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EP1074805A1 - Process for producing oxygen under pressure and device therefor - Google Patents

Process for producing oxygen under pressure and device therefor Download PDF

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Publication number
EP1074805A1
EP1074805A1 EP99118724A EP99118724A EP1074805A1 EP 1074805 A1 EP1074805 A1 EP 1074805A1 EP 99118724 A EP99118724 A EP 99118724A EP 99118724 A EP99118724 A EP 99118724A EP 1074805 A1 EP1074805 A1 EP 1074805A1
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EP
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Prior art keywords
pressure
pressure column
low
air
column
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EP99118724A
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German (de)
French (fr)
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EP1074805B1 (en
Inventor
Wilhelm Rohde
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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
    • F25J3/04151—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
    • F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
    • 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
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • F25J3/04054—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of 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
    • 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
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of 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
    • 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
    • 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
    • F25J2250/50—One fluid being oxygen

Definitions

  • the invention relates to a process for the production of oxygen under superatmospheric pressure through low-temperature air separation in one Rectification system that has at least one pressure column and one low pressure column has, wherein feed air is compressed to a first pressure which is approximately equal to Operating pressure of the pressure column is at least a first partial flow of the feed air cooled to the first pressure in a main heat exchanger and into the pressure column is initiated, an oxygen flow being taken from the low pressure column a discharge pressure that is higher than the operating pressure of the low pressure column, brought, warmed in the main heat exchanger and removed as a product, and whereby a process stream relaxes work and into the low pressure column is fed in and at least part of the work-related relaxation generated mechanical energy is used to drive a cold compressor.
  • the invention has for its object such a method energetically to make it cheaper.
  • This object is achieved in that the oxygen flow from the low pressure column brought to the delivery pressure in the liquid state and by indirect Heat exchange with a second partial flow which compresses to the first pressure Feed air is evaporated, the second partial stream upstream of the indirect Heat exchange is brought to a second pressure by means of the cold compressor.
  • the oxygen product stream itself is not by means of the Expansion machine driven cold compressor to an increased pressure brought, but a partial air flow, which is used to evaporate the liquid Oxygen flow serves under an increased pressure.
  • a greater effect can be achieved in this way, that means the discharge pressure of the oxygen is at the same loss of cold Cold compressors higher than in the previously known method.
  • the first pressure to which the first and the second partial flow of air share are compressed is slightly above the operating pressure of the pressure column.
  • the Pressure difference is preferably such that the first partial flow of air Flow resistance between the air compressor and the pressure column without pressure-changing measures can overcome, and is for example 0.1 to 0.5 bar.
  • the operating pressures at the head of the rectification columns are, for example, 2.5 to 10 bar, preferably 4 to 7 bar in the pressure column and 1.05 to 4 bar, preferably 1.1 to 1.5 bar in the low pressure column.
  • an air compressor is preferably the only one external driven machine used. This brings the total air to the first pressure, which is simultaneously the inlet pressure of the expansion machine and the cold compressor represents. In this way, the oxygen product can be released under a pressure can be obtained, for example, 0.5 to 4 bar, preferably 1 to 3 bar the operating pressure of the low pressure column is without an additional Energy consumption compared to the extraction of the oxygen product below Low pressure column pressure is connected.
  • the cold compressed partial air flow is used for indirect heat exchange with the evaporating oxygen at least partially, preferably completely or in essentially fully condensed.
  • the condensate is then released and fed to the pressure column and / or the low pressure column.
  • the method according to the invention is particularly suitable for the extraction of impure Oxygen with a purity of 80 to 99.5 mol%, preferably 90 to 95 mol% suitable under superatmospheric pressure.
  • the work-relieving relaxation can be nitrogen, for example fed from the top of the pressure column or any other fraction from the pressure column become.
  • the process stream is that of work-relieving relaxation is subjected, however, by a third partial flow to the first pressure compressed feed air formed.
  • the Braking device can for example by a brake blower and / or Brake generator be formed and is located outside of the cold box, which for Insulation of the cold parts of the apparatus is used. This allows energy to be transferred to the Given the environment and thus the cold necessary for the process without using another relaxation machine.
  • relaxation machine, cold compressor and braking device immediately mechanically coupled, for example via a common shaft.
  • the invention also relates to a device according to claim 5.
  • Atmospheric air 1 is passed through a filter 2 in an air compressor 3 compressed to a first pressure which is approximately equal to the operating pressure of the pressure column 13 is. (To overcome the line losses, the first pressure must be slightly above the Pressure column pressures are, for example, less than 1 bar, preferably 0.5 bar or less.)
  • compressed air flows through line 7 to Main heat exchanger 8 and is partially cooled there to about dew point.
  • the cold air 9 is at 10 into a first partial flow 11 and a second partial flow 12 divided up.
  • the first partial stream 11 is directly into the pressure column 13 of the Rectification system, directly above the swamp.
  • the Rectification system also has a low pressure column 14 which over a common condenser-evaporator, the main condenser 15 in Heat exchange relationship with the pressure column 13 is.
  • the second partial flow 12 is in a cold compressor 16 to a second, higher Bring pressure, via line 17 to a secondary condenser 18, which as Circulation evaporator is trained (not shown), performed, and there essential completely liquefied.
  • the liquefied air 19 is fed into the pressure column via a valve 20 13 throttled, either at the sump (see drawing) or at an intermediate point, the some theoretical or practical floors above the feed of the first partial stream 11.
  • Liquid raw oxygen 24 from the bottom of the pressure column 13 and liquid nitrogen 25 from the main condenser 15 are cooled in the subcooling countercurrent 26 and applied to the low pressure column 14 via the valves 27 and 28, respectively.
  • nitrogen-rich residual gas 29 is withdrawn and after heating in the supercooling counterflow 26 and in the main heat exchanger 8 discharged via line 30. It can also be used as a regeneration gas in the Cleaning device 6 are used (not shown).
  • liquid oxygen coincides with the required purity.
  • a portion is withdrawn liquid via line 31, by means of a pump 32 brought to the required delivery pressure and under this pressure evaporates in the secondary condenser 18.
  • the gaseous pressurized oxygen product flows via line 33 to the main heat exchanger and is via line 34 below Ambient temperature given.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Oxygen, Ozone, And Oxides In General (AREA)

