) un débit gazeux provenant de l'enceinte en est soutiré renvoyé à la première colonne basse pression, de préférence en cuve
  8. viii) une partie du débit enrichi en azote de l'étape ii) se condense au moins partiellement dans un condenseur alimenté par un liquide de cuve de la colonne basse pression et est envoyé à la colonne moyenne pression et/ou la colonne basse pression
  9. ix) un débit de gaz calorigène, éventuellement au moins une partie de l'air comprimé, épuré et refroidi dans l'échangeur de l'étape i), se condense au moins partiellement dans le condenseur vaporiseur de l'enceinte
  10. x) on soutire un fluide plus riche en oxygène de l'enceinte que le débit soutiré en cuve de la colonne basse pression
caractérisé en ce que l'on détend le débit riche en oxygène soutiré de la cuve de la colonne basse pression en amont de l'enceinte et on pressurise le débit gazeux de l'enceinte en amont de la première colonne basse pression.According to one object of the invention, there is provided a method of air separation by cryogenic distillation in which:
  1. i) a flow of compressed and purified air is cooled in an exchanger and sent to a column operating at a medium pressure
  2. ii) the airflow separates into a nitrogen enriched flow and an oxygen enriched flow rate
  3. iii) part of the nitrogen enriched flow is sent to a low pressure column
  4. iv) at least a portion of the oxygen enriched flow is sent to the low pressure column
  5. v) a nitrogen-rich flow is withdrawn from the head of the low pressure column
  6. vi) a flow rich in oxygen is withdrawn from the tank of the low pressure column and sent to an enclosure containing at least one condenser-vaporizer
  7. vii) a gas flow from the chamber is withdrawn returned to the first low pressure column, preferably in the tank
  8. viii) a part of the nitrogen enriched flow of step ii) is condensed at least partially in a condenser supplied with a bottom liquid from the low pressure column and is sent to the medium pressure column and / or the low pressure column
  9. ix) a flow of caloric gas, possibly at least a portion of the compressed air, purified and cooled in the exchanger of step i), is condensed at least partially in the vaporizer condenser of the enclosure
  10. x) a fluid richer in oxygen from the chamber is withdrawn than the flow withdrawn in the vat from the low pressure column
characterized in that the oxygen-rich flow rate withdrawn from the low pressure column tank is expanded upstream of the chamber and the gaseous flow rate of the chamber upstream of the first low pressure column is pressurized.

De préférence :

  • on comprime le débit gazeux provenant de l'enceinte dans un compresseur ayant une température d'entrée inférieure à -50°C, de préférence aucun étape de chauffage a lieu entre l'enceinte et le compresseur ;
  • on détend le débit riche en oxygène soutiré de la colonne basse pression à une pression au plus 1 bar en dessous de la pression en cuve de la colonne basse pression, de préférence au plus 0,5 bar, voire au plus 0,2 bar en dessous de cette pression et/ou on comprime le débit gazeux provenant de l'enceinte pour augmenter sa pression d'au plus 1 bar, de préférence au plus 0,5 bar, voire au plus 0,2 bar en amont de la colonne basse pression ;
  • l'enceinte ne contient pas de moyen d'échange de masse, voire ne contient ni garnissages ni plateaux de distillation ;
  • l'enceinte constitue une deuxième colonne basse pression et contient des moyens d'échange de masse, tels que des garnissages ou des plateaux de distillation, placés au moins au-dessus du condenseur.
Preferably:
  • the gas flow from the enclosure is compressed in a compressor having an inlet temperature lower than -50 ° C, preferably no heating step takes place between the enclosure and the compressor;
  • the oxygen-rich flow rate withdrawn from the low-pressure column is depressurized at a pressure at most 1 bar below the tank pressure of the low-pressure column, preferably at most 0.5 bar, or even at most 0.2 bar, below this pressure and / or compressing the gas flow from the chamber to increase its pressure by at most 1 bar, preferably at most 0.5 bar, or even at most 0.2 bar upstream of the lower column pressure;
  • the enclosure does not contain mass exchange means, or contains neither liners nor distillation trays;
  • the enclosure constitutes a second low pressure column and contains mass exchange means, such as packings or distillation trays, placed at least above the condenser.

