WO2007104449A1 - Procédé et dispositif de décomposition de l'air à basse température - Google Patents

Procédé et dispositif de décomposition de l'air à basse température Download PDF

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Publication number
WO2007104449A1
WO2007104449A1 PCT/EP2007/001917 EP2007001917W WO2007104449A1 WO 2007104449 A1 WO2007104449 A1 WO 2007104449A1 EP 2007001917 W EP2007001917 W EP 2007001917W WO 2007104449 A1 WO2007104449 A1 WO 2007104449A1
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WO
WIPO (PCT)
Prior art keywords
air
air flow
nitrogen
air stream
distillation column
Prior art date
Application number
PCT/EP2007/001917
Other languages
German (de)
English (en)
Inventor
Alexander Alekseev
Dietrich Rottmann
Florian Schliebitz
Dirk Schwenk
Original Assignee
Linde Aktiengesellschaft
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Linde Aktiengesellschaft filed Critical Linde Aktiengesellschaft
Priority to EP07723062A priority Critical patent/EP1994344A1/fr
Priority to US12/282,606 priority patent/US20090188280A1/en
Priority to JP2008558680A priority patent/JP2009529648A/ja
Priority to CN2007800135967A priority patent/CN101421575B/zh
Publication of WO2007104449A1 publication Critical patent/WO2007104449A1/fr

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Classifications

    • 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
    • F25J3/04054—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 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
    • 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
    • F25J3/04163—Hot end purification of the feed air
    • F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
    • F25J3/04175—Hot end purification of the feed air by adsorption of the impurities at a pressure of substantially more than the highest 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
    • F25J3/04151—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
    • 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
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—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.
    • F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work 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
    • F25J2240/04—Multiple expansion turbines in parallel

