DE202009004099U1 - Apparatus for the cryogenic separation of air - Google Patents

Apparatus for the cryogenic separation of air Download PDF

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Publication number
DE202009004099U1
DE202009004099U1 DE200920004099 DE202009004099U DE202009004099U1 DE 202009004099 U1 DE202009004099 U1 DE 202009004099U1 DE 200920004099 DE200920004099 DE 200920004099 DE 202009004099 U DE202009004099 U DE 202009004099U DE 202009004099 U1 DE202009004099 U1 DE 202009004099U1
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column
pressure column
feed air
pressure
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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
    • F25J3/04436—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 at least a triple pressure main column system
    • F25J3/04442—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 at least a triple pressure main column system in a double column flowsheet with a high pressure pre-rectifier
    • 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
    • F25J3/04084—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 nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04163—Hot end purification of the feed air
    • F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
    • F25J3/04175—Hot end purification of the feed air by adsorption of the impurities at a pressure of substantially more than the highest 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
    • F25J3/04248—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
    • F25J3/04248—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
    • F25J3/04436—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 at least a triple pressure main column system
    • F25J3/04454—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 at least a triple pressure main column system a main column system not otherwise provided, e.g. serially coupling of columns or more than three pressure levels
    • 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
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04709—Producing crude argon in a crude argon column as an auxiliary column system in at least a dual pressure main column system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step

Abstract

Vorrichtung zur Tieftemperaturzerlegung von Luft
– mit einem Destilliersäulen-System, das mindestens eine Hochdrucksäule (11) und eine Niederdrucksäule (12) aufweist,
– mit Mitteln zur Regelung,
– mit Mitteln zum Einleiten von Einsatzluft in das Destilliersäulen-System,
– wobei das Destilliersäulen-System außerdem eine Vorsäule (10) aufweist, deren Betriebsdruck bei Betrieb der Vorrichtung höher als der Betriebsdruck der Hochdrucksäule (11) ist,
– mit Mitteln zum Einleiten eines ersten Teilstroms (1; 301) der Einsatzluft in die Vorsäule (10),
– wobei die Vorsäule (10) einen Kopfkondensator (14) aufweist, der als Kondensator-Verdampfer mit Kondensationsraum und Verdampfungsraum ausgebildet ist, wobei der Verdampfungsraum mit dem Sumpfbereich der Hochdrucksäule in Strömungsverbindung steht,
– mit Mitteln zum Einleiten einer gasförmigen Fraktion (30, 31) aus dem oberen Bereich der Vorsäule (10) in den Kondensationsraum des Kopfkondensators (14),
– mit Mitteln zum Einspeisen im Kondensationsraum gebildeter Flüssigkeit (6) als Rücklauf (7) in die Vorsäule...Apparatus for the cryogenic separation of air
With a distillation column system having at least one high-pressure column (11) and one low-pressure column (12),
- with means of regulation,
With means for introducing feed air into the distillation column system,
- wherein the distillation column system further comprises a precolumn (10) whose operating pressure during operation of the device is higher than the operating pressure of the high-pressure column (11),
With means for introducing a first partial flow (1, 301) of the feed air into the precolumn (10),
- wherein the pre-column (10) has a top condenser (14), which is designed as a condenser-evaporator with condensation space and evaporation space, wherein the evaporation space is in flow communication with the bottom region of the high-pressure column,
With means for introducing a gaseous fraction (30, 31) from the upper region of the precolumn (10) into the condensation space of the top condenser (14),
- With means for feeding in the condensation space formed liquid (6) as return (7) in the guard column ...

Figure 00000001
Figure 00000001

Description

Die Erfindung betrifft eine Variante der in der älteren PCT-Anmeldung PCT/EP2009/000431 , deren Offenbarung in diese Anmeldung einbezogen wird. Die entsprechende Vorrichtung wird im Schutzanspruch 1 näher beschrieben. Eine besonders vorteilhafte Ausgestaltung ist im Schutzanspruch 2 erläutert.The invention relates to a variant of the in the older PCT application PCT / EP2009 / 000431 , the disclosure of which is incorporated in this application. The corresponding device is described in the protection claim 1 in more detail. A particularly advantageous embodiment is explained in the protection claim 2.