Selon un autre objet de l'invention, il est prévu un appareil de séparation d'air comprenant une colonne moyenne pression, une colonne basse pression, une enceinte, un échangeur, un condenseur de la colonne basse pression et un condenseur placé dans l'enceinte, une conduite pour envoyer de l'air comprimé, épuré et refroidi de l'échangeur à la colonne moyenne pression, une conduite pour envoyer un gaz calorigène au condenseur placé dans l'enceinte, une conduite pour envoyer un gaz enrichi en azote de la colonne moyenne pression au condenseur de la colonne basse pression, une conduite pour envoyer un débit enrichi en oxygène de la cuve de la colonne moyenne pression à la colonne basse pression, une conduite pour envoyer du liquide riche en oxygène de la cuve de la colonne basse pression à l'enceinte, une conduite pour soutirer de l'enceinte un fluide plus riche en oxygène que celui envoyé à l'enceinte, une conduite pour renvoyer un gaz de l'enceinte à la colonne basse pression, une conduite pour soutirer un gaz en tête de la colonne basse pression caractérisé en ce qu'il comprend un moyen de détente pour détendre le liquide riche en oxygène en aval de la cuve de la colonne basse pression et en amont de l'enceinte et un compresseur pour comprimer le gaz de l'enceinte en aval de l'enceinte et en amont de la colonne basse pression.According to another object of the invention, there is provided an air separation apparatus comprising a medium pressure column, a low pressure column, an enclosure, an exchanger, a condenser of the low pressure column and a condenser placed in the enclosure, a pipe for supplying compressed, purified and cooled air from the exchanger to the medium pressure column, a pipe for sending a heat-transfer gas to the condenser placed in the enclosure, a pipe for sending a gas enriched in nitrogen from the medium pressure column at the condenser of the low pressure column, a pipe for sending an oxygen enriched flow from the tank of the medium pressure column to the low pressure column, a pipe for sending oxygen-rich liquid from the column vessel low pressure to the enclosure, a pipe for withdrawing from the enclosure a fluid richer in oxygen than that sent to the enclosure, a pipe for returning a gas from the enclosure to the column low pressure, a pipe for withdrawing a gas at the top of the low pressure column, characterized in that it comprises an expansion means for expanding the oxygen-rich liquid downstream of the bottom of the low pressure column and upstream of the enclosure and a compressor for compressing the gas of the enclosure downstream of the enclosure and upstream of the low pressure column.

Eventuellement :

  • l'enceinte comprend des moyens d'échange de matière au-dessus du condenseur;
  • l'enceinte ne comprend aucun moyen d'échange de matière au-dessus du condenseur ;
  • l'appareil comprend une turbine et une conduite pour envoyer un gaz riche en azote de la colonne moyenne pression à la turbine ;
  • l'appareil comprend une pompe pour pressuriser un débit d'oxygène liquide provenant de la colonne basse pression et/ou de l'enceinte en amont de l'échangeur.
Eventually :
  • the enclosure comprises material exchange means above the condenser;
  • the enclosure does not include any material exchange means above the condenser;
  • the apparatus comprises a turbine and a pipe for supplying a nitrogen-rich gas from the medium pressure column to the turbine;
  • the apparatus comprises a pump for pressurizing a flow of liquid oxygen from the low pressure column and / or the chamber upstream of the exchanger.

L'invention sera décrite en plus de détail en se référant aux figures, qui représentent des appareils selon l'invention.The invention will be described in more detail with reference to the figures, which show apparatus according to the invention.

Dans la Figure 1, l'air 1 est comprimé entre 3 et 5 bars dans un compresseur 3, épuré dans une unité d'épuration 5 et divisé en deux. Une partie 9 se refroidit dans l'échangeur 13 et est envoyée au condenseur de cuve 15 d'une enceinte 141 où elle se condense partiellement avant être envoyé à la colonne moyenne pression 39 d'une double colonne.In the Figure 1 , the air 1 is compressed between 3 and 5 bar in a compressor 3, purified in a purification unit 5 and divided into two. A part 9 cools in the exchanger 13 and is sent to the tank condenser 15 of a chamber 141 where it partially condenses before being sent to the medium pressure column 39 of a double column.

La double colonne comprend la colonne moyenne pression 39 et une colonne basse pression 41 qui la surmonte, le lien thermique entre les deux colonnes étant assuré par un condenseur 25 dans la cuve de la colonne basse pression 41.The double column comprises the medium pressure column 39 and a low pressure column 41 which overcomes it, the thermal link between the two columns being provided by a condenser 25 in the tank of the low pressure column 41.

