EP0681153B1 - Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft - Google Patents

Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft Download PDF

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Publication number
EP0681153B1
EP0681153B1 EP95106750A EP95106750A EP0681153B1 EP 0681153 B1 EP0681153 B1 EP 0681153B1 EP 95106750 A EP95106750 A EP 95106750A EP 95106750 A EP95106750 A EP 95106750A EP 0681153 B1 EP0681153 B1 EP 0681153B1
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EP
European Patent Office
Prior art keywords
low
liquid
pressure stage
pressure
buffer tank
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.)
Expired - Lifetime
Application number
EP95106750A
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German (de)
English (en)
French (fr)
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EP0681153A1 (de
Inventor
Wilhelm Dipl.-Ing. Rohde
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
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04854—Safety aspects of operation
    • F25J3/0486—Safety aspects of operation of vaporisers for oxygen enriched liquids, e.g. purging of liquids
    • 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
    • F25J3/04472—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
    • F25J3/04478—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 controlling purposes, e.g. start-up or back-up procedures
    • 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
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
    • F25J3/04884—Arrangement of reboiler-condensers
    • 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
    • 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
    • F25J2250/04—Down-flowing type boiler-condenser, i.e. with evaporation of a falling liquid film
    • 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
    • F25J2280/00—Control of the process or apparatus
    • F25J2280/10—Control for or during start-up and cooling down of the installation
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/62—Details of storing a fluid in a tank

