EP1050728B1 - Single column process and device for cryogenic air separation - Google Patents

Single column process and device for cryogenic air separation Download PDF

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Publication number
EP1050728B1
EP1050728B1 EP00108864A EP00108864A EP1050728B1 EP 1050728 B1 EP1050728 B1 EP 1050728B1 EP 00108864 A EP00108864 A EP 00108864A EP 00108864 A EP00108864 A EP 00108864A EP 1050728 B1 EP1050728 B1 EP 1050728B1
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EP
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Prior art keywords
single column
air
charge
column
pressure
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EP00108864A
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German (de)
French (fr)
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EP1050728A1 (en
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Jürgen Dipl.-Phys. Voit
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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
    • F25J3/04248—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
    • F25J3/04296—Claude expansion, i.e. expanded into the main or 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
    • F25J3/04006—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
    • 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
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)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
    • 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
    • F25J3/044—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 single pressure main column system only
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/72—Refluxing the column with at least a part of the totally condensed overhead gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being nitrogen

Definitions

  • the invention relates to a single column method according to the preamble of Patent claim 1.

Abstract

Gas generation single-column fractionated distillation of air operates at lower pressure, reducing energy requirement withou sacrifice of process yield. A single-column process and assembly produces gases by the cryogenic fractionated distillation of air. The compressed incom air feed (101, 102, 103, 110) is first cooled (104) and fed (105, 114) to the column (107). An oxygen-rich liquid fraction (116) drawn from the column (107) and expanded (117) and fed to a condenser-evaporator (118). The oxygen is evaporated (118) by an indirect exchange of heat from condensed nitrogen (120) drawn from the upper section of the column (107). A portion (131) of the vapor (129, 130) generated by the condenser-evaporator (118) is compressed and fed (134, 135) to the column (118). A portion (10 110, 11) of the air feed (101) is released into the column (107) upstream of the inlet (114), where it decompresses to release energy.

Description

Die Erfindung betrifft ein Einzelsäulenverfahren gemäß dem Oberbegriff des Patentanspruchs 1.The invention relates to a single column method according to the preamble of Patent claim 1.

Ein derartiges Verfahren ist beispielsweise aus der EP-A-343065 bekannt. Hier wird Restgas aus dem sumpfflüssigkeitsbetriebenen Kopfkondensator der Einzelsäule in die Einzelsäule zurückgeführt. Dies führt zu einer Erhöhung der Reinheit des sauerstoffangereicherten Produkts und damit zu einer Verbesserung der Stickstoffausbeute. Kälte wird bei dem Verfahren durch Entspannung desjenigen Teils des Restgases aus dem Kopfkondensator erzeugt, der nicht in die Säule zurückgeführt wird.Such a method is known for example from EP-A-343065. Here is Residual gas from the sump liquid operated top condenser of the single column in the Returned to a single column. This leads to an increase in the purity of the oxygen-enriched product and thus to an improvement in the Nitrogen yield. Cold is in the process by relaxation of that part the residual gas generated from the top condenser, which is not returned to the column becomes.

Bei diesem Prozeß muß die Einzelsäule unter einem relativ hohen Druck (beispielsweise etwa 9 bar) betrieben werden. Dadurch wird relativ viel Energie bei der Verdichtung der Einsatzluft verbraucht und die Produktausbeute ist relativ niedrig.In this process, the single column must be under a relatively high pressure (For example, about 9 bar) are operated. This is relatively much energy in the Consumption of feed air consumed and the product yield is relatively low.

Der Erfindung liegt daher die Aufgabe zugrunde, ein Einzelsäulenverfahren der eingangs genannten Art und eine entsprechende Vorrichtung anzugeben, die wirtschaftlich günstiger sind, insbesondere durch einen besonders geringen Energieverbrauch und/oder eine besonders hohe Produktausbeute.The invention is therefore based on the object, a single column method of specify the type mentioned above and a corresponding device, the are economically favorable, in particular by a particularly low Energy consumption and / or a particularly high product yield.

