EP0399197A1 - Procédé et dispositif pour la séparation d'air à basse température - Google Patents

Procédé et dispositif pour la séparation d'air à basse température Download PDF

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Publication number
EP0399197A1
EP0399197A1 EP90106968A EP90106968A EP0399197A1 EP 0399197 A1 EP0399197 A1 EP 0399197A1 EP 90106968 A EP90106968 A EP 90106968A EP 90106968 A EP90106968 A EP 90106968A EP 0399197 A1 EP0399197 A1 EP 0399197A1
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EP
European Patent Office
Prior art keywords
oxygen
liquid
pressure stage
nitrogen
air
Prior art date
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Granted
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EP90106968A
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German (de)
English (en)
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EP0399197B1 (fr
Inventor
Wilhelm Rohde
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Linde GmbH
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Linde GmbH
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Priority to AT90106968T priority Critical patent/ATE77687T1/de
Publication of EP0399197A1 publication Critical patent/EP0399197A1/fr
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Publication of EP0399197B1 publication Critical patent/EP0399197B1/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
    • F25J3/04472—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 the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages
    • F25J3/04496—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 the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist
    • F25J3/04503—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 the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist by exchanging "cold" between at least two different cryogenic liquids, e.g. independently from the main heat exchange line of the air fractionation and/or by using external alternating storage systems
    • F25J3/04509—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 the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist by exchanging "cold" between at least two different cryogenic liquids, e.g. independently from the main heat exchange line of the air fractionation and/or by using external alternating storage systems within the cold part of the air fractionation, i.e. exchanging "cold" within the fractionation and/or main heat exchange line
    • F25J3/04515—Simultaneously changing air feed and products output
    • 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
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
    • 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
    • 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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/912—External refrigeration system
    • Y10S62/913—Liquified gas

