EP1074805B1 - Process for producing oxygen under pressure and device therefor - Google Patents
Process for producing oxygen under pressure and device therefor Download PDFInfo
- Publication number
- EP1074805B1 EP1074805B1 EP99118724A EP99118724A EP1074805B1 EP 1074805 B1 EP1074805 B1 EP 1074805B1 EP 99118724 A EP99118724 A EP 99118724A EP 99118724 A EP99118724 A EP 99118724A EP 1074805 B1 EP1074805 B1 EP 1074805B1
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- EP
- European Patent Office
- Prior art keywords
- pressure
- air
- pressure column
- low
- column
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Classifications
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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
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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
- F25J3/04248—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
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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
- F25J3/04406—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
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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
- 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 method for the production of oxygen according to the Preamble of claim 1.
- the invention is based on the object, such a method energetically cheaper.
- the first pressure, on which the first and the second partial flow of the air in common be compacted, is slightly above the operating pressure of the pressure column.
- the Pressure difference is preferably such that the first partial flow of the air Flow resistance between the air compressor and the pressure column without can overcome pressure-changing measures, and is for example 0.1 to 0.5 bar.
- the operating pressures at the top 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 the only one external used driven machine. This brings the total air to the first pressure, at the same time the inlet pressure of expansion machine and cold compressor represents.
- the oxygen product can under a discharge pressure be obtained, for example, 0.5 to 4 bar, preferably 1 to 3 bar over the operating pressure of the low pressure column, without that an additional Energy consumption compared to the recovery of the oxygen product Low pressure column pressure is connected.
- the cold-compressed partial air flow is in the indirect heat exchange with the evaporating oxygen at least partially, preferably completely or in the essentially completely condensed.
- the condensate is then released and fed to the pressure column and / or the low pressure column.
- the process of the invention is particularly for the production of impure Oxygen with a purity of 80 to 99.5 mol%, preferably 90 to 95 mol% suitable under superatmospheric pressure.
- the process stream, the work performing relaxation is subjected, however, by a third partial flow of the first pressure formed compressed compressed air.
- the indirect heat exchange in which the Product oxygen vaporizes against the condensing second partial stream of air, in the main heat exchanger.
- the Separate secondary condenser provided as the main heat exchanger Circulation evaporator is formed;
- a Countercurrent heat exchanger or a falling film evaporator as secondary condenser use.
- the Brake device can, for example, by a brake fan and / or a Brake generator can be formed and located outside the coldbox, the to Insulation of the cold parts of the apparatus is used. This can give energy to the Given environment and thus won the necessary for the process cold be without an additional relaxation machine is used.
- 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 after flowing 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 pressure are, for example, less than 1 bar, preferably 0.5 bar or less.)
- After removal of the compression heat in the aftercooler 4 flows compressed air to the first pressure 5 to a cleaning device 6, by a A pair of reversible molecular electroluminescent adsorbents is formed.
- the first Pressure compressed air flows after cleaning 6 via line 7 to Main heat exchanger 8 and is cooled there in part to about dew point.
- the cold air 9 is at 10 in a first partial flow 11 and a second partial flow 12th divided up.
- the first partial flow 11 is directly into the pressure column 13 of the Rectifier fed directly above the sump.
- the Rectification system also has a low-pressure column 14, which has a common condenser-evaporator, the main capacitor 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 Pressure, via line 17 to a secondary capacitor 18, as Circulation evaporator is madebiildet (not shown), guided, and there essential completely liquefied.
- the liquefied air 19 is via a valve 20 in the pressure column 13 throttled, either at the bottom (see drawing) or at an intermediate point, some theoretical or practical soils above the feed of the first partial flow 11 is located.
- Another proportion of the first pressure compressed and then purified Air 7 is at an intermediate temperature from the main heat exchanger. 8 led out and forms the third partial flow 21.
- This is in a Relaxation turbine 22 work-performing relaxed to about low-pressure column pressure and passed via line 23 directly to the low pressure column 14.
- the relaxation turbine 22 is over a common shaft with the cold compressor 16 and not one coupled brake generator coupled.
- 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 abandoned via the valves 27 and 28 to the low-pressure column 14.
- nitrogen-rich residual gas 29 is withdrawn and after heating in the subcooling countercurrent 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 falls with the required purity.
- a part is withdrawn via line 31 liquid, by means a pump 32 brought to the required discharge pressure and under this pressure evaporated in the secondary condenser 18.
- the gaseous pressure oxygen product flows via line 33 to the main heat exchanger and is via line 34 below about Ambient temperature delivered.