Diese Aufgabe wird dadurch gelöst, daß mindestens ein Teil der Einsatzluft stromaufwärts der Einleitung in die Einzelsäule arbeitsleistend entspannt wird.This object is achieved in that at least a portion of the feed air upstream of the introduction into the single column work is relaxed.

Bei der Erfindung wird zur Erzeugung der für das Verfahren benötigten Kälte nicht sauerstoffreicher Dampf aus dem Kondensator-Verdampfer entspannt, sondern mindestens ein Teil der Einsatzluft. Dadurch kann die Einzelsäule unter einem niedrigeren Druck betrieben werden, was zum einen zu einem verminderten Energiebedarf bei der Luftverdichtung führt und zum anderen eine erhöhte Produktausbeute aufgrund der erhöhten relativen Flüchtigkeit der Hauptkomponenten der Luft bewirkt. Der Betriebsdruck am Kopf der Einzelsäule beträgt beispielsweise 2 bis 5 bar, vorzugsweise 3 bis 4 bar. Der Energieverbrauch ist am günstigsten, wenn der Betriebsdruck der Einzelsäule so eingestellt wird, daß der Druck auf der Verdampfungsseite des Kondensator-Verdampfers gerade ausreicht, um einen Teil der verdampften sauerstoffreichen Fraktion aus dem Verfahren zu entfernen und/oder als Regeneriergas in einer Reinigungseinrichtung für die Einsatzluft zu verwenden.The invention does not produce the refrigeration needed for the process oxygen-rich vapor from the condenser-evaporator relaxes, but at least part of the feed air. This allows the single column under a operated lower pressure, resulting in a reduced to a Energy demand in the air compression leads and on the other an increased Product yield due to the increased relative volatility of the major components the air causes. The operating pressure at the top of the single column is for example 2 up to 5 bar, preferably 3 to 4 bar. Energy consumption is the cheapest if the operating pressure of the single column is adjusted so that the pressure on the Evaporating side of the condenser-evaporator is just enough to part of the vaporized oxygen-rich fraction from the process to remove and / or as To use regeneration gas in a cleaning device for the feed air.

Die sauerstoffreiche Fraktion wird im allgemeinen durch die Sumpfflüssigkeit der Einzelsäule gebildet Sie kann aber auch teilweise oder vollständig oberhalb der Zuspeisestelle der Einsatzluft aus der Säule abgezogen werden.The oxygen-rich fraction is generally due to the bottom liquid of the It can also be partially or completely above the Feed point of the feed air are withdrawn from the column.

Es ist günstig, wenn die Einsatzluft an einer Zwischenstelle in die Einzelsäule eingespeist wird. Die Stelle der Zuleitung der rückverdichteten sauerstoffreichen Fraktion liegt vorzugsweise unterhalb dieser Zwischenstelle, an der die Einsatzluft eingeleitet wird, in der Regel unmittelbar am Sumpf der Säule. Es befinden sich beispielsweise 2 bis 12 praktische beziehungsweise theoretische Böden zwischen der Zwischenstelle und der Einspeisung der rückverdichteten sauerstoffreichen Fraktion.It is favorable if the feed air at an intermediate point in the single column is fed. The place of supply of the recompressed oxygen-rich Fraction is preferably below this intermediate point at which the feed air is introduced, usually directly at the bottom of the column. There are For example, 2 to 12 practical or theoretical plates between the Intermediate point and the feed of the recompressed oxygen-rich fraction.

