EP1051588B1 - Method and device for evaporating liquid oxygen - Google Patents

Method and device for evaporating liquid oxygen 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)
French (fr)
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EP1051588A1 (en
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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.

Description

Die Erfindung betrifft ein Verfahren zum Verdampfen von flüssigem Sauerstoff sowie dessen Anwendung in einem Verfahren zur Gewinnung von Sauerstoff durch Tieftemperaturzerlegung von Luft.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.

Unter Sauerstoff wird in der vorliegenden Anmeldung jedes Gemisch verstanden, das einen gegenüber Luft erhöhten Sauerstoffgehalt aufweist, beispielsweise mindestens 70 %, vorzugsweise mindestens 98 %. (In dieser Anmeldung bezeichnen alle Prozentangaben molare Mengen, wenn nicht ausdrücklich etwas anderes angegeben ist.) Darunter fällt insbesondere unreiner Sauerstoff, ebenso wie technisch reiner Sauerstoff und hochreiner Sauerstoff mit einer Reinheit von 99,99 % oder höher. Für eine Fülle von Anwendungen ist es notwendig, flüssig vorliegenden Sauerstoff vor seiner Verwendung in die Gasform zu überführen, indem er in einem Hauptverdampfer durch indirekten Wärmeaustausch mit einem Wärmeträger verdampft wird.In the present application, 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%. (In this application everyone designates Percentages molar amounts, unless expressly stated otherwise ). This includes in particular impure oxygen, as well as technically cleaner Oxygen and high-purity oxygen with a purity of 99.99% or higher. For A plethora of applications require 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.

Eine solche Verdampfung kommt insbesondere bei der Gewinnung von gasförmigem Sauerstoff durch Tieftemperaturrektifikation vor, bei der das Sauerstoffprodukt flüssig am Sumpf einer Rektifiziersäule anfällt, da es schwererflüchtig als Stickstoff und Argon ist. Um das Produkt in Gasform zu erhalten und um aufsteigenden Dampf für die Rektifiziersäule zu erzeugen, muß der flüssig angefallene Sauerstoff ebenfalls in einem Hauptverdampfer verdampft werden. Am weitesten verbreitet ist dabei das klassische Linde-Doppelsäulenverfahren, bei dem der Hauptverdampfer im Sumpf einer Niederdrucksäule angeordnet ist und mit kondensierendem Stickstoff vom Kopf der Drucksäule betrieben wird (siehe Hausen/Linde, Tieftemperaturtechnik, 2. Auflage, Abschnitt 4.1.2 auf Seite 284). Der Hauptverdampfer wird in diesem Fall als Kondensator-Verdampfer betrieben und häufig als Hauptkondensator bezeichnet. Er wird durch einen oder mehrere Wärmetauscherblöcke realisiert, die als Umlauf- oder Fallfilmverdampfer betrieben werden. 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. To get the product in gaseous form and to get steam rising for to produce the rectification column, 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.

Die Erfindung betrifft auch andere Doppelsäulenprozesse, bei denen der Hauptverdampfer beispielsweise mit Luft betrieben wird, und auch Verfahren mit drei oder mehr Säulen zur Stickstoff-Sauerstoff-Trennung. Der oder den Rektifiziersäulen zur Stickstoff-Sauerstoff-Trennung können Vorrichtungen zur Gewinnung anderer Luftkomponenten, insbesondere von Edelgasen nachgeschaltet sein, beispielsweise zur Argongewinnung.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.

Wenn flüssiger Sauerstoff vollständig oder im wesentlichen vollständig verdampft wird, können sich in dem Verdampfer schwererflüchtige Verunreinigungen wie beispielsweise CO2 oder N2O anreichern, auch wenn diese in dem zu verdampfenden Sauerstoff (beziehungsweise in der zu zerlegenden Luft) nur in sehr geringen Konzentrationen enthalten sind. (Das früher gefürchtete Acetylen ist jedoch bei Luftzerlegungsanlagen mit adsorptiver Vorreinigung nicht mehr problematisch.) Manche dieser schwererflüchtigen Stoffe, zum Beispiel CO2 und N2O, können als Feststoffe ausfallen und müssen von Zeit zu Zeit entfernt werden, damit eine Verstopfung von Wärmetauscherpassagen im Hauptverdampfer vermieden wird. Um diese ausgeschiedenen Feststoffe zu beseitigen, muß die gesamte Anlage abgeschaltet werden. Dies kann bei einer großen Luftzerlegungsanlage einen Betriebsstillstand von beispielsweise zwei bis fünf Tagen bedeuten.If 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.