Definitions

  • the invention relates to a method and apparatus for the low-temperature separation of air with variable oxygen production, in which air is compressed, pre-cleaned, cooled and pre-separated in the pressure stage of a two-stage rectification into an oxygen-rich liquid fraction and a nitrogen fraction, and the oxygen-enriched liquid fraction into the low-pressure stage of the rectification , which is in heat-exchanging connection with the pressure stage, is introduced and further broken down into an oxygen and a nitrogen fraction and in which oxygen is removed from an oxygen tank when there is an increased demand for oxygen and liquid oxygen is fed from the low-pressure stage to the oxygen tank when the demand for oxygen is reduced.
  • the oxygen demand is subject to greater fluctuations over a period of minutes, hours or days. Because of the inertia of a low-temperature air separator, it would be uneconomical to adapt such a system by briefly changing the amount of air supplied and at the same time changing the sales in the rectification columns. Besides, one would have such a procedure has an unfavorable impact on the effectiveness of the separation process.
  • liquid oxygen is supplied to the bottom of the low-pressure stage from the oxygen tank and is evaporated there in the heat exchange with pressurized nitrogen at the top of the pressure stage. Nitrogen is liquefied during the heat exchange, removed from the pressure stage and stored in the nitrogen tank. At times when excess gaseous oxygen is produced, the stored liquid nitrogen is then available as a return in the low pressure column; Excess oxygen is removed from the bottom of the low-pressure column and stored in the oxygen tank.
  • the amount of additional oxygen that can be removed is set by the amount of pressurized nitrogen which is drawn off in gaseous form under normal load.
  • This part of the nitrogen generated in the pressure stage is generally not fed into the low-pressure stage, but is removed from the process, either directly as a gaseous product (under normal load and with reduced oxygen demand) or through intermediate storage in the nitrogen tank (with increased oxygen demand). Regardless of the current load, this amount of nitrogen is not available as a return for the low pressure stage.
  • the object of the invention is now to develop a method which enables variable oxygen production with cheaper product yields, in particular with an attached argon rectification.
  • This object is achieved in that when the oxygen requirement is reduced, at least part of the oxygen-enriched liquid fraction is introduced into a liquid air tank, stored there and removed again when the oxygen requirement is increased.
  • the intermediate storage of sump liquid from the pressure stage according to the invention permits an operation of the system in which, on the one hand, the reflux conditions in the pressure and low pressure stage and the conversion in the low pressure stage can be kept constant, on the other hand, all nitrogen generated in the pressure stage can be withdrawn in liquid and the Low pressure stage are supplied. This means that the optimum amount of reflux is available for low-pressure rectification, and the maximum achievable argon concentration is achieved.
  • the amount of air supplied is increased when there is an increased demand for oxygen.
  • This causes the desired increase in column turnover and thus the evaporation of the liquid additionally introduced from the oxygen tank into the sump of the low-pressure column.
  • the air supply is throttled and liquid is removed from the liquid air tank and the nitrogen tank in order to keep the sales in the low pressure column constant. Due to the lower conversion at the top of the pressure stage, a smaller part of the oxygen accumulating in the low pressure column is evaporated. The corresponding amount is drawn off in liquid form and stored in the oxygen tank.
  • the process according to the invention is advantageously controlled such that both the reflux ratio and the conversion in the low-pressure stage are kept essentially constant in the event of fluctuations in the amount of oxygen produced.
  • the return ratio also remains constant in the pressure stage.
  • an argon-containing oxygen fraction can be taken from the middle area of the low-pressure stage and in one Raw argon rectification can be broken down into raw argon and into a residual fraction.
  • the invention further relates to a device for carrying out the method described above with a two-stage rectification column which consists of a pressure column and a low pressure column with a common condenser / evaporator, a nitrogen tank which is connected to the pressure and low pressure column by means of nitrogen lines, and with an oxygen tank , which is connected to the low pressure column by means of oxygen lines.
  • the device according to the invention is characterized by a liquid air tank, a first liquid air line between the sump of the pressure column and the liquid air tank and a second liquid air line which connects the liquid air tank and the low pressure column.
  • the device has measuring devices for the liquid level in the pressure column and low-pressure column sump, a flow measuring device in the nitrogen line between the pressure column and nitrogen tank, throttle devices for controlling the flow in liquid air, oxygen and nitrogen line and control devices, which with the Measuring devices are connected and control the throttle devices.
