EP2390604A1 - Method and device for separating a fluid mixture using deep temperature distillation, in particular for acquiring pure krypton - Google Patents
Method and device for separating a fluid mixture using deep temperature distillation, in particular for acquiring pure krypton Download PDFInfo
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- EP2390604A1 EP2390604A1 EP11003607A EP11003607A EP2390604A1 EP 2390604 A1 EP2390604 A1 EP 2390604A1 EP 11003607 A EP11003607 A EP 11003607A EP 11003607 A EP11003607 A EP 11003607A EP 2390604 A1 EP2390604 A1 EP 2390604A1
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- Prior art keywords
- separation column
- buffer
- container
- column
- liquid
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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
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
- F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
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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
- F25J3/04642—Recovering noble gases from air
- F25J3/04745—Krypton and/or Xenon
- F25J3/04751—Producing pure krypton and/or xenon recovered from a crude krypton/xenon mixture
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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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/34—Krypton
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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
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/62—Details of storing a fluid in a tank
Definitions
- the invention relates to a method according to the preamble of patent claim 1.
- the process is carried out at low temperature, ie well below ambient temperature, in particular below 200 K, in particular below 150 K. It can for example be used to obtain liquid pure krypton (boiling point 120 K at 1.013 bar) by separating volatile components.
- the separation column is cooled by a top condenser which simultaneously serves to generate reflux liquid and to liquefy the product.
- the top condenser is designed as a heat exchanger, which each has a group of passages for the cooling medium and for the condensation of the top gas.
- the separation column may comprise a bottom evaporator, which is heated, for example, electrically or by indirect heat exchange with a heating medium.
- FIG. 1 shown schematically.
- the fluid mixture to be separated is introduced as feed fluid 1 into a separation column 2, in the example in liquid form.
- the separation column has at least one mass transfer section 3, 4 which contains mass transfer elements which consist of ordered or unordered packing, mass transfer trays or a combination of these types of mass transfer elements.
- a top condenser 5 is arranged, which is cooled with a cooling medium 6.
- the top gas of the separation column flowing out of the top of the top mass transfer section 3 is at least partially condensed.
- the condensate flows back into the column and is fed to a first part as reflux to the upper mass transfer section 3.
- a second part 8 is collected in a cup 7 and introduced via a pipe and a valve 9 in a buffer tank 10. From the buffer tank is - usually intermittently - Removed a liquid product stream 11.
- formed gas is returned via a further pipe and a valve 13 as a gaseous reflux 12 in the head of the separation column 2 and the top condenser.
- the separation column 2 also has a bottom evaporator 14, which is operated here with a heating medium 15, which enters into indirect heat exchange with the bottom liquid of the column. At the bottom, a residual stream 16 is removed liquid, with the unwanted heavier volatile impurities leave the separation column.
- the liquid stream 8 to the buffer tank is at its boiling point. Even with good insulation heat is introduced into the buffer tank, which has no further source of cold next to the incoming liquid 8. Therefore, the circulation stream from the separation column to the buffer tank (8) and back as a gaseous return flow (12) must be operated at a relatively high throughput in order to compensate for the amount of heat introduced into the buffer tank. Correspondingly smaller is the amount of liquid product stream 11 which can be withdrawn from the buffer container as the final product. In addition, it may be difficult to control the separation column so that set stable liquid levels.
- the invention has for its object to provide a method of the type mentioned above and a corresponding device that can be operated particularly low and in which in particular the disadvantages described are avoided.
- the liquid buffer volume of the buffer tank is greater than the mass transfer volume of the separation column.
- the liquid buffer volume is more than twice, preferably more than eight times, the mass transfer volume.
- the "liquid buffer volume” of the buffer container is to be understood as meaning the maximum volume that can be filled with liquid during the orderly operation of the method and thus serve to buffer the condensate from the top condenser.
- the "mass transfer volume" of the separation column encloses all mass transfer elements and the associated distribution elements. For an ordered (structured) packing or disordered (unstructured) pack, this volume ranges from the topmost manifold to the bottom of the bottommost mass transfer layer. In a pure tray column, the mass transfer volume encloses all trays including the space between the trays.
- the invention results in a particularly easy-to-control process; There are (with closed product line) a steadily increasing liquid level in the buffer tank and a stable liquid level in the bottom of the column.
