EP2770286B1 - Procédé et dispositif de collecte d'oxygène et d'azote sous haute pression - Google Patents

Procédé et dispositif de collecte d'oxygène et d'azote sous haute pression Download PDF

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EP2770286B1
EP2770286B1 EP14000438.3A EP14000438A EP2770286B1 EP 2770286 B1 EP2770286 B1 EP 2770286B1 EP 14000438 A EP14000438 A EP 14000438A EP 2770286 B1 EP2770286 B1 EP 2770286B1
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Prior art keywords
pressure
stream
heat exchanger
sub
feed air
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German (de)
English (en)
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EP2770286A1 (fr
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Tobias Lautenschlager
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Linde GmbH
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Linde GmbH
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04084—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • 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
    • F25J3/042—Division of the main heat exchange line in consecutive sections having different functions having an intermediate feed connection
    • 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
    • F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04296—Claude expansion, i.e. expanded into the main or 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
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04387—Details relating to the work expansion, e.g. process parameter etc. using liquid or hydraulic turbine expansion
    • 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/10—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream the fluid being air

Definitions

  • the main capacitor is designed as a "condenser-evaporator".
  • Condenser-evaporator refers to a heat exchanger in which a first condensing fluid stream undergoes indirect heat exchange with a second evaporating fluid stream.
  • Each condenser-evaporator has a liquefaction space and an evaporation space, which consist of liquefaction passages or evaporation passages. In the liquefaction space, the condensation (liquefaction) of a first fluid flow is performed, in the evaporation space the evaporation of a second fluid flow. Evaporation and liquefaction space are formed by groups of passages that are in heat exchange relationship with each other.
  • the “main heat exchanger” is used to cool feed air under a first, subcritical pressure that is less than 1 bar above the operating pressure of the high pressure column, in indirect heat exchange with recycle streams from the distillation column system. It may be formed from a single or multiple parallel and / or serially connected heat exchanger sections, for example one or more plate heat exchanger blocks. When the heat exchanger sections are connected in parallel, an air feed stream flows below each of them below the first, subcritical pressure.
  • wound heat exchanger In a "wound heat exchanger" several layers of tubes are wound onto a core tube. Through the individual tubes a medium is passed, which occurs in heat exchange with a flowing in the space between the tubes and a surrounding jacket medium. The tubes are brought together at the upper heat exchanger end in several groups and led out in the form of bundles from the outside.
  • wound heat exchangers their preparation and their application are, for example, in Hausen / Linde, Tiefftemperaturtechnik, 2nd ed. 1985, p. 471-475 described.
  • the invention has for its object to provide such a method and a corresponding device, which have a high efficiency at the same time relatively low expenditure on equipment and are particularly suitable for the supply of a coal gasification power plant (IGCC - Integrated Combined Cycle).
  • IGCC coal gasification power plant
  • the further increase in the energy efficiency of the process is the joint work-relaxing of the two parts of the second feed air flow in a liquid turbine (DLE - dense liquid expander).
  • the mechanical energy generated at the liquid turbine can either be delivered directly to a compressor or converted into electrical energy via a generator.
  • an equalizing flow (“third partial flow” of the second feed air stream) is taken from the high pressure heat exchanger system at an intermediate temperature and introduced into the main heat exchanger.
  • the high-pressure heat exchanger system has at least two serially connected wound heat exchangers, between which the third partial flow is led out.
  • These two serially connected coiled heat exchangers can be realized by two heat exchanger bundles in separate containers or by two serially connected heat exchanger bundles, which are arranged one above the other in the same container.
  • the intermediate temperature at which the third partial flow is withdrawn from the high-pressure heat exchanger system and introduced into the main heat exchanger. is between 220 and 120 K, preferably between 190 and 150 K.
  • the third partial flow can be conducted separately from the second partial flow through the high-pressure heat exchanger system; Preferably, however, it is guided together with the second partial flow through the warmer of the two wound heat exchanger.