Um die Anreicherung schwererflüchtiger Komponenten zu verringern, ist es üblich, aus dem Hauptverdampfer kontinuierlich oder von Zeit zu Zeit etwas Flüssigkeit in Form eines Spülstroms zu entnehmen und zu verwerfen. Mit dieser Spülmenge werden auch die in dem flüssig verbliebenen Sauerstoff angereicherten schwererflüchtigen Verunreinigungen entfernt, so daß deren Konzentration im Hauptverdampfer begrenzt werden kann. Die Spülmenge beträgt bei einer Luftzerlegungsanlage mit adsorptiver Vorreinigung üblicherweise 0,02 bis 0,04 % der gesamten in den Verdampfer eingeleiteten Menge an flüssigem Sauerstoff. Seitdem zur Luftreinigung stromaufwärts der Rektifikation Molekularsiebadsorber anstelle der früher verwendeten umschaltbaren Wärmetauscher (Revex) oder Regeneratoren eingesetzt werden, haben sich die Probleme durch die Ansammlung von brennbaren schwererflüchtigen Komponenten in einem derartigen Sauerstoffverdampfer (Hauptverderdampfer) soweit verringert, daß ein derartiger Spülstrom ausreicht, um bedenkliche Konzentrationen von Kohlenwasserstoffen zu verhindern, ohne daß zusätzliche Maßnahmen notwendig wären (siehe Hausen/Linde, Tieftemperaturtechnik, 2. Auflage, Abschnitt 4.5.1.5 auf den Seiten 312 und 313).In order to reduce the accumulation of less volatile components, it is common to some liquid from the main evaporator continuously or from time to time Take the form of a flushing stream and discard. With this flush amount the oxygen remaining in the liquid is also enriched less volatile impurities removed, so that their concentration in Main evaporator can be limited. 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. Since for air purification upstream of the rectification molecular sieve adsorber instead of the previously used switchable heat exchangers (Revex) or regenerators used, the problems have arisen due to the accumulation of flammable less volatile components in such an oxygen evaporator (Main evaporator) reduced so far that such a purge flow is sufficient to prevent dangerous concentrations of hydrocarbons without additional measures would be necessary (see Hausen / Linde, low-temperature technology, 2. Edition, section 4.5.1.5 on pages 312 and 313).

Aus US 2664719 ist ein Verfahren der eingangs genannten Art bekannt, das die Merkmale des Oberbegriffs des Anspruchs 1 aufweist. Flüssiger Sauerstoff aus einem Hauptverdampfer wird in einen Zusatzverdampfer eingeleitet, der eine Spülleitung aufweist.From US 2664719 a method of the type mentioned is known, which has the features of the preamble of claim 1. liquid Oxygen from a main evaporator is introduced into an additional evaporator that has a purge line.

Der Erfindung liegt die Aufgabe zugrunde, die Verfügbarkeit eines Hauptverdampfers zur Verdampfung von flüssigem Sauerstoff zu erhöhen und insbesondere Betriebsunterbrechungen soweit wie möglich zu verhindern.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.

Diese Aufgabe wird durch die Merkmale des Patentanspruchs 1 gelöst. Dabei wird der (erste) Spülstrom, der aus dem Hauptverdampfer abgezogen wird, in einen Zusatzverdampfer geleitet, der getrennt vom Hauptverdampfer angeordnet ist. In diesem Zusatzverdampfer wird ein großer Teil des ersten Spülstroms verdampft und kann damit als Sauerstoffprodukt oder - zwischenprodukt gewonnen werden. Dem Zusatzverdampfer wird wiederum ein zweiter Spülstrom entnommen und verworfen. (In dem Spezialfall, daß aus dem flüssigen Sauerstoff Krypton und/oder Xenon gewonnen werden sollen, ist auch eine weitere Aufarbeitung möglich.) Während der erste Spülstrom kontinuierlich vom Hauptverdampfer zum Zusatzverdampfer geleitet wird, kann die Entnahme des zweiten Spülstroms kontinuierlich oder diskontinuierlich erfolgen.This object is achieved by the features of patent claim 1. The (first) Purge stream, which is withdrawn from the main evaporator, passed into an additional evaporator, which is arranged separately from the main evaporator. In 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. (In the special case that from the liquid oxygen Further processing is also possible if krypton and / or xenon are to be obtained.) During the first flushing flow continuously from the main evaporator to the additional evaporator is conducted, the removal of the second purge stream can be continuous or discontinuous respectively.