In den Ausführungsbeispielen der älteren Anmeldung weist die Vorsäule einen von der Hochdrucksäule getrennten Kopfkondensator auf, in dessen Verdampfungsraum wird die gesamte Flüssigluft (zweiter Teil der Einsatzluft) direkt eingeleitet wird. Bei der hier beanspruchten Variante dieses Verfahrens wirkt der Kopfkondensator der Vorsäule gleichzeitig als Sumpfverdampfer der Hochdrucksäule. Hierbei kann die gesamte flüssige Einsatzluft grundsätzlich ebenfalls direkt in den Verdampfungsraum des Kopfkondensators der Vorsäule eingeleitet werden; in diesem Falle ist es jedoch günstiger, die Flüssigluft oder einen Teil davon alternativ oder zu, muss aber nicht wird dagegen mindestens ein Teil der flüssigen Einsatzluft auf indirektem Wege in den Verdampfungsraum des Kopfkondensators (also den Sumpf der Hochdrucksäule) einzuleiten, indem sie an einer besonders geeigneten Zwischenstelle in die Hochdrucksäule eingeleitet wird. Die Zwischenstelle liegt 1 bis 12 theoretische beziehungsweise praktische Böden oberhalb des Sumpfs.In the embodiments of the earlier application the guard column has one from the high pressure column separated head capacitor, in the evaporation chamber is all liquid air (second part of the feed air) is initiated directly. In the variant claimed here Procedure, the head capacitor of the guard column acts simultaneously as bottom evaporator of the high pressure column. Here, the entire liquid feed air in principle also directly into the evaporation space of the head capacitor of the precolumn be initiated; but in this case it is better the liquid air or a part thereof alternatively or to But it does not have to be at least part of the liquid Feed air in an indirect way in the evaporation space of the top condenser (ie the bottom of the high-pressure column) initiate by at a particularly suitable intermediate point in the high-pressure column is initiated. The intermediate position is 1 to 12 theoretical or practical soils above the swamp.

Die Erfindung sowie weitere Einzelheiten der Erfindung werden im Folgenden anhand eines in der Zeichnung 1 schematisch dargestellten Ausführungsbeispiels näher erläutert. Das Destilliersäulen-System wird hier durch eine klassische Dreifachsäule gebildet, bei denen Vorsäule 10, Hochdrucksäule 11 und Niederdrucksäule 12 übereinander angeordnet sind und die Wärmeaustauschbeziehung zwischen jeweils zwei Säulen durch zwei Kondensator-Verdampfer, den Kopfkondensator 14 der Vorsäule, der im Sumpf der Hochdrucksäule angeordnet ist, und den Hauptkondensator 13 im Sumpf. Bei entsprechenden räumlichen Vorgaben können die Säulen auch teilweise oder vollständig nebeneinander angeordnet sein; hierbei können allerdings Pumpen zum Transport von Flüssigkeiten von oder zu den Kondensatoren erforderlich werden, die bei der in der Zeichnung dargestellten Anordnung nicht benötigt werden.The invention and further details of the invention are explained in more detail below with reference to an embodiment schematically illustrated in the drawing 1. The distillation column system is formed here by a classic triple column, where precolumn 10 , High-pressure column 11 and low pressure column 12 are arranged one above the other and the heat exchange relationship between each two columns by two condenser-evaporator, the top condenser 14 the precolumn located in the bottom of the high pressure column and the main condenser 13 in the swamp. With appropriate spatial specifications, the columns can also be arranged partially or completely next to each other; however, pumps may be required to transport liquids from or to the capacitors, which are not required in the arrangement shown in the drawing.

In der Zeichnung sind die Verdichtung, die Reinigung und die Abkühlung der Einsatzluft nicht dargestellt. Das Destilliersäulen-System umfasst hier eine Vorsäule 10, eine Hochdrucksäule 11 und eine Niederdrucksäule 12 sowie die damit verknüpften Kondensator-Verdampfer, den Hauptkondensator 13 und den Kopfkondensator 14 der Vorsäule. Fakultativ kann das Destilliersäulen-System zusätzlich einen Argon-Teil 15 aufweisen, der insbesondere mindestens eine Rohargonsäule und deren Kopfkondensator enthält; zusätzlich kann der Argon-Teil eine Reinargonsäule zur Argon-Stickstoff-Trennung aufweisen.In the drawing, the compression, cleaning and cooling of the feed air are not shown. The distillation column system here includes a guard column 10 , a high pressure column 11 and a low pressure column 12 and the associated condenser-evaporator, the main capacitor 13 and the top condenser 14 the guard column. Optionally, the distillation column system may additionally contain an argon part 15 in particular containing at least one crude argon column and its overhead condenser; In addition, the argon part may have a pure argon column for argon-nitrogen separation.