L'autre partie de l'air 7 est comprimé dans un compresseur 11, refroidi dans l'échangeur 13 et utilisé pour vaporiser de l'oxygène liquide sous pression. Comme l'oxygène est vaporisé à une basse pression la vaporisation a lieu dans un vaporiseur extérieur 27, distinct de l'échangeur 13. L'air liquéfié ainsi formé est envoyé à la colonne moyenne pression 39 après détente dans une vanne 19. L'air liquide peut également être envoyé à la colonne basse pression.The other part of the air 7 is compressed in a compressor 11, cooled in the exchanger 13 and used to vaporize liquid oxygen under pressure. As the oxygen is vaporized at a low pressure, the vaporization takes place in an external vaporizer 27, distinct from the exchanger 13. The liquefied air thus formed is sent to the medium pressure column 39 after expansion in a valve 19. Liquid air can also be sent to the low pressure column.

Un liquide enrichi en oxygène 17 est soutiré en cuve de la colonne moyenne pression 39, refroidi dans l'échangeur 43, détendu dans une vanne et envoyé à la colonne basse pression 41. Un liquide 49 ayant substantiellement la composition de l'air est soutiré à un niveau intermédiaire de la colonne moyenne pression 39, refroidi dans l'échangeur 43, détendu dans une vanne et envoyé à la colonne basse pression 41. Un liquide enrichi en azote 47 est soutiré en tête de la colonne moyenne pression 39, refroidi dans l'échangeur 43, détendu dans une vanne et envoyé en tête de la colonne basse pression 41.An oxygen enriched liquid 17 is withdrawn in the vat from the medium pressure column 39, cooled in the exchanger 43, expanded in a valve and sent to the low pressure column 41. A liquid 49 having substantially the composition of the air is drawn off. at an intermediate level of the medium pressure column 39, cooled in the exchanger 43, expanded in a valve and sent to the low pressure column 41. A nitrogen-enriched liquid 47 is withdrawn at the top of the medium pressure column 39, cooled in the exchanger 43, expanded in a valve and sent to the top of the low pressure column 41.

Un gaz 45 riche en azote est soutiré en tête de la colonne basse pression, chauffé dans l'échangeur 43 et ensuite dans l'échangeur 13. Une partie de ce gaz peut être comprimé dans le compresseur 35 pour former le débit 37 qui participe à la régénération de l'unité d'épuration 5.A gas 45 rich in nitrogen is withdrawn at the top of the low pressure column, heated in the exchanger 43 and then in the exchanger 13. Part of this gas can be compressed in the compressor 35 to form the flow 37 which participates in the regeneration of the purification unit 5.

Un débit d'azote moyenne pression 33 est soutiré en tête de la colonne moyenne pression 39, chauffé dans l'échangeur 13, détendu dans la turbine 23 et de nouveau chauffé dans l'échangeur 13 avant de servir à la régénération de l'unité d'épuration 5.A medium pressure nitrogen flow 33 is withdrawn at the top of the medium pressure column 39, heated in the exchanger 13, expanded in the turbine 23 and again heated in the exchanger 13 before serving for the regeneration of the purification unit 5.

Un débit riche en oxygène 53 contenant entre 45 et 75 % d'oxygène est soutiré de la cuve de la colonne basse pression 41, détendu dans une vanne 51 et envoyé en tête de l'enceinte 141 qui dans cette variante est une colonne de distillation avec un condenseur de cuve 15. Au-dessus du condenseur se trouvent des moyens d'échange de chaleur et de masse 143, par exemple des garnissages, structurés ou pas, ou des plateaux. La vanne 51 ne fait baisser la pression du liquide que de 0.15 .bar environA flow rich in oxygen 53 containing between 45 and 75% of oxygen is withdrawn from the tank of the low pressure column 41, expanded in a valve 51 and sent to the top of the chamber 141 which in this variant is a distillation column With a tank condenser 15. Above the condenser there are means for heat and mass exchange 143, for example packings, structured or not, or trays. The valve 51 only lowers the liquid pressure by about 0.15 bar.

Le liquide 53 est séparé dans l'enceinte pour former un liquide plus riche en oxygène 29 en cuve. C'est ce liquide 29 qui est envoyé au vaporiseur 27 après pressurisation dans la pompe 63. Un liquide de purge 61 est soutiré du vaporiseur 27. Alternativement un gaz riche en oxygène peut être soutiré de l'enceinte 141.The liquid 53 is separated in the chamber to form a richer oxygen-rich liquid 29 in the tank. It is this liquid 29 which is sent to the vaporizer 27 after pressurization in the pump 63. A purge liquid 61 is withdrawn from the vaporizer 27. Alternatively an oxygen-rich gas can be withdrawn from the chamber 141.

