EP1051588B1 - Procede et dispositif pour vaporiser de l'oxygene liquide - Google Patents

Procede et dispositif pour vaporiser de l'oxygene liquide Download PDF

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Publication number
EP1051588B1
EP1051588B1 EP99906129A EP99906129A EP1051588B1 EP 1051588 B1 EP1051588 B1 EP 1051588B1 EP 99906129 A EP99906129 A EP 99906129A EP 99906129 A EP99906129 A EP 99906129A EP 1051588 B1 EP1051588 B1 EP 1051588B1
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Prior art keywords
evaporator
oxygen
liquid
low
additional
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German (de)
English (en)
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EP1051588A1 (fr
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Franz Habicht
Gerhard Pompl
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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
    • F25J3/04406—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
    • F25J3/04418—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 with thermally overlapping high and low pressure columns
    • 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
    • F25J3/04812—Different modes, i.e. "runs" of operation
    • F25J3/04824—Stopping of the process, e.g. defrosting or deriming; 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • 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
    • F25J2250/04—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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/10—Boiler-condenser with superposed stages
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/40—One fluid being air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/42—One fluid being nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/50—One fluid being oxygen
    • 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
    • Y10S62/902—Apparatus
    • Y10S62/905—Column

Definitions

  • the invention relates to a method for evaporating liquid oxygen as well its application in a process for the production of oxygen by Cryogenic air separation.
  • oxygen is understood to mean any mixture which has an increased oxygen content compared to air, for example at least 70%, preferably at least 98%.
  • liquid oxygen to be present gasify its use by being in a Main evaporator through indirect heat exchange with a heat transfer medium is evaporated.
  • Such evaporation occurs particularly when gaseous is extracted Oxygen through low temperature rectification, in which the oxygen product is liquid at the bottom of a rectification column, since it is less volatile than nitrogen and Is argon.
  • the liquid oxygen must also be in be evaporated from a main evaporator.
  • This is the most common Classic Linde double column process, in which the main evaporator in the sump a low pressure column is arranged and with condensing nitrogen from the head the pressure column is operated (see Hausen / Linde, low-temperature technology, 2nd edition, section 4.1.2 on page 284).
  • the main evaporator is in this case operated as a condenser-evaporator and often referred to as the main condenser. It is implemented by one or more heat exchanger blocks, which are or falling film evaporators are operated.
  • the invention also relates to other double-column processes in which the Main evaporator is operated with air, for example, and also processes with three or more columns for nitrogen-oxygen separation.
  • the rectification column or columns for nitrogen-oxygen separation can devices for the production of others Air components, in particular of noble gases, for example for argon production.
  • liquid oxygen is completely or essentially completely evaporated, less volatile impurities such as CO 2 or N 2 O can accumulate in the evaporator, even if they contain only very low concentrations in the oxygen to be evaporated (or in the air to be separated) are. (However, the previously feared acetylene is no longer a problem in air separation plants with adsorptive pre-cleaning.)
  • Some of these less volatile substances for example CO 2 and N 2 O, can precipitate out as solids and must be removed from time to time in order to block the heat exchanger passages in the Main evaporator is avoided. The entire system must be switched off to remove these separated solids. In a large air separation plant, this can mean a shutdown of, for example, two to five days.
  • the flush volume is one Air separation plant with adsorptive pre-cleaning usually 0.02 to 0.04% of total amount of liquid oxygen introduced into the evaporator.
  • the invention has for its object to the availability of a main evaporator Increase vaporization of liquid oxygen and in particular To prevent business interruptions as far as possible.
  • the (first) Purge stream which is withdrawn from the main evaporator, passed into an additional evaporator, which is arranged separately from the main evaporator.
  • This additional evaporator is a large part of the first flushing stream evaporates and can thus be used as an oxygen product or intermediate product can be obtained.
  • the additional evaporator is in turn a second Rinsing stream removed and discarded.
  • the removal of the second purge stream can be continuous or discontinuous respectively.