  • the figure shows this variant of the method according to the invention in a schematic sketch.
  • Air is drawn in by an air compressor 1, then pre-cooled and cleaned (2) and passed via line 3 through a main heat exchanger 4, in which it is cooled in countercurrent to product gases. 70 to 95%, preferably 88% of the air is led to the cold end of the main heat exchanger 4 and fed via line 5 at a temperature of 95 to 105 K and under a pressure of 4 to 8 bar into the pressure stage 10 of a two-stage rectification 9.
  • the remaining portion of the air is led out from the main heat exchanger 4 via line 6 at a temperature of 130 to 190 K in a pressure relief turbine 7 to a pressure of 2.0 to 1.1 bar and fed to the low pressure stage 11 of the rectification 9.
  • the air introduced via line 5 is broken down into liquid nitrogen and into an oxygen-enriched bottom liquid. Both fractions are withdrawn in liquid form, the nitrogen via line 14 and the bottom liquid via line 12.
  • the nitrogen is expanded using valve 134 and fed into a nitrogen tank which stores liquid nitrogen under a pressure of 1 to 6 bar.
  • the liquid is at least partially passed on via line 37, subcooled in a heat exchanger 23 and applied via line 15 to the top of the low-pressure stage 11.
  • the bottom liquid in line 12 is also depressurized (valve 132) and introduced into a liquid air tank 40 in which pressure conditions similar to those in the nitrogen tank 35 prevail. Liquid is removed from the tank 40 via line 42, cooled in the heat exchanger 23 and introduced into the low-pressure stage 11 via line 13b. There the oxygen-enriched liquid from pressure stage 10 is further broken down.
  • low-pressure stage 11 gaseous oxygen is taken off above the sump via line 16 and warmed to almost ambient temperature in main heat exchanger 4 (line 19).
  • nitrogen is drawn off at the top via line 18, heated in heat exchanger 23 against the liquid fractions 37 and 42 from the pressure stage 10 or from the tanks 35, 40, passed through line 19 through the main heat exchanger 4 and continues there except for im essential ambient temperature warmed.
  • liquid oxygen can be withdrawn from the bottom of the low-pressure stage 11 by means of the pump 31 and introduced into an oxygen tank 32.
  • liquid can be fed from the oxygen tank 32 into the low-pressure column 11 via line 34.
  • an argon-rich oxygen fraction is drawn off from the low pressure stage 11 via line 20, fed to a crude argon rectification 21 and there in crude argon, which is withdrawn via line 22 at the top of the crude argon rectification 21, and into one liquid residual fraction that over Line 20 flows back into the low pressure stage 11, disassembled.
  • the head of the crude argon rectification 21 is cooled by liquid from the bottom of the pressure column 10 or from the liquid air tank 40.
  • a secondary line 24 branches off from line 42 and leads into the top condenser 45 of the crude argon rectification 21.
  • the oxygen-enriched air evaporated there is drawn off via line 46 and via line 13a somewhat below the feed point of the liquid fraction (line 13b) into the low-pressure stage 11 introduced.
  • an increased flow is set on the air compressor 1.
  • the flow rate is monitored by the measuring device 125, which is connected to the air compressor 1 (line shown in broken lines in the figure).
  • the flow through line 6 via the expansion turbine 7 to the low pressure stage 11 is kept essentially constant by controlling the flow through the expansion turbine 7 according to the indications indicated by the measuring device 127 (see dashed line in the drawing).
  • the amount of air additionally sucked in by the air compressor 1 is thus practically completely introduced into the pressure stage 10 and increases the column turnover there. For example, to remove a 25% increase in the amount of gaseous product oxygen, the total amount of air must be increased by approximately 6.8%.
  • the increased conversion in the pressure stage 10 now causes an increased heat input via the condenser / evaporator 48 into the bottom of the low pressure stage 11.
  • the additionally evaporated oxygen can be drawn off via line 16 as an increased amount of product. This process is controlled by the flow meter 126 and valve 136 in line 17.
  • a quantity of liquid oxygen corresponding to the additionally removed oxygen gas is removed from the oxygen tank 32 (line 34).
  • the replenishment of liquid oxygen is controlled by means of the liquid level measurement 123 at the bottom of the low pressure stage 11 and the valve 133.
  • the pressure in the liquid tanks 32, 35, 40 is monitored by means of measuring devices 101, 102, 103. If necessary, gas is released from tanks 32, 35, 40 by opening valves 111, 112 and 113, from liquid air tank 40 via lines 41 and 13a to the low pressure stage, from oxygen tank 32 via line 33 into product line 17 and from the nitrogen tank 35 via line 36 into the product line 19.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Solid-Sorbent Or Filter-Aiding Compositions (AREA)
  • Processing Of Solid Wastes (AREA)
  • Treatment Of Sludge (AREA)
EP90106968A 1989-04-27 1990-04-11 Procédé et dispositif pour la séparation d'air à basse température Expired - Lifetime EP0399197B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT90106968T ATE77687T1 (de) 1989-04-27 1990-04-11 Verfahren und vorrichtung zur tieftemperaturzerlegung von luft.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3913880A DE3913880A1 (de) 1989-04-27 1989-04-27 Verfahren und vorrichtung zur tieftemperaturzerlegung von luft
DE3913880 1989-04-27