Die Trennsäulen zur Stickstoff-Sauerstoff-Trennung weisen in dem Beispiel folgende Betriebsdrücke auf (jeweils am Kopf):
Vorsäule 10 ... 7,5 bis 12 bar,
Hochdrucksäule 11 ... 5,0 bis 6,5 bar,
Niederdrucksäule 12 ... 1,3 bis 1,6 bar.The separation columns for nitrogen-oxygen separation have the following operating pressures in the example (in each case at the top):
precolumn 10 ... 7.5 to 12 bar,
High-pressure column 11 ... 5.0 to 6.5 bar,
Low-pressure column 12 ... 1.3 to 1.6 bar.

Ein erster Teilstrom 1 der Einsatzluft kommt gasförmig vom kalten Ende des Hauptwärmetauschers (nicht dargestellt) oder aus einer Turbine. Er steht unter einem Druck, der knapp über dem Betriebsdruck der Vorsäule 10 liegt und wird ummittelbar oberhalb des Sumpfes eingeleitet.A first partial flow 1 The feed air comes in gaseous form from the cold end of the main heat exchanger (not shown) or from a turbine. He is under a pressure just above the operating pressure of the guard column 10 lies and is introduced immediately above the swamp.

Die Vorsäule 10 weist einen Kopfkondensator 14 auf, in dessen Verdampfungsraum ein zweiter Teilstrom 2c der Luft in flüssigem Zustand eingeleitet wird. Die Einleitung findet in dem Beispiel 10 theoretische Böden oberhalb des Sumpfs der Hochdrucksäule 11 statt. Der "zweite Teilstrom" wird in dem Beispiel durch zwei Unterströme 2a, 2b gebildet. Unterstrom 2a stammt vom Austritt einer VS-Claude-Turbine, Unterstrom 2b stammt von kalten Ende des Hauptwärmetauschers (nicht dargestellt) und wurde gegen einen flüssig aus dem Destilliersäulen-System entnommenen und anschließend flüssig auf Druck gebrachten kondensiert beziehungsweise (bei überkritischem Druck) pseudo-kondensiert. Bei der Einleitung in den Verdampfungsraum des Kopfkondensators 14 besteht der zweite Teilstrom 2c im Wesentlichen (zu 85 bis 95 mol-%) aus Flüssigkeit. Sein flüssiger Anteil umfasst 30 bis 50 mol-% der Gesamteinsatzluft. Die übrige Einsatzluft wird gasförmig in das Destilliersäulensystem eingeleitet. Die gasförmige Einleitung erfolgt – bis auf mögliche gasförmige Anteile in den Strömen 2a und 2b und den Turbinenstrom 3 – vollständig über den ersten Teilstrom 1 ins Innere der Vorsäule 10.The guard column 10 has a top condenser 14 on, in the evaporation chamber, a second partial flow 2c the air is introduced in the liquid state. The introduction finds in the example 10 theoretical plates above the bottom of the high pressure column 11 instead of. The "second sub-stream" is in the example by two sub-streams 2a . 2 B educated. undercurrent 2a comes from the exit of a VS Claude turbine, undercurrent 2 B originates from the cold end of the main heat exchanger (not shown) and was condensed against a liquid taken from the distillation column system and subsequently brought to liquid pressure or pseudo-condensed (at supercritical pressure). When introducing into the evaporation space of the top condenser 14 there is the second partial flow 2c essentially (to 85 to 95 mol%) of liquid. Its liquid portion comprises 30 to 50 mol% of the total feed air. The remaining feed air is introduced in gaseous form into the distillation column system. The gaseous introduction takes place - except for possible gaseous components in the streams 2a and 2 B and the turbine flow 3 - completely over the first partial flow 1 inside the precolumn 10 ,