  • the high pressure heat exchanger system may also have three or more heat exchanger bundles.
  • all three partial streams of the second feed air stream are expanded in the liquid turbine work.
  • the first, subcritical pressure of the first feed air stream is preferably equal to the operating pressure of the high pressure column plus line losses and is for example between 5.0 and 6.0 bar, preferably between 5.3 and 5.7 bar.
  • a third feed air stream may - optionally after recompression to a third pressure, which is between the first and the second pressure, be expanded in a gaseous state in an air turbine to perform cold work for the process; the inlet temperature of the air turbine is then at an intermediate level between the hot and cold end of the main heat exchanger. Alternatively or additionally, part of the air compressed to the second, supercritical pressure is released from an intermediate temperature to perform work.
  • the total air is compressed to the first, subcritical pressure, pre-cooled and cleaned under this pressure and then divided into the first and second feed air stream.
  • a completely separate compression of the first and the second feed air stream is possible.
  • the total air is compressed in a main air compressor to a "first, subcritical pressure" of 6 bar and then pre-cooled and cleaned (not shown).
  • the purified feed air 1 is divided into a first feed air stream 100, a second feed air stream 200 and a third feed air stream 300.
  • the first feed air stream 100 is introduced under the first pressure in a main heat exchanger 2 and flows through this completely from the warm to the cold end.
  • the cooled to about dew point temperature first feed air stream 101 is introduced via line 3 in the high pressure column 4 of a distillation column system, which also has a low pressure column 5 and a main capacitor 6.
  • the two columns can be arranged one above the other as shown as a classic double column; alternatively they stand side by side.
  • the second feed air stream 200 is further compressed in a first after-compressor 7 with aftercooler 8 and further in a second after-compressor 9 with aftercooler 10 to a second, supercritical pressure of 85 bar and then branched again at 201.
  • a first partial flow 210/211 of the second feed air stream 200 also flows through the main heat exchanger 2 completely from the hot to the cold end. Not at all through the main heat exchanger 2 flows a second feed air stream 202/220/221. This is completely cooled in a high-pressure heat exchanger system, which is formed in the embodiment of two coiled heat exchangers 11, 12, which are arranged in separate containers.
  • the three sub-streams are reunited and then in a liquid turbine 13 to the operating pressure of the high-pressure column (about 6 bar) doing work relaxed.
  • the liquid turbine is braked by a generator 14.
  • the working expanded second feed air stream 205 is introduced into the high-pressure column 4 in a predominantly liquid state.
  • a third partial stream 230 of the second feed air stream 200 is cooled together with the second partial stream 220 in the warm wound heat exchanger 11 to an intermediate temperature of 165 K and led out via line 203.
  • they are further branched and the third substream 230 is fed to the main heat exchanger 2 at an intermediate location corresponding to its temperature and finally cooled there to the cold end.
  • the fully cooled third substream 231 is combined at 204 with the remainder of the second feed air stream.
  • a third feed air stream 300 is recompressed together with the second feed air stream 200 to a third pressure of 55 bar in the secondary compressor 7 and enters under this pressure in the warm end of the main heat exchanger.
  • stream 301 At a temperature which is slightly higher than the intermediate temperature of the second partial flow 230, it (stream 301) is removed again and expanded in an air turbine 15 to approximately the operating pressure of the high-pressure column 4 to perform work.
  • the air turbine 15 drives the after-compressor 9.
  • the expanded turbine air 302 is introduced in gaseous form into the high-pressure column 4 via line 3.
  • a liquid oxygen stream 16 from the low-pressure column 5 is brought to a first product pressure in an oxygen pump 17 in the liquid state, which in the example is 115 bar, under this first product pressure in the high-pressure heat exchanger system 12/11 warmed to about ambient temperature and finally recovered as a high pressure oxygen product stream 18.
  • the oxygen flows through the interior of the wound tubes of the heat exchangers 11 and 12, the feed air 202 or 206 through their outer space.
  • a liquid nitrogen stream 19 from the high-pressure column 4 (it could also be taken from the main condenser 6) is brought in a nitrogen pump 20 in the liquid state to a second product pressure, which in the embodiment at 80 bar, warmed under this second product pressure to about ambient temperature and finally recovered as a high pressure nitrogen product stream 21.
  • a portion of the low-pressure nitrogen 23, 25 can be used for regeneration of the cleaning unit for the feed air (not shown).
  • the warm pressure nitrogen can be used as a sealing gas 28 and / or medium-pressure product 29.