Definitions

  • the invention relates to a method for the cryogenic separation of air according to the preamble of patent claim 1.
  • the distillation column system of the invention can be designed as a single-column system for nitrogen-oxygen separation, as a two-column system (for example as a classic Linde double column system), or as a three-column or multi-column system.
  • other devices may be provided to recover other air components, particularly noble gases, such as argon or krypton-xenon recovery.
  • the invention relates to a process in which at least one gaseous product is obtained by withdrawing a liquid product stream from the nitrogen-oxygen separation distillation column system, bringing it to an elevated pressure in the liquid state, and evaporating it under this increased pressure by indirect heat exchange or (at supercritical pressure) is pseudo-evaporated.
  • the invention has for its object to make such a method and a corresponding device economically particularly favorable.
  • both booster are operated with an inlet temperature which is higher than 250 K, in particular higher than 270 K.
  • Both booster compressors are therefore operated in warm conditions. This can be used well proven technology, for example, two identical turbine booster combinations.
  • the heat exchanger volume is relatively low and thus investment costs are saved.
  • the expansion machines are preferably designed as turbines. They have "substantially the same inlet pressure", that is to say their inlet pressures differ at most by different pressure losses in lines, heat exchanger passages or the like.
  • the inlet temperatures of the two expansion machines are the same or different and are at one or two intermediate levels between the hot and cold ends of the main heat exchanger.
  • the invention is applicable to methods with exactly two air streams and the subdivision of the second air stream into exactly two sub-streams.
  • one or more additional air streams and / or one or more additional partial streams can be used.
  • the two or more expansion machines of the invention may also be connected in parallel on the outlet side, that is to say have substantially the same outlet pressure and substantially the same outlet temperature.
  • the transmission of the mechanical energy from the working expansion is preferably effected by a direct mechanical coupling of a first of the two parallel relaxation machines with the first of the two serially connected booster and by a direct mechanical coupling of the second of the two expansion machines with the second of the two booster.
  • a first of the two partial streams is introduced downstream of its work-performing expansion in the high-pressure column.
  • the outlet pressure of the corresponding expansion turbine is approximately at the level of the operating pressure of the high pressure column.
  • the second of the two partial streams can then also be expanded to about high-pressure column pressure and, for example, introduced into the high-pressure column together with the first.
  • the second of the two partial streams of the second air stream is at least partially introduced into the low-pressure column. This makes it possible to choose the outlet pressure of the corresponding expansion turbine lower and to perform more work in the relaxation and thus more cold by the increased pressure ratio.
  • the first partial flow can at least partially in the high-pressure column and the second Partial flow at least partially into the medium-pressure column and / or the low-pressure column are introduced.
  • the first air stream upstream of the first post-compressor and the first air stream downstream of the second post-compressor are brought into indirect heat exchange.
  • the first air stream is heated before the first booster and cooled again after the second booster.
  • the first air flow occurs at a temperature in the main heat exchanger, which is lower than the temperature after the second booster or after the aftercooler.
  • this temperature difference is 1 to 10 K, preferably 2 to 5 K.
  • the product streams can be removed at lower temperature from the main heat exchanger, which has favorable effects for the pre-cooling of the air and for cooling the molecular sieve for air purification.
  • classic intermediate or aftercoolers are used which remove the compression occurring in the after-compressors by indirect heat exchange with an external coolant, for example with cooling water.
  • one or two aftercoolers can be used by only the first booster, only the second booster or both
  • After-compressor each have an aftercooler.
  • at least the first after-compressor has an aftercooler (intercooler).
  • the invention also relates to a device for the cryogenic separation of air according to claim 9.
  • Figure 1 shows a first embodiment of the invention and Figure 2 shows a second embodiment with cold compressor.
  • atmospheric air is sucked as the main air flow via line 1 from an air compressor 2, there brought to a first pressure of 10 to 30 bar, preferably about 19 bar, cooled in a pre-cooling 3 to about ambient temperature and an adsorptive air cleaning. 4 fed.
  • the purified main air stream 5 is branched at 6 into a first air stream 7 and a second air stream 8.
  • the first air stream is heated in a booster heat exchanger 9 to about the cooling water temperature and further compressed in a first booster 10 to an intermediate pressure of 15 to 60 bar, preferably about 25 bar. Subsequently, the heat of compression is at least partially removed in a first aftercooler 11.
  • the first air stream 12 is then further compressed in a second booster 13 to a final pressure of 22 to 90 bar, preferably about 40 bar and then heated in a second aftercooler 14 and the booster heat exchanger 9 to slightly above the cooling water temperature. Under this final pressure, the first air stream 15 enters a main heat exchanger 16 and is cooled and liquefied there, or (at supercritical pressure) pseudo-liquefied.
  • the cold first air stream 17 is expanded to a pressure of 4 to 10 bar, preferably about 6 bar (in the example in a throttle valve 18) and under this pressure in at least partially liquid state via line 19 into the high-pressure column 21 of a distillation column system Nitrogen-oxygen separation 20 introduced, which also has a low-pressure column 22, a not shown condenser-evaporator and a supercooling countercurrent 23.
  • the second air stream 8 It is not recompressed, the second air stream 8. It is introduced under the first pressure in the main heat exchanger 16 and there cooled to an intermediate temperature of 125 to 200 K, preferably about 140 K. The second air stream is branched at this intermediate temperature into two partial streams 24, 27 and subjected to the work-performing expansion in two parallel-connected turbines 25, 28, which both relax to approximately the operating pressure of the high-pressure column 21. The two relaxed partial streams 26, 29 are reunited and introduced into the high-pressure column 21 via line 30 essentially in the gas state.
  • nitrogen for example from the main condenser or from the high-pressure column of the distillation column system for nitrogen-oxygen separation 20, can also be internally compressed in an analogous manner.
  • Post-compressor 10 and the second turbine 28 and the second booster 13 mechanically coupled in pairs via a common shaft.
  • the booster heat exchanger 9 and the aftercooler 14 are optional. They can be omitted individually or altogether.
  • Figure 2 shows an embodiment containing two modifications to the method of Figure 1, both of which are independently applicable.
  • the same or comparable method steps bear the same reference numerals as in FIG. 1.
  • the first modification relates to the outlet pressure of the second turbine 28. This relaxes here to 1, 2 to 4 bar, preferably about 1, 4 bar, that is about the operating pressure of the low pressure column 22. The relaxed lower part stream 129 is then blown into the low pressure column. The entry pressures of the two
  • Turbines 25, 28 are still the same, the inlet temperatures may be the same or different.
  • the second after-compressor 113 is designed as a cold compressor.
  • the first air flow 12a, 12b, 12c is therefore already below the Intermediate pressure introduced into the main heat exchanger 16 and removed at a second intermediate temperature of 120 to 180 K, preferably about 48 K again from the main heat exchanger 16.
  • This second intermediate temperature may be less than or equal to the inlet temperature of the turbines 25, 28, preferably it is - contrary to the representation in the drawing - higher.
  • the second air stream 115 is reintroduced into the main heat exchanger 16 at a third intermediate temperature which is higher than the turbine inlet temperature and 140 to 220 K, preferably about 180 K.
  • the second air flow upstream of the cold booster 1 13 can also be led to the cold end of the main heat exchanger 16 and thereby at least partially liquefied. He is then then slightly throttled, reintroduced into the cold end of the main heat exchanger, again vaporized and finally heated to the inlet temperature of the compressor 113, as explained in detail for example in EP 1067345 B1.