Abstract

A cryogenic rectification process and assembly extract oxygen from air at above ambient atmospheric pressure. The rectification has one or more pressurized columns (13) and a low pressure column (14). Incoming ambient process air (1) is compressed to a first pressure (3) which is approximately the same as that of the pressurized column (13). A portion (11) of the pressurized incoming ambient air (7) is fed to a heat exchanger (8) and cooled prior to release in the pressurized column (13). A flow of oxygen (31) is drawn from the low pressure column (14) and brought to a pressure which is higher than that of the operating pressure in the low pressure column (14). This gas (31) is then heated in the main heat exchanger (8) and discharged as the product (34). A process flow (21) is allowed to expand (22) yielding energy, and is then charged (23) into the low-pressure column (14). A portion of the energy yielded (22) is used to power a cold compressor (16). Especially, the flow of oxygen (31) from the low-pressure column (14) is brought to the release pressure (32) in liquid form, and evaporated by an indirect exchange of heat (18) with a second portion (12, 17) of compressed ambient air (7). The second portion (12) of compressed (3) air is then further compressed by the cold compressor (16) upstream of the indirect heat exchanger (18).

Description

Die Erfindung betrifft ein Verfahren zur Gewinnung von Sauerstoff unter überatmosphärischem Druck durch Tieftemperatur-Luftzerlegung in einem Rektifiziersystem, das mindestens eine Drucksäule und eine Niederdrucksäule aufweist, wobei Einsatzluft auf einen ersten Druck verdichtet wird, der etwa gleich dem Betriebsdruck der Drucksäule ist, mindestens ein erster Teilstrom der Einsatzluft unter dem ersten Druck in einem Hauptwärmetauscher abgekühlt und in die Drucksäule eingeleitet wird, wobei der Niederdrucksäule ein Sauerstoffstrom entnommen, auf einen Abgabedruck, der höher als der Betriebsdruck der Niederdrucksäule ist, gebracht, im Hauptwärmetauscher angewärmt und als Produkt abgeführt wird, und wobei ein Prozeßstrom arbeitsleistend entspannt und in die Niederdrucksäule eingespeist wird und mindestens ein Teil der bei der arbeitsleistenden Entspannung erzeugten mechanischen Energie zum Antrieb eines Kaltverdichters verwendet wird.The invention relates to a process for the production of oxygen under superatmospheric pressure through low-temperature air separation in one Rectification system that has at least one pressure column and one low pressure column has, wherein feed air is compressed to a first pressure which is approximately equal to Operating pressure of the pressure column is at least a first partial flow of the feed air cooled to the first pressure in a main heat exchanger and into the pressure column is initiated, an oxygen flow being taken from the low pressure column a discharge pressure that is higher than the operating pressure of the low pressure column, brought, warmed in the main heat exchanger and removed as a product, and whereby a process stream relaxes work and into the low pressure column is fed in and at least part of the work-related relaxation generated mechanical energy is used to drive a cold compressor.

Ein derartiges Verfahren und eine entsprechende Vorrichtung sind aus DE 2544340 A bekannt. Hier wird die Tatsache ausgenutzt, daß die Kälteleistung einer Entspannungsturbine in vielen Fällen höher als der Kältebedarf der Anlage ist. Die überschüssige Energie wird zum Antrieb eines Kaltverdichters genutzt, der den Produktsauerstoff aus der Niederdrucksäule in gasförmigem Zustand verdichtet, bevor er im Hauptwärmetauscher angewärmt wird.Such a method and a corresponding device are known from DE 2544340 A known. Here the fact is used that the cooling capacity of a Expansion turbine is in many cases higher than the cooling requirement of the system. The Excess energy is used to drive a cold compressor that Product oxygen from the low pressure column is compressed in the gaseous state before it is warmed up in the main heat exchanger.

Der Erfindung liegt die Aufgabe zugrunde, ein derartiges Verfahren energetisch günstiger zu gestalten.The invention has for its object such a method energetically to make it cheaper.

Diese Aufgabe wird dadurch gelöst, daß der Sauerstoffstrom aus der Niederdrucksäule in flüssigem Zustand auf den Abgabedruck gebracht und durch indirekten Wärmeaustausch mit einem zweiten Teilstrom der auf den ersten Druck verdichteten Einsatzluft verdampft wird, wobei der zweite Teilstrom stromaufwärts des indirekten Wärmeaustauschs mittels des Kaltverdichters auf einen zweiten Druck gebracht wird. This object is achieved in that the oxygen flow from the low pressure column brought to the delivery pressure in the liquid state and by indirect Heat exchange with a second partial flow which compresses to the first pressure Feed air is evaporated, the second partial stream upstream of the indirect Heat exchange is brought to a second pressure by means of the cold compressor.

Bei der Erfindung wird also nicht der Sauerstoffproduktstrom selbst mittels des von der Entspannungsmaschine angetriebenen Kaltverdichters auf einen erhöhten Druck gebracht, sondern ein Teilluftstrom, der zur Verdampfung des flüssig abgezogenen Sauerstoffstroms unter einem erhöhten Druck dient. Trotz dieser indirekten Übertragung der Energie auf den Sauerstoffproduktstrom hat sich im Rahmen der Erfindung herausgestellt, daß sich auf diese Weise ein größerer Effekt erzielen läßt, das heißt der Abgabedruck des Sauerstoffs wird bei gleichem Kälteverlust am Kaltverdichter höher als bei dem vorbekannten Verfahren.In the invention, therefore, the oxygen product stream itself is not by means of the Expansion machine driven cold compressor to an increased pressure brought, but a partial air flow, which is used to evaporate the liquid Oxygen flow serves under an increased pressure. Despite this indirect Transfer of energy to the oxygen product stream has been under way Invention discovered that a greater effect can be achieved in this way, that means the discharge pressure of the oxygen is at the same loss of cold Cold compressors higher than in the previously known method.