Publications (2)

Publication Number Publication Date
EP0399197A1 true EP0399197A1 (fr) 1990-11-28
EP0399197B1 EP0399197B1 (fr) 1992-06-24

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Application Number Title Priority Date Filing Date
EP90106968A Expired - Lifetime EP0399197B1 (fr) 1989-04-27 1990-04-11 Procédé et dispositif pour la séparation d'air à basse température

Country Status (13)

Country Link
US (1) US5084081A (fr)
EP (1) EP0399197B1 (fr)
JP (1) JP3048373B2 (fr)
AT (1) ATE77687T1 (fr)
AU (1) AU627869B2 (fr)
CA (1) CA2015458C (fr)
CZ (1) CZ277911B6 (fr)
DE (2) DE3913880A1 (fr)
ES (1) ES2033556T3 (fr)
HU (1) HU207154B (fr)
RU (1) RU1838732C (fr)
UA (1) UA19155A (fr)
ZA (1) ZA903182B (fr)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0489617A1 (fr) * 1990-12-06 1992-06-10 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et installation de distillation d'air en régime variable de production d'oxygène gazeux
EP0519688A1 (fr) * 1991-06-20 1992-12-23 Air Products And Chemicals, Inc. Procédé et dispositif de contrôle d'une unité de séparation d'air par voie cryogénique au cours des changements rapides de la production
EP0756144A2 (fr) * 1995-07-26 1997-01-29 Teisan Kabushiki Kaisha Générateur de gaz pour la production d'azote de haute pureté
FR2929697A1 (fr) * 2008-04-07 2009-10-09 Air Liquide Procede de production d'azote gazeux variable et d'oxygene gazeux variable par distillation d'air

