EP1199532A1 - Système de séparation d'air cryogénique à trois colonnes - Google Patents

Système de séparation d'air cryogénique à trois colonnes Download PDF

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Publication number
EP1199532A1
EP1199532A1 EP01103828A EP01103828A EP1199532A1 EP 1199532 A1 EP1199532 A1 EP 1199532A1 EP 01103828 A EP01103828 A EP 01103828A EP 01103828 A EP01103828 A EP 01103828A EP 1199532 A1 EP1199532 A1 EP 1199532A1
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European Patent Office
Prior art keywords
pressure column
oxygen
medium
column
gas turbine
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Granted
Application number
EP01103828A
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German (de)
English (en)
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EP1199532B1 (fr
Inventor
Christian Kunz
Dietrich Dipl.-Ing. Rottmann
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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
    • F25J3/04151—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
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    • 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
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/04018—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of main feed air
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    • 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
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    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
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    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/42—One fluid being nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/50—One fluid being oxygen
    • 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
    • F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
    • F25J2260/42—Integration in an installation using nitrogen, e.g. as utility gas, for inerting or purging purposes in IGCC, POX, GTL, PSA, float glass forming, incineration processes, for heat recovery or for enhanced oil recovery

Definitions

  • the invention relates to a method for the low-temperature decomposition of air and Power generation.
  • the air separation is carried out in a three-pillar system.
  • a gas turbine system which is a gas turbine, is used to generate energy (Gas turbine expander), a gas turbine compressor driven by the gas turbine and has a combustion chamber.
  • one or more Air separation products used in the energy generation system for example, oxygen generated in the air separator can be used to generate a Fuel gas can be used with which the combustion chamber is loaded, in particular as an oxidizing agent in a coal or heavy oil gasification.
  • nitrogen from the air separator can be used to extract coal and / or used in the gas turbine stream; in the latter case Nitrogen is fed into the combustion chamber or into the gas turbine or with the Gas turbine exhaust gas between the combustion chamber and the gas turbine of the combustion chamber mixed.
  • the basics of low temperature air separation in general are in the Monograph "Low Temperature Technology” by Hausen / Linde (2nd edition, 1985) and in one Article by Latimer in Chemical Engineering Progress (Vol. 63, No.2, 1967, page 35) described.
  • the three-pillar system is preferably one Triple column, in which the head of the high pressure column and the bottom of the Medium pressure column and on the other hand the head of the medium pressure column and the sump of the Low pressure column are in heat-exchanging connection.
  • triple columns are also from DE 1041989 or from Springmann, Chem.-Ing.-Techn., 46 (1974), 881 known.
  • the invention is also with other column arrangements and / or others Capacitor configurations applicable (see for example EP 768503 A2, DE 2920270 or EP 572962 A or EP 634617 A).
  • Capacitor configurations applicable (see for example EP 768503 A2, DE 2920270 or EP 572962 A or EP 634617 A).
  • Devices for extracting other air components, in particular from Noble gases can be provided, for example argon extraction.
  • the gas turbine compressor brings air to a very high pressure of over about 7 bar, for example of 17 bar.
  • This air usually serves as a part Combustion air for the combustion chamber of the gas turbine system.
  • Another part is the first feed air stream to be led into air separation.
  • a second feed air flow independent of the first in a separate air compressor compressed, preferably to a pressure lower than that Outlet pressure of the gas turbine compressor; this is in itself from EP 717249 A2 known.
  • the air compressor is not driven by the gas turbine, but rather for example from an engine or a steam turbine. (The term “not from the However, gas turbine driven "does not exclude that generated in the gas turbine electrical energy is transmitted to an electric motor, which in turn the drives a separate air compressor.)
  • such a double column system is based on three columns reduced, which preserves its essential advantages, but the expenditure on equipment greatly reduced.
  • the medium-pressure column of the three-column system simultaneously the low pressure part of the double column for the air under the higher pressure as well represents the high pressure part of the double column for the air under the lower pressure So the first feed air flow is introduced into the high pressure column, and the Medium pressure column is both with oxygen-enriched liquid from the High pressure column as well as the second feed air flow.
  • Return for the Low pressure column can come from one or more of the following sources: im first condenser formed condensate, in the second main condenser condensate formed, liquid nitrogen flow from an intermediate point of High pressure column, liquid nitrogen flow from an intermediate point of the medium pressure column.