  • a relatively large amount of liquid can flow from the first rinse stream Main evaporator are removed, so that all less volatile components are discharged and their concentration on the main evaporator is kept low. In particular, there are no solids deposits in the main evaporator. This size However, the amount of flushing liquid is not completely lost because part of the first flushing stream evaporated in an additional evaporator and drawn off in gas form. From the additional evaporator subtracted only a usual flushing quantity as a second flushing stream, for example 0.02 to 0.5%, preferably 0.02 to 0.2% of the amount introduced into the main evaporator liquid oxygen. (In the case of discontinuous withdrawal of the second flushing stream the numbers refer to the time average.) The rest of the first Flushing stream is evaporated in the additional evaporator and can be a gaseous oxygen product be used.
  • Solids can only be separated in the additional evaporator, but not in the Main evaporator.
  • the additional evaporator can be much easier as the main evaporator by heating solids. This will normal operation is occasionally interrupted by a heating operation, whereby in Heating operation of the auxiliary evaporator is separated from the main evaporator by no liquid is led from the main evaporator into the additional evaporator.
  • the additional evaporator is brought to a temperature that is clear is higher than its temperature in normal operation, for example by at least 20 K, preferably 20 to 50 K.
  • the amount of the first flushing stream, which is in normal operation from Main evaporator is withdrawn, at least 1%, preferably at least 3% and / or at most 10%, preferably at most 5% of those in the main evaporator amount of liquid oxygen introduced.
  • the invention also relates to the application of the method according to claim 1 or 2 in a process for cryogenic air separation according to Claim 3 and in a corresponding device according to claim 6, in particular air separation processes and plants with air pre-cleaning Adsorption, for example on a molecular sieve.
  • air separation processes and plants with air pre-cleaning Adsorption for example on a molecular sieve.
  • Such procedures and facilities are used for the production of oxygen, nitrogen and / or others in gases contained in atmospheric air.
  • the invention relates to a device for evaporating liquid Oxygen according to claims 4 and 5.
  • Figure 1 shows a section of a double column for low-temperature decomposition of Air, namely the upper part of the pressure column 1 and the lower portion of the Low pressure column 2.
  • a main evaporator 3 is used to evaporate liquid Oxygen coming from the lowest mass transfer section of the low pressure column 2 flows. (The bottom mass transfer section is in the drawing as bottom 4 shown, but it could also be an orderly pack.)
  • About Line 9 is withdrawn gaseous oxygen product from the low pressure column.
  • the main evaporator can - as shown in Figure 1 - inside the double column, be arranged in particular in the sump of the low pressure column. Alternatively, it can be used as separate component realized outside the double column or in another, from the Double column separate component can be integrated, for example in a methane discharge column, as shown in DE 4332870 A1 or DE 2055099 A.
  • about a line 5 arranged in the lower region of the main evaporator 3 becomes a the first rinsing stream is continuously withdrawn and into an additional evaporator 6 initiated. From the lower area of the additional evaporator 6 there is a second flushing stream 7 withdrawn continuously or discontinuously while vaporized oxygen 8 is returned to the low pressure column.
  • the steam 8 into the Oxygen product line 9 are passed from the low pressure column or into one other apparatus, for example in the lower area of a methane discharge column according to DE 4332870 A1 or DE 2055099 A.
  • Nitrogen is used as the heat transfer medium 10 for indirectly heating the main evaporator inserted from the head of the pressure column 1.
  • the condensed in the main evaporator Nitrogen 11 is used as the return in the two columns.
  • the Additional evaporator 6 is either also in normal operation with nitrogen from the Pressure column or heated with air as a heat transfer medium 12.
  • the condensed heat transfer medium is withdrawn via line 13 and into one or more of the rectification columns fed.
  • Switching from normal operation to heating operation takes about six months, by closing the valve 14 in the first flushing line 5. Also the supply of the Heat transfer medium 12 is closed. Instead, about 300 K warm air is over Line 15 led into the liquefaction space of the additional evaporator 6 and over Line 16 removed.
  • a warm-up phase includes switching off, emptying, Warming up, cooling down and commissioning and takes for example 10 to 24 hours, preferably about 20 hours.
  • the embodiment of Figure 2 differs from Figure 1 in that the Main evaporator is formed by a plurality of blocks 3a, 3b.
  • the blocks 3a, 3b are arranged, for example, concentrically around a central tube, which for Feed 10 of gaseous nitrogen from the pressure column 1 is used.
  • a device for removal less volatile components (19 in Figure 1) are equipped.

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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)
  • Oxygen, Ozone, And Oxides In General (AREA)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)

Claims (7)