Derjenige Teil der sauerstoffangereicherten Fraktion, der nicht in die Säule zurückgeführt wird, kann - stromaufwärts und/oder stromabwärts der Rückverdichtung als gasförmiges Sauerstoffprodukt (Reinheit beispielsweise 30 bis 99,8 vol%; es ist aber auch jede beliebige höhere Reinheit erreichbar) abgezogen, als Restgas verworfen und/oder als Regeneriergas für eine Reinigungseinrichtung für die Einsatzluft eingesetzt werden.The part of the oxygen-enriched fraction that does not enter the column can be recycled, upstream and / or downstream of recompression as a gaseous oxygen product (purity, for example, 30 to 99.8 vol%, it is but also any higher purity achievable) deducted, as residual gas discarded and / or as a regeneration gas for a cleaning device for the Feed air can be used.

Die Entspannungsmaschine zur arbeitsleistenden Entspannung von Einsatzluft wird vorzugsweise durch eine Turbine gebildet, die beispielsweise durch einen Generator, oder durch einen Verdichter für Einsatzluft beziehungsweise ein Produktgas gebremst wird.The relaxation machine for job-creating relaxation of feed air is preferably formed by a turbine, for example by a generator, or braked by a compressor for feed air or a product gas becomes.

Das Verfahren der Erfindung ist auch apparate- und regeltechnisch relativ einfach. Es kommt im Vergleich zu anderen Prozessen, die zwei oder mehr Turbinen und/oder zwei oder mehr Kondensatoren aufweisen, mit einer einzigen Turbine und einem einzigen Kondensator-Verdampfer aus.The process of the invention is also relatively simple in terms of apparatus and control technology. It comes in comparison to other processes, the two or more turbines and / or have two or more capacitors, with a single turbine and a single condenser evaporator off.

Bei dem erfindungsgemäßen Verfahren ist es günstig, wenn ein erster Teil der Einsatzluft, der unter einem ersten Druck steht, abgekühlt, teilweise verflüssigt und der Einzelsäule zugeleitet wird und wenn ein zweiter Teil der Einsatzluft auf einen zweiten Druck gebracht wird, der höher als der erste Druck ist, anschließend auf eine Zwischentemperatur oberhalb der Betriebstemperatur der Einzelsäule abgekühlt, der arbeitsleistenden Entspannung zugeführt und in die Einzelsäule eingeleitet wird. Vorzugsweise werden der erste und der zweite Teil der Einsatzluft der Einzelsäule an einer ersten beziehungsweise zweiten Zwischenstelle zugespeist, wobei die zweite Zwischenstelle mindestens einen theoretischen oder praktischen Boden oberhalb der ersten Zwischenstelle angeordnet ist.In the method according to the invention, it is favorable if a first part of the Feed air, which is under a first pressure, cooled, partially liquefied and the Single column is fed and if a second part of the feed air to a second Pressure is higher than the first pressure, then on a Intermediate temperature above the operating temperature of the single column cooled, the supplied work-performing relaxation and introduced into the single column. Preferably, the first and the second part of the feed air to the single column fed to a first and second intermediate point, wherein the second Intermediate at least one theoretical or practical ground above the first intermediate point is arranged.

Durch die getrennte Einspeisung der teilweise verflüssigten und der arbeitsleistenden entspannten Luft wird die Rektifizierwirkung der Einzelsäule weiter verbessert und damit die Produktausbeute erhöht.Due to the separate feed of the partially liquefied and the work relaxed air the rectification effect of the single column is further improved and thus increasing the product yield.

Dabei ist es günstig, wenn der erste und der zweite Teil der Einsatzluft gemeinsam auf den ersten Druck verdichtet werden und der zweite Teil der Einsatzluft in einem Nachverdichter auf den zweiten Druck nachverdichtet wird.It is advantageous if the first and the second part of the feed air together the first pressure to be compressed and the second part of the feed air in one After-compressor is recompressed to the second pressure.

