EP2531794B1 - Procede et appareil de separation d'air par distillation cryogenique - Google Patents

Procede et appareil de separation d'air par distillation cryogenique Download PDF

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Publication number
EP2531794B1
EP2531794B1 EP11707452.6A EP11707452A EP2531794B1 EP 2531794 B1 EP2531794 B1 EP 2531794B1 EP 11707452 A EP11707452 A EP 11707452A EP 2531794 B1 EP2531794 B1 EP 2531794B1
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EP
European Patent Office
Prior art keywords
condenser
evaporator
cryogenic
compressor
air
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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.)
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EP11707452.6A
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German (de)
English (en)
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EP2531794A1 (fr
Inventor
Benoît 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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Publication of EP2531794A1 publication Critical patent/EP2531794A1/fr
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—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
    • F25J3/04418—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 with thermally overlapping high and low pressure columns
    • 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
    • F25J3/0406—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 nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04309—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
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, 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
    • 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
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04854—Safety aspects of operation
    • F25J3/0486—Safety aspects of operation of vaporisers for oxygen enriched liquids, e.g. purging of liquids
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/40—Features relating to the provision of boil-up in the bottom of a 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
    • F25J2200/54—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the low pressure column of a double pressure main column system
    • 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/04—Down-flowing type boiler-condenser, i.e. with evaporation of a falling liquid film
    • 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 methods and apparatus for air separation by cryogenic distillation. It is known to distill the air in a double column comprising a medium pressure column thermally connected to a low pressure column which overcomes it.
  • the thermal bond between the two columns can be obtained by using two vaporizers placed one above the other in the low pressure column.
  • the lowest vaporizer can be heated by means of a flow of nitrogen withdrawn from the medium pressure column and then compressed in a cold compressor and the upper vaporizer can be heated by a flow of medium pressure nitrogen taken from the medium pressure column. without having been compressed upstream of the vaporizer.
  • a cold compressor is a compressor having a cryogenic inlet temperature, a cryogenic temperature being below -50 ° C.
  • the compressed nitrogen in the cold compressor must be condensed in the lower vaporizer of the low pressure column.
  • the cold compressed fluid therefore arrives relatively hot in the vaporizer, with a large ⁇ T before starting to condense: this means that even if the vaporizer has a low temperature nip, the ⁇ T hot end is relatively important.
  • vaporizer-condenser If the vaporizer-condenser has malfunctions, including partial blockage or poor distribution, there is a high risk of dry vaporization locally, which affects the safety of the device due to the presence of impurities of the type CnHm with a fluid rich in oxygen. This is especially noticeable on a film evaporator-condenser.
