[go: up one dir, main page]

WO2011110301A2 - Procédé et dispositif de séparation de l'air à basse température - Google Patents

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

Info

Publication number
WO2011110301A2
WO2011110301A2 PCT/EP2011/001002 EP2011001002W WO2011110301A2 WO 2011110301 A2 WO2011110301 A2 WO 2011110301A2 EP 2011001002 W EP2011001002 W EP 2011001002W WO 2011110301 A2 WO2011110301 A2 WO 2011110301A2
Authority
WO
WIPO (PCT)
Prior art keywords
air
pressure
heat exchanger
main heat
compressed
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/EP2011/001002
Other languages
German (de)
English (en)
Other versions
WO2011110301A3 (fr
Inventor
Stefan Lochner
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Original Assignee
Linde GmbH
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 GmbH filed Critical Linde GmbH
Publication of WO2011110301A2 publication Critical patent/WO2011110301A2/fr
Publication of WO2011110301A3 publication Critical patent/WO2011110301A3/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

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
    • F25J3/04151—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
    • F25J3/04006—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
    • F25J3/04084—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
    • F25J3/04248—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.
    • F25J3/04381—Details relating to the work expansion, e.g. process parameter etc. using work extraction by mechanical coupling of compression and expansion so-called companders
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/20—Integrated compressor and process expander; Gear box arrangement; Multiple compressors on a common shaft