Der erste Druck, auf den der erste und der zweite Teilstrom der Luft gemeinsam verdichtet werden, liegt geringfügig über dem Betriebsdruck der Drucksäule. Die Druckdifferenz ist vorzugsweise so bemessen, daß der erste Teilstrom der Luft den Strömungswiderstand zwischen dem Luftverdichter und der Drucksäule ohne druckverändemde Maßnahmen überwinden kann, und beträgt beispielsweise 0,1 bis 0,5 bar.The first pressure to which the first and the second partial flow of air share are compressed, is slightly above the operating pressure of the pressure column. The Pressure difference is preferably such that the first partial flow of air Flow resistance between the air compressor and the pressure column without pressure-changing measures can overcome, and is for example 0.1 to 0.5 bar.

Die Betriebsdrücke am Kopf der Rektifiziersäulen betragen beispielsweise 2,5 bis 10 bar, vorzugsweise 4 bis 7 bar in der Drucksäule und 1,05 bis 4 bar, vorzugsweise 1,1 bis 1,5 bar in der Niederdrucksäule.The operating pressures at the head of the rectification columns are, for example, 2.5 to 10 bar, preferably 4 to 7 bar in the pressure column and 1.05 to 4 bar, preferably 1.1 to 1.5 bar in the low pressure column.

Vorzugsweise wird bei dem Verfahren ein Luftverdichter als einzige extern angetriebene Maschine eingesetzt. Dieser bringt die Gesamtluft auf den ersten Druck, der gleichzeitig den Eintrittsdruck von Entspannungsmaschine und Kaltverdichter darstellt. Auf diese Weise kann das Sauerstoffprodukt unter einem Abgabedruck gewonnen werden, der beispielsweise 0,5 bis 4 bar, vorzugsweise 1 bis 3 bar über dem Betriebsdruck der Niederdrucksäule liegt, ohne daß damit ein zusätzlicher Energieverbrauch gegenüber der Gewinnung des Sauerstoffprodukts unter Niederdrucksäulendruck verbunden ist.In the method, an air compressor is preferably the only one external driven machine used. This brings the total air to the first pressure, which is simultaneously the inlet pressure of the expansion machine and the cold compressor represents. In this way, the oxygen product can be released under a pressure can be obtained, for example, 0.5 to 4 bar, preferably 1 to 3 bar the operating pressure of the low pressure column is without an additional Energy consumption compared to the extraction of the oxygen product below Low pressure column pressure is connected.

Der kaltverdichtete Teilluftstrom wird bei dem indirekten Wärmeaustausch mit dem verdampfenden Sauerstoff mindestens teilweise, vorzugsweise vollständig oder im wesentlichen vollständig kondensiert. Das Kondensat wird anschließend entspannt und der Drucksäule und/oder der Niederdrucksäule zugeleitet. The cold compressed partial air flow is used for indirect heat exchange with the evaporating oxygen at least partially, preferably completely or in essentially fully condensed. The condensate is then released and fed to the pressure column and / or the low pressure column.

Das erfindungsgemäße Verfahren ist insbesondere zur Gewinnung von unreinem Sauerstoff mit einer Reinheit von 80 bis 99,5 mol%, vorzugsweise 90 bis 95 mol% unter überatmosphärischem Druck geeignet.The method according to the invention is particularly suitable for the extraction of impure Oxygen with a purity of 80 to 99.5 mol%, preferably 90 to 95 mol% suitable under superatmospheric pressure.

Bei dem Verfahren kann der arbeitsleistenden Entspannung beispielsweise Stickstoff vom Kopf der Drucksäule oder jede andere Fraktion aus der Drucksäule zugeführt werden. Vorzugsweise wird der Prozeßstrom, der der arbeitsleistenden Entspannung unterworfen wird, jedoch durch einen dritten Teilstrom der auf den ersten Druck verdichteten Einsatzluft gebildet.In the process, the work-relieving relaxation can be nitrogen, for example fed from the top of the pressure column or any other fraction from the pressure column become. Preferably, the process stream is that of work-relieving relaxation is subjected, however, by a third partial flow to the first pressure compressed feed air formed.