  • FR-A-2930329 discloses a method according to the preamble of claim 1.
  • One of the aims of the invention is to avoid malfunctions of the vaporizer-condenser.
  • a circulating fluid for example medium pressure nitrogen
  • a circulating fluid for example medium pressure nitrogen
  • a part condensed fluid in the condenser vaporizer at the inlet of the vaporizer-condenser, to bring it back to its dew point, before being condensed.
  • a method of separating air in a column system by cryogenic distillation in which compressed, purified and cooled air is separated in the column system to form a flow enriched with oxygen and a flow enriched in nitrogen in which at least one column of the column system contains a vaporizer-condenser for vaporizing an oxygen-enriched liquid with respect to the air by means of a heat exchange with a fluid calorigenic, the caloric fluid having been compressed upstream of the vaporizer-condenser in a compressor having a cryogenic inlet temperature, the calorigenic fluid being at least partially condensed in the vaporizer-condenser characterized in that a cryogenic liquid is added to the fluid calorigen upstream of the vaporizer-condenser.
  • the invention also includes an oxy-fuel combustion plant comprising an air separation apparatus as described above and an oxygen-supplied boiler produced by the air separation apparatus.
  • An air flow 1 is compressed in a compressor (not shown) to 4 bar and then divided into two; a part 3 of the air cools in an exchange line 9 and is sent to the medium pressure column 11 of a double column.
  • the double column comprises a medium pressure column 11 and a low pressure column 13 thermally connected to each other, the low pressure column surmounting the medium pressure column.
  • the low pressure column 13 contains a tank vaporizer 15 and an intermediate vaporizer 17.
  • the intermediate vaporizer 17 is heated by means of a fraction 33 of a nitrogen flow 31 withdrawn from the medium pressure column at the pressure of the head of the medium pressure column.
  • Another fraction 37 of the nitrogen medium nitrogen pressure is compressed in a compressor 61 having a cryogenic inlet temperature.
  • the fraction is cooled at the outlet of this cold compressor 61 by direct contact with a cryogenic liquid 45, to be returned to its dew point, before being condensed.
  • the cryogenic liquid 45 preferably comprises a portion of the fluid that has just condensed in the vessel vaporizer 15.
  • the cryogenic liquid contains at least 70 mol%. nitrogen, or even at least 90 mol%. nitrogen.
  • the gas and the liquid 45 can be brought into contact directly in the pipework or in specific equipment, by means of injection nozzles, of physical contactors, the liquid 45 being compressed either by hydrostatic height or using a pump.
  • the remainder of the condensed liquid in the vessel vaporizer 15 is sent at the top of the low pressure column 13 to form reflux.
  • An oxygen-enriched liquid 49 and a nitrogen-enriched liquid 53 are sent from the medium-pressure column 11 to the low-pressure column 13.
  • a flow of liquid oxygen 19 is withdrawn from the tank of the low pressure column, pressurized to a low pressure of 1.5 to 4 bar by a pump 21 and then vaporized in a vaporizer 23 by heat exchange with the air.
  • a non-vaporized portion of the oxygen is withdrawn as purge 25.
  • the vessel vaporizer 15 is preferably a film.
  • a portion 39 of the medium pressure nitrogen is heated in the exchange line 9, is expanded in a turbine 41 and then again warms in the exchange line 9.
  • the invention applies to any compressed gas in a cold compressor, which must condense in a vaporizer where there is a risk of dry vaporization vis-à-vis oxygen in the presence of impurity type C n H m.
  • cryogenic liquid added upstream of the cold compressor comes from the column system but the liquid can come from an external source and can for example be taken from a storage of liquid or liquid liquids stored in a rocking system .