  1. Procédé d'évaporation d'oxygène liquide, lors duquel,
    en mode de fonctionnement normal, de l'oxygène liquide est introduit dans un évaporateur principal (3) et y est partiellement évaporé,
    un premier courant de purge (5) est éliminé sous forme fluide de l'évaporateur principal (3),
    le premier courant de purge (5) est évaporé partiellement dans un évaporateur auxiliaire (6) et
    un deuxième courant de purge (7) est prélevé de l'évaporateur auxiliaire (6) sous forme fluide,
    caractérisé en ce que, lors du procédé, le fonctionnement normal est interrompu par un fonctionnement d'échauffement et que, dans le fonctionnement d'échauffement,
    aucun fluide (5) en provenance de l'évaporateur principal (3) n'est conduit dans l'évaporateur auxiliaire (6) et
    l'évaporateur auxiliaire (6) est amené à une température, qui est nettement plus élevée que sa température au cours du fonctionnement normal.
  2. Procédé selon la revendication 1, lors duquel, en mode de fonctionnement normal, la quantité du premier courant de purge (5), qui est prélevé de l'évaporateur principal (3), est d'au moins 1%, de préférence d'au moins 3% et/ou au plus de 10%, de préférence au plus 5% de la quantité d'oxygène liquide introduite dans l'évaporateur principal (3).
  3. Utilisation du procédé selon la revendication 1 ou 2 dans un procédé en vue de l'extraction d'oxygène par fractionnement à basse température d'air dans un système de rectification, qui présente une colonne sous pression (1) et une colonne basse pression (2), en vue de l'évaporation d'oxygène liquide en provenance de la colonne basse pression (2), une partie au moins de la vapeur produite (8) dans l'évaporateur principal (3) et dans l'évaporateur auxiliaire (6) étant introduite dans la colonne basse pression (2) et/ou en étant prélevée sous la forme d'un produit d'oxygène gazeux (9).
  4. Dispositif en vue de l'évaporation d'oxygène liquide, avec
    un évaporateur principal (3),
    un évaporateur auxiliaire (6),
    des moyens d'introduction d'oxygène liquide dans l'évaporateur principal,
    un premier conduit de purge (5) en vue du prélèvement d'un premier courant de purge fluide en provenance de l'évaporateur principal (3) et en vue de l'introduction du premier courant de purge fluide dans l'évaporateur auxiliaire (6),
    un deuxième conduit de purge (7) en vue du prélèvement d'une deuxième courant de purge fluide en provenance de l'évaporateur auxiliaire (6), et
    un conduit de produit gazeux (8) en vue du prélèvement de vapeur en provenance de l'évaporateur auxiliaire,
    caractérisé par
    un dispositif d'échauffement (15, 16) en vue de l'échauffement de l'évaporateur auxiliaire (6) à une température qui est nettement plus élevée que sa température en mode de fonctionnement normal, et
    des moyens (14), en vue de l'interruption de l'introduction du premier courant de purge fluide dans l'évaporateur auxiliaire (6).
  5. Dispositif selon la revendication 4, avec un équipement de régulation en vue du réglage de la quantité du premier courant de purge (5) en mode de fonctionnement normal à au moins 1%, de préférence à au moins 3% et/ou au plus à 10%, de préférence au plus à 5% de la quantité d'oxygène liquide introduite dans l'évaporateur principal (3).
  6. Utilisation du dispositif selon la revendication 4 ou 5, dans un dispositif en vue de l'extraction d'oxygène par fractionnement à basse température d'air à l'aide d'un système de rectification, qui présente une colonne sous pression (1) et une colonne basse pression (2), les moyens d'introduction d'oxygène liquide dans l'évaporateur principal (3) étant reliés à la colonne basse pression (2) et le dispositif présentant un conduit de produit d'oxygène (9, 8) en vue du prélèvement de produit oxygène gazeux en provenance de l'évaporateur principal (3) et/ou de l'évaporateur auxiliaire (6).
  7. Utilisation selon la revendication 6, lors de laquelle le dispositif en vue de l'extraction d'oxygène par fractionnement à basse température d'air présente un conduit de produit gazeux (8) en vue du prélèvement de vapeur en provenance de l'évaporateur auxiliaire (6), qui est relié à la colonne basse pression (2) ou à un conduit de produit (9) relié à la colonne basse pression.
EP99906129A 1998-01-30 1999-01-15 Procede et dispositif pour vaporiser de l'oxygene liquide Expired - Lifetime EP1051588B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP99906129A EP1051588B1 (fr) 1998-01-30 1999-01-15 Procede et dispositif pour vaporiser de l'oxygene liquide

Applications Claiming Priority (6)

Application Number Priority Date Filing Date Title
DE19803583 1998-01-30
DE19803583 1998-01-30
EP98107128 1998-04-20
EP98107128 1998-04-20
EP99906129A EP1051588B1 (fr) 1998-01-30 1999-01-15 Procede et dispositif pour vaporiser de l'oxygene liquide
PCT/EP1999/000203 WO1999039143A1 (fr) 1998-01-30 1999-01-15 Procede et dispositif pour vaporiser de l'oxygene liquide

Publications (2)

Publication Number Publication Date
EP1051588A1 EP1051588A1 (fr) 2000-11-15
EP1051588B1 true EP1051588B1 (fr) 2002-04-03