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 two-column system for nitrogen-oxygen separation (for example as a classical Linde double column system) or as a three-column or multi-column system. It may in addition to the columns for nitrogen-oxygen separation, other devices for obtaining high purity products and / or other
  • Air components in particular of noble gases, for example, an argon and / or a krypton-xenon recovery.
  • the invention has for its object to provide a method of the type mentioned above and a corresponding device, which are economically particularly favorable to operate by having a particularly low energy consumption and / or particularly low investment costs.
  • a gearless combination of turbine, cold compressor and oil brake is used, preferably a combination machine, in which the oil brake sits on the shaft between the wheels for turbine and cold compressor.
  • Balancing group no heat withdrawn. Since the process of the invention has only a single turbine, a second part of the mechanical energy generated during the work-relaxing relaxation is transferred to a warm braking device, namely to a dissipative braking device, which is formed by an oil brake to generate process refrigeration.
  • a warm braking device namely to a dissipative braking device, which is formed by an oil brake to generate process refrigeration.
  • first and / or the second air stream may be introduced into the low-pressure column, in particular after flowing through a separator for phase separation and optionally after supercooling.
  • the "main heat exchanger” may be formed of one or more parallel and / or serially connected heat exchanger sections, for example one or more plate heat exchanger blocks.
  • the first pressure, to which the total air is compressed is "significantly higher” than the operating pressure of the high-pressure column. This means here that the pressure difference between the first pressure and the
  • Operating pressure of the high-pressure column not only corresponds to the natural pressure drop through lines, heat exchangers and other apparatus, but at least 1 bar, preferably at least 3 bar, most preferably at least 5 bar.
  • the pressure difference between the first pressure and the operating pressure of the high-pressure column is, for example, 5 to 25 bar, preferably 7 to 15 bar. (All pressures given here and below are absolute pressures.)
  • the first pressure is 10 to 25 bar, preferably 13 to 20 bar
  • the operating pressure of the high-pressure column is 4 to 8 bar, preferably 5 to 7 bar.
  • the second pressure downstream of the first pressure is 10 to 25 bar, preferably 13 to 20 bar
  • the operating pressure of the high-pressure column is 4 to 8 bar, preferably 5 to 7 bar.
  • Cold compressor for example, 1 1, 5 to 55 bar, preferably 21 to 44 bar, the increased pressure of the product pressure stream, for example 6 to 50 bar, preferably 6 to 35 bar.
  • every level of product pressure is possible, in particular also a plurality of pressure levels.
  • liquid oxygen can be brought to 30 bar in an internal compression pump and divided in cold into two partial streams upstream of the main heat exchanger, one of which is throttled to a lower pressure before it is vaporized and heated in the main heat exchanger.
  • one or more liquid nitrogen streams in the main heat exchanger are evaporated.
  • the pressures of the pressurized product stream and the first air stream are subcritical, they are vaporized or liquefied in the main heat exchanger. At supercritical pressure no real phase transition takes place, then the corresponding stream is pseudo-vaporized or pseudo-liquefied. It is favorable if the entire cold-compressed second air flow in the
  • Pressure increase which is caused by the cold compressor, concentrated on that part of air, which is used for (pseudo) evaporation of the liquid product stream. This allows the first pressure to be chosen correspondingly lower and energy saved.
  • the entire introduced into the main heat exchanger compressed feed air is divided into the first and the second air flow. So there is no third air flow, but the entire feed air is either under the second pressure (pseudo) liquefied (first air flow) or supplied under the first pressure of the work-performing expansion (second air flow).
  • first air flow the second pressure liquefied
  • second air flow the first pressure of the work-performing expansion
  • the outlet pressure of the work-performing expansion is preferably approximately equal to the operating pressure of the high-pressure column. "About the same” concludes small Pressure differences in the order of magnitude of the natural pressure drop between the outlet pressure of the work-performing expansion and the operating pressure of
  • Products here the molar amount of liquid products such as liquid oxygen, liquid nitrogen and optionally liquid argon, which are obtained in the process as a final product.
  • the invention also relates to a device for the cryogenic separation of air according to the claims 7 to 9.
  • Atmospheric air 1 is sucked in via a filter 2 from an air compressor 3 and there compressed as feed air to a first pressure of about 17 bar. Subsequently, the compressed feed air flows through a direct contact cooler 4 and is cooled there in direct contact with cooling water 5. The cooled feed air 6 is cleaned in a cleaning device 7.
  • the cleaning device 7 comprises a pair of containers filled with adsorbent material, preferably molecular sieve.
  • the purified feed air 8 is - apart from a not shown
  • Cold water aftercooler which is operated with cold water from an evaporative cooler.
  • Cooling water heating of more than 10 ° C is operated.
  • a refrigeration system can be used to pre-cool the feed air.
  • the first air stream is removed via line 12 at a first intermediate temperature of about 140 K from the corresponding cooling passage of the main heat exchanger 11 and densified in a cold compressor 13 from the first pressure to a second pressure of about 31 bar.
  • a second intermediate temperature of about 170 K the recompressed second air stream 14 is again in the
  • Main heat exchanger 11 introduced and further cooled and liquefied there and finally introduced via line 15 and a throttle valve 16 in the high pressure column 17 of a distillation column system for nitrogen-oxygen separation, which also has a low-pressure column 18 and a main condenser 19, as
  • Condenser-evaporator is formed.
  • the operating pressures are (at the top) 5 to 6.5 bar in the high pressure column and 1, 3 bar in the low pressure column.
  • the second air stream 10 is cooled in the embodiment separately from the first air stream 9 in the main heat exchanger 1 1 to a third intermediate temperature of about 139 K. Typically, this temperature is in the range of the boiling temperature (s) of the vapor product stream (s). Via line 20, the second air flow is supplied under this intermediate temperature and the first pressure of a turbine 21 and there relaxes work to about the operating pressure of the high pressure column.
  • the working expanded second air stream 22 occurs immediately above the sump in the high-pressure column 17 a.
  • the turbine 21 is mechanically coupled to the cold compressor 3 and an oil brake 23 via a common shaft. Contrary to the graphic representation is the Oil brake disposed directly on the shaft, the turbine 21 and cold compressor 13 connects and is located between them.
  • the head nitrogen 24 of the high pressure column is a first part 25 in the
  • the resulting liquid nitrogen 26 is fed to a first part 27 as reflux to the high-pressure column 17, to a second part 28 it is fed via a supercooling countercurrent 29, line 30 and throttle valve 31 in the head of the low pressure column 18.
  • Bottom product 32 of the high pressure column 17 is also cooled in the subcooling countercurrent 29 and then fed via line 33 and throttle valve 34 of the low pressure column 18 at an intermediate point.
  • a second part 35 of the top nitrogen 24 of the high-pressure column 17 is in
  • Main heat exchanger 11 warmed to about ambient temperature and finally delivered via line 36 as a pressure nitrogen product or as instrument or sealing gas (seal gas).
  • the oxygen in the bottom of the low pressure column 18 is removed via line 37 as a liquid product stream, brought in a pump 38 to an elevated pressure of 30 bar, evaporated under this increased pressure in the main heat exchanger and finally withdrawn as gaseous pressure product stream 39 (GOX IC).
  • GAN EC gaseous pressure product
  • a second embodiment corresponds largely to the first, but a portion of the liquid nitrogen 26 is brought from the main condenser as a further liquid product stream in a nitrogen pump to an increased product pressure and in the main heat exchanger 1 (pseudo) evaporated and heated to about ambient temperature and finally as another gaseous pressure product stream obtained in the form of high-pressure nitrogen.
  • a portion of the liquid high-pressure oxygen downstream of the oxygen pump 38 is throttled to a pressure which is between the "elevated pressure" (the discharge pressure of the oxygen pump 38) and the operating pressure of the low-pressure column 18.
  • This stream is also vaporized and warmed in the main heat exchanger and finally recovered as the third pressure product stream in the form of intermediate pressure oxygen.