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

Description

  • La présente invention est relative aux procédés et aux appareils de séparation d'air par distillation cryogénique. Il est connu de distiller l'air dans une double colonne comprenant une colonne moyenne pression reliée thermiquement avec une colonne basse pression qui la surmonte.
  • Le lien thermique entre les deux colonnes peut être obtenu en utilisant deux vaporiseurs placés l'un au dessus de l'autre dans la colonne basse pression. Le vaporiseur le plus bas peut être chauffé au moyen d'une débit d'azote soutiré de la colonne moyenne pression puis comprimé dans un compresseur froid et le vaporiseur supérieur peut être chauffé par un débit d'azote moyenne pression pris dans la colonne moyenne pression sans avoir été comprimé en amont du vaporiseur.
  • Un compresseur froid est un compresseur ayant une température d'entrée cryogénique, une température cryogénique étant inférieure à -50°C.
  • L'azote comprimé dans le compresseur froid doit être condensé dans le vaporiseur inférieur de la colonne basse pression. Le fluide comprimé à froid arrive donc relativement chaud dans le vaporiseur, avec un ΔT important avant de commencer à se condenser : cela signifie que même si le vaporiseur a un pincement faible de température, le ΔT au bout chaud est relativement important.
  • Si le vaporiseur-condenseur a des disfonctionnements, notamment de bouchage partiel ou de mauvaise distribution, il y a un fort risque de vaporisation à sec localement, ce qui nuit à la sécurité de l'appareil du fait de la présence d'impuretés de type CnHm avec un fluide riche en oxygène. Cela est d'autant plus sensible sur un vaporiseur-condenseur à film.
  • FR-A-2930329 décrit un procédé selon le préambule de la revendication 1.
  • Un des buts de l'invention est d'éviter des dysfonctionnements du vaporiseur-condenseur.
  • Selon l'invention, un fluide calorigène, par exemple de l'azote moyenne pression, est refroidi en sortie d'un compresseur froid, en injectant une partie du fluide condensé dans le vaporiseur condenseur à l'entrée du vaporiseur-condenseur, pour le ramener à son point de rosée, avant d'être condensé. Ceci permet d'annuler la surchauffe du fluide, et permet un usage facilité en termes de sécurité pour le vaporiseur, notamment à film. Ceci se fait sans pénalité énergétique notable.
  • L'injection d'autres fluides cryogéniques peut remplacer ce fluide condensé.
  • Selon un objet de l'invention, il est proposé un procédé de séparation d'air dans un système de colonnes par distillation cryogénique dans lequel de l'air comprimé, épuré et refroidi est séparé dans le système de colonnes pour former un débit enrichi en oxygène et un débit enrichi en azote dans lequel au moins une colonne du système de colonnes contient un vaporiseur-condenseur devant assurer la vaporisation d'un liquide enrichi en oxygène par rapport à l'air au moyen d'un échange de chaleur avec un fluide calorigène, le fluide calorigène ayant été comprimé en amont du vaporiseur-condenseur dans un compresseur ayant une température d'entrée cryogénique, le fluide calorigène étant au moins partiellement condensé dans le vaporiseur-condenseur caractérisé en ce qu'un liquide cryogénique est rajouté au fluide calorigène en amont du vaporiseur-condenseur.
  • Selon d'autres caractéristiques facultatives :
    • le liquide cryogénique est constitué par une partie du fluide calorigène après sa condensation dans le vaporiseur-condenseur ;
    • le système de colonnes est une double ou une triple colonne, le fluide calorigène est un débit enrichi en azote soutiré d'une des colonnes fonctionnant à pression plus élevée et le rebouilleur est dans une autre des colonnes fonctionnant à pression plus basse ;
    • le vaporiseur-condenseur est un vaporiseur à film;
    • le liquide cryogénique est pressurisé soit par pression hydrostatique soit par une pompe ;
    • le liquide cryogénique contient au moins 75% mol. d'azote, voire au moins 90% mol. d'azote;
    • le liquide cryogénique est rajouté au fluide calorigène en aval du compresseur.
  • Selon un autre objet de l'invention, il est prévu un appareil de séparation d'air dans un système de colonnes par distillation cryogénique comprenant :
    1. a) un système de colonnes
    2. b) un vaporiseur-condenseur capable de vaporiser un liquide enrichi en oxygène par rapport à l'air
    3. c) un compresseur d'air
    4. d) une conduite reliant le compresseur d'air avec le système de colonnes
    5. e) un compresseur cryogénique de fluide calorigène relié à une entrée du vaporiseur-condenseur