- the heat input into the buffer container has no direct influence on the product yield in the method according to the invention.
- the buffer tank can be completely emptied without affecting the operation of the separation column.
- the system is easier by eliminating a return line from the buffer tank to the top condenser. This requires an unusual compared to the separation column and the top condenser large buffer tank, especially in comparison to a conventional condenser tank whose size is adapted to the volume of the top condenser and / or to the diameter of the separation column.
- the separation column and the buffer tank are designed as communicating vessels.
- the top gas of the separation column flows directly into the gas space of the buffer container and the top condenser arranged there, without the need for a pipeline.
- the buffer tank and the top condenser only a single container sealed to the outside is required.
- the separation column may be arranged in a separate container from the buffer container, wherein the head gas is introduced via a head gas line into the top condenser.
- the head gas is introduced via a head gas line into the top condenser.
- the invention also relates to a device for separating a fluid mixture by cryogenic distillation according to the claims 4 to 7, as well as an application of the method or the device for pure Krypton beltung by separation of less volatile impurities according to claim 8.
- the fluid mixture to be separated is introduced as feed fluid 1 into a separation column 2, in the example in liquid form.
- the separation column has at least one mass transfer section 3, 4 containing mass transfer elements, each consisting of ordered or unordered packing, mass transfer trays or a combination of these types of mass transfer elements. In the example, only ordered packing elements are used as mass transfer elements in the separation column 2.
- a sump evaporator 14 is arranged, which is operated here with a heating medium 15, which occurs in indirect heat exchange with the bottom liquid of the column; In principle, electrical heating of the sump is also possible in the method according to the invention.
- the feed fluid can also be introduced as a two-phase mixture or completely in gaseous form.
- the sump heater 14 and the mass transfer elements 4 can be omitted below the feed.
- a residual stream 16 is removed liquid, with the unwanted heavier volatile impurities leave the separation column.
- the top gas of the separation column flowing out of the top of the top mass transfer section 3 is at least partially condensed.
- the top condenser 5 is arranged inside a buffer container 10.
- the head condenser is in the example designed as a tube condenser with a plurality of vertical tubes, which are open at the top and bottom and communicate with the head region of the separation column 2. It is designed so that the gas chambers above and below the condenser communicate exclusively through the tubes.
- the top condenser may also be formed as a helically wound heat exchanger in whose tubes the cooling medium flows, or as a plate heat exchanger block with downwardly open condensation passages.
- the buffer tank 10 also has at its upper end a gas outlet (not shown in the drawings), via which continuously or from time to time non-condensable inert gas can be discharged.
- a first part of the condensate formed in the top condenser 5 and stored in the buffer tank 10 is fed to the separation column 2 via a return line and a return valve 21 as reflux liquid (20).
- a second part is removed via a product valve 17 as a liquid product stream 11 (pure product).
- the pure product is either led directly to a consumer or bottled.
- Product removal is generally intermittent. If desired, a portion of the overhead gas can also be withdrawn directly as gaseous top product (not shown).
- FIG. 3 is different from the one of FIG. 2 merely in that the separation column 2 is arranged in a container separate from the buffer container 10. Therefore, the head gas does not flow directly, but via a head gas line 22 from the head of the separation column into the buffer tank 10 and to the top condenser 5.
- the two embodiments are particularly suitable for pure KryptonGewinnung.
- liquid, almost pure krypton is introduced as the feed fluid into the separation column 2, which is operated as a pure krypton column.
- the feed fluid originates from a krypton-xenon column to separate krypton and xenon (or from a crypt column to remove more volatile components). It still contains small amounts of less volatile impurities, especially in the form of halogenated hydrocarbons or carbons such as CF 4 .
- the pure krypton column can be connected directly to the upstream krypton-xenon or krypton column. Alternatively, the almost pure krypton is collected from one or more upstream units and further processed from time to time in the pure krypton column.
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
Description
Die Erfindung betrifft ein Verfahren gemäß dem Oberbegriff des Patentanspruchs 1.The invention relates to a method according to the preamble of patent claim 1.