Grundsätzlich ist es möglich, den indirekten Wärmeaustausch, bei dem der Produktsauerstoff gegen den kondensierenden zweiten Teilstrom der Luft verdampft, im Hauptwärmetauscher durchzuführen. Vorzugsweise ist dazu jedoch ein vom Hauptwärmetauscher getrennter Nebenkondensator vorgesehen, der als Umlaufverdampfer ausgebildet ist; alternativ dazu ist es im Prinzip auch möglich, einen Gegenstrom-Wärmetauscher oder einen Fallfilmverdampfer als Nebenkondensator einzusetzen.In principle, it is possible to use indirect heat exchange, in which the Product oxygen evaporates against the condensing second partial flow of air, to be carried out in the main heat exchanger. Preferably, however, is one of the Main heat exchanger separate sub-condenser provided as Circulation evaporator is formed; alternatively, in principle it is also possible to use one Counterflow heat exchanger or a falling film evaporator as a secondary condenser to use.

Günstig ist es außerdem, wenn ein Teil der bei der arbeitsleistenden Entspannung erzeugten mechanischen Energie an eine Bremseinrichtung abgegeben wird. Die Bremseinrichtung kann beispielsweise durch ein Bremsgebläse und/oder einen Bremsgenerator gebildet sein und befindet sich außerhalb der Coldbox, die zur Isolierung der kalten Teile des Apparats dient. Dadurch kann Energie an die Umgebung abgegeben und damit die für das Verfahren notwendige Kälte gewonnen werden, ohne daß eine weitere Entspannungsmaschine eingesetzt wird. Vorzugsweise sind Entspannungsmaschine, Kaltverdichter und Bremseinrichtung unmittelbar mechanisch gekoppelt, beispielsweise über eine gemeinsame Welle.It is also beneficial if some of the work-related relaxation generated mechanical energy is delivered to a braking device. The Braking device can for example by a brake blower and / or Brake generator be formed and is located outside of the cold box, which for Insulation of the cold parts of the apparatus is used. This allows energy to be transferred to the Given the environment and thus the cold necessary for the process without using another relaxation machine. Preferably are relaxation machine, cold compressor and braking device immediately mechanically coupled, for example via a common shaft.

Die Erfindung betrifft außerdem eine Vorrichtung gemäß Patentanspruch 5.The invention also relates to a device according to claim 5.

Die Erfindung sowie weitere Einzelheiten der Erfindung werden im folgenden anhand eines in der Zeichnung schematisch dargestellten Ausführungsbeispiels näher erläutert. The invention and further details of the invention are described below an embodiment shown schematically in the drawing explained.

Atmosphärische Luft 1 wird nach Durchströmen eines Filters 2 in einem Luftverdichter 3 auf einen ersten Druck verdichtet, der etwa gleich dem Betriebsdruck der Drucksäule 13 ist. (Zu Überwindung der Leitungsverluste muß der erste Druck etwas über dem Drucksäulendruck liegen beispielsweise von weniger als 1 bar, vorzugsweise 0,5 bar oder weniger.) Nach Entfernung der Kompressionswärme im Nachkühler 4 strömt die auf den ersten Druck verdichtete Luft 5 zu einer Reinigungseinrichtung 6, die durch ein Paar von umschaltbaren Molelukarsiebadsorbern gebildet wird. Die auf den ersten Druck verdichtete Luft fließt nach der Reinigung 6 über Leitung 7 zum Hauptwärmetauscher 8 und wird dort zu einem Teil auf etwa Taupunkt abgekühlt. Die kalte Luft 9 wird bei 10 in einen ersten Teilstrom 11 und einen zweiten Teilstrom 12 aufgeteilt. Der erste Teilstrom 11 wird direkt in die Drucksäule 13 des Rektifiziersystems eingespeist, und zwar unmittelbar oberhalb des Sumpfs. Das Rektifiziersystem weist außerdem eine Niederdrucksäule 14 auf, die über einen gemeinsamen Kondensator-Verdampfer, den Hauptkondensator 15 in Wärmeaustauschbeziehung mit der Drucksäule 13 steht.Atmospheric air 1 is passed through a filter 2 in an air compressor 3 compressed to a first pressure which is approximately equal to the operating pressure of the pressure column 13 is. (To overcome the line losses, the first pressure must be slightly above the Pressure column pressures are, for example, less than 1 bar, preferably 0.5 bar or less.) After removal of the compression heat in the aftercooler 4, the flows Air 5 compressed to the first pressure to a cleaning device 6, which by a Pair of switchable Molelukarsiebadorbern is formed. At first After cleaning 6, compressed air flows through line 7 to Main heat exchanger 8 and is partially cooled there to about dew point. The cold air 9 is at 10 into a first partial flow 11 and a second partial flow 12 divided up. The first partial stream 11 is directly into the pressure column 13 of the Rectification system, directly above the swamp. The Rectification system also has a low pressure column 14 which over a common condenser-evaporator, the main condenser 15 in Heat exchange relationship with the pressure column 13 is.