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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
Description
Die Erfindung betrifft ein Verfahren zur Gewinnung von Sauerstoff gemäß dem
Oberbegriff des Patentanspruchs 1.The invention relates to a method for the production of oxygen according to the
Preamble of
Ein derartiges Verfahren und eine entsprechende Vorrichtung sind aus US 5626036 bekannt.Such a method and a corresponding device are known from US 5626036 known.
Der Erfindung liegt die Aufgabe zugrunde, ein derartiges Verfahren energetisch günstiger zu gestalten.The invention is based on the object, such a method energetically cheaper.
Diese Aufgabe wird durch die Merkmale des Anspruchs 1 gelöst. This object is solved by the features of
Bei der Erfindung wird nicht der Sauerstoffproduktstrom selbst mittels des von der Entspannungsmaschine angetriebenen Kaltverdichters auf einen erhöhten Druck gebracht, wie es in DE 2544350 A beschrieben wird, sondem 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, not the oxygen product stream itself by means of the Relaxation machine driven cold compressor to increased pressure brought as described in DE 2544350 A, but a partial air flow, the Evaporation of the liquid withdrawn oxygen stream under an elevated pressure serves. Despite this indirect transfer of energy to the oxygen product stream has been found within the scope of the invention that in this way a Achieves greater effect, that is, the discharge pressure of the oxygen is at same cold loss at the cold compressor higher than in the prior art 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, on which the first and the second partial flow of the air in common be compacted, is slightly above the operating pressure of the pressure column. The Pressure difference is preferably such that the first partial flow of the air Flow resistance between the air compressor and the pressure column without can overcome pressure-changing measures, 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 top 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.Preferably, in the method, an air compressor is the only one external used driven machine. This brings the total air to the first pressure, at the same time the inlet pressure of expansion machine and cold compressor represents. In this way, the oxygen product can under a discharge pressure be obtained, for example, 0.5 to 4 bar, preferably 1 to 3 bar over the operating pressure of the low pressure column, without that an additional Energy consumption compared to the recovery of the oxygen product 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 in the indirect heat exchange with the evaporating oxygen at least partially, preferably completely or in the essentially completely 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 process of the invention is particularly for the production 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 method of work-performing expansion, for example, nitrogen supplied from the head of the pressure column or any other fraction from the pressure column become. Preferably, the process stream, the work performing relaxation is subjected, however, by a third partial flow of the first pressure formed compressed compressed air.
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.Basically, it is possible, the indirect heat exchange, in which the Product oxygen vaporizes against the condensing second partial stream of air, in the main heat exchanger. Preferably, however, is one of the Separate secondary condenser provided as the main heat exchanger Circulation evaporator is formed; Alternatively, it is also possible in principle, a Countercurrent heat exchanger or a falling film evaporator as secondary condenser 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 a part of the work-relaxing generated mechanical energy is delivered to a braking device. The Brake device can, for example, by a brake fan and / or a Brake generator can be formed and located outside the coldbox, the to Insulation of the cold parts of the apparatus is used. This can give energy to the Given environment and thus won the necessary for the process cold be without an additional relaxation machine is used. 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
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 schematically shown 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 Molelukarsiebadsorbem 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.
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
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 proportion of the first pressure compressed and then purified
Air 7 is at an intermediate temperature from the main heat exchanger. 8
led out and forms the third
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
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-
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-
Claims (8)
- Process for obtaining oxygen under super-atmospheric pressure by low-temperature fractionation of air in a rectification system which has at least a pressure column (13) and a low-pressure column (14), feed air (1) being compressed (3) to a first pressure, which is approximately equal to the operating pressure of the pressure column (13), at least a first part-stream (11) of the feed air (7) which is under the first pressure being cooled in a principal heat exchanger (8) and being introduced into the pressure column (13), a second part-stream (12, 17) of the feed air (7) which has been compressed to the first pressure being brought (16) to a second pressure, an oxygen stream (31) being removed from the low-pressure column (14), brought (32), in the liquid state, to a release pressure which is higher than the operating pressure of the low-pressure column (14), being evaporated by indirect heat exchange (18) with the second part-stream (12, 17) downstream of the compression (16) to the second pressure, being heated in the principal heat exchanger (8) and being discharged as product (34), and a process stream (21) being subjected to work-performing expansion (22) and being fed (23) into the low-pressure column (14), characterized in that the second part-stream (12), upstream of the indirect heat exchange (18), is brought to the second pressure by means of a cold compressor (16), and at least some of the mechanical energy generated during the work-performing expansion (22) is used to drive the cold compressor (16).