Die gesamte Sumpfflüssigkeit 5 der Vorsäule wird hier in die Hochdrucksäule 11 eingeleitet, und zwar unmittelbar an deren Sumpf. Alternativ oder zusätzlich kann die Sumpfflüssigkeit 5 der Vorsäule oder ein Teil davon – nach Abkühlung im Unterkühlungs-Gegenströmer 37, in die Niederdrucksäule 12 und/oder den Argon-Teil 15 eingespeist werden (in der Zeichnung nicht dargestellt). Die im Kondensationsraum des Kopfkondensators 14 aus einem Teil 31 des Kopfstickstoffs 30 der Vorsäule 10 erzeugte Flüssigkeit 6 wird zu einem ersten Teil als Kopf-Rücklauf in die Vorsäule 10 eingespeist und zu einem zweiten Teil 8 zum Kopf der Hochdrucksäule 11 geführt. Zusätzlich kann eine stickstoffangereicherte Unrein-Fraktion 9 aus der Vorsäule in die Hochdrucksäule geleitet werden; diese Unrein-Fraktion 9 wird an einer Zwischenstelle der Vorsäule 10 entnommen, die etwa 8 bis 16 theoretische beziehungsweise praktische Böden unterhalb des Kopfs angeordnet ist, und der Hochdrucksäule 11 an einer Zwischenstelle zugeleitet.The entire bottoms liquid 5 the guard column is here in the high pressure column 11 initiated, directly to the swamp. Alternatively or additionally, the bottoms liquid 5 the precolumn or part of it - after cooling in the subcooling countercurrent 37 , in the low-pressure column 12 and / or the argon part 15 are fed (not shown in the drawing). The in the condensation chamber of the top condenser 14 from one part 31 of the head nitrogen 30 the guard column 10 generated liquid 6 becomes a first part as head-return into the precolumn 10 fed and a second part 8th to the head of the high pressure column 11 guided. In addition, a nitrogen-enriched Un pure fraction 9 are passed from the precolumn into the high-pressure column; this impure faction 9 is at an intermediate point of the guard column 10 taken, about 8th to 16 theoretical or practical trays below the head, and the high pressure column 11 forwarded to an intermediate body.

Die im Verdampfungsraum des Kopfkondensators gebildete verdampfte Fraktion strömt als aufsteigender Dampf in den Stoffaustauschbereich der Hochdrucksäule, gemeinsam mit einem dritten Teilstrom 3 der Einsatzluft, der vom Austritt einer HDS-Claude-Turbine stammt.The evaporated fraction formed in the evaporation space of the top condenser flows as ascending vapor into the mass transfer region of the high-pressure column, together with a third partial flow 3 the feed air coming from the exit of a HDS Claude turbine.

Im Übrigen funktionieren die Doppelsäule 11/12/13 und der fakultative Argonteil 15 auf die allgemein bekannte Weise.Incidentally, the double column work 11 / 12 / 13 and the optional argon part 15 in the well-known way.

Aus der Hochdrucksäule 11 werden flüssiger Rohsauerstoff 33 am Sumpf, eine flüssige Luftfraktion 34 an der Zwischenstelle, an welcher der zweite Teilstrom 2 eingeleitet wird, und Unrein-Stickstoff 35 von einer weiter oben gelegenen Zwischenstelle in einem Unterkühlungs-Gegenströmer 37 in indirektem Wärmeaustausch mit Rückströmen abgekühlt und über die Leitungen 38, 39, 40 beziehungsweise 41 an den geeigneten Stellen in die Niederdrucksäule 12 eingeleitet. Außerdem können gasförmige Luft 42 von einer Lachmann-Turbine und/oder flüssige Luft 43 von der HDS-Claude-Turbine in die Niederdrucksäule 12 eingespeist werden.From the high pressure column 11 become liquid crude oxygen 33 at the swamp, a liquid air fraction 34 at the intermediate point, at which the second partial flow 2 initiated, and impure nitrogen 35 from an upper intermediate point in a subcooler countercurrent 37 cooled in indirect heat exchange with return streams and over the lines 38 . 39 . 40 respectively 41 at the appropriate places in the low-pressure column 12 initiated. In addition, gaseous air 42 from a Lachmann turbine and / or liquid air 43 from the HDS Claude turbine to the low pressure column 12 be fed.