Definitions

  • the invention relates to a method and a device for the low-temperature separation of air, wherein in the process air is compressed, cleaned, cooled and at least partially fed to the pressure stage of a two-stage rectification and at least one fraction from the pressure stage is further broken down in the low-pressure stage, the low-pressure stage being a Oxygen fraction and a nitrogenous fraction can be taken as products and the lower area of the low pressure stage is in heat-exchanging connection with the upper area of the pressure stage.
  • the basics of air separation by rectification can be found in relevant manuals (e.g. Hausen / Linde, low-temperature technology, 2nd edition 1985, chapter 4.5 or Winnacker / Küchler, Chemical Technology, volume 2, 3rd edition, chapter 4) and in Latimer, Distillation of Air , Chem. Eng. Progr., 63 , pages 35 to 59.
  • the two-stage rectification usually takes place in a double column, the low pressure stage of which is arranged above the pressure stage. (In principle, it is also possible to arrange the low-pressure and pressure stages of a double column separately.)
  • the return for the pressure stage is generated by the evaporation of liquid from the low-pressure stage, with steam rising at the same time in the low-pressure stage.
  • This indirect heat exchange is carried out in a condenser-evaporator, which is arranged in the low pressure column, usually in the sump.
  • This arrangement is fundamentally advantageous since there are no separate lines for connecting the evaporation passages of the condenser-evaporator to the low-pressure column.
  • the condenser-vaporizer contributes significantly to the total height of the double column and thus causes relatively high system costs.
  • the entire return liquid from the low-pressure stage runs into the sump and contaminates it with nitrogen. As a result, when the system is restarted, it takes a long time before pure oxygen product can be released again.
  • a device for air separation is known from JP-A-5306884, in which liquid is passed into a storage container while the system is being shut down.
  • the invention is based on the object of specifying a method and a device of the type mentioned at the outset which are economically more favorable, in particular due to reduced capital costs or greater flexibility in operation.
  • This object is achieved in that, in stationary operation, essentially all of the return liquid flowing down in the low pressure stage from the lower one
  • the area of the low-pressure stage is withdrawn and passed into a buffer tank, liquid is removed from the buffer tank and partially condensed in indirect heat exchange with condensing gas from the upper area of the pressure stage, and that at least some of the resulting steam is fed to the lower area of the low-pressure stage and the liquid remaining portion is at least partially returned to the buffer tank.
  • the term "stationary operation” means the usual operating state of an air separation plant after the start-up phase, in which the input and product flows over a longer period (at least 10 minutes in the case of a removable storage system up to many days or weeks in systems with constant product requirements) in remain essentially constant.
  • a buffer container for example a liquid tank.
  • a buffer container for example a liquid tank.
  • smaller parts of the return liquid can be guided in another way, for example as a liquid product or through a withdrawal through a safety drain.
  • that part of the reflux liquid which is required to generate steam rising in the column is fed into the buffer tank.
  • the buffer container is preferably designed as an insulated liquid tank.
  • liquid is taken from it, which is evaporated from the pressure column in indirect heat exchange with nitrogen-rich steam.
  • At least a part, preferably the largest part, of the gas formed is introduced into the low-pressure column and forms the vapor rising there in counterflow to the return liquid; another part can be withdrawn as a gaseous oxygen product if necessary. This is usually warmed up to air to be broken down to about ambient temperature.
  • the portion of the liquid withdrawn from the tank that has not evaporated during the indirect heat exchange is fed back into the buffer tank, for example together with the return liquid from the column.
  • the liquid can be pumped inexpensively by a pump.
  • This can be located downstream of the buffer tank, for example; alternatively or additionally, a pump can be arranged in the line from the low-pressure stage to the buffer tank, the tank itself either above the heat exchanger is arranged to evaporate the liquid from the tank or is under positive pressure.
  • the external evaporation of the return liquid in connection with the storage in a tank eliminates the need to maintain a sump liquid level in the low pressure column.
  • a very low liquid level is maintained (for example 10 to a maximum of 50 mm water column compared to a bottom liquid level of about 300 to 2000 mm water in previously known methods), or there is no liquid storage in the bottom of the low-pressure stage.
  • the integrated buffer tank also offers the possibility of obtaining an oxygen product of essentially constant purity by evaporation of the tank contents, even when the columns are not operating completely constantly (for example in the event of a fault or due to a change in the air throughput).
  • the process can be used very flexibly.
  • the integration of the buffer tank also simplifies the control of the process.
  • the control variable is the liquid level in the tank. This is easy to read and highly uncritical: it only has to be ensured that the tank is not completely empty or filled; in between, its content can basically fluctuate arbitrarily. (In practice, however, a medium liquid level is maintained in order to actually be able to use the buffer effect.) It is sufficient to read the liquid level in the tank from time to time and then to increase the external cooling supply and / or the internal cooling generation when the liquid level falls or rises increase or decrease. In principle, this can happen automatically. Because the adjustment of the cooling capacity in the usual If operation is only necessary at relatively large intervals (depending on the tank size, approximately every ten hours to five days), the control can also be carried out in manual mode. If, for example, cold is obtained in the process by relieving air or nitrogen from work in a turbine, the throughput through this turbine can be adjusted accordingly, for example by hand, in order to regulate the cooling capacity.
  • Air separators are often operated discontinuously due to changing energy costs during the day. If the system is restarted after such interruptions in operation (or even after an interruption in operation), it takes a long time (even with the apparatus still cold) (up to two hours) until the rectification has returned to its steady state and products with the provided purity.
  • the method of the invention makes significant progress if, at the beginning of an interruption in operation, the return liquid is led from the low-pressure stage into the lower region of the pressure stage.
  • the invention relates to a device for performing the method according to claim 1 according to claim 4.
  • Compressed and cleaned air is fed via line 1 into pressure stage 3, a double column 2. (Part of the air to be separated can also be introduced directly into the low-pressure stage 4, for example after relaxation during work.)
  • Top gas of the pressure stage is fed via line 5 to a condenser-evaporator 6 and is fully condensed there.
  • the liquid formed flows back via line 7 to the top of the pressure column 3. It acts partly as a return in the pressure column 3, and partly it is applied to the low pressure column 4 (8th).
  • the line 8 to the low-pressure column can also be connected directly to the condensate line 7 from the condenser-evaporator 6 instead of the connection to the pressure column 3.
  • bottom liquid 9 from the pressure column is throttled at an intermediate point into the low-pressure column 4, from the top of which a nitrogen-rich one Product 10 is withdrawn.
  • the reflux liquid of the low pressure column 4 is taken off at the lower end of the column via a line 11. In stationary operation it consists of oxygen with residual impurities of 100 ppm to 20%, preferably 0.3 to 10%.
  • the line 11 is relatively close to the bottom of the container, which forms the low pressure column 4, so that very little or practically no liquid is present in the column bottom.
  • the liquid oxygen flows on (12) to an oxygen tank 13 used as a buffer tank. If required, a part can be removed as a liquid product via a product line 14.
  • the tank 13 is kept under pressure by a pump 15, so that liquid from the tank is pressed via line 16 to the condenser-evaporator 6, which works as a falling film evaporator. (In the case of an unpressurized storage, the pump would have to be arranged in line 16.)
  • a two-phase mixture emerges via line 17 from the evaporator passages of the condenser-evaporator 6, the vaporous portion of which partly flows back into the low-pressure column 4 (18), while another part is drawn off as a gaseous oxygen product 19.
  • the remaining liquid portion is returned to the buffer tank 13 via line 12.
  • Another liquid line 20 is connected to the lower region of the low-pressure stage 4, preferably below the outlet of the line 11. It is closed during normal operation of the system. (At most, for safety's sake, small amounts of liquid are occasionally drawn off and discarded via a safety drain, not shown.)
  • valve 21 in line 11 is closed after the air compressor has returned, so that the connection to tank 13 is interrupted.
  • the shut-off valve 22 is opened so that the return liquid arriving in the sump of the low pressure column flows into the pressure column and is stored in the sump thereof.
  • valve 21 in line 11 can be omitted.
  • the return liquid (11) flowing out of the low-pressure column also has the usual composition immediately after starting up and can be piped into the tank 13 flow.
  • connections 18 and 11 between the low pressure stage 4 on one side and the line 17/12 between the evaporation passages of the condenser-evaporator 6 and the buffer tank 13 on the other side can also be realized by a single tube with a large cross section, in the liquid and vapor flow against each other.