Das Verfahren wird bei Tieftemperatur durchgeführt, also deutlich unter Umgebungstemperatur, insbesondere unterhalb von 200 K, insbesondere unterhalb von 150 K. Es kann beispielsweise zur Gewinnung von flüssigem Rein-Krypton (Siedepunkt 120 K bei 1,013 bar) durch Abtrennung schwererflüchtiger Komponenten eingesetzt werden.The process is carried out at low temperature, ie well below ambient temperature, in particular below 200 K, in particular below 150 K. It can for example be used to obtain liquid pure krypton (boiling point 120 K at 1.013 bar) by separating volatile components.
Die Trennsäule wird durch einen Kopfkondensator gekühlt, der gleichzeitig zur Erzeugung von Rücklaufflüssigkeit und zur Produktverflüssigung dient. Der Kopfkondensator ist als Wärmetauscher ausgebildet, der je eine Gruppe von Passagen für das Kühlmedium und für die Kondensation des Kopfgases aufweist. Außerdem kann die Trennsäule einen Sumpfverdampfer aufweisen, der beispielsweise elektrisch oder durch indirekten Wärmeaustausch mit einem Heizmedium beheizt wird.The separation column is cooled by a top condenser which simultaneously serves to generate reflux liquid and to liquefy the product. The top condenser is designed as a heat exchanger, which each has a group of passages for the cooling medium and for the condensation of the top gas. In addition, the separation column may comprise a bottom evaporator, which is heated, for example, electrically or by indirect heat exchange with a heating medium.
Bisher ist es üblich, den Kopfkondensator in den Kopf der Kolonne einzubauen. Diese Verfahrensweise und die entsprechende Vorrichtung sind in
Diese Verfahrensführung kann zu Nachteilen führen.This procedure can lead to disadvantages.
Der flüssige Strom 8 zum Pufferbehälter befindet sich an seinem Siedepunkt. Auch bei guter Isolierung wird in den Pufferbehälter Wärme eingetragen, der neben der einströmenden Flüssigkeit 8 keine weitere Kältequelle besitzt. Daher muss der Kreislaufstrom von der Trennsäule zum Pufferbehälter (8) und zurück als gasförmiger Rückstrom (12) mit relativ hohem Durchsatz betrieben werden, um die in den Pufferbehälter eingetragene Wärmemenge auszugleichen. Entsprechend geringer ist die Menge an flüssigem Produktstrom 11, die aus dem Pufferbehälter als Endprodukt abgezogen werden kann. Außerdem kann es schwierig werden, die Trennsäule so zu regeln, dass sich stabile Flüssigkeitsstände einstellen.The
Bei Reinheitsschwankungen am Kopf der Trennsäule können Verunreinigungen mit der Flüssigkeit 8 in den Pufferbehälter 10 gelangen und damit den gesamten dort gespeicherten Produktvorrat unbrauchbar machen. Bei dem Verfahren der
Der Erfindung liegt die Aufgabe zugrunde, ein Verfahren der eingangs genannten Art und eine entsprechende Vorrichtung anzugeben, die besonders günstig betrieben werden können und bei denen insbesondere die beschriebenen Nachteile vermieden werden.The invention has for its object to provide a method of the type mentioned above and a corresponding device that can be operated particularly low and in which in particular the disadvantages described are avoided.
Diese Aufgabe wird dadurch gelöst, dass Kopfkondensator und Pufferbehälter gemäß dem kennzeichnenden Teil des Patentanspruchs 1 integriert werden. Der Pufferbehälter bildet damit gleichzeitig den Behälter des Kopfkondensators und wird somit ebenfalls durch das Kühlmittel und nicht durch Verdampfung wertvollen Produkts gekühlt. Im Falle der Verunreinigung der im Pufferbehälter gespeicherten Flüssigkeit kann diese über die normale Rücklaufleitung in die Trennsäule zurückgeführt, so dass die Verunreinigungen im Normalbetrieb wieder entfernt werden können, entweder durch Verdünnung über einen begrenzten Zeitraum oder durch Ablassen der kompletten im Pufferbehälter gespeicherten Flüssigkeit in die Trennsäule. Im Gegensatz zu bekannten kleineren Puffereinrichtungen an Kopfkondensatoren, die regelmäßig anderen Zwecken dienen, ist bei der Erfindung das Flüssigkeitspuffervolumen des Pufferbehälters größer als das Stoffaustauschvolumen der Trennsäule. Beispielsweise ist das Flüssigkeitspuffervolumen mehr als zweimal, vorzugsweise mehr als achtmal so groß wie das Stoffaustauschvolumen.This object is achieved in that head capacitor and buffer container are integrated according to the characterizing part of patent claim 1. Of the Buffer tank thus simultaneously forms the container of the top condenser and is therefore also cooled by the coolant and not by evaporation of valuable product. In the case of contamination of the liquid stored in the buffer container, this can be returned via the normal return line in the separation column, so that the impurities can be removed again in normal operation, either by dilution for a limited period of time or by draining the entire liquid stored in the buffer tank in the separation column , In contrast to known smaller buffer devices on top condensers, which regularly serve other purposes, in the invention, the liquid buffer volume of the buffer tank is greater than the mass transfer volume of the separation column. For example, the liquid buffer volume is more than twice, preferably more than eight times, the mass transfer volume.