Un gaz de tête 145 est soutiré de l'enceinte, comprimé à la température de soutirage dans un compresseur 21 qui fait augmenter sa pression d'au plus 0.15.bars. Le gaz produit est réinjecté dans la cuve de la colonne basse pression à la pression de sortie du compresseur 21.A top gas 145 is withdrawn from the chamber, compressed at the withdrawal temperature in a compressor 21 which increases its pressure by at most 0.15 bar. The product gas is reinjected into the vessel of the low pressure column at the outlet pressure of the compressor 21.

Avec un écart de température dans l'échangeur 13 de 2°C au bout chaud, on obtient un gain d'environ 2.5% par rapport au même schéma sans le compresseur froid en cuve de la colonne basse pressionWith a temperature difference in the exchanger 13 of 2 ° C. at the hot end, a gain of approximately 2.5% is obtained with respect to the same scheme without the cold compressor in the tank of the low pressure column.

L'appareil de la figure 2 diffère de celui de la figure 1 en ce que l'enceinte 141 ne contient pas de garnissages ou de plateaux. Il y a aussi la condensation partielle ascendante dans le vaporiseur 15. Ainsi la différence de composition entre le liquide 53 envoyé à l'enceinte et le liquide 29 soutiré de l'enceinte est très réduite même si le liquide 29 est tout de même plus riche en oxygène que le liquide 53. Le gaz 145 est le gaz produit par vaporisation partielle du liquide 53 dans l'enceinte 141 par échange de chaleur avec l'air 9.The apparatus of the figure 2 differs from that of the figure 1 in that the enclosure 141 does not contain packings or trays. There is also the ascending partial condensation in the vaporizer 15. Thus the difference in composition between the liquid 53 sent to the chamber and the liquid 29 withdrawn from the chamber is very small even if the liquid 29 is still richer. The gas 145 is the gas produced by partial vaporization of the liquid 53 in the chamber 141 by heat exchange with the air 9.

Si on serre l'écart de température au bout chaud de l'échangeur 13 à 2°C, on a un gain d'environ 1.5% par rapport au même schéma sans compresseur froid en cuve BP.If we tighten the temperature difference at the hot end of the exchanger 13 at 2 ° C, we have a gain of about 1.5% compared to the same scheme without cold compressor in LP tank.

On obtient une énergie très légèrement meilleure celui du procédé de WO-A-2007/129152 avec l'échangeur serré à 2°C au bout chaud. Même si dans les deux procédés, on utilise un compresseur froid, dans la variante de l'invention la puissance du compresseur froid est 10 fois plus petite que dans la variante de l'art antérieur et la turbine azote 2 fois plus petite. On constate aussi que le taux de compression dans la variante selon l'invention est très faible et qu'une technologie proche d'un ventilateur doit suffire pour le compresseur 21 : ces éléments permettent de dire que le compresseur froid 21 et la turbine 23 seront moins coûteux que dans le procédé de l'art antérieur.A slightly better energy is obtained than that of the process of WO-2007/129152 with the exchanger tight at 2 ° C at the hot end. Even if in both processes, a cold compressor is used, in the variant of the invention the power of the cold compressor is 10 times smaller than in the variant of the prior art and the nitrogen turbine 2 times smaller. It can also be seen that the compression ratio in the variant according to the invention is very low and that a technology close to a fan must suffice for the compressor 21: these elements make it possible to say that the cold compressor 21 and the turbine 23 will be less expensive than in the method of the prior art.

La compression cryogénique d'un fluide relativement riche en oxygène ne doit pas poser de problème de sécurité.Cryogenic compression of a relatively oxygen-rich fluid should not pose a safety problem.

Le concept de compression de la partie vapeur dans la colonne basse pression peut être étendu au cas des schémas avec trois condenseurs dans la colonne basse pression, avec un ou deux compresseurs froid à placer entre les trois condenseurs de la colonne basse pression.The concept of compression of the vapor part in the low pressure column can be extended to the case of diagrams with three condensers in the low pressure column, with one or two cold compressors to be placed between the three condensers of the low pressure column.