Bei der Erfindung kann eine relativ große Flüssigkeitsmenge als erster Spülstrom vom Hauptverdampfer abgezogen werden, so daß sämtliche schwererflüchtigen Komponenten ausgeschleust werden und ihre Konzentration am Hauptverdampfer gering gehalten wird. Insbesondere treten auch keine Feststoffabscheidungen im Hauptverdampfer auf. Diese große Spülflüssigkeitsmenge geht jedoch nicht vollständig verloren, da ein Teil des ersten Spülstroms im Zusatzverdampfer verdampft und in Gasform abgezogen wird. Vom Zusatzverdampfer wird lediglich eine übliche Spülmenge als zweiter Spülstrom abgezogen, beispielsweise 0,02 bis 0,5 %, vorzugsweise 0,02 bis 0,2 % der in den Hauptverdampfer eingeleiteten Menge an flüssigem Sauerstoff. (Im Falle der diskontinuierlichen Entnahme des zweiten Spülstroms beziehen sich die Zahlenangaben auf den zeitlichen Mittelwert.) Der Rest des ersten Spülstroms wird im Zusatzverdampfer verdampft und kann als gasförmiges Sauerstoffprodukt verwertet werden.In the invention, 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.

Mit Hilfe der Erfindung ist es möglich, den Hauptverdampfer so stark zu spülen, daß der Gehalt an schwererflüchtigen Komponenten, die zu Feststoffabscheidungen führen könnten, extrem gering gehalten wird. Die schwererflüchtigen Komponenten werden vollständig zum Zusatzverdampfer geleitet und dort über den zweiten Spülstrom und durch den von Zeit zu Zeit vorgenommenen Anwärmbetrieb entfernt.With the help of the invention it is possible to rinse the main evaporator so strongly that the content of less volatile components that lead to solid deposits could lead to being kept extremely low. The less volatile components are completely directed to the additional evaporator and there via the second Flushing current and removed by the heating operation carried out from time to time.

Feststoffausscheidungen können also nur im Zusatzverdampfer, nicht aber im Hauptverdampfer anfallen. Der Zusatzverdampfer kann jedoch wesentlich einfacher als der Hauptverdampfer durch Anwärmung von Feststoffen befreit werden. Dazu wird der Normalbetrieb gelegentlich durch einen Anwärmbetrieb unterbrochen, wobei im Anwärmbetrieb der Zusatzverdampfer vom Hauptverdampfer getrennt wird, indem keine Flüssigkeit aus dem Hauptverdampfer in den Zusatzverdampfer geleitet wird. Gleichzeitig wird der Zusatzverdampfer auf eine Temperatur gebracht, die deutlich höher als seine Temperatur im Normalbetrieb ist, beispielsweise um mindestens 20 K, vorzugsweise 20 bis 50 K. Der Betrieb des Hauptverdampfers und der Anlage, in die er eingebaut ist, braucht dabei nicht unterbrochen zu werden. Durch die verstärkte Spülung des Hauptverdampfers braucht dieser nicht mehr zur Entfernung von Feststoffen angewärmt zu werden.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. At the same time, 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 operation of the main evaporator and the plant in which it does not need to be interrupted. Through the reinforced The main evaporator no longer needs to be flushed to remove Solids to be warmed.

Es ist günstig, wenn die Menge des ersten Spülstroms, die im Normalbetrieb vom Hauptverdampfer abgezogen wird, mindestens 1 %, vorzugsweise mindestens 3 % und/oder höchstens 10 %, vorzugsweise höchstens 5 % der in den Hauptverdampfer eingeleiteten Menge an flüssigem Sauerstoff beträgt.It is advantageous if 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.

Die Erfindung betrifft außerdem die Anwendung des Verfahrens nach Anspruch 1 oder 2 in einem Verfahren zur Tieftemperaturzerlegung von Luft gemäß Patentanspruch 3 und in einer entsprechenden Vorrichtung gemäß Patentanspruch 6, insbesondere Luftzeriegungsverfahren und -anlagen mit Luftvorreinigung durch Adsorption, beispielsweise an einem Molekularsieb. Solche Verfahren und Anlagen dienen zur Gewinnung von Sauerstoff, Stickstoff und/oder anderen in atmosphärischer Luft enthaltenen Gasen.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. Such procedures and facilities are used for the production of oxygen, nitrogen and / or others in gases contained in atmospheric air.

Weiterhin betrifft die Erfindung eine Vorrichtung zum Verdampfen von flüssigem Sauerstoff gemäß den Patentansprüchen 4 und 5. Furthermore, the invention relates to a device for evaporating liquid Oxygen according to claims 4 and 5.