Die Erfindung betrifft außerdem eine Vorrichtung gemäß den Patentansprüchen 4 bis 6.The invention also relates to a device according to claims 4 to 6th

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

Gereinigte und auf einen ersten Druck verdichtete Luft 101 wird herangeführt und in einen ersten Teil 102 und einen zweiten Teil 103 aufgeteilt. Der erste Luftteil 102 strömt dem warmen Ende eines Hauptwärmetauschers 104 zu und wird dort gegen Rückströme abgekühlt und teilweise verflüssigt. Der erste Luftteil wird dann über Leitung 105 der Einzelsäule 107 an einer ersten Zwischenstelle 106 zugeführt. Der zweite Teil 103 der Einsatzluft wird in einem Nachverdichter 108 auf einen zweiten, höheren Druck nachverdichtet, nachgekühlt (109) und über Leitung 110 zum Hauptwärmetauscher 104 geführt. Der zweite Luftteil verläßt den Hauptwärmetauscher bei einer Zwischentemperatur über Leitung 111 und wird in einer Turbine 112 arbeitsleistend entspannt, die von einem Generator 113 gebremst wird. Die arbeitsleistend entspannte Luft wird über Leitung 114 zu einer zweiten Zwischenstelle 115 der Einzelsäule 107 geführt.Purified and compressed to a first pressure air 101 is introduced and in a first part 102 and a second part 103 divided. The first air part 102 flows to the warm end of a main heat exchanger 104 and is there against Reverse streams cooled and partially liquefied. The first air part is then over Line 105 of the single column 107 is supplied at a first intermediate point 106. Of the second part 103 of the feed air is in a secondary compressor 108 to a second, recompressed higher pressure, postcooled (109) and via line 110 to Main heat exchanger 104 out. The second air part leaves the main heat exchanger at an intermediate temperature via line 111 and is in a turbine 112 work performed relaxed, which is braked by a generator 113. The working air released air is via line 114 to a second intermediate point 115 of the single column 107 out.

Die sauerstoffreiche Fraktion wird in dem Ausführungsbeispiel durch die Sumpfflüssigkeit 116 der Einzelsäule gebildet. Sie wird entspannt (117) und in den Verdampfungsraum eines Kondensator-Verdampfers 118, des Kopfkondensators der Einzelsäule, eingeführt und dort mindestens teilweise verdampft.The oxygen-rich fraction is in the embodiment by the Sump liquid 116 formed the single column. She is relaxed (117) and in the Evaporation space of a condenser-evaporator 118, the top condenser of Single column, introduced and there at least partially evaporated.

Gasförmiger Kopfstickstoff 119 wird mindestens zum Teil über Leitung 120 dem Verflüssigungsraum des Kondensator-Verdampfers 118 zugeleitet. Das dort entstandene Kondensat 121 wird mindestens zum Teil 122 als Rücklauf auf die Einzelsäule 107 aufgegeben. Ein anderer Teil 123 kann bei Bedarf als Flüssigprodukt abgeführt werden.Gaseous nitrogen head 119 is at least partially via line 120 the Liquefied space of the condenser-evaporator 118 fed. That there resulting condensate 121 is at least in part 122 as a return to the Single column 107 abandoned. Another part 123 may be liquid as needed be dissipated.

Ein Teil 124 des gasförmigen Kopfstickstoffs 119 wird im Hauptwärmetauscher 104 auf etwa Umgebungstemperatur angewärmt und als gasförmiges Stickstoffprodukt 125 abgeführt. Falls der Stickstoff unter höherem als Kolonnendruck benötigt wird, kann er in einem Produktverdichter 126 auf diesen höheren Druck gebracht werden. Die Verdichtungswärme kann in einem Nachkühler 127 entfernt werden.A portion 124 of the gaseous head nitrogen 119 is in the main heat exchanger 104 warmed to about ambient temperature and as gaseous nitrogen product 125 dissipated. If the nitrogen is needed under higher than column pressure, he can be brought in a product compressor 126 to this higher pressure. The Compaction heat can be removed in an aftercooler 127.