  • a liquid nitrogen stream has at least one theoretical bottom below the head of the medium pressure column and the Low pressure column is fed. This is particularly advantageous if in the Low pressure column no pure nitrogen is generated. Between the medium pressure column head and the liquid nitrogen discharge to the low pressure column are, for example, 5 to 20, preferably 10 to 15 practical floors.
  • the second oxygen-enriched fraction which is in the Low pressure column is initiated, withdrawn from the high pressure column.
  • the first oxygen-enriched fraction (insert for the medium pressure column) and the second oxygen-enriched fraction (insert for the low pressure column) preferably withdrawn together from the bottom of the high pressure column and before their introduction into the medium pressure column or low pressure column.
  • an oxygen fraction 1 is generated in the low pressure column is, at least part of the oxygen fraction liquid from the low pressure column removed, brought to an increased pressure in the liquid state and into the Medium pressure column is introduced and that the medium pressure column is an oxygen product is removed.
  • the oxygen product is therefore already in the process of being removed from the three-pillar system at an increased pressure. The effort for Further compression on the product pressure is noticeably reduced or can even drop completely.
  • the pressurized liquid oxygen fraction from the Low pressure column at least one theoretical floor (for example one to five practical trays) is introduced into the medium pressure column above the sump. This can result in a lower purity in the bottom of the low pressure column than in Medium pressure column sump prevail. With thermal coupling of low pressure column and medium pressure column this enables a relatively high pressure in the low pressure column or a particularly low operating air pressure.
  • the oxygen product is liquid from the Stripped medium pressure column, introduced into a secondary condenser and through there indirect heat exchange with a heating medium, especially with nitrogen the high pressure column is at least partially evaporated.
  • the oxygen product is often required under a pressure higher than that Operating pressure of the medium pressure column.
  • a pressure higher than that Operating pressure of the medium pressure column for example be compressed outside by being gaseous from the medium pressure column or a Secondary condenser, which is operated under medium-pressure column pressure, removed, warmed to about ambient temperature and in an oxygen compressor is compressed.
  • the oxygen product or part of it compress inside by flowing it out of the medium pressure column or out of the Secondary condenser is removed, brought to a pressure in the liquid state, which is higher than the operating pressure of the medium pressure column, and under this pressure indirect heat exchange is evaporated.
  • the evaporation of the liquid under pressure brought oxygen product can be carried out in the main heat exchanger in which the cooling of the feed air for the high pressure column and the Heating of other products takes place; alternatively, this can be indirect Heat exchange step take place in a separate heat exchanger.
  • the heat of vaporization is available through a high pressure flow provided, either by a correspondingly highly compressed part of the feed air or is formed by circulating nitrogen. Because the inner compression also on supercritical pressures, the term "evaporation" is here in another To understand the meaning that also includes pseudo-evaporation.
  • a nitrogen fraction can be drawn directly from the high pressure column and / or the Medium pressure column removed, warmed up and obtained as a pressure nitrogen product become.
  • the high-pressure column nitrogen can also be internally compressed if necessary, by making the nitrogen fraction liquid from the high pressure column or their Head condenser removed, is brought to a pressure in the liquid state, the is higher than the operating pressure of the high pressure column, and under this pressure indirect heat exchange is evaporated.
  • the indirect heat exchange will preferably carried out in the main heat exchanger with high pressure air as the heating fluid.
  • the second Feed air flow separate from the first feed air flow only to approximately Operating pressure of the medium pressure column (plus line losses) compressed and without further pressure-changing measures are introduced into the medium pressure column.
  • (only) part of the separation air from a gas turbine compressor is delivered (for example the first feed air flow), this saves How energy works.
  • a third feed air stream can be compressed to generate process cold, cleaned, cooled, relieved of work and into the low pressure column or in the Medium pressure column are introduced.
  • Work relaxation Mechanical energy generated can be used to recompress the third feed air flow be used, for example by using a turbine-booster combination.
  • the invention also relates to a combined device for cryogenic decomposition of air and for energy generation according to claim 14.
  • An air stream 10 is brought to a pressure in a gas turbine compressor 11, which is at least equal to the operating pressure of the high pressure column 1.
  • the gas turbine compressor 11 is part of a gas turbine system. (Part of the air compressed in 11 is branched off as combustion air to the combustion chamber of the gas turbine unit, what is not shown in the drawing).
  • a cleaning device 13 preferably a molecular sieve station.
  • a first feed air stream 15 is branched off from the cleaned high-pressure air 14, in a main heat exchanger 40 cooled and via line 16 of the high pressure column 1 fed.
  • a partial air flow (not shown here) has to be described in detail higher pressure further compressed and downstream of the main heat exchanger 40 be throttled.