Unter dem "Flüssigkeitspuffervolumen" des Pufferbehälters ist der maximale Rauminhalt zu verstehen, der bei geordnetem Betrieb des Verfahrens mit Flüssigkeit gefüllt werden und damit zur Pufferung des Kondensats aus dem Kopfkondensator dienen kann.The "liquid buffer volume" of the buffer container is to be understood as meaning the maximum volume that can be filled with liquid during the orderly operation of the method and thus serve to buffer the condensate from the top condenser.
Das "Stoffaustauschvolumen" der Trennsäule umschließt sämtliche Stoffaustauschelemente und die dazugehörigen Verteilelemente. Bei einer mit geordneter (strukturierter) Packung oder ungeordneter (unstrukturierter) Packung ausgestatteten Kolonne reicht dieses Volumen vom obersten Verteiler bis zum unteren Ende der untersten Stoffaustauschschicht. In einer reinen Bodenkolonne umschließt das Stoffaustauschvolumen alle Böden einschließlich des Zwischenraums zwischen den Böden.The "mass transfer volume" of the separation column encloses all mass transfer elements and the associated distribution elements. For an ordered (structured) packing or disordered (unstructured) pack, this volume ranges from the topmost manifold to the bottom of the bottommost mass transfer layer. In a pure tray column, the mass transfer volume encloses all trays including the space between the trays.
Durch die Erfindung ergibt sich ein besonders einfach zu regelnder Prozess; es stellen sich (bei geschlossener Produktleitung) ein stetig steigender Flüssigkeitsspiegel im Pufferbehälter und ein stabiler Flüssigkeitsstand im Sumpf der Säule ein.The invention results in a particularly easy-to-control process; There are (with closed product line) a steadily increasing liquid level in the buffer tank and a stable liquid level in the bottom of the column.
Der Wärmeeintrag in den Pufferbehälter hat bei dem erfindungsgemäßen Verfahren keinen unmittelbaren Einfluss auf die Produktausbeute. Der Pufferbehälter kann vollständig geleert werden, ohne dass der Betrieb der Trennsäule beeinflusst wird.The heat input into the buffer container has no direct influence on the product yield in the method according to the invention. The buffer tank can be completely emptied without affecting the operation of the separation column.
Auch apparativ und regelungstechnisch wird die Anlage einfacher, indem eine Rückleitung von dem Pufferbehälter zum Kopfkondensator entfällt. Dafür benötigt man einen im Vergleich zur Trennsäule und zum Kopfkondensator ungewöhnlichen großen Pufferbehälter, insbesondere im Vergleich zu einem üblichen Kondensatorbehälter, dessen Größe an das Volumen des Kopfkondensators und/oder an den Durchmesser der Trennsäule angepasst ist.Also apparatus and control technology, the system is easier by eliminating a return line from the buffer tank to the top condenser. This requires an unusual compared to the separation column and the top condenser large buffer tank, especially in comparison to a conventional condenser tank whose size is adapted to the volume of the top condenser and / or to the diameter of the separation column.