    caractérisé en ce qu'il comprend une conduite d'amenée de liquide cryogénique reliée à la sortie du compresseur cryogénique et à une entrée du vaporiseur-condenseur.
  • L'appareil peut comprendre les caractéristiques suivantes :
    • au moins une conduite de fluide condensé qui relie une sortie du vaporiseur-condenseur à au moins une colonne du système de colonnes ;
    • le système de colonnes est une double ou une triple colonne, une des colonnes opérant à plus basse pression comprenant le vaporiseur-condenseur en vaporiseur de cuve ;
    • le compresseur cryogénique est relié à la tête d'une des colonnes opérant à pression plus élevée ;
    • des moyens pour pressuriser un liquide cryogénique adaptés à pressuriser un liquide circulant dans la conduite reliant la sortie du vaporiseur-condenseur à la sortie du compresseur cryogénique ;
    • la conduite d'amenée de liquide cryogénique est reliée à un stockage de liquide cryogénique ;
    • la conduite d'amenée de liquide cryogénique est reliée à la sortie du vaporiseur-condenseur.
  • L'invention comprend également une installation d'oxycombustion comprenant un appareil de séparation d'air tel que décrit ci-dessus et une chaudière alimentée par l'oxygène produit par l'appareil de séparation d'air.
  • L'invention sera décrite en plus de détail en se référant à la figure qui montre un procédé selon l'invention.
  • Un débit d'air 1 est comprimé dans un compresseur (non-illustré) jusqu'à 4 bars puis divisé en deux; une partie 3 de l'air se refroidit dans une ligne d'échange 9 et est envoyé à la colonne moyenne pression 11 d'une double colonne. La double colonne comprend une colonne moyenne pression 11 et une colonne basse pression 13 reliées thermiquement entre elles, la colonne basse pression surmontant la colonne moyenne pression.
  • Le reste 5 de l'air est surpressé dans un surpresseur 7, refroidi dans la ligne d'échange, condensé dans un vaporiseur produit 23 et puis envoyé à la colonne moyenne pression 11.
  • La colonne basse pression 13 contient un vaporiseur de cuve 15 et un vaporiseur intermédiaire 17. Le vaporiseur intermédiaire 17 est chauffé au moyen d'une fraction 33 d'un débit d'azote 31 soutiré de la colonne moyenne pression à la pression de la tête de la colonne moyenne pression.
  • Une autre fraction 37 de l'azote moyenne pression azote est comprimée dans un compresseur 61 ayant une température d'entrée cryogénique. La fraction est refroidie en sortie de ce compresseur froid 61 par contact direct avec un liquide cryogénique 45, pour être ramené à son point de rosée, avant d'être condensé. Le liquide cryogénique 45 préférentiellement comprend une partie du fluide qui vient de se condenser dans le vaporiseur de cuve 15. Le liquide cryogénique contient au moins 70% mol. d'azote, voire au moins 90% mol. d'azote. Ainsi une conduite ramène vers la sortie du compresseur froid une partie de l'azote condensé dans le vaporiseur de cuve.
  • La mise en contact du gaz et du liquide 45 peut se faire directement dans la tuyauterie ou dans un équipement spécifique, à l'aide de buses d'injection, de contacteurs physiques, le liquide 45 étant comprimé soit par hauteur hydrostatique, soit à l'aide d'une pompe.
  • Le reste du liquide condensé dans le vaporiseur de cuve 15 est envoyé en partie en tête de la colonne basse pression 13 pour former du reflux.
  • Un liquide enrichi en oxygène 49 et un liquide enrichi en azote 53 sont envoyés de la colonne moyenne pression 11 à la colonne basse pression 13.
  • Un débit d'oxygène liquide 19 est soutiré de la cuve de la colonne basse pression, pressurisé jusqu'à une basse pression de 1,5 à 4 bars par une pompe 21 et puis vaporisé dans un vaporiseur 23 par échange de chaleur avec l'air. Une partie non-vaporisée de l'oxygène est soutirée en tant que purge 25.
  • Le vaporiseur de cuve 15 est de préférence à film.
  • Une partie 39 de l'azote moyenne pression se réchauffe dans la ligne d'échange 9, est détendue dans une turbine 41 puis de nouveau se réchauffe dans la ligne d'échange 9.
  • L'invention s'applique à tout gaz comprimé dans un compresseur froid, qui doit se condenser dans un vaporiseur où il y a un risque de vaporisation à sec vis-à-vis d'oxygène en présence d'impureté de type CnHm.
  • Dans l'exemple le liquide cryogénique rajouté en amont du compresseur froid vient du système de colonnes mais le liquide peut provenir d'une source extérieure et peut par exemple être pris dans un stockage de liquide de biberonnage ou de liquide stocké dans un système de bascule.

