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EP2503270A1 - Procédé et dispositif destinés à la production de produits à base d'oxygène par la décomposition à basse température de l'air - Google Patents

Procédé et dispositif destinés à la production de produits à base d'oxygène par la décomposition à basse température de l'air Download PDF

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Publication number
EP2503270A1
EP2503270A1 EP12001386A EP12001386A EP2503270A1 EP 2503270 A1 EP2503270 A1 EP 2503270A1 EP 12001386 A EP12001386 A EP 12001386A EP 12001386 A EP12001386 A EP 12001386A EP 2503270 A1 EP2503270 A1 EP 2503270A1
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EP
European Patent Office
Prior art keywords
liquid
pressure column
main
buffer
oxygen
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.)
Withdrawn
Application number
EP12001386A
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German (de)
English (en)
Inventor
Alexander Dr. Alekseev
Georg Demski
Gerhard Pompl
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Original Assignee
Linde GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Priority to EP12001386A priority Critical patent/EP2503270A1/fr
Publication of EP2503270A1 publication Critical patent/EP2503270A1/fr
Withdrawn legal-status Critical Current

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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
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04896—Details of columns, e.g. internals, inlet/outlet devices
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/042—Division of the main heat exchange line in consecutive sections having different functions having an intermediate feed connection
    • 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
    • F25J3/04472—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
    • F25J3/0449—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 for rapid load change of the air fractionation unit
    • 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
    • F25J3/04896—Details of columns, e.g. internals, inlet/outlet devices
    • F25J3/04927—Liquid or gas distribution devices
    • 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
    • F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
    • 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
    • F25J2250/10—Boiler-condenser with superposed stages