- Process according to Claim 1, characterized in that the process stream, which is subjected to the work-performing expansion (22), is formed by a third part-stream (21) of the feed air (7) which has been compressed to the first pressure.
- Process according to Claim 1 or 2, characterized in that the indirect heat exchange is carried out in an auxiliary condenser (18) which is separate from the principal heat exchanger (8).
- Process according to any of Claims 1 to 3, characterized in that some of the mechanical energy generated during the work-performing expansion (22) is released to a braking device.
- Apparatus for obtaining oxygen under super-atmospheric pressure by low-temperature fractionation of air, having a rectification system which has at least a pressure column (13) and a low-pressure column (14), having 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), having 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 principal heat exchanger (8), having an oxygen product line (31, 33, 34), which is connected to the low-pressure column (14), has a means (32) for increasing pressure, is formed as a liquid line between the low-pressure column (14) and the means (32) for increasing pressure, and is connected to the evaporation space of a condenser-evaporator (18), having a second partial air line (5, 7, 9, 12, 17), which leads from the air compressor (3) via a recompressor (16) into the liquefaction space of the condenser/evaporator (18), and having an expansion machine (22), characterized in that the recompressor is designed as a cold compressor (16), and in that the expansion machine (22) is coupled to the cold compressor (16).
- Apparatus according to Claim 5, characterized by a third partial air line (21), which leads from the air compressor (3) to the expansion machine (22).
- Apparatus according to Claim 5 or 6, characterized in that the condenser-evaporator (18) is formed by an auxiliary condenser (18) which is separate from the principle heat exchanger (8).
- Apparatus according to any of Claims 5 to 7, characterized in that the expansion machine (22) is coupled to a braking device.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE19936816 | 1999-08-05 | ||
DE19936816A DE19936816A1 (en) | 1999-08-05 | 1999-08-05 | Method and device for extracting oxygen under superatmospheric pressure |
Publications (2)
Publication Number | Publication Date |
---|---|
EP1074805A1 EP1074805A1 (en) | 2001-02-07 |
EP1074805B1 true EP1074805B1 (en) | 2005-01-19 |
Family
ID=7917229
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP99118724A Revoked EP1074805B1 (en) | 1999-08-05 | 1999-09-22 | Process for producing oxygen under pressure and device therefor |
Country Status (5)
Country | Link |
---|---|
US (1) | US6332337B1 (en) |
EP (1) | EP1074805B1 (en) |
AT (1) | ATE287518T1 (en) |
DE (2) | DE19936816A1 (en) |
ES (1) | ES2237008T3 (en) |
Families Citing this family (20)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2830928B1 (en) | 2001-10-17 | 2004-03-05 | Air Liquide | PROCESS FOR SEPARATING AIR BY CRYOGENIC DISTILLATION AND AN INSTALLATION FOR CARRYING OUT SAID METHOD |
DE102007031765A1 (en) | 2007-07-07 | 2009-01-08 | Linde Ag | Process for the cryogenic separation of air |
DE102007031759A1 (en) | 2007-07-07 | 2009-01-08 | Linde Ag | Method and apparatus for producing gaseous pressure product by cryogenic separation of air |
DE102009034979A1 (en) | 2009-04-28 | 2010-11-04 | Linde Aktiengesellschaft | Method for producing pressurized oxygen by evaporating liquid oxygen using a copper and nickel heat exchanger block |
EP2312248A1 (en) | 2009-10-07 | 2011-04-20 | Linde Aktiengesellschaft | Method and device for obtaining pressurised oxygen and krypton/xenon |
DE102010052544A1 (en) | 2010-11-25 | 2012-05-31 | Linde Ag | Process for obtaining a gaseous product by cryogenic separation of air |
DE102010052545A1 (en) | 2010-11-25 | 2012-05-31 | Linde Aktiengesellschaft | Method and apparatus for recovering a gaseous product by cryogenic separation of air |
EP2520886A1 (en) | 2011-05-05 | 2012-11-07 | Linde AG | Method and device for creating gaseous oxygen pressurised product by the cryogenic decomposition of air |
DE102011112909A1 (en) | 2011-09-08 | 2013-03-14 | Linde Aktiengesellschaft | Process and apparatus for recovering steel |