Abstract

L'invention concerne un procédé et un dispositif de décomposition de l'air à basse température au moyen d'un système de colonnes de distillation pour la séparation de l'azote et de l'oxygène (20), ce système comprenant au moins une colonne de séparation (21,22). Un flux d'air principal (1,5) est comprimé dans un compresseur d'air (2) et nettoyé dans un dispositif de nettoyage (4). Un premier et un deuxième flux d'air (7,8) sont séparés du flux d'air principal (5). Le premier flux d'air (7) est de nouveau comprimé dans deux compresseurs d'air (10,13) reliés en série en aval. Le premier flux d'air recomprimé (15) est refroidi par échange thermique indirect (16), il est au moins partiellement liquéfié ou pseudo-liquéfié et introduit ensuite dans le système de colonnes de distillation pour la séparation de l'azote et de l'oxygène (20). Le deuxième flux d'air (8) est refroidi par échange thermique indirect (16), puis il est séparé en deux flux partiels (24,27), détendu dans deux installations de détente (25,28) en produisant une énergie, les deux installations de détente ayant sensiblement la même pression d'entrée. Les flux partiels (26,29) détendus et produisant de l'énergie du deuxième flux d'air sont au moins en partie introduits (30,129) dans le système de colonnes de distillation pour la séparation de l'azote et de l'oxygène (20). L'énergie mécanique développée lors de la détente (25,28) produisant de l'énergie du deuxième flux d'air est au moins partiellement utilisée pour entraîner les deux compresseurs d'air (10,13) reliés en série en aval. Un flux liquide produit (31) est extrait du système de colonnes de distillation pour la séparation de l'azote et de l'oxygène (20), il est, à l'état liquide, soumis à une pression accrue (32) et, sous cette pression accrue, il est évaporé ou pseudo-évaporé avec le premier flux d'air (15) par échange thermique indirect (16), avant d'être extrait sous forme de flux gazeux produit (34). Les deux compresseurs d'air (10,13) fonctionnent à une température d'entrée supérieure à 250 K, notamment supérieure à 270 K.
PCT/EP2007/001917 2006-03-15 2007-03-06 Procédé et dispositif de décomposition de l'air à basse température WO2007104449A1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
EP07723062A EP1994344A1 (fr) 2006-03-15 2007-03-06 Procédé et dispositif de décomposition de l'air à basse température
US12/282,606 US20090188280A1 (en) 2006-03-15 2007-03-06 Process and device for low-temperature separation of air
JP2008558680A JP2009529648A (ja) 2006-03-15 2007-03-06 低温空気分離方法及び装置
CN2007800135967A CN101421575B (zh) 2006-03-15 2007-03-06 用于低温分离空气的方法和装置

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102006012241A DE102006012241A1 (de) 2006-03-15 2006-03-15 Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
DE102006012241.0 2006-03-15

Publications (1)

Publication Number Publication Date
WO2007104449A1 true WO2007104449A1 (fr) 2007-09-20

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Application Number Title Priority Date Filing Date
PCT/EP2007/001917 WO2007104449A1 (fr) 2006-03-15 2007-03-06 Procédé et dispositif de décomposition de l'air à basse température

Country Status (6)

Country Link
US (1) US20090188280A1 (fr)
EP (1) EP1994344A1 (fr)
JP (1) JP2009529648A (fr)
CN (1) CN101421575B (fr)
DE (1) DE102006012241A1 (fr)
WO (1) WO2007104449A1 (fr)

Cited By (16)