Landscapes

  • 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)

Abstract

L'invention concerne un procédé et un dispositif utilisés pour la séparation de l'air à basse température dans un système de colonnes de distillation pour la séparation de l'azote et de l'oxygène comprenant une colonne haute pression (17) et une colonne basse pression (18). L'air de charge (1) est comprimé dans un compresseur d'air principal (3) à une première pression, qui est nettement supérieure à la pression de service de la colonne haute pression (17). L'air de charge comprimé (8) est introduit dans un échangeur thermique principal (11) pour y être refroidi contre les flux de retour. Un premier flux d'air (9), qui est formé par une partie de l'air de charge comprimé (8), est prélevé hors de l'échangeur thermique principal (11) après un refroidissement partiel dans l'échangeur thermique principal (11) avec une première température intermédiaire, et est soumis à une nouvelle compression à une deuxième pression dans un compresseur à froid (13). Le premier flux d'air comprimé à froid (14) est acheminé avec une deuxième température intermédiaire, supérieure à la première température intermédiaire, à nouveau vers l'échangeur thermique principal (11) et, dans ledit échangeur thermique principal (11), est davantage refroidi, puis liquéfié ou pseudo-liquéfié. Le premier flux d'air (pseudo-)liquéfié (15) est introduit dans le système de colonnes de distillation pour la séparation de l'azote et de l'oxygène. Un deuxième flux d'air (10), qui est formé par une autre partie de l'air de charge comprimé (8) n'ayant pas traversé le compresseur à froid (13), est prélevé (20) avec une troisième température intermédiaire hors de l'échangeur thermique principal (11) et est soumis ensuite à une détente à rendement effectif dans une turbine (21). Le deuxième flux d'air détendu à rendement effectif (22) est également introduit dans le système de colonnes de distillation pour la séparation de l'azote et de l'oxygène. Un flux de produit liquide (37) est prélevé hors du système de colonnes de distillation, et, à l'état liquide, est amené (38) à une pression plus élevée, puis est évaporé ou pseudo-évaporé sous cette pression élevée dans l'échangeur thermique principal (11), et est retiré finalement sous forme de flux de produit gazeux sous pression (39). Une première partie de l'énergie mécanique générée dans la turbine (21) lors de la détente à rendement effectif est utilisée pour l'entraînement du compresseur à froid (13). Une deuxième partie de l'énergie mécanique générée dans la turbine (21) lors de la détente à rendement effectif est acheminée vers un amortisseur à huile (23). On utilise une combinaison sans engrenage, formée par la turbine (21), le compresseur à froid (13) et l'amortisseur à huile (21).
PCT/EP2011/001002 2010-03-09 2011-03-01 Procédé et dispositif de séparation de l'air à basse température Ceased WO2011110301A2 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP10002439.7 2010-03-09
EP10002439A EP2369281A1 (fr) 2010-03-09 2010-03-09 Procédé et dispositif destinés à la décomposition à basse température d'air

Publications (2)

Publication Number Publication Date
WO2011110301A2 true WO2011110301A2 (fr) 2011-09-15
WO2011110301A3 WO2011110301A3 (fr) 2012-08-23

Family

ID=42727812

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2011/001002 Ceased WO2011110301A2 (fr) 2010-03-09 2011-03-01 Procédé et dispositif de séparation de l'air à basse température

Country Status (2)

Country Link
EP (1) EP2369281A1 (fr)
WO (1) WO2011110301A2 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102012017488A1 (de) 2012-09-04 2014-03-06 Linde Aktiengesellschaft Verfahren zur Erstellung einer Luftzerlegungsanlage, Luftzerlegungsanlage und zugehöriges Betriebsverfahren
WO2015003785A1 (fr) 2013-07-09 2015-01-15 Linde Aktiengesellschaft Procédé et dispositif de production d'un flux de gaz comprimé et procédé et dispositif de séparation d'air à basse température

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR3010778B1 (fr) * 2013-09-17 2019-05-24 Air Liquide Procede et appareil de production d'oxygene gazeux par distillation cryogenique de l'air
CN112392558B (zh) * 2019-08-13 2024-05-03 江苏国富氢能技术装备股份有限公司 一种低温气液化用透平膨胀装置

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20050126221A1 (en) 2003-12-10 2005-06-16 Bao Ha Process and apparatus for the separation of air by cryogenic distillation