Claims (7)

  1. Procédé de collecte d'oxygène sous haute pression et d'azote sous haute pression par décomposition de l'air à basse température dans un système de colonnes de distillation, qui présente une colonne à haute pression (4) et une colonne à basse pression (5), qui sont en liaison d'échange de chaleur par l'intermédiaire d'un condenseur principal (6), qui est réalisé sous forme de condenseur-évaporateur, dans lequel
    - on refroidit un premier courant d'air d'alimentation (100, 101) sous une première pression sous-critique, qui se situe moins de 1 bar au-dessus de la pression de service de la colonne à haute pression (4), dans un échangeur de chaleur principal (2) environ jusqu'au point de rosée et on l'introduit (3) au moins partiellement dans la colonne à haute pression (4),
    - on refroidit un deuxième courant d'air d'alimentation (200) sous une deuxième pression supercritique, on le détend ensuite et on l'introduit au moins partiellement dans le système de colonnes de distillation,
    - on porte un premier courant d'oxygène liquide (16) provenant de la colonne à basse pression (5) à l'état liquide à une première pression de produit (17), qui est supérieure à la pression de service de la colonne à basse pression, on le chauffe sous cette première pression de produit dans un système d'échangeur de chaleur à haute pression (11, 12) environ à la température ambiante et on le collecte finalement sous la forme d'un courant de produit d'oxygène sous haute pression (18),
    - on porte un courant d'azote liquide (26) provenant de la colonne à haute pression (4) ou du condenseur principal (6) à l'état liquide à une deuxième pression de produit (20), qui est supérieure à la pression de service de la colonne à haute pression (4), on le chauffe sous cette deuxième pression de produit environ à la température ambiante et on le collecte finalement sous la forme d'un courant de produit d'azote sous haute pression (21),
    - on effectue le refroidissement d'un premier courant partiel (201) du deuxième courant d'air d'alimentation (200) par un échange de chaleur indirect à l'extérieur du système d'échangeur de chaleur à haute pression (11, 12),
    - on effectue le refroidissement d'un deuxième courant partiel (202, 221) du deuxième courant d'air d'alimentation (200) dans le système d'échangeur de chaleur à haute pression (11, 12), et dans lequel
    - on réunit le premier et le deuxième courants partiels (211, 221) du deuxième courant d'air d'alimentation en aval de leur refroidissement,
    - on effectue le chauffage du courant d'azote mis sous pression à l'état liquide dans l'échangeur de chaleur principal (2),
    - on effectue le refroidissement du premier courant partiel (201) du deuxième courant d'air d'alimentation (200) dans l'échangeur de chaleur principal (2),
    - on dévie un troisième courant partiel (230) du deuxième courant d'air d'alimentation (200) à un point intermédiaire du système d'échangeur de chaleur à haute pression (11, 12) à partir du deuxième courant partiel (206) et on l'introduit dans l'échangeur de chaleur principal (2) en un point intermédiaire et on l'y refroidit encore,
    - pendant que le deuxième courant partiel (206) du deuxième courant d'air d'alimentation est encore refroidi dans le système d'échangeur de chaleur à haute pression (12);
    caractérisé en ce que
    - on détend le deuxième courant d'air d'alimentation réuni avant son introduction (205, 3) dans le système de colonnes de distillation dans une turbine à liquide (13) avec production de travail,
    - le système d'échangeur de chaleur à haute pression (11, 12) présente au moins deux échangeurs de chaleur enroulés et deux d'entre eux sont reliés en série, et
    - on dévie le troisième courant partiel (230) du deuxième courant d'air d'alimentation (200) à partir du deuxième courant partiel (206) entre les deux échangeurs de chaleur (11, 12) enroulés et reliés en série.
  2. Procédé selon la revendication 1, caractérisé en ce que l'on réunit le troisième courant partiel (231) avec le premier et le deuxième courants partiels (211, 221) en amont de la turbine à liquide (13).
  3. Procédé selon la revendication 1 ou 2, caractérisé en ce que la première pression de produit est supérieure à 100 bar, en particulier supérieure à 110 bar.
  4. Procédé selon l'une quelconque des revendications 1 à 3, caractérisé en ce que la deuxième pression de produit est inférieure à 100 bar, en particulier inférieure à 90 bar.
  5. Procédé selon l'une quelconque des revendications 1 à 4, caractérisé en ce que la deuxième pression supercritique est inférieure à la première pression de produit et en particulier vaut moins de 100 bar, en particulier moins de 90 bar.