Definitions

  • the invention relates to a method for producing an oxygen product by cryogenic separation of air according to the preamble of patent claim 1.
  • the distillation column system of the invention may be designed as a two-column system (for example as a classic Linde double column system) or as a three-column or multi-column system. It may in addition to the columns for nitrogen-oxygen separation, further devices for obtaining high purity products and / or other air components, in particular of noble gases, for example, an argon production and / or a krypton-xenon recovery.
  • the low pressure column has a lower operating pressure than the high pressure column.
  • the low-pressure column has a bottom evaporator, which is referred to as the main condenser.
  • This is designed as a condenser-evaporator, that is, in indirect heat exchange with the evaporating bottom liquid of the low-pressure column, a gaseous heating fluid is liquefied, for example top nitrogen of the high-pressure column.
  • the main condenser is often placed directly inside the low-pressure column (internal main condenser); Alternatively, it is housed in a separate container outside the low-pressure column and connected by piping to the low pressure column (external main condenser).
  • Each "condenser-evaporator” has a liquefaction space and an evaporation space, which consist of liquefaction passages or evaporation passages.
  • the condensation of a first fluid flow is performed, in the evaporation space the evaporation a second fluid stream.
  • the two fluid streams are in indirect heat exchange.
  • Evaporation and liquefaction space are formed by groups of passages that are in heat exchange relationship with each other.
  • the main capacitor may be formed as a falling film evaporator or bath evaporator.
  • the present invention relates to air separation processes in which the main condenser is designed as a bath evaporator.
  • a bath evaporator sometimes also called “circulation evaporator” or “thermosiphon evaporator”
  • the heat exchanger block is in a liquid bath of the fluid to be evaporated. This flows by means of the thermosiphon effect from bottom to top through the evaporation passages and exits the top again as a two-phase mixture. The remaining liquid flows outside the heat exchanger block back into the liquid bath.
  • the evaporation space may comprise both the evaporation passages and the outside space around the heat exchanger block.
  • additional measures are necessary to overturn the liquid through the evaporation passages.
  • Two or more juxtaposed bath evaporator can be used as the main capacitor, which are then connected in parallel evaporation and liquefaction side.
  • Each of these bath evaporator or the only bath evaporator, which forms the main capacitor can be designed as one-storey or multi-storey.
  • a "multi-storey bath evaporator" has two or more floors arranged one above the other, each realized by a heat exchanger section. In this case, each individual floor can be realized by a separate heat exchanger block, or at least two or even all floors are formed by sections of a common heat exchanger block. The floors can be connected in series or parallel on both the evaporation and the liquefaction side.
  • a specific embodiment of a multi-storey bath evaporator is a "cascade evaporator".
  • the floors on the evaporation side are connected in series, ie non-evaporated liquid from an upper floor continues to flow to the floor below.
  • cascade evaporator are preferably also connected in series, for example by through all floors continuous liquefaction passages of a common heat exchanger block.
  • the floors can be connected in parallel on the liquefaction side.
  • the "main heat exchanger” may be formed of one or more parallel and / or serially connected heat exchanger sections, for example one or more plate heat exchanger blocks.
  • the invention has for its object to provide such a method and a corresponding device that allow a particularly stable operation of the system, especially during rapid load changes.
  • a load change is an operating case in which the plant is in a non-stationary transition phase from a first production amount of oxygen product to a second production amount. With a "load increase” the second production quantity is higher than the first, with a “load reduction” lower.
  • a liquid buffer is arranged above the main capacitor. This can be filled during stationary operation of the process with a suitable liquid, for example with a part of the return liquid, which flows from the lowest mass transfer section of the low-pressure column. For example, the liquid buffer is slowly filled during steady state operation so that the buffered liquid is available for non-steady state load increase operation.
  • a load reduction liquid from the bottom of the main condenser is introduced into the liquid buffer, thereby increasing the storage capacity of the liquid buffer, that is, a total of more liquid is introduced into the liquid buffer and it is withdrawn.
  • liquid is introduced from the liquid buffer into the main capacitor and thereby reduces the storage capacity of the liquid buffer, that is, more liquid is withdrawn from the liquid buffer than is introduced into it.
  • a bath evaporator in comparison to the falling film evaporator has the advantage that no such external liquid circulation is necessary.
  • the application of such an artificial fluid circulation from the sump to the buffer thus appears at first unrealistic.
  • the operational advantage is surprisingly so great that it justifies the corresponding additional expense.
  • the system according to the invention also has the advantage that the relatively high amount of liquid, which in this case flows with low purity from the upper mass transfer sections of the low-pressure column, can be at least partially absorbed in the buffer, thus preventing or reducing the contamination of the bottoms liquid becomes.
  • the liquid buffer is arranged below the lowermost mass transfer section of the low-pressure column and above the main condenser, that is to say that due to the natural gradient, liquid can flow from the buffer into the evaporation space of the main condenser or its uppermost floor.
  • the liquid buffer may for example be formed by one or more shells which are arranged on the column wall, for example by a peripheral shell, or by one or more chimney trays.
  • the sump of a one-storey bath evaporator is regularly formed by its liquid bath, whereas in a multi-storey bath evaporator the bottom liquid bath is usually operated as a sump Alternatively, the sump can be formed by a separate space below the main condenser.
  • the liquid circulation from the sump to the liquid buffer can also be used in steady-state operation, without necessarily increasing the storage contents;
  • the circulation otherwise unusual in bath evaporators, serves to compensate for differences in purity in the evaporating liquid over the height of the evaporator.
  • a particularly stable operation can be achieved.
  • the liquid is introduced from the bottom of the main condenser by means of a liquid pump in the liquid buffer.
  • the bottoms liquid must be raised in order to reach the liquid buffer.
  • any method for lifting a liquid can be used for this purpose.
  • a liquid pump is used.
  • the invention offers particular advantages when used on multistage bath evaporators.
  • the greatest advantage is that the main capacitor is designed as a cascade evaporator.
  • the liquid circulation from the sump to the buffer not only prevents a possible lack of liquid, but also the concentration differences on the evaporation side of the different floors (levels) are compensated.
  • Each stage of a cascade evaporator acts as a partial evaporation, that is, from top to bottom increases the oxygen concentration and thus the evaporation temperature.
  • the liquefaction side however, the same nitrogen flows everywhere with a practically constant liquefaction temperature.
  • the upper stages of a cascade evaporator basically work with a greater temperature difference than the lower ones.
  • the use of the process according to the invention is particularly favorable if the oxygen-enriched product stream has an oxygen concentration of less than 98%, for example 90 to 95%. (All percentages here and below refer to the molar amount, unless stated otherwise.)
  • the method can be run with two modes of operation, in which, in a first mode of operation, more liquid is introduced into the liquid buffer than withdrawn therefrom, and in a second mode more liquid is withdrawn from the liquid buffer than is introduced into it.
  • the first mode of operation corresponds, for example, to steady-state operation with a constant load
  • the second mode corresponds to a load change case, for example an increase in load during the transitional period from a first steady-state operation with a first production quantity to a second steady-state operation with a second, higher production quantity.
  • the invention also relates to a device for cryogenic separation of air according to claims 5 to 7.
  • Compressed and purified feed air 1 flows under a pressure of about 5.5 bar in the warm end of a main heat exchanger 2, and branched into one A portion of the dry air 1 can be diverted via line 5 as instrument air or to supply other compressed air consumers.
  • the first partial air stream 3 is cooled in the main heat exchanger 2 to about dew point and introduced via line 5 in the high-pressure column 6, which is part of a distillation column system for nitrogen-oxygen separation, which also has a low-pressure column 7 and a main condenser 8, as Cascade evaporator is formed.
  • the operating pressures in the columns are about 5.2 bar in the high pressure column 6 and about 1.3 bar in the low pressure column. 7
  • the second partial air stream 4 is cooled in the main heat exchanger 2 only to an intermediate temperature and fed under this intermediate temperature of an expansion turbine 9, which is braked by means of a generator 10. There he is working expanded to about low-pressure column pressure, fed back via line 11 to the main heat exchanger 2 and finally and via line 12 of the low-pressure column 7 at an intermediate point.
  • Gaseous head nitrogen 13 of the high-pressure column 6 is introduced to a part 14 in the liquefaction space of the main capacitor 8.
  • the remainder 15 is warmed in the main heat exchanger 2 to about ambient temperature and finally withdrawn via line 16 as gaseous nitrogen pressure product (PGAN).
  • GPN gaseous nitrogen pressure product
  • the liquid nitrogen 17 produced in the main condenser 8 is fed to a first part 18 as reflux to the top of the high-pressure column 6.
  • a second part 19 is cooled in a supercooling countercurrent 23 and fed via line 20 as reflux to the top of the low-pressure column 7.
  • a third part 21 can be discharged as a liquid nitrogen product (LIN).
  • the oxygen-enriched bottoms liquid 24 of the high-pressure column 6 is likewise cooled in the subcooling countercurrent 23 and introduced via line 25 at an intermediate point into the low-pressure column 7.
  • gaseous nitrogen 26 is withdrawn, warmed in the supercooling countercurrent 23 and the main heat exchanger 2 and withdrawn via line 27. It can be used, for example, as a regeneration gas in the air purification, not shown.
  • An oxygen-enriched product stream 28 is withdrawn from the lower region of the low-pressure column 7 (here directly above the main condenser 8), heated to approximately ambient temperature in the main heat exchanger 2 and recovered via line 29 as an oxygen product (GOX). Via the lines 30, 31, 33 and a pump 32, part of the liquid can be recovered from the sump 35 of the main condenser 8 as a liquid product (LOX), for example for filling a liquid tank for emergency supply.
  • LOX liquid product
  • a pressure oxygen product could be obtained by internal compression, by bringing a portion of the liquid oxygen 31 liquid pressure and vaporized in the main heat exchanger 2 or pseudo-evaporated.
  • a liquid buffer 33 in the form of an annular shell.
  • the liquid buffer 33 may be filled with a portion of the liquid draining from the lowermost mass transfer section 32.
  • liquid is selectively directed out of the buffer 33 into the main condenser 8, specifically into the liquid bath of its uppermost floor.
  • liquid is introduced from the sump 36 into the liquid buffer 33.