EP2600090B1 (en) | 2011-12-01 | 2014-07-16 | Linde Aktiengesellschaft | Method and device for generating pressurised oxygen by cryogenic decomposition of air |
DE102011121314A1 (en) | 2011-12-16 | 2013-06-20 | Linde Aktiengesellschaft | Method for producing gaseous oxygen product in main heat exchanger system in distillation column system, involves providing turbines, where one of turbines drives compressor, and other turbine drives generator |
DE102012017488A1 (en) | 2012-09-04 | 2014-03-06 | Linde Aktiengesellschaft | Method for building air separation plant, involves selecting air separation modules on basis of product specification of module set with different air pressure requirements |
EP2784420A1 (en) | 2013-03-26 | 2014-10-01 | Linde Aktiengesellschaft | Method for air separation and air separation plant |
WO2014154339A2 (en) | 2013-03-26 | 2014-10-02 | Linde Aktiengesellschaft | Method for air separation and air separation plant |
EP2801777A1 (en) | 2013-05-08 | 2014-11-12 | Linde Aktiengesellschaft | Air separation plant with main compressor drive |
DE102013017590A1 (en) | 2013-10-22 | 2014-01-02 | Linde Aktiengesellschaft | Method for recovering methane-poor fluids in liquid air separation system to manufacture air product, involves vaporizing oxygen, krypton and xenon containing sump liquid in low pressure column by using multi-storey bath vaporizer |
EP2963369B1 (en) | 2014-07-05 | 2018-05-02 | Linde Aktiengesellschaft | Method and device for the cryogenic decomposition of air |
EP2963370B1 (en) | 2014-07-05 | 2018-06-13 | Linde Aktiengesellschaft | Method and device for the cryogenic decomposition of air |
EP2963367A1 (en) | 2014-07-05 | 2016-01-06 | Linde Aktiengesellschaft | Method and device for cryogenic air separation with variable power consumption |
EP2963371B1 (en) | 2014-07-05 | 2018-05-02 | Linde Aktiengesellschaft | Method and device for creating a pressurised gas product by the cryogenic decomposition of air |
Family Cites Families (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE2544340A1 (en) | 1975-10-03 | 1977-04-14 | Linde Ag | PROCEDURE FOR AIR SEPARATION |
US4702757A (en) * | 1986-08-20 | 1987-10-27 | Air Products And Chemicals, Inc. | Dual air pressure cycle to produce low purity oxygen |
US5315833A (en) * | 1991-10-15 | 1994-05-31 | Liquid Air Engineering Corporation | Process for the mixed production of high and low purity oxygen |
US5228296A (en) * | 1992-02-27 | 1993-07-20 | Praxair Technology, Inc. | Cryogenic rectification system with argon heat pump |
US5379598A (en) * | 1993-08-23 | 1995-01-10 | The Boc Group, Inc. | Cryogenic rectification process and apparatus for vaporizing a pumped liquid product |
US5355682A (en) * | 1993-09-15 | 1994-10-18 | Air Products And Chemicals, Inc. | Cryogenic air separation process producing elevated pressure nitrogen by pumped liquid nitrogen |
FR2711778B1 (en) * | 1993-10-26 | 1995-12-08 | Air Liquide | Process and installation for the production of oxygen and / or nitrogen under pressure. |
US5386692A (en) * | 1994-02-08 | 1995-02-07 | Praxair Technology, Inc. | Cryogenic rectification system with hybrid product boiler |
GB9410686D0 (en) * | 1994-05-27 | 1994-07-13 | Boc Group Plc | Air separation |
FR2724011B1 (en) * | 1994-08-29 | 1996-12-20 | Air Liquide | PROCESS AND PLANT FOR THE PRODUCTION OF OXYGEN BY CRYOGENIC DISTILLATION |
US5765396A (en) * | 1997-03-19 | 1998-06-16 | Praxair Technology, Inc. | Cryogenic rectification system for producing high pressure nitrogen and high pressure oxygen |
-
1999
- 1999-08-05 DE DE19936816A patent/DE19936816A1/en not_active Withdrawn
- 1999-09-22 DE DE59911495T patent/DE59911495D1/en not_active Expired - Lifetime
- 1999-09-22 EP EP99118724A patent/EP1074805B1/en not_active Revoked
- 1999-09-22 AT AT99118724T patent/ATE287518T1/en active
- 1999-09-22 ES ES99118724T patent/ES2237008T3/en not_active Expired - Lifetime
-
2000
- 2000-08-07 US US09/634,006 patent/US6332337B1/en not_active Expired - Fee Related
Also Published As
Publication number | Publication date |
---|---|
EP1074805A1 (en) | 2001-02-07 |
US6332337B1 (en) | 2001-12-25 |
DE59911495D1 (en) | 2005-02-24 |
ES2237008T3 (en) | 2005-07-16 |
ATE287518T1 (en) | 2005-02-15 |
DE19936816A1 (en) | 2001-02-08 |
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