  6. Dispositif de collecte d'oxygène sous haute pression et d'azote sous haute pression par décomposition de l'air à basse température avec un système de colonnes de distillation, qui présente une colonne à haute pression (4) et une colonne à basse pression (5), qui sont en liaison d'échange de chaleur par l'intermédiaire d'un condenseur principal (6), qui est réalisé sous forme de condenseur-évaporateur, et avec
    - des moyens pour refroidir un premier courant d'air d'alimentation (100) sous une première pression sous-critique, qui se situe moins de 1 bar au-dessus de la pression de service de la colonne à haute pression (4), dans un échangeur de chaleur principal (2) environ jusqu'au point de rosée,
    - des moyens (3) pour introduire le premier courant d'air d'alimentation refroidi (101) dans la colonne à haute pression (4),
    - des moyens pour refroidir un deuxième courant d'air d'alimentation (200) sous une deuxième pression supercritique,
    - des moyens pour détendre et introduire dans le système de colonnes de distillation le deuxième courant d'air d'alimentation refroidi (211, 221, 231),
    - des moyens (17) pour porter un courant d'oxygène liquide (16) provenant de la colonne à basse pression (5) à une première pression de produit, qui est supérieure à la pression de service de la colonne à basse pression,
    - des moyens pour chauffer le courant d'oxygène mis sous pression sous cette première pression de produit dans un système d'échangeur de chaleur à haute pression (11, 12) environ à la température ambiante, et
    - des moyens pour collecter le courant d'oxygène chauffé sous la forme d'un courant d'un produit d'oxygène sous haute pression (18),
    - des moyens (20) pour porter un courant d'azote liquide (26) provenant de la colonne à haute pression (4) ou du condenseur principal (6) à une deuxième pression de produit, qui est supérieure à la pression de service de la colonne à haute pression (4),
    - des moyens pour chauffer le courant d'azote liquide mis sous pression sous cette deuxième pression de produit,
    - des moyens pour collecter le courant d'azote chauffé sous la forme d'un courant de produit d'azote sous haute pression (21),
    - des moyens pour refroidir un premier courant partiel (201) du deuxième courant d'air d'alimentation (200) par échange de chaleur indirect,
    - des moyens pour introduire un deuxième courant partiel (202, 221) du deuxième courant d'air d'alimentation (200) dans l'extrémité chaude du système d'échangeur de chaleur à haute pression (11, 12),
    - des moyens pour réunir le premier courant partiel refroidi (211) et le deuxième courant partiel refroidi (221) du deuxième courant d'air d'alimentation en aval de l'échangeur de chaleur principal (2) ou du système d'échangeur de chaleur à haute pression (11, 12),
    - des moyens pour introduire le courant d'azote mis sous pression à l'état liquide dans l'échangeur de chaleur principal (2),
    - des moyens pour introduire un premier courant partiel (201) du deuxième courant d'air d'alimentation (200) dans l'extrémité chaude de l'échangeur de chaleur principal (2),
    - des moyens pour dévier un troisième courant partiel (230) du deuxième courant d'air d'alimentation (200) à partir du deuxième courant partiel (206) à un point intermédiaire du système d'échangeur de chaleur à haute pression (11, 12),
    - des moyens pour introduire le troisième courant partiel (230) dans l'échangeur de chaleur principal (2) en un point intermédiaire, et avec
    - des moyens pour refroidir encore le deuxième courant partiel (206) du deuxième courant d'air d'alimentation dans le système d'échangeur de chaleur à haute pression (12),
    caractérisé par
    - une turbine à liquide (13) pour détendre le deuxième courant d'air d'alimentation réuni avant son introduction (205, 3) dans le système de colonnes de distillation avec production de travail, dans lequel
    - le système d'échangeur de chaleur à haute pression (11, 12) présente au moins deux échangeurs de chaleur enroulés, dans lequel deux d'entre eux sont reliés en série, et caractérisé en outre en ce que le point intermédiaire du système d'échangeur de chaleur à haute pression (11, 12) se trouve entre les deux échangeurs de chaleur enroulés et reliés en série (11, 12).
  7. Dispositif selon la revendication 6, caractérisé par des moyens pour réunir le troisième courant partiel (230) au premier et au deuxième courants partiels (211, 221) en amont de la turbine à liquide (13).
EP14000438.3A 2013-02-21 2014-02-06 Procédé et dispositif de collecte d'oxygène et d'azote sous haute pression Active EP2770286B1 (fr)