  • a second feed air stream 20, 24 is through an air compressor 21, a Aftercooler 22 and a separate cleaning device 23 performed, also in Main heat exchanger 40 cooled, but then led into the medium pressure column 2 (25), without throttling or other pressure-changing measures downstream of the second air compressor.
  • the second feed air flow needs in the second Air compressor 21 only compresses to approximately the operating pressure of the medium pressure column 2 become.
  • the air compressor is not driven by the gas turbine, but rather preferably by means of external energy, for example by an electric motor.
  • This is in a post-compressor 31 further compresses and occurs after post-cooling 32 in the Main heat exchanger 40. After cooling to an intermediate temperature, it becomes led out of the main heat exchanger 40 via line 33, in one Turbine 34 relaxed while working and blown into the low-pressure column 3 (35).
  • the turbine 34 is mechanically coupled to the post-compressor 31.
  • Gaseous nitrogen 41 is generated at the top of the high-pressure column 1. He's going to liquefied a first part 42 in the first main condenser 4. The one won Liquid nitrogen 43 is returned to the high pressure column 1 (line 44) or abandoned to the medium pressure column 2 (line 45). The Liquid nitrogen 45 is in one before the feed 46 into the medium pressure column Supercooling counterflow 47 supercooled. A second part 48 of the top nitrogen 41 the high pressure column is at least partially in a secondary condenser 49 condenses and flows back via line 50 to the high pressure column 1. A third Part 51 of the high pressure column nitrogen 41 is in the main heat exchanger 40 warmed up and obtained via line 52 as a pressure nitrogen product GAN.
  • Liquid crude oxygen is obtained in the sump of the high-pressure column 1. This is called deducted oxygen-enriched fraction 53 and - after hypothermia 47 - to one first part 54 as the first oxygen-enriched fraction in the medium pressure column 2 initiated. A second part 56, 57 is after further supercooling 55 in the Throttled low pressure column.
  • a second part 61 of the top nitrogen 58 of the medium pressure column is in the Main heat exchanger 40 warmed up and via line 62 - if necessary after Further compression 63 with after-cooling 64 - as a further pressure nitrogen product PGAN won.
  • Liquid oxygen of 95% purity is generated in the bottom of the low pressure column. That part of the bottom liquid that is not in the second main condenser 5 is evaporated, flows as an oxygen fraction 67 to a pump 68 and is in there brought liquid state to about medium pressure column pressure. The oxygen fraction 69 is heated under this increased pressure in the supercooling counterflow 47 and introduced into the medium pressure column 2 via line 70. The feed is here immediately above the sump of the medium pressure column. In the swamp, the represents the evaporation space of the first main condenser 4, the Oxygen fraction 70 from the low pressure column with that within the medium pressure column flowing down liquid mixed. The mixture is liquid as line 71 Oxygen product taken, slightly throttled (72), in the Evaporation chamber of the secondary condenser 49 initiated and there partially evaporated.
  • a first part 73 of the oxygen product 71 is gaseous from the Auxiliary condenser removed, warmed up in the main heat exchanger and finally delivered via line 74 as a product (GOX). If product printing is desired, which is higher than the medium pressure column pressure, the warmed oxygen product be further compressed in a product compressor 75 (with aftercooler 78) (Outer compression).
  • the liquid portion of the oxygen product 71 is discharged via line 79 deducted the evaporation space of the secondary condenser 49 and one Subjected to internal compression. To do this, it is pumped to product pressure in a pump 80 brought about the same as the product pressure of the outer compression or different of this is.
  • the high pressure oxygen product 81 is in the main heat exchanger evaporates (or pseudo-evaporates if the product pressure is above the critical pressure lies) and warmed to ambient temperature. This leaves via line 76 internally compressed oxygen product (GOX-IC) the plant. If desired, he can be combined with the oxygen product 74, which is compressed in 75.
  • impure nitrogen 82 Another product of the low pressure column 3 is impure nitrogen 82 from the head deducted, in the supercooling countercurrent 55 and 47 and in Main heat exchanger 40 warmed up.
  • the warm impure nitrogen 83 (UN2) can be used as unpressurized by-product used as regeneration gas for the cleaning devices 13 and / or 23 used and / or released into the atmosphere.
  • Figure 2 is largely identical to Figure 1. However, here is the third Feed air flow 230, 233 in the expansion machine 234 only approximately Medium pressure column pressure relaxed. The relaxed third feed airflow 235 will via line 236 together with the second feed air flow 225 downstream of the Main heat exchanger 40 fed into the medium pressure column 2. A direct air introduction there is no low pressure column 3 in this process variant.
  • the cleaning of the two air streams 10, 20 can in principle also be carried out in one be carried out common device. For example, it is possible to Compress the total air initially only to approximately medium pressure column pressure, below this medium pressure, and then the first (and possibly the third) to further compress the air flow from the medium pressure.
  • the for the Processes also require cold from work-relieving nitrogen the medium pressure column 2 can be obtained.
  • the relaxed medium pressure column nitrogen can then be mixed with the impure nitrogen from the low pressure column 3 and be heated together with this in the main heat exchanger 40.
EP01103828A 2000-10-20 2001-02-15 Système de séparation d'air cryogénique à trois colonnes Expired - Lifetime EP1199532B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE10052180A DE10052180A1 (de) 2000-10-20 2000-10-20 Drei-Säulen-System zur Tieftemperatur-Zerlegung von Luft
DE10052180 2000-10-20