Aus dem Verdampfungsraum des Kondensator-Verdampfers 118 wird aus Sicherheitsgründen zumindest eine kleine Spülmenge flüssig über Leitung 128 entnommen. Falls Bedarf für ein flüssiges Sauerstoffprodukt besteht, kann eine entsprechend höhere Menge über die Leitung 128 abgeführt werden.From the evaporation space of the condenser-evaporator 118 turns off For safety reasons, at least a small amount of flush liquid via line 128 taken. If there is a need for a liquid oxygen product, a correspondingly higher amount are discharged via the line 128.

Der in dem Kondensator-Verdampfer 118 verdampfte Teil 129 der sauerstoffreichen Fraktion wird im Hauptwärmetauscher 104 angewärmt. Ein erster Teil 131 der angewärmten sauerstoffreichen Fraktion 130 wird in einem Rückverdichter 132 auf etwas über den Betriebsdruck der Einzelsäule gebracht, nach Entfernung 133 der Verdichtungswärme über Leitung 134 zum Hauptwärmetauscher und schließlich über Leitung 135 zum Sumpf der Einzelsäule geführt. The portion 129 of the oxygen-rich vaporized in the condenser-evaporator 118 Fraction is heated in the main heat exchanger 104. A first part 131 of the warmed oxygen-rich fraction 130 is in a recompressor 132 on slightly above the operating pressure of the single column, after removal 133 of the Compression heat via line 134 to the main heat exchanger and finally over Line 135 led to the bottom of the single column.

Der Rest 136 der angewärmten sauerstoffreichen Fraktion 130 wird als gasförmiges Sauerstoffprodukt 137 abgezogen und/oder als Regeneriergas 138 für die nicht dargestellte Reinigungseinrichtung für die Einsatzluft verwendet.The remainder 136 of the warmed oxygen-rich fraction 130 is called gaseous Obtained oxygen product 137 and / or as a regeneration gas 138 for not shown used cleaning device for the feed air.

Die folgenden Tabellen zeigen zwei konkrete Zahlenbeispiele für das Verfahren und die Vorrichtung, die in der Zeichnung schematisch dargestellt sind. Pos. Nr. T [K] P [bara] F [Nm 3 w/h] VF [%] N 2 [%] Ar [%] O 2 [%] 2 298 3,91 44268 100 78,118 0,932 20,95 3 298 3,91 3453 100 78,118 0,932 20,95 4 298 3,91 40815 100 78,118 0,932 20,95 5 298 9,49 3453 100 78,118 0,932 20,95 6 143 9,39 3453 100 78,118 0,932 20,95 7 113 3,77 3453 100 78,118 0,932 20,95 8 102 3,82 15215 97,4 32,4 2,6 65,0 9 95 3,81 40815 96,5 78,118 0,932 20,95 10 98 3,82 29483 0 32,4 2,6 65,0 11 90 1,30 29483 100 32,4 2,6 65,0 12 90 1,30 29483 100 32,4 2,6 65,0 13 90 3,66 30000 100 99,86 0,14 1 ppm 14 297 3,56 30000 100 99,86 0,14 1 ppm 15 297 1,20 14268 100 32,4 2,6 65,0 Pos. Nr. T [K] P [bara] F [Nm 3 /h] VF [%] N 2 [%] Ar [%] O 2 [%] 2 298 4,82 38488 100 78,118 0,932 20,95 3 298 4,82 8903 100 78,118 0,932 20,95 4 298 4,82 29585 100 78,118 0,932 20,95 5 298 7,01 8903 100 78,118 0,932 20,95 6 115 6,91 8903 100 78,118 0,932 20,95 7 104 4,72 8903 100 78,118 0,932 20,95 8 108 4,75 23660 97 1 4 95,00 9 97 4,72 29585 95 78,118 0,932 20,95 10 108 4,75 32148 0 1 4 95,00 11 92 1,3 32148 100 1 4 95,00 12 92 1,3 32148 100 1 4 95,00 13 93 4,58 30000 100 99,92 0,08 1 ppm 14 297 4,48 30000 100 99,92 0,08 1 ppm 15 297 1,20 8488 100 1 4 95,00 The following tables show two concrete numerical examples of the method and apparatus shown schematically in the drawing. Pos. No. T [K] P [bara] F [Nm 3 w / h] VF [%] N 2 [%] Ar [%] O 2 [%] 2 298 3.91 44268 100 78.118 0.932 20.95 3 298 3.91 3453 100 78.118 0.932 20.95 4 298 3.91 40815 100 78.118 0.932 20.95 5 298 9.49 3453 100 78.118 0.932 20.95 6 143 9.39 3453 100 78.118 0.932 20.95 7 113 3.77 3453 100 78.118 0.932 20.95 8th 102 3.82 15215 97.4 32.4 2.6 65.0 9 95 3.81 40815 96.5 78.118 0.932 20.95 10 98 3.82 29483 0 32.4 2.6 65.0 11 90 1.30 29483 100 32.4 2.6 65.0 12 90 1.30 29483 100 32.4 2.6 65.0 13 90 3.66 30000 100 99.86 0.14 1 ppm 14 297 3.56 30000 100 99.86 0.14 1 ppm 15 297 1.20 14268 100 32.4 2.6 65.0 Pos. No. T [K] P [bara] F [Nm 3 / h] VF [%] N 2 [%] Ar [%] O 2 [%] 2 298 4.82 38488 100 78.118 0.932 20.95 3 298 4.82 8903 100 78.118 0.932 20.95 4 298 4.82 29585 100 78.118 0.932 20.95 5 298 7.01 8903 100 78.118 0.932 20.95 6 115 6.91 8903 100 78.118 0.932 20.95 7 104 4.72 8903 100 78.118 0.932 20.95 8th 108 4.75 23660 97 1 4 95,00 9 97 4.72 29585 95 78.118 0.932 20.95 10 108 4.75 32148 0 1 4 95,00 11 92 1.3 32148 100 1 4 95,00 12 92 1.3 32148 100 1 4 95,00 13 93 4.58 30000 100 99.92 0.08 1 ppm 14 297 4.48 30000 100 99.92 0.08 1 ppm 15 297 1.20 8488 100 1 4 95,00