Families Citing this family (52)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE4040389C2 (de) * 1990-12-17 1994-03-03 Air Prod Gmbh Verfahren zur Vermeidung oder Verringerung von störfallbedingten Zeitverzögerungen bei der Lösungsmittelrückgewinnung aus Fertigungsprozessen
US5133790A (en) * 1991-06-24 1992-07-28 Union Carbide Industrial Gases Technology Corporation Cryogenic rectification method for producing refined argon
FR2681415B1 (fr) * 1991-09-18 1999-01-29 Air Liquide Procede et installation de production d'oxygene gazeux sous haute pression par distillation d'air.
US5257504A (en) * 1992-02-18 1993-11-02 Air Products And Chemicals, Inc. Multiple reboiler, double column, elevated pressure air separation cycles and their integration with gas turbines
CN1071444C (zh) * 1992-02-21 2001-09-19 普拉塞尔技术有限公司 生产气体氧的低温空气分离系统
FR2694383B1 (fr) * 1992-07-29 1994-09-16 Air Liquide Production et installation de production d'azote gazeux à plusieurs puretés différentes.
FR2697620B1 (fr) * 1992-10-30 1994-12-23 Air Liquide Procédé et installation de production d'azote gazeux à débit variable.
FR2704632B1 (fr) * 1993-04-29 1995-06-23 Air Liquide Procede et installation pour la separation de l'air.
FR2706195B1 (fr) * 1993-06-07 1995-07-28 Air Liquide Procédé et unité de fourniture d'un gaz sous pression à une installation consommatrice d'un constituant de l'air.
FR2706595B1 (fr) * 1993-06-18 1995-08-18 Air Liquide Procédé et installation de production d'oxygène et/ou d'azote sous pression à débit variable.
US5471843A (en) * 1993-06-18 1995-12-05 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and installation for the production of oxygen and/or nitrogen under pressure at variable flow rate
US6082136A (en) * 1993-11-12 2000-07-04 Daido Hoxan Inc. Oxygen gas manufacturing equipment
FR2716816B1 (fr) * 1994-03-02 1996-05-03 Air Liquide Procédé de redémarrage d'une colonne auxiliaire de séparation argon/oxygène par distillation, et installation correspondante.
DE4415747C2 (de) * 1994-05-04 1996-04-25 Linde Ag Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
US5431023A (en) * 1994-05-13 1995-07-11 Praxair Technology, Inc. Process for the recovery of oxygen from a cryogenic air separation system
US5406800A (en) * 1994-05-27 1995-04-18 Praxair Technology, Inc. Cryogenic rectification system capacity control method
FR2723184B1 (fr) * 1994-07-29 1996-09-06 Grenier Maurice Procede et installation de production d'oxygene gazeux sous pression a debit variable
US5522224A (en) * 1994-08-15 1996-06-04 Praxair Technology, Inc. Model predictive control method for an air-separation system
DE19526785C1 (de) * 1995-07-21 1997-02-20 Linde Ag Verfahren und Vorrichtung zur variablen Erzeugung eines gasförmigen Druckprodukts
GB9521996D0 (en) * 1995-10-27 1996-01-03 Boc Group Plc Air separation
US5666823A (en) 1996-01-31 1997-09-16 Air Products And Chemicals, Inc. High pressure combustion turbine and air separation system integration
US5682763A (en) * 1996-10-25 1997-11-04 Air Products And Chemicals, Inc. Ultra high purity oxygen distillation unit integrated with ultra high purity nitrogen purifier
FR2757282B1 (fr) * 1996-12-12 2006-06-23 Air Liquide Procede et installation de fourniture d'un debit variable d'un gaz de l'air
US5778700A (en) * 1997-04-30 1998-07-14 The Boc Group, Inc. Method of producing gaseous oxygen at variable rate
DE19748966B4 (de) * 1997-11-06 2008-09-04 Air Liquide Deutschland Gmbh Vorrichtung und Verfahren zur Herstellung und Lagerung von flüssiger Luft
US5996373A (en) * 1998-02-04 1999-12-07 L'air Liquide, Societe Ananyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Cryogenic air separation process and apparatus
DE19815885A1 (de) * 1998-04-08 1999-10-14 Linde Ag Verfahren und Vorrichtung zur Erzeugung von gasförmigem Druckprodukt bei der Tieftemperaturzerlegung von Luft
US6006546A (en) * 1998-04-29 1999-12-28 Air Products And Chemicals, Inc. Nitrogen purity control in the air separation unit of an IGCC power generation system
US5983668A (en) * 1998-04-29 1999-11-16 Air Products And Chemicals, Inc. Air separation unit feed flow control in an IGCC power generation system
US6082135A (en) * 1999-01-29 2000-07-04 The Boc Group, Inc. Air separation method and apparatus to produce an oxygen product
DE19912155C5 (de) * 1999-03-18 2005-09-01 Air Liquide Deutschland Gmbh Kryogener vakuumisolierter Sauerstoff-Generator
US6182471B1 (en) * 1999-06-28 2001-02-06 Praxair Technology, Inc. Cryogenic rectification system for producing oxygen product at a non-constant rate
US6233970B1 (en) 1999-11-09 2001-05-22 Air Products And Chemicals, Inc. Process for delivery of oxygen at a variable rate
US6357259B1 (en) * 2000-09-29 2002-03-19 The Boc Group, Inc. Air separation method to produce gaseous product
KR20020024169A (ko) * 2002-01-23 2002-03-29 황재원 캡모자 분실방지 밴드
US20030213688A1 (en) * 2002-03-26 2003-11-20 Wang Baechen Benson Process control of a distillation column
FR2842124B1 (fr) * 2002-07-09 2005-03-25 Air Liquide Procede de conduite d'une installation de production de gaz alimentee en electricite et cette installation de production
DE10249383A1 (de) * 2002-10-23 2004-05-06 Linde Ag Verfahren und Vorrichtung zur variablen Erzeugung von Sauerstoff durch Tieftemperatur-Zerlegung von Luft
US7228715B2 (en) * 2003-12-23 2007-06-12 L'air Liquide, Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Procedes Georges Claude Cryogenic air separation process and apparatus
US7272954B2 (en) * 2004-07-14 2007-09-25 L'air Liquide, Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Proceded Georges Claude Low temperature air separation process for producing pressurized gaseous product
US7555918B1 (en) * 2006-05-24 2009-07-07 Cosmodyne, LLC Liquid production modulation in self-refrigerated cryogenic nitrogen gas generators
US20080115531A1 (en) * 2006-11-16 2008-05-22 Bao Ha Cryogenic Air Separation Process and Apparatus
EP2591300A2 (fr) * 2010-07-05 2013-05-15 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Appareil et procede de separation d'air par distillation cryogenique
SG186906A1 (en) * 2010-07-28 2013-02-28 Air Prod & Chem Integrated liquid storage
CN102072612B (zh) * 2010-10-19 2013-05-29 上海加力气体有限公司 N型模式节能制气方法
DE102012006746A1 (de) 2012-04-03 2013-10-10 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Erzeugung elektrischer Energie
ES2746755T3 (es) * 2013-03-28 2020-03-06 Linde Ag Método y dispositivo para producir oxígeno gaseoso comprimido con consumo variable de energía
CN104501529B (zh) * 2014-12-23 2017-04-12 首钢水城钢铁（集团）有限责任公司 一种粗氩泵倒换装置及其倒换方法
CA3063409A1 (fr) 2017-05-16 2018-11-22 Terrence J. Ebert Appareil et procede de liquefaction de gaz
US10914517B2 (en) * 2018-11-16 2021-02-09 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method for utilizing waste air to improve the capacity of an existing air separation unit
JP7460973B2 (ja) * 2020-03-05 2024-04-03 日本エア・リキード合同会社 空気分離装置
CN114593358A (zh) * 2022-01-21 2022-06-07 杭州制氧机集团股份有限公司 一种与空分装置耦合进行储能生产的方法及其装置