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AT (1) ATE301271T1 (fr)
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ES (1) ES2246945T3 (fr)

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1120616A2 (fr) * 2000-01-28 2001-08-01 The BOC Group plc Méthode de séparation de l'air
EP1120617A2 (fr) * 2000-01-28 2001-08-01 The BOC Group plc Séparation de l'air
EP2634517A1 (fr) * 2012-02-29 2013-09-04 L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Procédé et appareil pour la séparation d'air par distillation cryogénique
US20130340476A1 (en) * 2011-03-18 2013-12-26 L'air Liquide Societe Anonyme Pour I'etude Et I'exploitation Des Procedes Georges Claude Apparatus and method for separating air by cryogenic distillation
CN104067079B (zh) * 2011-03-18 2016-11-30 乔治洛德方法研究和开发液化空气有限公司 用于通过低温蒸馏分离空气的设备和方法
US20220090855A1 (en) * 2020-09-18 2022-03-24 L'Air Liquide, Societe Anonyme pour l'Etude et l'Exploitation des Procedeseorges Claude Method and apparatus for producing high-purity nitrogen and low-purity oxygen

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102009023900A1 (de) 2009-06-04 2010-12-09 Linde Aktiengesellschaft Dreisäulenverfahren und -vorrichtung zur Tieftemperaturzerlegung von Luft
EP3438585A3 (fr) * 2017-08-03 2019-04-17 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé de dégivrage d'un appareil de séparation d'air par distillation cryogénique et appareil adapté pour être dégivré par ce procédé