Der zweite Teilstrom 12 wird in einem Kaltverdichter 16 auf einen zweiten, höheren Druck gebracht, über Leitung 17 zu einem Nebenkondensator 18, der als Umlaufverdampfer ausgebiildet ist (nicht dargestellt), geführt, und dort wesentlichen vollständig verflüssigt. Die verflüssigte Luft 19 wird über ein Ventil 20 in die Drucksäule 13 eingedrosselt, entweder am Sumpf (siehe Zeichnung) oder an einer Zwischenstelle, die einige theoretische beziehungsweise praktische Böden oberhalb der Zuspeisung des ersten Teilstroms 11 liegt.The second partial flow 12 is in a cold compressor 16 to a second, higher Bring pressure, via line 17 to a secondary condenser 18, which as Circulation evaporator is trained (not shown), performed, and there essential completely liquefied. The liquefied air 19 is fed into the pressure column via a valve 20 13 throttled, either at the sump (see drawing) or at an intermediate point, the some theoretical or practical floors above the feed of the first partial stream 11.

Ein weiterer Anteil der auf den ersten Druck verdichteten und anschließend gereinigten Luft 7 wird bei einer Zwischentemperatur aus dem Hauptwärmetauscher 8 herausgeführt und bildet den dritten Teilstrom 21. Dieser wird in einer Entspannungsturbine 22 arbeitsleistend auf etwa Niederdrucksäulendruck entspannt und über Leitung 23 direkt zur Niederdrucksäule 14 geführt. Die Entspannungsturbine 22 ist über eine gemeinsame Welle mit dem Kaltverdichter 16 und einem nicht dargestellten Bremsgenerator gekoppelt.Another part of the compressed to the first pressure and then cleaned Air 7 is at an intermediate temperature from the main heat exchanger 8 led out and forms the third partial stream 21. This is in a Relaxation turbine 22 relaxed to work at about low pressure column pressure and led directly to low pressure column 14 via line 23. The relaxation turbine 22 is on a common shaft with the cold compressor 16 and one is not brake generator shown coupled.

Flüssiger Rohsauerstoff 24 vom Sumpf der Drucksäule 13 und flüssiger Stickstoff 25 aus dem Hauptkondensator 15 werden im Unterkühlungs-Gegenströmer 26 abgekühlt und über die Ventile 27 beziehungsweise 28 auf die Niederdrucksäule 14 aufgegeben. Liquid raw oxygen 24 from the bottom of the pressure column 13 and liquid nitrogen 25 from the main condenser 15 are cooled in the subcooling countercurrent 26 and applied to the low pressure column 14 via the valves 27 and 28, respectively.