Claims (10)

  1. Method of separating air by cryogenic distillation, wherein:
    i) a flow of compressed purified air is cooled in a heat exchanger (13) and sent to a column (39) operating at a medium pressure,
    ii) the air flow is separated into a nitrogen-enriched flow and an oxygen-enriched flow,
    iii) a part of the nitrogen-enriched flow is sent to a low-pressure column (41),
    iv) at least a part of the oxygen-enriched flow is sent to the low-pressure column,
    v) a nitrogen-rich flow is drawn off from the head of the low-pressure column,
    vi) an oxygen-rich flow is drawn off from the tank of the low-pressure column and sent to a chamber (141) containing at least a condenser-vaporiser (15),
    vii) a gaseous flow originating from the chamber is drawn off therefrom and returned to the low-pressure column, preferably to the tank,
    viii) a part of the nitrogen-enriched flow of step ii) is at least partly condensed in a condenser (25) supplied with liquid originating from the low-pressure column and is sent to the medium-pressure column and/or the low-pressure column,
    ix) a flow of calorigenic gas, optionally at least a part of the compressed air, purified and cooled in the heat exchanger of step i), is at least partly condensed in the condenser-vaporiser of the chamber,
    x) a fluid is drawn off from the chamber that is richer in oxygen than the flow drawn off from the tank of the low-pressure column,
    xi) characterised in that the pressure of the oxygen-rich flow drawn off from the tank of the low-pressure column is reduced upstream of the chamber and the gaseous flow of the chamber is pressurised upstream of the first low-pressure column.
  2. Method according to claim 1, wherein the gaseous flow originating from the chamber is compressed in a compressor (21) having an entry temperature of less than -50 °C, and preferably no heating step takes place between the chamber and the compressor.
  3. Method according to either claim 1 or claim 2, wherein the pressure of the oxygen-rich flow drawn off from the low-pressure column (41) is reduced to a pressure of at most 1 bar below the pressure in the tank of the low-pressure column, preferably 0.5 bar at most, or even 0.2 bar at most below this pressure and/or the gaseous flow originating from the chamber (141) is compressed to increase the pressure thereof by 1 bar at most, preferably 0.5 bar at most, or even 0.2 bar at most upstream of the low-pressure column.
  4. Method according to any one of the preceding claims, wherein the chamber (141) does not contain any mass exchange means, nor does it contain either packing or distillation trays.
  5. Method according to any one of claims 1 to 3, wherein the chamber (141) forms a second low-pressure column and contains mass exchange means (143), such as packing or distillation trays, placed at least above the condenser.
  6. Air separation apparatus comprising a medium-pressure column (39), a low-pressure column (41), a chamber (141), a heat exchanger (13), a condenser (25) of the low-pressure column and a condenser (15) placed in the chamber, a pipe for sending the cooled, purified and compressed air from the heat exchanger to the medium-pressure column, a pipe for sending a calorigenic gas to the condenser placed in the chamber, a pipe for sending a nitrogen-enriched gas from the medium-pressure column to the condenser of the low-pressure column, a pipe for sending an oxygen-enriched flow from the tank of the medium-pressure column to the low-pressure column, a pipe for sending oxygen-rich liquid from the tank of the low-pressure column to the chamber, a pipe for drawing off a fluid from the chamber that is richer in oxygen than that sent to the chamber, a pipe for returning a gas from the chamber to the low-pressure column, a pipe for drawing off a gas from the head of the low-pressure column, characterised in that it comprises pressure reduction means (51) for reducing the pressure of the oxygen-rich liquid downstream of the tank of the low-pressure column and upstream of the chamber and a compressor (21) to compress the gas from the chamber downstream of the chamber and upstream of the low-pressure column.
  7. Apparatus according to claim 6, wherein the chamber (141) comprises material exchange means (143) above the condenser (15).
  8. Apparatus according to claim 6, wherein the chamber (141) does not comprise any material exchange means above the condenser (15).
  9. Apparatus according to any one of the preceding claims 6 to 8, comprising a turbine (23) and a pipe for sending a nitrogen-rich gas from the medium-pressure column to the turbine.
  10. Apparatus according to any one of claims 6 to 9, comprising a pump (63) for pressurising a flow of liquid oxygen originating from the low-pressure column and/or from the chamber upstream of the heat exchanger.
EP10776785.7A 2009-12-11 2010-10-05 Process and unit for the separation of air by cryogenic distillation Not-in-force EP2510294B1 (en)

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FR0958880A FR2953915B1 (en) 2009-12-11 2009-12-11 METHOD AND APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION
PCT/FR2010/052099 WO2011070257A1 (en) 2009-12-11 2010-10-05 Process and unit for the separation of air by cryogenic distillation