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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)
EP95106750A 1994-05-04 1995-05-04 Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft Expired - Lifetime EP0681153B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE4415747 1994-05-04
DE4415747A DE4415747C2 (de) 1994-05-04 1994-05-04 Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft

Publications (2)

Publication Number Publication Date
EP0681153A1 EP0681153A1 (de) 1995-11-08
EP0681153B1 true EP0681153B1 (de) 1997-09-10

Family

ID=6517292

Family Applications (1)

Application Number Title Priority Date Filing Date
EP95106750A Expired - Lifetime EP0681153B1 (de) 1994-05-04 1995-05-04 Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft

Country Status (9)

Country Link
EP (1) EP0681153B1 (enrdf_load_stackoverflow)
JP (1) JPH0842962A (enrdf_load_stackoverflow)
KR (1) KR950033380A (enrdf_load_stackoverflow)
CN (1) CN1124345A (enrdf_load_stackoverflow)
DE (2) DE4415747C2 (enrdf_load_stackoverflow)
ES (1) ES2106594T3 (enrdf_load_stackoverflow)
GR (1) GR3025534T3 (enrdf_load_stackoverflow)
PL (1) PL308454A1 (enrdf_load_stackoverflow)
TW (1) TW288984B (enrdf_load_stackoverflow)

Families Citing this family (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19732887A1 (de) * 1997-07-30 1999-02-04 Linde Ag Verfahren zur Luftzerlegung
US6272884B1 (en) 1998-04-08 2001-08-14 Praxair Technology, Inc. Rapid restart system for cryogenic air separation plant
FR2797942B1 (fr) * 1999-08-24 2001-11-09 Air Liquide Vaporiseur-condenseur et installation de distillation d'air correspondante
FR2802825B1 (fr) * 1999-12-23 2002-05-03 Air Liquide Appareil de separation par distillation et procede de nettoyage d'un vaporisateur-condenseur de l'appareil
FR2855598B1 (fr) * 2003-05-28 2005-10-07 Air Liquide Procede et installation de fourniture de secours d'un gaz sous pression par vaporisation de liquide cryogenique
CN100436989C (zh) * 2004-01-29 2008-11-26 宝山钢铁股份有限公司 一种用全低压空分装置制取高纯氧的方法
EP2503270A1 (de) * 2011-03-22 2012-09-26 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Erzeugung eines Sauerstoffprodukts durch Tieftemperaturzerlegung von Luft
CN103537107B (zh) * 2012-07-11 2015-04-22 蓝星(北京)化工机械有限公司 一种蒸发系统及其应用
DE102016013091A1 (de) * 2016-11-04 2018-05-09 Linde Aktiengesellschaft Verfahren und Anlage zum Reinigen eines Gases
CN108072234B (zh) * 2016-11-15 2020-03-06 北大方正集团有限公司 空气分离装置的控制方法
KR102354278B1 (ko) 2017-10-12 2022-01-21 주식회사 엘지에너지솔루션 전지 충방전기
CN112629160A (zh) * 2020-12-21 2021-04-09 华能（天津）煤气化发电有限公司 一种空分自然复热检修方法

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
LU35441A1 (enrdf_load_stackoverflow) * 1956-09-25
DE1501760A1 (de) * 1966-12-27 1969-11-27 Rudisleben Chemieanlagenbau Verfahren zur Luftzerlegung
DE3732363A1 (de) * 1987-09-25 1989-04-06 Linde Ag Verfahren und vorrichtung zum wiederanfahren einer gaszerlegungsanlage
DE3913880A1 (de) * 1989-04-27 1990-10-31 Linde Ag Verfahren und vorrichtung zur tieftemperaturzerlegung von luft
JPH0420783A (ja) * 1990-05-11 1992-01-24 Hitachi Ltd 空気分離装置
JPH05306884A (ja) * 1992-03-18 1993-11-19 Hitachi Ltd 空気分離装置及びその運転方法

Also Published As

Publication number Publication date
PL308454A1 (en) 1995-11-13
EP0681153A1 (de) 1995-11-08
DE4415747C2 (de) 1996-04-25
KR950033380A (ko) 1995-12-22
GR3025534T3 (en) 1998-02-27
TW288984B (enrdf_load_stackoverflow) 1996-10-21
JPH0842962A (ja) 1996-02-16
ES2106594T3 (es) 1997-11-01
DE4415747A1 (de) 1995-11-16
DE59500625D1 (de) 1997-10-16
CN1124345A (zh) 1996-06-12

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