Am Kopf der Niederdrucksäule 14 wird stickstoffreiches Restgas 29 abgezogen und nach Anwärmung im Unterkühlungs-Gegenströmer 26 und im Hauptwärmetauscher 8 über Leitung 30 abgeführt. Es kann auch als Regeneriergas in der Reinigungseinrichtung 6 eingesetzt werden (nicht dargestellt).At the top of the low pressure column 14, nitrogen-rich residual gas 29 is withdrawn and after heating in the supercooling counterflow 26 and in the main heat exchanger 8 discharged via line 30. It can also be used as a regeneration gas in the Cleaning device 6 are used (not shown).

Als Sumpfprodukt der Niederdrucksäule 14 fällt flüssiger Sauerstoff mit der erforderlichen Reinheit an. Ein Teil wird über Leitung 31 flüssig abgezogen, mittels einer Pumpe 32 auf den erforderlichen Abgabedruck gebracht und unter diesem Druck im Nebenkondensator 18 verdampft. Das gasförmige Drucksauerstoffprodukt strömt über Leitung 33 zum Hauptwärmetauscher und wird über Leitung 34 unter etwa Umgebungstemperatur abgegeben.As the bottom product of the low pressure column 14, liquid oxygen coincides with the required purity. A portion is withdrawn liquid via line 31, by means of a pump 32 brought to the required delivery pressure and under this pressure evaporates in the secondary condenser 18. The gaseous pressurized oxygen product flows via line 33 to the main heat exchanger and is via line 34 below Ambient temperature given.

Claims (5)