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5475980A (en) 1993-12-30 1995-12-19 L'air Liquide, Societe Anonyme Pour L'etude L'exploitation Des Procedes Georges Claude Process and installation for production of high pressure gaseous fluid
GB9404991D0 (en) * 1994-03-15 1994-04-27 Boc Group Plc Cryogenic air separation
DE59909750D1 (de) * 1999-07-05 2004-07-22 Linde Ag Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
FR2851330B1 (fr) * 2003-02-13 2006-01-06 Air Liquide Procede et installation de production sous forme gazeuse et sous haute pression d'au moins un fluide choisi parmi l'oxygene, l'argon et l'azote par distillation cryogenique de l'air
FR2854683B1 (fr) 2003-05-05 2006-09-29 Air Liquide Procede et installation de production de gaz de l'air sous pression par distillation cryogenique d'air
FR2854682B1 (fr) * 2003-05-05 2005-06-17 Air Liquide Procede et installation de separation d'air par distillation cryogenique
EP1767884A1 (fr) * 2005-09-23 2007-03-28 L'Air Liquide Société Anon. à Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Procédés Georges Claude Procédé et dispositif pour la séparation cryogénique d'air
FR2913760B1 (fr) * 2007-03-13 2013-08-16 Air Liquide Procede et appareil de production de gaz de l'air sous forme gazeuse et liquide a haute flexibilite par distillation cryogenique

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20050126221A1 (en) 2003-12-10 2005-06-16 Bao Ha Process and apparatus for the separation of air by cryogenic distillation

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
"Beispiel aus Hausen/Linde, Tieftemperaturtechnik", 1985, pages: 281 - 337

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102012017488A1 (de) 2012-09-04 2014-03-06 Linde Aktiengesellschaft Verfahren zur Erstellung einer Luftzerlegungsanlage, Luftzerlegungsanlage und zugehöriges Betriebsverfahren
WO2015003785A1 (fr) 2013-07-09 2015-01-15 Linde Aktiengesellschaft Procédé et dispositif de production d'un flux de gaz comprimé et procédé et dispositif de séparation d'air à basse température

Also Published As

Publication number Publication date
EP2369281A1 (fr) 2011-09-28
WO2011110301A3 (fr) 2012-08-23

Similar Documents

Publication Publication Date Title
EP3164654B1 (fr) Procédé et dispositif de fractionnement de l'air à basse température à consommation d'énergie variable
EP2235460B1 (fr) Procédé et installation pour la séparation cryogénique d'air
EP3410050B1 (fr) Procédé de production d'un ou de plusieurs produits pneumatiques et installation de séparation d'air
EP1994344A1 (fr) Procédé et dispositif de décomposition de l'air à basse température
EP2015012A2 (fr) Procédé pour la séparation cryogénique d'air
DE102010052545A1 (de) Verfahren und Vorrichtung zur Gewinnung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft
EP3290843A2 (fr) Procédé et dispositif destiné à fabriquer de l'azote pressurisé et liquide par décomposition à basse température de l'air
EP2963370B1 (fr) Procede et dispositif cryogeniques de separation d'air
EP2236964A1 (fr) Procédé et dispositif de séparation de l'air à basse température
EP3343158A1 (fr) Procédé de production d'un ou plusieurs produits pneumatiques et unité de fractionnement d'air
EP2299221A2 (fr) Procédé et dispositif destinés à la décomposition à basse température d'air
EP2520886A1 (fr) Procédé et dispositif de production d'un produit comprimé à oxygène gazeux par décomposition à basse température d'air
EP2489968A1 (fr) Procédé et dispositif destinés à la décomposition à basse température d'air
EP2603754A2 (fr) Procédé et dispositif permettant d'obtenir de l'oxygène sous pression et de l'azote sous pression par fractionnement cryogénique de l'air
WO2014146779A2 (fr) Procédé et dispositif de production d'azote gazeux sous pression
EP2963369B1 (fr) Procede et dispositif cryogeniques de separation d'air
WO2020164799A1 (fr) Procédé et installation pour fournir un ou plusieurs produits présents dans l'air, gazeux et à teneur élevée en oxygène
WO2011110301A2 (fr) Procédé et dispositif de séparation de l'air à basse température
EP2551619A1 (fr) Procédé et dispositif destinés à l'obtention d'oxygène pressurisé et d'azote pressurisé par la décomposition à basse température de l'air
EP3980705A1 (fr) Procédé et installation de décomposition d'air à basse température
DE102007042462A1 (de) Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
EP2600090B1 (fr) Procédé et dispositif destinés à la production d'oxygène sous pression par décomposition à basse température de l'air
WO2017108187A1 (fr) Procédé et dispositif de production d'azote pur et d'oxygène pur par séparation cryogénique d'air
EP4065910A1 (fr) Procédé et installation pour fractionnement à basse température de l'air
EP2963371B1 (fr) Procede et dispositif de production d'un produit de gaz sous pression par decomposition a basse temperature d'air

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 11707092

Country of ref document: EP

Kind code of ref document: A2

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 11707092

Country of ref document: EP

Kind code of ref document: A2