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Families Citing this family (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2990500A1 (en) * 2012-05-11 2013-11-15 Air Liquide METHOD AND APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION
GB201409669D0 (en) 2014-05-30 2014-07-16 Highview Entpr Ltd Improvements in air purification units
EP3026380A1 (en) * 2014-11-27 2016-06-01 Linde Aktiengesellschaft Method and device for discharging heavier than air volatile components from an air separation facility
EP3290843A3 (en) * 2016-07-12 2018-06-13 Linde Aktiengesellschaft Method and device for extracting pressurised nitrogen and pressurised nitrogen by cryogenic decomposition of air
CN106440660A (en) * 2016-10-10 2017-02-22 浙江海天气体有限公司 Air separation device with high-pressure heat exchange and oxygen supply
FR3074274B1 (en) * 2017-11-29 2020-01-31 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude METHOD AND APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION
FR3090082B1 (en) * 2018-12-13 2021-01-29 Air Liquide Apparatus for separating or liquefying a gas operating at cryogenic temperatures.
US20220074657A1 (en) * 2018-12-19 2022-03-10 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method for starting up a cryogenic air separation unit and associated air separation unit
FR3090831B1 (en) * 2018-12-21 2022-06-03 L´Air Liquide Sa Pour L’Etude Et L’Exploitation Des Procedes Georges Claude Cryogenic distillation air separation apparatus and method

Family Cites Families (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4617036A (en) * 1985-10-29 1986-10-14 Air Products And Chemicals, Inc. Tonnage nitrogen air separation with side reboiler condenser
CN1025067C (en) * 1989-02-23 1994-06-15 琳德股份公司 Process and method of seperating air by rectification
DE4126945A1 (en) * 1991-08-14 1993-02-18 Linde Ag METHOD FOR AIR DISASSEMBLY BY RECTIFICATION
JP2966999B2 (en) * 1992-04-13 1999-10-25 日本エア・リキード株式会社 Ultra high purity nitrogen / oxygen production equipment
DE19537913A1 (en) * 1995-10-11 1997-04-17 Linde Ag Triple column process for the low temperature separation of air
EP0793069A1 (en) * 1996-03-01 1997-09-03 Air Products And Chemicals, Inc. Dual purity oxygen generator with reboiler compressor
US5664438A (en) * 1996-08-13 1997-09-09 Praxair Technology, Inc. Cryogenic side column rectification system for producing low purity oxygen and high purity nitrogen
GB9711258D0 (en) * 1997-05-30 1997-07-30 Boc Group Plc Air separation
US5934104A (en) * 1998-06-02 1999-08-10 Air Products And Chemicals, Inc. Multiple column nitrogen generators with oxygen coproduction
JP2003014373A (en) * 2001-07-02 2003-01-15 Hitachi Ltd Air separator apparatus
FR2844039B1 (en) * 2002-09-04 2005-04-29 Air Liquide PROCESS AND PLANT FOR PRODUCING OXYGEN AND RARE GASES BY CRYOGENIC AIR DISTILLATION
US6622520B1 (en) * 2002-12-11 2003-09-23 Praxair Technology, Inc. Cryogenic rectification system for producing low purity oxygen using shelf vapor turboexpansion
JP4230213B2 (en) * 2002-12-24 2009-02-25 大陽日酸株式会社 Air liquefaction separation apparatus and method
FR2854683B1 (en) * 2003-05-05 2006-09-29 Air Liquide METHOD AND INSTALLATION FOR PRODUCING PRESSURIZED AIR GASES BY AIR CRYOGENIC DISTILLATION
US20070251267A1 (en) 2006-04-26 2007-11-01 Bao Ha Cryogenic Air Separation Process
US20090241595A1 (en) * 2008-03-27 2009-10-01 Praxair Technology, Inc. Distillation method and apparatus
WO2009136077A2 (en) * 2008-04-22 2009-11-12 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and apparatus for separating air by cryogenic distillation
FR2930327A1 (en) * 2008-04-22 2009-10-23 Air Liquide Air separating method for carbon oxycombustion frame, involves sending oxygen and nitrogen enrich liquids, and reheating nitrogen rich flow from low pressure columns and oxygen rich flow in exchange line

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AU2010329766A1 (en) 2012-07-05
WO2011070257A1 (en) 2011-06-16
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JP2013513775A (en) 2013-04-22
CA2782958A1 (en) 2011-06-16

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FR2825453A1 (en) Process for further purifying a nitrogen-rich feed involves adding a single column to a cryogenic distillation air separator producing a gas which is ninety percent or more nitrogen

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