Claims (14)

  1. Procédé de séparation d'air dans un système de colonnes (11, 13) par distillation cryogénique dans lequel de l'air comprimé, épuré et refroidi est séparé dans le système de colonnes pour former un débit enrichi en oxygène et un débit enrichi en azote dans lequel au moins une colonne (13) du système de colonnes contient un vaporiseur-condenseur (15) devant assurer la vaporisation d'un liquide enrichi en oxygène par rapport à l'air au moyen d'un échange de chaleur avec un fluide calorigène (37), le fluide calorigène ayant été comprimé en amont du vaporiseur-condenseur dans un compresseur (61) ayant une température d'entrée cryogénique, le fluide calorigène étant au moins partiellement condensé dans le vaporiseur-condenseur caractérisé en ce qu'un liquide cryogénique (45) est rajouté au fluide calorigène en amont du vaporiseur-condenseur.
  2. Procédé selon la revendication 1 dans lequel le liquide cryogénique (45) est constitué par une partie du fluide calorigène après sa condensation dans le vaporiseur-condenseur (15).
  3. Procédé selon la revendication 1 ou 2 dans lequel le système de colonnes (11, 13) est une double ou une triple colonne, le fluide calorigène est un débit enrichi en azote (37) soutiré d'une des colonnes (11) fonctionnant à pression plus élevée et le rebouilleur est dans une autre des colonnes fonctionnant à pression plus basse (13).
  4. Procédé selon l'une des revendications précédentes dans lequel le vaporiseur-condenseur (11) est un vaporiseur à film.
  5. Procédé selon l'une des revendications précédentes dans lequel le liquide cryogénique (45) est pressurisé soit par pression hydrostatique soit par une pompe.
  6. Procédé selon l'une des revendications précédentes dans lequel le liquide cryogénique est rajouté au fluide calorigène en aval du compresseur.
  7. Procédé selon l'une des revendications précédentes dans lequel le liquide cryogénique contient au moins 75% mol. d'azote, voire au moins 90% mol. d'azote
  8. Appareil de séparation d'air dans un système de colonnes par distillation cryogénique comprenant :
    a) un système de colonnes (11, 13),
    b) un vaporiseur-condenseur (15) capable de vaporiser un liquide enrichi en oxygène par rapport à l'air,
    c) un compresseur d'air,
    d) une conduite reliant le compresseur d'air avec le système de colonnes,
    e) un compresseur cryogénique (61) de fluide calorigène relié à une entrée du vaporiseur-condenseur,
    caractérisé en ce qu'il comprend une conduite (45) d'amenée de liquide cryogénique reliée à la sortie du compresseur cryogénique et à une entrée du vaporiseur-condenseur.
  9. Appareil selon la revendication 8 dans lequel le système de colonnes est une double ou une triple colonne, une des colonnes opérant à plus basse pression (13) comprenant le vaporiseur-condenseur (15) en vaporiseur de cuve.
  10. Appareil selon la revendication 9 dans lequel le compresseur cryogénique (61) est relié à la tête d'une des colonnes (11) opérant à pression plus élevée.
  11. Appareil selon l'une des revendications 8 à 10 comprenant des moyens pour pressuriser un liquide cryogénique adaptés à pressuriser un liquide circulant dans la conduite reliant la sortie du vaporiseur-condenseur (15) à la sortie du compresseur cryogénique (61).
  12. Appareil selon l'une des revendications 8 à 11 comprenant un stockage et la conduite d'amenée de liquide cryogénique reliant le stockage à un point en aval du compresseur cryogénique et en amont du vaporiseur-condenseur.
  13. Appareil selon l'une des revendications 8 à 12 dans lequel la conduite relie la sortie du vaporiseur-condenseur à la sortie du compresseur cryogénique sans passer par le vaporiseur-condenseur.
  14. Installation d'oxycombustion comprenant un appareil de séparation d'air selon l'une des revendications 8 à 13 et une chaudière alimentée par l'oxygène produit par l'appareil de séparation d'air.
EP11707452.6A 2010-02-04 2011-02-03 Procede et appareil de separation d'air par distillation cryogenique Not-in-force EP2531794B1 (fr)

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FR1050775A FR2955926B1 (fr) 2010-02-04 2010-02-04 Procede et appareil de separation d'air par distillation cryogenique
PCT/FR2011/050212 WO2011095739A1 (fr) 2010-02-04 2011-02-03 Procede et appareil de separation d'air par distillation cryogenique

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FR2990500A1 (fr) * 2012-05-11 2013-11-15 Air Liquide Procede et appareil de separation d'air par distillation cryogenique
US11566841B2 (en) * 2019-11-27 2023-01-31 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Cryogenic liquefier by integration with power plant

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GB2129115B (en) * 1982-10-27 1986-03-12 Air Prod & Chem Producing gaseous nitrogen
US5341646A (en) * 1993-07-15 1994-08-30 Air Products And Chemicals, Inc. Triple column distillation system for oxygen and pressurized nitrogen production
DE10205878A1 (de) * 2002-02-13 2003-08-21 Linde Ag Tieftemperatur-Luftzerlegungsverfahren
US20070251267A1 (en) * 2006-04-26 2007-11-01 Bao Ha Cryogenic Air Separation Process
FR2930331B1 (fr) * 2008-04-22 2013-09-13 Air Liquide Procede et appareil de separation d'air par distillation cryogenique
FR2930329A1 (fr) * 2008-04-22 2009-10-23 Air Liquide Procede et appareil de separation d'air par distillation cryogenique

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US9140491B2 (en) 2015-09-22
WO2011095739A1 (fr) 2011-08-11
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FR2955926B1 (fr) 2012-03-02
ES2476285T3 (es) 2014-07-14
FR2955926A1 (fr) 2011-08-05

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