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR1166300A (fr) * 1957-02-13 1958-11-04 Air Liquide Procédé de stabilisation du fonctionnement d'une installation de rectification d'un mélange de gaz à basse température
FR1267502A (fr) * 1960-09-12 1961-07-21 Lindes Eismaschinen Ag Zweigni Procédé et installation pour la décomposition de gaz en cas de grandes variations de la charge

Family Cites Families (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3174293A (en) * 1960-11-14 1965-03-23 Linde Eismasch Ag System for providing gas separation products at varying rates
US3411308A (en) * 1967-01-03 1968-11-19 Phillips Petroleum Co Method and apparatus for controlling by a material balance the bottoms flow rate in a fractional distillation system
US3605422A (en) * 1968-02-28 1971-09-20 Air Prod & Chem Low temperature frocess for the separation of gaseous mixtures
IN153160B (fr) * 1979-07-12 1984-06-09 Petrocarbon Dev Ltd
US4345925A (en) * 1980-11-26 1982-08-24 Union Carbide Corporation Process for the production of high pressure oxygen gas
GB2125949B (en) * 1982-08-24 1985-09-11 Air Prod & Chem Plant for producing gaseous oxygen
US4604116A (en) * 1982-09-13 1986-08-05 Erickson Donald C High pressure oxygen pumped LOX rectifier
GB2129115B (en) * 1982-10-27 1986-03-12 Air Prod & Chem Producing gaseous nitrogen
JPS61190277A (ja) * 1985-02-16 1986-08-23 大同酸素株式会社 高純度窒素および酸素ガス製造装置
FR2584803B1 (fr) * 1985-07-15 1991-10-18 Air Liquide Procede et installation de distillation d'air
EP0235295B1 (fr) * 1985-08-23 1989-06-14 Daidousanso Co., Ltd. Unite de production d'oxygene a l'etat gazeux
US4702757A (en) * 1986-08-20 1987-10-27 Air Products And Chemicals, Inc. Dual air pressure cycle to produce low purity oxygen
GB8620754D0 (en) * 1986-08-28 1986-10-08 Boc Group Plc Air separation
GB2198514B (en) * 1986-11-24 1990-09-19 Boc Group Plc Air separation
DE3722746A1 (de) * 1987-07-09 1989-01-19 Linde Ag Verfahren und vorrichtung zur luftzerlegung durch rektifikation
US4780118A (en) * 1987-07-28 1988-10-25 Union Carbide Corporation Process and apparatus to produce ultra high purity oxygen from a liquid feed
US4869741A (en) * 1988-05-13 1989-09-26 Air Products And Chemicals, Inc. Ultra pure liquid oxygen cycle
EP0383994A3 (fr) * 1989-02-23 1990-11-07 Linde Aktiengesellschaft Procédé et dispositif de rectification d'air

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR1166300A (fr) * 1957-02-13 1958-11-04 Air Liquide Procédé de stabilisation du fonctionnement d'une installation de rectification d'un mélange de gaz à basse température
FR1267502A (fr) * 1960-09-12 1961-07-21 Lindes Eismaschinen Ag Zweigni Procédé et installation pour la décomposition de gaz en cas de grandes variations de la charge

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
LINDE, Nr. 54, 1984, Seiten 18-20; W. ROHDE: "Luftzerlegungsanlage mit Wechselspeicherung für variable Sauerstofflieferung" *

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0489617A1 (fr) * 1990-12-06 1992-06-10 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et installation de distillation d'air en régime variable de production d'oxygène gazeux
FR2670278A1 (fr) * 1990-12-06 1992-06-12 Air Liquide Procede et installation de distillation d'air en regime variable de production d'oxygene gazeux.
US5209070A (en) * 1990-12-06 1993-05-11 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and arrangement for the distillation of air in the production of gaseous oxygen under variable operating conditions
EP0519688A1 (fr) * 1991-06-20 1992-12-23 Air Products And Chemicals, Inc. Procédé et dispositif de contrôle d'une unité de séparation d'air par voie cryogénique au cours des changements rapides de la production
EP0756144A2 (fr) * 1995-07-26 1997-01-29 Teisan Kabushiki Kaisha Générateur de gaz pour la production d'azote de haute pureté
EP0756144A3 (fr) * 1995-07-26 1998-02-04 Teisan Kabushiki Kaisha Générateur de gaz pour la production d'azote de haute pureté
FR2929697A1 (fr) * 2008-04-07 2009-10-09 Air Liquide Procede de production d'azote gazeux variable et d'oxygene gazeux variable par distillation d'air

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ZA903182B (en) 1991-04-24
HU207154B (en) 1993-03-01
UA19155A (uk) 1997-12-25
HU902576D0 (en) 1990-08-28
US5084081A (en) 1992-01-28
ES2033556T3 (es) 1993-03-16
JP3048373B2 (ja) 2000-06-05
CS9002111A2 (en) 1991-08-13
CA2015458A1 (fr) 1990-10-27
CZ277911B6 (en) 1993-06-16
RU1838732C (ru) 1993-08-30
ATE77687T1 (de) 1992-07-15
DE59000177D1 (de) 1992-07-30
DE3913880A1 (de) 1990-10-31
CA2015458C (fr) 1998-09-29
AU5398390A (en) 1990-11-01
EP0399197B1 (fr) 1992-06-24
AU627869B2 (en) 1992-09-03
JPH0363490A (ja) 1991-03-19
HUT54310A (en) 1991-02-28

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