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EP2784420A1 (fr) 2013-03-26 2014-10-01 Linde Aktiengesellschaft Procédé de séparation de l'air et installation de séparation de l'air
WO2014154339A2 (fr) 2013-03-26 2014-10-02 Linde Aktiengesellschaft Procédé de séparation d'air et installation de séparation d'air
EP2801777A1 (fr) 2013-05-08 2014-11-12 Linde Aktiengesellschaft Installation de décomposition de l'air dotée d'un entraînement de compresseur principal
EP2963367A1 (fr) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Procédé et dispositif cryogéniques de séparation d'air avec consommation d'énergie variable
EP2963370A1 (fr) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Procede et dispositif cryogeniques de separation d'air
EP2963369A1 (fr) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Procede et dispositif cryogeniques de separation d'air
EP2963371A1 (fr) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Procede et dispositif de production d'un produit de gaz sous pression par decomposition a basse temperature d'air
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DE102009048456A1 (de) * 2009-09-21 2011-03-31 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
DE102010055448A1 (de) * 2010-12-21 2012-06-21 Linde Ag Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
FR2973487B1 (fr) * 2011-03-31 2018-01-26 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede et appareil de production d'un gaz de l'air sous pression par distillation cryogenique
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Publication number Priority date Publication date Assignee Title
EP2458311A1 (fr) 2010-11-25 2012-05-30 Linde Aktiengesellschaft Procédé et dispositif de production d'un produit d'impression gazeux par décomposition à basse température d'air
DE102010052545A1 (de) 2010-11-25 2012-05-31 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Gewinnung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft
DE102010052544A1 (de) 2010-11-25 2012-05-31 Linde Ag Verfahren zur Gewinnung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft
EP2466236A1 (fr) 2010-11-25 2012-06-20 Linde Aktiengesellschaft Procédé de production d'un produit d'impression gazeux par décomposition à basse température de l'air
EP2520886A1 (fr) 2011-05-05 2012-11-07 Linde AG Procédé et dispositif de production d'un produit comprimé à oxygène gazeux par décomposition à basse température d'air
DE102011112909A1 (de) 2011-09-08 2013-03-14 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Gewinnung von Stahl
EP2568242A1 (fr) 2011-09-08 2013-03-13 Linde Aktiengesellschaft Procédé et dispositif destinés à la production d'acier
EP2600090A1 (fr) 2011-12-01 2013-06-05 Linde Aktiengesellschaft Procédé et dispositif destinés à la production d'oxygène sous pression par décomposition à basse température de l'air
US20130139548A1 (en) * 2011-12-01 2013-06-06 Linde Aktiengesellschaft Method and apparatus for producing pressurized oxygen by low-temperature separation of air
DE102011121314A1 (de) 2011-12-16 2013-06-20 Linde Aktiengesellschaft Verfahren zur Erzeugung eines gasförmigen Sauerstoff-Druckprodukts durch Tieftemperaturzerlegung von Luft
DE102012017488A1 (de) 2012-09-04 2014-03-06 Linde Aktiengesellschaft Verfahren zur Erstellung einer Luftzerlegungsanlage, Luftzerlegungsanlage und zugehöriges Betriebsverfahren
EP2784420A1 (fr) 2013-03-26 2014-10-01 Linde Aktiengesellschaft Procédé de séparation de l'air et installation de séparation de l'air
WO2014154339A2 (fr) 2013-03-26 2014-10-02 Linde Aktiengesellschaft Procédé de séparation d'air et installation de séparation d'air
EP2801777A1 (fr) 2013-05-08 2014-11-12 Linde Aktiengesellschaft Installation de décomposition de l'air dotée d'un entraînement de compresseur principal
DE102013017590A1 (de) 2013-10-22 2014-01-02 Linde Aktiengesellschaft Verfahren zur Gewinnung eines Krypton und Xenon enthaltenden Fluids und hierfür eingerichtete Luftzerlegungsanlage
EP2963367A1 (fr) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Procédé et dispositif cryogéniques de séparation d'air avec consommation d'énergie variable
EP2963370A1 (fr) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Procede et dispositif cryogeniques de separation d'air
EP2963369A1 (fr) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Procede et dispositif cryogeniques de separation d'air
EP2963371A1 (fr) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Procede et dispositif de production d'un produit de gaz sous pression par decomposition a basse temperature d'air
WO2016005031A1 (fr) 2014-07-05 2016-01-14 Linde Aktiengesellschaft Procédé et dispositif de fractionnement de l'air à basse température à consommation d'énergie variable
CN109442867A (zh) * 2018-12-19 2019-03-08 杭州特盈能源技术发展有限公司 一种新型外增压内液化纯氮制取装置及方法
CN109442867B (zh) * 2018-12-19 2023-11-07 杭州特盈能源技术发展有限公司 一种外增压内液化纯氮制取装置及方法

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CN101421575B (zh) 2012-11-07
EP1994344A1 (fr) 2008-11-26

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