Verfahren zur Gewinnung von Sauerstoff unter überatmosphärischem Druck durch Tieftemperatur-Luftzerlegung in einem Rektifiziersystem, das mindestens eine Drucksäule (13) und eine Niederdrucksäule (14) aufweist, wobei Einsatzluft (1) auf einen ersten Druck verdichtet (3) wird, der etwa gleich dem Betriebsdruck der Drucksäule (13) ist, mindestens ein erster Teilstrom (11) der Einsatzluft (7) unter dem ersten Druck in einem Hauptwärmetauscher (8) abgekühlt und in die Drucksäule (13) eingeleitet wird, wobei der Niederdrucksäule (14) ein Sauerstoffstrom (31) entnommen, auf einen Abgabedruck, der höher als der Betriebsdruck der Niederdrucksäule (14) ist, gebracht (32), im Hauptwärmetauscher (8) angewärmt und als Produkt (34) abgeführt wird, und wobei ein Prozeßstrom (21) arbeitsleistend entspannt (22) und in die Niederdrucksäule (14) eingespeist (23) wird und mindestens ein Teil der bei der arbeitsleistenden Entspannung (22) erzeugten mechanischen Energie zum Antrieb eines Kaltverdichters (16) verwendet wird, dadurch gekennzeichnet, daß der Sauerstoffstrom (31) aus der Niederdrucksäule (14) im flüssigen Zustand auf den Abgabedruck gebracht (32) und durch indirekten Wärmeaustausch (18) mit einem zweiten Teilstrom (12, 17) der auf den ersten Druck verdichteten Einsatzluft (7) verdampft wird, wobei der zweite Teilstrom (12) stromaufwärts des indirekten Wärmeaustauschs (18) mittels des Kaltverdichters (16) auf einen zweiten Druck gebracht wird.Method for obtaining oxygen under superatmospheric pressure by low-temperature air separation in a rectification system which has at least one pressure column (13) and one low-pressure column (14), feed air (1) being compressed (3) to a first pressure which is approximately equal to that Operating pressure of the pressure column (13), at least a first partial flow (11) of the feed air (7) is cooled under the first pressure in a main heat exchanger (8) and introduced into the pressure column (13), the low pressure column (14) being an oxygen flow ( 31) removed, brought to a discharge pressure which is higher than the operating pressure of the low pressure column (14), 32), heated in the main heat exchanger (8) and discharged as product (34), and a process stream (21) relieving work ( 22) and in the low pressure column (14) is fed (23) and at least part of the mechanical energy generated during the relaxation work (22) to drive a Ka lt compressor (16) is used, characterized in that the oxygen flow (31) from the low pressure column (14) is brought to the discharge pressure (32) in the liquid state and by indirect heat exchange (18) with a second partial flow (12, 17) the first pressure compressed feed air (7) is evaporated, the second partial stream (12) upstream of the indirect heat exchange (18) being brought to a second pressure by means of the cold compressor (16). Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß der Prozeßstrom, der der arbeitsleistenden Entspannung (22) unterworfen wird, durch einen dritten Teilstrom (21) der auf den ersten Druck verdichteten Einsatzluft (7) gebildet wird.Method according to Claim 1, characterized in that the process stream which is subjected to the relaxation (22) which provides work is formed by a third partial stream (21) of the feed air (7) compressed to the first pressure. Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, daß der indirekte Wärmeaustausch in einem vom Hauptwärmetauscher (8) getrennten Nebenkondensator (18) durchgeführt wird.Method according to Claim 1 or 2, characterized in that the indirect heat exchange is carried out in a secondary condenser (18) which is separate from the main heat exchanger (8). Verfahren nach einem der Ansprüche 1 bis 3, dadurch gekennzeichnet, daß ein Teil der bei der arbeitsleistenden Entspannung (22) erzeugten mechanischen Energie an eine Bremseinrichtung abgegeben wird. Method according to one of claims 1 to 3, characterized in that part of the mechanical energy generated during the relaxation work (22) is delivered to a braking device. Vorrichtung zur Gewinnung von Sauerstoff unter überatmosphärischem Druck durch Tieftemperatur-Luftzerlegung, mit einem Rektifiziersystem, das mindestens eine Drucksäule (13) und eine Niederdrucksäule (14) aufweist, mit einem Luftverdichter (3) zur Verdichtung von Einsatzluft (1) auf einen ersten Druck, der etwa gleich dem Betriebsdruck der Drucksäule (13) ist, mit einer ersten Teilluftleitung (5, 7, 9, 11), die mit dem Luftverdichter (3) und der Drucksäule (13) verbunden ist und durch einen Hauptwärmetauscher (8) führt, mit einer Sauerstoffproduktleitung (31, 33, 34), die mit der Niederdrucksäule (14) verbunden ist und ein Mittel (32) zur Druckerhöhung aufweist, und mit einer Entspannungsmaschine (22), die mit einem Kaltverdichter (16) gekoppelt ist, dadurch gekennzeichnet, daß die Sauerstoffproduktleitung (31, 33, 34) zwischen der Niederdrucksäule (14) und dem Mittel (32) zur Druckerhöhung als Flüssigkeitsleitung ausgebildet ist, die mit dem Verdampfungsraum eines Kondensator-Verdampfers (18) verbunden ist, und daß die Vorrichtung eine zweite Teilluftleitung (5, 7, 9, 12, 17) aufweist, die vom Luftverdichter (3) über den Kaltverdichter (16) in den Verflüssigungsraum des Kondensator-Verdampfers (18) führt.Device for obtaining oxygen under superatmospheric pressure by low-temperature air separation, with a rectification system which has at least one pressure column (13) and a low-pressure column (14), with an air compressor (3) for compressing feed air (1) to a first pressure, which is approximately equal to the operating pressure of the pressure column (13), with a first partial air line (5, 7, 9, 11) which is connected to the air compressor (3) and the pressure column (13) and leads through a main heat exchanger (8), having an oxygen product line (31, 33, 34), which is connected to the low pressure column (14) and having means (32) for increasing the pressure, and marked with an expansion machine (22) which is coupled to a cold compressor (16) characterized that the oxygen product line (31, 33, 34) is formed between the low-pressure column (14) and the means (32) for increasing pressure as a liquid line connected to the evaporation chamber of a condensate sator-evaporator (18), and that the device has a second partial air line (5, 7, 9, 12, 17) which from the air compressor (3) via the cold compressor (16) into the liquefaction chamber of the condenser-evaporator (18 ) leads.
EP99118724A 1999-08-05 1999-09-22 Process for producing oxygen under pressure and device therefor Revoked EP1074805B1 (en)

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ATE287518T1 (en) 2005-02-15
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ES2237008T3 (en) 2005-07-16
DE19936816A1 (en) 2001-02-08

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