Die Erfindung sowie weitere Einzelheiten der Erfindung werden im folgenden anhand von in den Zeichnungen dargestellten Ausführungsbeispielen näher erläutert. Hierbei zeigen:

Figur 1
ein erstes Ausführungsbeispiel mit einem aus einem Block bestehenden Hauptverdampfer und
Figur 2
ein zweites Ausführungsbeispiel mit einem aus mehreren Blöcken bestehenden Hauptverdampfer.
The invention and further details of the invention are explained in more detail below with reference to exemplary embodiments shown in the drawings. Here show:
Figure 1
a first embodiment with a main evaporator consisting of a block and
Figure 2
a second embodiment with a main evaporator consisting of several blocks.

Figur 1 zeigt einen Ausschnitt einer Doppelsäule zur Tieftemperaturzerlegung von Luft, nämlich den oberen Teil der Drucksäule 1 und den unteren Abschnitt der Niederdrucksäule 2. Ein Hauptverdampfer 3 dient zur Verdampfung von flüssigem Sauerstoff, der vom untersten Stoffaustauschabschnitt der Niederdrucksäule 2 abfließt. (Der unterste Stoffaustauschabschnitt ist in der Zeichnung als Boden 4 dargestellt, es könnte sich jedoch auch um eine geordnete Packung handeln.) Über Leitung 9 wird gasförmiges Sauerstoffprodukt aus der Niederdrucksäule abgezogen.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.

Der Hauptverdampfer kann - wie in Figur 1 gezeigt - innerhalb der Doppelsäule, insbesondere im Sumpf der Niederdrucksäule angeordnet sein. Alternativ kann er als separates Bauteil außerhalb der Doppelsäule realisiert oder in ein anderes, von der Doppelsäule getrenntes Bauteil integriert sein, beispielsweise in eine Methan-Ausschleussäule, wie sie in DE 4332870 A1 oder DE 2055099 A gezeigt ist. Über eine im unteren Bereich des Hauptverdampfers 3 angeordnete Leitung 5 wird ein erster Spülstrom kontinuierlich entnommen und in einen Zusatzverdampfer 6 eingeleitet. Vom unteren Bereich des Zusatzverdampfers 6 wird ein zweiter Spülstrom 7 kontinuierlich oder diskontinuierlich abgezogen, während verdampfter Sauerstoff 8 in die Niederdrucksäule zurückgeleitet wird. Alternativ dazu kann der Dampf 8 in die Sauerstoffproduktleitung 9 von der Niederdrucksäule geleitet werden oder in einen anderen Apparat, beispeilsweise in den unteren Bereich einer Methan-Ausschleussäule gemäß DE 4332870 A1 oder DE 2055099 A.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. Alternatively, 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.

Als Wärmeträger 10 zur indirekten Beheizung des Hauptverdampfers wird Stickstoff vom Kopf der Drucksäule 1 eingesetzt. Der im Hauptverdampfer kondensierte Stickstoff 11 wird als Rücklauf in den beiden Säulen eingesetzt. Der Zusatzverdampfer 6 wird im Normalbetrieb entweder ebenfalls mit Stickstoff aus der Drucksäule oder mit Luft als Wärmeträger 12 beheizt. Der kondensierte Wärmeträger wird über Leitung 13 abgezogen und in eine oder mehrere der Rektifiziersäulen eingespeist.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.

In gewissen Zeitabständen von beispielsweise drei bis zwölf Monaten, vorzugsweise etwa sechs Monaten wird vom Normalbetrieb auf den Anwärmbetrieb umgeschaltet, indem das Ventil 14 in der ersten Spülleitung 5 geschlossen wird. Auch die Zufuhr des Wärmeträger 12 wird geschlossen. Stattdessen wird etwa 300 K warme Luft über Leitung 15 in den Verflüssigungsraum des Zusatzverdampfers 6 geführt und über Leitung 16 wieder entfernt. Eine Anwärmphase umfaßt Abstellen, Entleeren, Anwärmen, Wiederabkühlen und Inbetriebnahme und dauert beispielsweise 10 bis 24 Stunden, vorzugsweise etwa 20 Stunden.At certain intervals of, for example, three to twelve months, preferably 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.

Es ist vorteilhaft, aber im Rahmen der Erfindung nicht unbedingt notwendig, wenn der erste Spülstrom 5 vor seiner Einleitung in den Zusatzverdampfer 6 durch eine Einrichtung 19 zur Entfernung schwererflüchtiger Komponenten, beispielsweise durch Adsorption, geleitet wird.It is advantageous, but not absolutely necessary within the scope of the invention, if the first flushing stream 5 before its introduction into the additional evaporator 6 by a Device 19 for the removal of less volatile components, for example by Adsorption.