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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)
EP12001386A 2011-03-22 2012-03-01 Procédé et dispositif destinés à la production de produits à base d'oxygène par la décomposition à basse température de l'air Withdrawn EP2503270A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP12001386A EP2503270A1 (fr) 2011-03-22 2012-03-01 Procédé et dispositif destinés à la production de produits à base d'oxygène par la décomposition à basse température de l'air

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP11002364 2011-03-22
EP12001386A EP2503270A1 (fr) 2011-03-22 2012-03-01 Procédé et dispositif destinés à la production de produits à base d'oxygène par la décomposition à basse température de l'air

Publications (1)

Publication Number Publication Date
EP2503270A1 true EP2503270A1 (fr) 2012-09-26

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EP12001386A Withdrawn EP2503270A1 (fr) 2011-03-22 2012-03-01 Procédé et dispositif destinés à la production de produits à base d'oxygène par la décomposition à basse température de l'air

Country Status (3)

Country Link
US (1) US20120240620A1 (fr)
EP (1) EP2503270A1 (fr)
CN (1) CN102692114A (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2022258222A1 (fr) * 2021-06-07 2022-12-15 Linde Gmbh Installation de séparation d'air et procédé de séparation d'air

Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1152432B (de) 1962-04-21 1963-08-08 Linde Eismasch Ag Platten-Kondensator-Verdampfer, insbesondere fuer Gas- und Luftzerleger
DE1949609A1 (de) 1969-10-01 1971-04-08 Linde Ag Kondensatorverdampfer fuer eine Rektifikationssaeule
US5222549A (en) * 1988-07-04 1993-06-29 Japan Oxygen Co., Ltd. Condenser/evaporator
EP0681153A1 (fr) * 1994-05-04 1995-11-08 Linde Aktiengesellschaft Procédé et dispositif pour la séparation de l'air à basse température
JPH1054656A (ja) * 1996-08-12 1998-02-24 Nippon Sanso Kk 空気液化分離装置及び方法
WO2001092798A2 (fr) 2000-05-31 2001-12-06 Linde Ag Condenseur a bain a plusieurs etages
EP1287302B1 (fr) 2000-05-31 2005-09-21 Linde AG Condenseur a bain a plusieurs etages
DE102005028012A1 (de) * 2005-06-16 2006-09-14 Linde Ag Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
DE102007003437A1 (de) 2007-01-23 2007-09-20 Linde Ag Mehrstöckiger Badkondensator im Flüssigkeitsbad

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1152432B (de) 1962-04-21 1963-08-08 Linde Eismasch Ag Platten-Kondensator-Verdampfer, insbesondere fuer Gas- und Luftzerleger
DE1949609A1 (de) 1969-10-01 1971-04-08 Linde Ag Kondensatorverdampfer fuer eine Rektifikationssaeule
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