Weist die Anlage keinen Argon-Teil auf, so können die folgenden Produkte abgezogen werden:

  • – gasförmiger Stickstoff (GAN) 44, 45 vom Kopf der Niederdrucksäule 12
  • – flüssiger Stickstoff (LIN) 46 vom Kopf der Niederdrucksäule 12
  • – gasförmiger Unrein-Stickstoff (UN2) 47, 48 von einer Zwischenstelle im oberen Bereich der Niederdrucksäule 12
  • – gasförmiger Sauerstoff (GOX) 49 unmittelbar oberhalb des Sumpfs der Niederdrucksäule 12
  • – flüssiger Sauerstoff (LOX) 50 vom Sumpf der Niederdrucksäule 12
  • – gasförmiger Druckstickstoff (HPGAN) 51 vom Kopf der Hochdrucksäule 11
  • – flüssiger Druckstickstoff (HP-LIN) 52 aus dem Kondensationsraum des Hauptkondensators 13 oder aus der Hochdrucksäule 11
  • – gasförmiger Stickstoff besonders hohen Drucks (VHPGAN) 53 vom Kopf der Vorsäule 10
If the system does not contain any argon part, the following products can be withdrawn:
  • - gaseous nitrogen (GAN) 44 . 45 from the top of the low-pressure column 12
  • - liquid nitrogen (LIN) 46 from the top of the low-pressure column 12
  • - gaseous impure nitrogen (UN2) 47 . 48 from an intermediate point in the upper region of the low-pressure column 12
  • - gaseous oxygen (GOX) 49 immediately above the bottom of the low pressure column 12
  • - liquid oxygen (LOX) 50 from the bottom of the low-pressure column 12
  • - gaseous pressure nitrogen (HPGAN) 51 from the head of the high pressure column 11
  • - liquid nitrogen (HP-LIN) 52 from the condensation chamber of the main capacitor 13 or from the high pressure column 11
  • - gaseous nitrogen of particularly high pressure (VHPGAN) 53 from the head of the guard column 10

Die Anlage kann, muss aber nicht alle diese Produkte gleichzeitig erzeugen.The Plant may or may not produce all of these products simultaneously.

Die gasförmigen Produktströme werden in einem nicht dargestellten Hauptwärmetauscher in indirektem Wärmeaustausch mit Einsatzluft angewärmt. Der Hauptwärmetauscher kann aus einem Block oder aus zwei oder mehreren parallel und/oder seriell verbundenen Blöcken bestehen. Der flüssige Sauerstoff kann als Flüssigprodukt gewonnen werden; Alternativ oder zusätzlich wird mindestens ein Teil des flüssig aus der Niederdrucksäule abgezogenen Sauerstoffs flüssig auf Druck gebracht und anschließend in dem Hauptwärmetauscher verdampft oder (bei überkritischem Druck) pseudo-verdampft und angewärmt und anschließend als gasförmiges Druckprodukt abgezogen werden (so genannte Innenverdichtung).The gaseous product streams are not in one illustrated main heat exchanger in indirect heat exchange warmed with feed air. The main heat exchanger can be one block or two or more parallel and / or serial consist of connected blocks. The liquid oxygen can be obtained as a liquid product; Alternatively or In addition, at least part of the liquid becomes from the low pressure column withdrawn oxygen liquid brought to pressure and then in the main heat exchanger evaporated or (at supercritical pressure) pseudo-evaporated and warmed and then as gaseous printed product be deducted (so-called internal compression).

In einer Variante des Ausführungsbeispiels weist das System einen Argon-Teil 15 zur Gewinnung von flüssigem Reinargon (LAR) 54 auf. Der Argon-Teil enthält eine oder mehrere Rohargonsäulen zur Argon-Sauerstoff-Trennung und eine Reinargonsäule zur Argon-Stickstofftrennung, die auf die allgemein bekannte Weise betrieben werden. Das untere Ende der Rohargonsäule kommuniziert über die Leitungen 61 und 62 mit einem Zwischenbereich der Niederdrucksäule 12. Der flüssige Rohsauerstoff aus der Hochdrucksäule 11 wird in diesem Fall über die Leitung 33A in den Argon-Teil geleitet und insbesondere mindestens teilweise in dem Kopfkondensator der Rohargonsäule(n) mindestens teilweise verdampft (nicht dargestellt). Der mindestens teilweise gasförmige Rohsauerstoff wird über Leitung 38A in die Niederdrucksäule 12 eingespeist. Aus dem Argon-Teil 15 wird außerdem ein gasförmiger Reststrom (Waste) 55 abgezogen.In a variant of the embodiment, the system has an argon part 15 for the production of liquid pure argon (LAR) 54 on. The argon portion contains one or more argon-oxygen separation argon columns and an argon-nitrogen separation purge column operated in the well-known manner. The lower end of the crude argon column communicates over the pipes 61 and 62 with an intermediate region of the low-pressure column 12 , The liquid raw oxygen from the high-pressure column 11 will in this case over the line 33A passed into the argon part and in particular at least partially evaporated in the top condenser of the crude argon column (s) at least partially (not shown). The at least partially gaseous crude oxygen is via line 38A in the low pressure column 12 fed. From the argon part 15 In addition, a gaseous residual stream (Waste) 55 deducted.