Das Ausführungsbeispiel von Figur 2 unterscheidet sich dadurch von Figur 1, daß der Hauptverdampfer durch eine Mehrzahl von Blöcken 3a, 3b gebildet wird. Die Blöcke 3a, 3b sind beispielsweise konzentrisch um ein Zentralrohr angeordnet, das zur Zufuhr 10 von gasförmigem Stickstoff aus der Drucksäule 1 dient. Selbstverständlich kann auch dieses Ausführungsbeispiel mit einer Einrichtung zur Entfernung schwererflüchtiger Komponenten (19 in Figur 1) ausgerüstet werden.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. Of course can also this embodiment with a device for removal less volatile components (19 in Figure 1) are equipped.

Claims (7)

  1. Process for vaporizing liquid oxygen in which, in standard operation,
    liquid oxygen is introduced into a main evaporator (3) and is there partially vaporized,
    a first bleed stream (5) is removed in the liquid state from the main evaporator (3),
    the first bleed stream (5) is partially vaporized in an additional evaporator (6) and
    a second bleed stream (7) is withdrawn in the liquid state from the additional evaporator (6),
    characterized in that, in the process, the standard operation is interrupted by a heating operation and in the heating operation
    no liquid (5) is passed from the main evaporator (3) into the additional evaporator (6) and
    the additional evaporator (6) is brought to a temperature which is markedly higher than its temperature in the standard operation.
  2. Process according to Claim 1, in which in the standard operation the volume of the first bleed stream (5) which is taken off from the main evaporator (3) is at least 1%, preferably at least 3% and/or at most 10%, preferably at most 5%, of the volume of liquid oxygen introduced into the main evaporator (3).
  3. Use of the process according to Claim 1 or 2 in a process for producing oxygen by low-temperature fractionation of air in a rectification system which has a pressure column (1) and a low-pressure column (2) for vaporizing liquid oxygen from the low-pressure column (2), in which at least a part of the vapour (8) produced in the main evaporator (3) and in the additional evaporator (6) is introduced into the low-pressure column (2) and/or is taken off as gaseous oxygen product (9).
  4. Apparatus for vaporizing liquid oxygen having
    a main evaporator (3),
    an additional evaporator (6),
    means for introducing liquid oxygen into the main evaporator,
    a first bleed line (5) for withdrawing a first liquid bleed stream from the main evaporator (3) and for introducing the first liquid bleed stream into the additional evaporator (6),
    a second bleed line (7) for withdrawing a second liquid bleed stream from the additional evaporator (6) and
    a gas product line (8) for withdrawing vapour from the additional evaporator, characterized by
    a heating apparatus (15, 16) for heating the additional evaporator (6) to a temperature which is markedly higher than its temperature in the standard operation, and
    means (14) for interrupting the introduction of the first liquid bleed stream into the additional evaporator (6).
  5. Apparatus according to Claim 4 having a control device for setting the volume of the first bleed stream (5) in the standard operation to at least 1%, preferably at least 3% and/or at most 10%, preferably at most 5%, of the volume of liquid oxygen introduced into the main evaporator (3).
  6. Use of the apparatus according to Claim 4 or 5 in an apparatus for producing oxygen by low-temperature fractionation of air having a rectification system which has a pressure column (1) and a low-pressure column (2), in which the means for introducing liquid oxygen into the main evaporator (3) are connected to the low-pressure column (2) and the apparatus has an oxygen product line (9, 8) for withdrawing gaseous oxygen product from the main evaporator (3) and/or from the additional evaporator (6).
  7. Use according to Claim 6 in which the apparatus for producing oxygen by low-temperature fractionation of air has a gas product line (8) for withdrawing vapour from the additional evaporator (6), which gas product line is connected to the low-pressure column (2) or to a product line (9) which is connected to the low-pressure column.
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BR9908350A (en) 2000-12-05
ES2175944T3 (en) 2002-11-16
KR100528570B1 (en) 2005-11-15
WO1999039143A1 (en) 1999-08-05
DE59901114D1 (en) 2002-05-08
US6351968B1 (en) 2002-03-05
EP1051588A1 (en) 2000-11-15
AU2617499A (en) 1999-08-16
CN1289404A (en) 2001-03-28
DK1051588T3 (en) 2002-07-01
JP2002502017A (en) 2002-01-22
KR20010034421A (en) 2001-04-25

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