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Publication number Priority date Publication date Assignee Title
EP0476989A1 (fr) * 1990-09-20 1992-03-25 Air Products And Chemicals, Inc. Générateur de l'azote à triple colonne de distillation avec plusieurs évaporateurs/condenseurs
EP0694745A1 (fr) * 1994-07-25 1996-01-31 The BOC Group plc Séparation de l'air
EP0717249A2 (fr) * 1994-12-16 1996-06-19 The BOC Group plc Séparation d'air
JPH11132652A (ja) * 1997-10-27 1999-05-21 Nippon Sanso Kk 低純度酸素の製造方法及び装置
DE19936962A1 (de) * 1999-08-05 2000-09-28 Linde Tech Gase Gmbh Dreisäulenverfahren und -vorrichtung zur Tieftemperaturzerlegung von Luft

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0476989A1 (fr) * 1990-09-20 1992-03-25 Air Products And Chemicals, Inc. Générateur de l'azote à triple colonne de distillation avec plusieurs évaporateurs/condenseurs
EP0694745A1 (fr) * 1994-07-25 1996-01-31 The BOC Group plc Séparation de l'air
EP0717249A2 (fr) * 1994-12-16 1996-06-19 The BOC Group plc Séparation d'air
JPH11132652A (ja) * 1997-10-27 1999-05-21 Nippon Sanso Kk 低純度酸素の製造方法及び装置
DE19936962A1 (de) * 1999-08-05 2000-09-28 Linde Tech Gase Gmbh Dreisäulenverfahren und -vorrichtung zur Tieftemperaturzerlegung von Luft

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PATENT ABSTRACTS OF JAPAN vol. 1999, no. 10 31 August 1999 (1999-08-31) *

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1120616A2 (fr) * 2000-01-28 2001-08-01 The BOC Group plc Méthode de séparation de l'air
EP1120617A2 (fr) * 2000-01-28 2001-08-01 The BOC Group plc Séparation de l'air
EP1120617A3 (fr) * 2000-01-28 2002-08-28 The BOC Group plc Séparation de l'air
EP1120616A3 (fr) * 2000-01-28 2002-08-28 The BOC Group plc Méthode de séparation de l'air
US20130340476A1 (en) * 2011-03-18 2013-12-26 L'air Liquide Societe Anonyme Pour I'etude Et I'exploitation Des Procedes Georges Claude Apparatus and method for separating air by cryogenic distillation
CN104067079A (zh) * 2011-03-18 2014-09-24 乔治洛德方法研究和开发液化空气有限公司 用于通过低温蒸馏分离空气的设备和方法
CN104067079B (zh) * 2011-03-18 2016-11-30 乔治洛德方法研究和开发液化空气有限公司 用于通过低温蒸馏分离空气的设备和方法
AU2012230171B2 (en) * 2011-03-18 2017-03-30 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Device and method for separating air by cryogenic distillation
EP2634517A1 (fr) * 2012-02-29 2013-09-04 L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Procédé et appareil pour la séparation d'air par distillation cryogénique
US9360250B2 (en) 2012-02-29 2016-06-07 L'Air Liquide Société Anonyme Pour L'Étude Et L'Exploitation Des Procedes Georges Claude Process and apparatus for the separation of air by cryogenic distillation
US20220090855A1 (en) * 2020-09-18 2022-03-24 L'Air Liquide, Societe Anonyme pour l'Etude et l'Exploitation des Procedeseorges Claude Method and apparatus for producing high-purity nitrogen and low-purity oxygen

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Publication number Publication date
ES2246945T3 (es) 2006-03-01
DE10052180A1 (de) 2002-05-02
EP1199532B1 (fr) 2005-08-03
ATE301271T1 (de) 2005-08-15
DE50106958D1 (de) 2005-09-08

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