Hierbei bedeutenMean here

Pos.Nr.Pos.Nr.
in Rechtecke eingeschlossenen Zahlen in der Zeichnungin rectangles enclosed numbers in the drawing
TT
Temperaturtemperature
PP
Druckprint
FF
Mengenstromstream
VFVF
gasförmiger Anteilgaseous portion
N2 N 2
Stickstoffgehaltnitrogen content
ArAr
Argongehaltargon content
O2 O 2
Sauerstoffgehaltoxygen content

Das Ausführungsbeispiel ist einer Vielzahl fachmännischer Abwandlungen zugänglich. So kann beispielsweise die Turbine 112 statt mit dem Generator 113 mit dem Nachverdichter 108, dem Rückverdichter 132 und/oder dem Produktverdichter 126 gekoppelt sein. Die Rückverdichtung der verdampften sauerstoffreichen Fraktion kann abweichend vom Ausführungsbeispiel bei etwa der Betriebstemperatur der Einzelsäule durch einen Kaltverdichter vorgenommen werden.The embodiment is accessible to a variety of expert modifications. For example, the turbine 112 instead of the generator 113 with the After-compressor 108, the recompressor 132 and / or the product compressor 126th be coupled. The recompression of the vaporized oxygen-rich fraction can differing from the embodiment at about the operating temperature of the single column be made by a cold compressor.