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EP99906129A Expired - Lifetime EP1051588B1 (fr) 1998-01-30 1999-01-15 Procede et dispositif pour vaporiser de l'oxygene liquide

Country Status (11)

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US (1) US6351968B1 (fr)
EP (1) EP1051588B1 (fr)
JP (1) JP2002502017A (fr)
KR (1) KR100528570B1 (fr)
CN (1) CN1154831C (fr)
AU (1) AU2617499A (fr)
BR (1) BR9908350A (fr)
DE (1) DE59901114D1 (fr)
DK (1) DK1051588T3 (fr)
ES (1) ES2175944T3 (fr)
WO (1) WO1999039143A1 (fr)

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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
DE10205878A1 (de) * 2002-02-13 2003-08-21 Linde Ag Tieftemperatur-Luftzerlegungsverfahren
FR2853723B1 (fr) * 2003-04-10 2007-03-30 Air Liquide Procede et installation de traitement d'un bain de liquide riche en oxygene recueilli en pied d'une colonne de distillation cryogenique
FR2910604B1 (fr) 2006-12-22 2012-10-26 Air Liquide Procede et appareil de separation d'un melange gazeux par distillation cryogenique
FR2916523B1 (fr) * 2007-05-21 2014-12-12 Air Liquide Capacite de stockage, appareil et procede de production de monoxyde de carbone et/ou d'hydrogene par separation cryogenique integrant une telle capacite.
US9651301B2 (en) 2009-09-28 2017-05-16 Koninklijke Philips N.V. System and method for liquefying and storing a fluid
EP2591301B1 (fr) * 2010-07-05 2020-09-02 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Appareil et procédé de séparation d'air par distillation cryogénique
DE102011111630A1 (de) * 2011-08-25 2013-02-28 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Tieftemperatur-Zerlegung eines Fluidgemischs
US9453674B2 (en) 2013-12-16 2016-09-27 Praxair Technology, Inc. Main heat exchange system and method for reboiling
US9366476B2 (en) 2014-01-29 2016-06-14 Praxair Technology, Inc. Condenser-reboiler system and method with perforated vent tubes
US9488408B2 (en) * 2014-01-29 2016-11-08 Praxair Technology, Inc. Condenser-reboiler system and method
JP6871962B2 (ja) * 2019-03-28 2021-05-19 大陽日酸株式会社 縦積型凝縮蒸発器、及び空気分離装置
FR3099816B1 (fr) 2019-08-05 2022-10-21 Air Liquide Procédé, dispositif et installation de réfrigération et/ou de liquéfaction
US20230074304A1 (en) * 2021-09-07 2023-03-09 Uop Llc Vapor distribution system in a concentric reboiler

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US2650482A (en) 1948-04-29 1953-09-01 Kellogg M W Co Method of separating gas mixtures
US2688238A (en) 1949-05-26 1954-09-07 Air Prod Inc Gas separation
US2664719A (en) 1950-07-05 1954-01-05 Union Carbide & Carbon Corp Process and apparatus for separating gas mixtures
DE1501760A1 (de) 1966-12-27 1969-11-27 Rudisleben Chemieanlagenbau Verfahren zur Luftzerlegung
JPS60253782A (ja) * 1984-05-30 1985-12-14 日本酸素株式会社 大型空気分離装置用凝縮器
US4871382A (en) 1987-12-14 1989-10-03 Air Products And Chemicals, Inc. Air separation process using packed columns for oxygen and argon recovery
FR2650379B1 (fr) * 1989-07-28 1991-10-18 Air Liquide Appareil de vaporisation-condensation pour double colonne de distillation d'air, et installation de distillation d'air comportant un tel appareil
FR2674947B1 (fr) * 1991-04-03 1998-06-05 Air Liquide Procede de vaporisation d'un liquide, echangeur de chaleur pour sa mise en óoeuvre, et application a une installation de distillation d'air a double colonne.
DE4300131C2 (de) * 1993-01-06 1999-08-05 Hoechst Ag Kolonne mit integriertem Wärmetauscher

Also Published As

Publication number Publication date
DE59901114D1 (de) 2002-05-08
JP2002502017A (ja) 2002-01-22
WO1999039143A1 (fr) 1999-08-05
AU2617499A (en) 1999-08-16
KR20010034421A (ko) 2001-04-25
DK1051588T3 (da) 2002-07-01
EP1051588A1 (fr) 2000-11-15
US6351968B1 (en) 2002-03-05
CN1289404A (zh) 2001-03-28
CN1154831C (zh) 2004-06-23
ES2175944T3 (es) 2002-11-16
BR9908350A (pt) 2000-12-05
KR100528570B1 (ko) 2005-11-15

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