Alternativ zu der zeichnerischen Darstellung kann die Sumpfflüssigkeit 5 der Vorsäule 10 kann teilweise oder vollständig statt in die Hochdrucksäule 11 nach Unterkühlung in 37 in die Niederdrucksäule 12 eingeleitet werden. Falls Argon gewonnen wird, kann ein Teil oder die gesamte unterkühlte Flüssigkeit vor ihrer Einleitung in die Niederdrucksäule zur Kühlung des Kopfkondensators der Rohargonsäule eingesetzt werden.Alternatively to the graphic representation, the bottom liquid 5 the guard column 10 may be partial or complete instead of in the high pressure column 11 after hypothermia in 37 in the low pressure column 12 be initiated. If argon is recovered, some or all of the supercooled liquid may be used to cool the top condenser of the crude argon column prior to its introduction into the low pressure column.

ZITATE ENTHALTEN IN DER BESCHREIBUNGQUOTES INCLUDE IN THE DESCRIPTION

Diese Liste der vom Anmelder aufgeführten Dokumente wurde automatisiert erzeugt und ist ausschließlich zur besseren Information des Lesers aufgenommen. Die Liste ist nicht Bestandteil der deutschen Patent- bzw. Gebrauchsmusteranmeldung. Das DPMA übernimmt keinerlei Haftung für etwaige Fehler oder Auslassungen.This list The documents listed by the applicant have been automated generated and is solely for better information recorded by the reader. The list is not part of the German Patent or utility model application. The DPMA takes over no liability for any errors or omissions.

Zitierte PatentliteraturCited patent literature

  • - EP 2009/000431 [0001] - EP 2009/000431 [0001]

Claims (2)