Claims (6)

  1. Single-column process for the generation of gaseous nitrogen by low-temperature fractionation of air, in which compressed charge air (101, 102, 103, 110) is cooled (104) and fed (105, 114) to the single column (107), which has a single condenser/evaporator (118) for generation of return flow liquid and an oxygen-rich fraction (116) is extracted in liquid form from the single column (107), is expanded (117) and in the condenser/evaporator (118) is at least partially evaporated by indirect heat exchange with condensing nitrogen (120) from the upper region of the single column (107), at least a part (131) of the vapour (129, 130) generated in the condenser/evaporator (118) being recompressed (132) and fed (134, 135) to the single column (107) separately from the charge air (105, 114), characterized in that at least a part (103, 110, 111) of the charge air (101) undergoes work-performing expansion (112) upstream of the point where it is introduced (114) into the single column (107).
  2. Process according to Claim 1, characterized in that a first part (102) of the charge air (101), which is under a first pressure, is cooled and partially liquefied (104) and is fed to the single column (107), and in that a second part (103) of the charge air (101) is brought (108) to a second pressure, which is higher than the first pressure, is cooled (104) to an intermediate temperature above the operating temperature of the single column, is fed to the work-performing expansion (112) and is then introduced (114) into the single column (107).
  3. Process according to Claim 2, characterized in that the first and second part of the charge air are together compressed to the first pressure, and the second part (103) of the charge air is compressed further, to the second pressure, in an after-compressor (108).
  4. Apparatus for the generation of gaseous nitrogen by low-temperature fractionation of air, having a charge-air line (101, 103, 110, 111, 114), which leads through a main heat exchanger (104) to an intermediate point (115) of a single column (107), which has a single condenser/evaporator (118) for generation of return flow liquid having a liquid line (116) for transferring a liquid, oxygen-rich fraction out of the single column (107) into the evaporation space of a condenser/evaporator (118), the liquefaction space of which is connected (110, 120) to the upper region of the single column (107), having a recompressor (132), which is connected (134, 135; 129, 130, 131) at its inlet to the evaporation space of the condenser/evaporator (118) and at its outlet to the single column (107) but not to the or one of the charge-air lines (101, 103, 110, 111, 114), characterized by an expansion machine (112) which is arranged in the charge-air line (101, 103, 110, 111, 114).
  5. Apparatus according to Claim 4, characterized by a first charge-air line (102, 105) for introducing a first part of the charge air under a first pressure into the single column (107), and by a second charge-air line (103, 110, 111, 114) for feeding a second part of the charge air under a second pressure, which is higher than the first pressure, to the expansion machine (112) and for introducing air which has been expanded in the expansion machine into the single column (107).
  6. Apparatus according to Claim 5, characterized by an after-compressor (108) which is arranged in the second charge-air line (103, 110) upstream of the expansion machine (112).
EP00108864A 1999-04-30 2000-04-26 Single column process and device for cryogenic air separation Expired - Lifetime EP1050728B1 (en)

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DE19919933A DE19919933A1 (en) 1999-04-30 1999-04-30 Single column process and device for low temperature separation of air
DE19919933 1999-04-30

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DE102008064117A1 (en) 2008-12-19 2009-05-28 Linde Ag Air dissecting method for distilling column system, involves withdrawing liquid rinsing stream from lower area of wash column, where cooled auxiliary air flow is essentially liquid-free during introduction into wash column
EP2236964B1 (en) 2009-03-24 2019-11-20 Linde AG Method and device for low-temperature air separation

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IT1034544B (en) * 1975-03-26 1979-10-10 Siad PROCEDURE AND PLANT FOR AIR FRACTION WITH A SIMPLE GRINDING COLUMN
US4595405A (en) * 1984-12-21 1986-06-17 Air Products And Chemicals, Inc. Process for the generation of gaseous and/or liquid nitrogen
DE4030750A1 (en) * 1990-09-28 1992-04-02 Linde Ag Combination triple duty compressor for prodn. of nitrogen@ and oxygen@ - has multiple shaft machine providing compression for feed air, first main stage, and coolant nitrogen streams
US5251450A (en) * 1992-08-28 1993-10-12 Air Products And Chemicals, Inc. Efficient single column air separation cycle and its integration with gas turbines

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ATE298071T1 (en) 2005-07-15
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DE50010546D1 (en) 2005-07-21

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