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PL14000438T PL2770286T3 (pl) 2013-02-21 2014-02-06 Sposób i urządzenie do pozyskiwania tlenu pod wysokim ciśnieniem i azotu pod wysokim ciśnieniem
EP14000438.3A EP2770286B1 (fr) 2013-02-21 2014-02-06 Procédé et dispositif de collecte d'oxygène et d'azote sous haute pression

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EP2980514A1 (fr) * 2014-07-31 2016-02-03 Linde Aktiengesellschaft Procédé de séparation cryogénique de l'air et installation de séparation d'air
CN109737691B (zh) * 2019-01-31 2020-05-19 东北大学 一种钢铁企业空气分离系统

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DE3216510A1 (de) * 1982-05-03 1983-11-03 Linde Ag, 6200 Wiesbaden Verfahren zur gewinnung von gasfoermigem sauerstoff unter erhoehtem druck
US5355682A (en) 1993-09-15 1994-10-18 Air Products And Chemicals, Inc. Cryogenic air separation process producing elevated pressure nitrogen by pumped liquid nitrogen
EP0793069A1 (fr) * 1996-03-01 1997-09-03 Air Products And Chemicals, Inc. Générateur d'oxygène à deux degrés de pureté avec compresseur pour le rebouilleur
FR2761762B1 (fr) * 1997-04-03 1999-05-07 Air Liquide Procede et installation de separation d'air par distillation cryogenique
FR2789165B1 (fr) * 1999-02-01 2001-03-09 Air Liquide Echangeur de chaleur, notamment echangeur de chaleur a plaques d'un appareil de separation d'air
US6718795B2 (en) * 2001-12-20 2004-04-13 Air Liquide Process And Construction, Inc. Systems and methods for production of high pressure oxygen
GB0422635D0 (en) * 2004-10-12 2004-11-10 Air Prod & Chem Process for the cryogenic distillation of air
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DE102007051183A1 (de) * 2007-10-25 2009-04-30 Linde Aktiengesellschaft Verfahren zur Tieftemperatur-Luftzerlegung
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CN104006628B (zh) 2017-11-28
US20140230486A1 (en) 2014-08-21
CN104006628A (zh) 2014-08-27
US9989306B2 (en) 2018-06-05
PL2770286T3 (pl) 2017-10-31

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