Vorrichtung zur Tieftemperaturzerlegung von Luft – mit einem Destilliersäulen-System, das mindestens eine Hochdrucksäule (11) und eine Niederdrucksäule (12) aufweist, – mit Mitteln zur Regelung, – mit Mitteln zum Einleiten von Einsatzluft in das Destilliersäulen-System, – wobei das Destilliersäulen-System außerdem eine Vorsäule (10) aufweist, deren Betriebsdruck bei Betrieb der Vorrichtung höher als der Betriebsdruck der Hochdrucksäule (11) ist, – mit Mitteln zum Einleiten eines ersten Teilstroms (1; 301) der Einsatzluft in die Vorsäule (10), – wobei die Vorsäule (10) einen Kopfkondensator (14) aufweist, der als Kondensator-Verdampfer mit Kondensationsraum und Verdampfungsraum ausgebildet ist, wobei der Verdampfungsraum mit dem Sumpfbereich der Hochdrucksäule in Strömungsverbindung steht, – mit Mitteln zum Einleiten einer gasförmigen Fraktion (30, 31) aus dem oberen Bereich der Vorsäule (10) in den Kondensationsraum des Kopfkondensators (14), – mit Mitteln zum Einspeisen im Kondensationsraum gebildeter Flüssigkeit (6) als Rücklauf (7) in die Vorsäule (10) und mit – Mitteln zum Einleiten eines zweiten Teilstroms (2a; 2b) der Einsatzluft mindestens teilweise in flüssigem Zustand in den Verdampfungsraum des Kopfkondensators (14) auf direktem Weg und/oder über die Einspeisung an einer Zwischenstelle der Hochdrucksäule, – wobei die Mittel zur Regelung so ausgebildet sind, dass beim Betrieb der Vorrichtung – mindestens 30 mol-% der gesamten Einsatzluftmenge in flüssigem Zustand in das Destilliersäulen-System eingeleitet werden.Apparatus for the cryogenic separation of air - comprising a distillation column system comprising at least one high-pressure column ( 11 ) and a low pressure column ( 12 ), - with means for regulation, - with means for introducing feed air into the distillation column system, - the distillation column system also having a precolumn ( 10 ), whose operating pressure during operation of the device higher than the operating pressure of the high-pressure column ( 11 ), - with means for introducing a first partial flow ( 1 ; 301 ) of the feed air into the guard column ( 10 ), - where the guard column ( 10 ) a head capacitor ( 14 ), which is formed as a condenser-evaporator with condensation space and evaporation space, the evaporation space is in flow communication with the bottom region of the high-pressure column, - means for introducing a gaseous fraction ( 30 . 31 ) from the upper area of the guard column ( 10 ) in the condensation space of the top condenser ( 14 ), - liquid formed by means for feeding in the condensation space ( 6 ) as return ( 7 ) in the guard column ( 10 ) and with - means for introducing a second partial flow ( 2a ; 2 B ) of the feed air at least partially in the liquid state in the evaporation space of the top condenser ( 14 ) by direct route and / or via the feed at an intermediate point of the high-pressure column, - wherein the means for regulating are designed so that during operation of the device - at least 30 mol% of the total amount of feed air in liquid state are introduced into the distillation column system , Vorrichtung nach Anspruch 1, dadurch gekennzeichnet, dass die Mittel zur Regelung so ausgebildet sind, dass beim Betrieb der Vorrichtung der flüssige Anteil des zweiten Teilstroms (2a; 2b) bei der Einleitung in den Verdampfungsraum des Kopfkondensators (14) der Einsatzluft mehr als 30 mol-% der gesamten Einsatzluftmenge umfasst.Apparatus according to claim 1, characterized in that the means for regulating are designed so that during operation of the device, the liquid portion of the second partial flow ( 2a ; 2 B ) during the introduction into the evaporation space of the top condenser ( 14 ) the feed air comprises more than 30 mol% of the total amount of feed air.
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Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102013012606A1 (en) 2013-02-19 2014-08-21 CRYOTEC Anlagenbau GmbH Modular process plant, in particular air separation plant with a variety of plant components
WO2014146779A3 (en) * 2013-03-19 2015-11-26 Linde Aktiengesellschaft Method and device for generating gaseous compressed nitrogen.
WO2020169257A1 (en) 2019-02-22 2020-08-27 Linde Gmbh Method and system for low-temperature air separation
US20220090855A1 (en) * 2020-09-18 2022-03-24 L'Air Liquide, Societe Anonyme pour l'Etude et l'Exploitation des Procedeseorges Claude Method and apparatus for producing high-purity nitrogen and low-purity oxygen

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WO2009000431A1 (en) 2007-06-25 2008-12-31 Rhode & Schwarz Gmbh & Co. Kg Broadband directional coupler with adjustable directionality

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WO2009000431A1 (en) 2007-06-25 2008-12-31 Rhode & Schwarz Gmbh & Co. Kg Broadband directional coupler with adjustable directionality

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102013012606A1 (en) 2013-02-19 2014-08-21 CRYOTEC Anlagenbau GmbH Modular process plant, in particular air separation plant with a variety of plant components
WO2014128120A2 (en) 2013-02-19 2014-08-28 CRYOTEC Anlagenbau GmbH Modular processing system, in particular air separating system with a plurality of system components
DE102013012606B4 (en) * 2013-02-19 2015-08-06 CRYOTEC Anlagenbau GmbH Modular process plant, in particular air separation plant with a variety of plant components
WO2014146779A3 (en) * 2013-03-19 2015-11-26 Linde Aktiengesellschaft Method and device for generating gaseous compressed nitrogen.
WO2020169257A1 (en) 2019-02-22 2020-08-27 Linde Gmbh Method and system for low-temperature air separation
US20220090855A1 (en) * 2020-09-18 2022-03-24 L'Air Liquide, Societe Anonyme pour l'Etude et l'Exploitation des Procedeseorges Claude Method and apparatus for producing high-purity nitrogen and low-purity oxygen

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