In einer ersten Variante der Erfindung sind die Trennsäule und der Pufferbehälter als miteinander kommunizierende Gefäße ausgebildet. Das Kopfgas der Trennsäule strömt dabei unmittelbar in den Gasraum des Pufferbehalters und den dort angeordneten Kopfkondensator ein, ohne dass es einer Rohrleitung bedürfte. Für die Trennsäule, den Pufferbehälter und den Kopfkondensator ist nur ein einziger nach außen abgeschlossener Behälter erforderlich.In a first variant of the invention, the separation column and the buffer tank are designed as communicating vessels. The top gas of the separation column flows directly into the gas space of the buffer container and the top condenser arranged there, without the need for a pipeline. For the separation column, the buffer tank and the top condenser only a single container sealed to the outside is required.
Alternativ dazu kann in einer zweiten Variante der Erfindung die Trennsäule in einem von dem Pufferbehälter getrennten Behälter angeordnet sein, wobei das Kopfgas über eine Kopfgasleitung in den Kopfkondensator eingeleitet wird. Hierbei ist man besonders flexibel bei der Anordnung der beiden Apparateteile innerhalb der isolierenden Hülle (Coldbox), die bei Tieftemperaturanlagen regelmäßig die kalten Bauteile umgibt.Alternatively, in a second variant of the invention, the separation column may be arranged in a separate container from the buffer container, wherein the head gas is introduced via a head gas line into the top condenser. Here, one is particularly flexible in the arrangement of the two parts of the apparatus within the insulating sheath (cold box), which surrounds the cold components regularly at low temperature systems.
Die Erfindung betrifft außerdem eine Vorrichtung zur Trennung eines Fluidgemischs durch Tieftemperatur-Destillation gemäß den Patentansprüchen 4 bis 7, sowie eine Anwendung des erfindungsgemäßen Verfahrens beziehungsweise der Vorrichtung zur Rein-Kryptongewinnung durch Abtrennung von schwererflüchtigen Verunreinigungen gemäß dem Patentanspruch 8.The invention also relates to a device for separating a fluid mixture by cryogenic distillation according to the
Die Erfindung sowie weitere Einzelheiten der Erfindung werden im Folgenden anhand zweier in den Zeichnungen dargestellten Ausführungsbeispielen näher erläutert. Hierbei zeigen:
Figur 2- ein erstes Ausführungsbeispiel der Erfindung mit Integration von Trennsäule und Pufferbehälter und
Figur 3- ein zweites Ausführungsbeispiel, bei dem die Trennsäule in einem von dem Pufferbehälter getrennten Behälter angeordnet ist.
- FIG. 2
- a first embodiment of the invention with integration of separation column and buffer tank and
- FIG. 3
- A second embodiment, wherein the separation column is arranged in a separate container from the buffer tank.
In
In dem Kopfkondensator wird das Kopfgas der Trennsäule, das aus der Oberseite des oberen Stoffaustauschabschnitts 3 ausströmt, mindestens teilweise kondensiert. Erfindungsgemäß ist der Kopfkondensator 5 im Inneren eines Pufferbehälters 10 angeordnet. Der Kopfkondensator ist in dem Beispiel als Röhrenkondensator mit einer Vielzahl vertikaler Röhren ausgeführt, die oben und unten offen sind und mit dem Kopfbereich der Trennsäule 2 kommunizieren. Er ist so konstruiert, dass die Gasräume oberhalb und unterhalb des Kondensators ausschließlich über die Röhren kommunizieren. (Alternativ kann der Kopfkondensator auch als schraubenförmig gewickelter Wärmetauscher, in dessen Rohren das Kühlmedium strömt, oder als Plattenwärmetauscherblock mit unten offenen Kondensationspassagen ausgebildet sein.) In der in
Der Pufferbehälter 10 weist an seinem oberen Ende außerdem einen Gasablass auf (in den Zeichnungen nicht dargestellt), über den kontinuierlich oder von Zeit zu Zeit nicht kondensierbares Inertgas abgelassen werden kann.The
Ein erster Teil des in dem Kopfkondensator 5 gebildeten und im Pufferbehälter 10 gespeicherten Kondensats wird über eine Rücklaufleitung und ein Rücklaufventil 21 als Rücklaufflüssigkeit (20) auf die Trennsäule 2 aufgegeben. Ein zweiter Teil wird über ein Produktventil 17 als flüssiger Produktstrom 11 (Reinprodukt) entnommen. Das Reinprodukt wird entweder direkt zu einem Verbraucher geführt oder in Flaschen abgefüllt. Die Produktentnahme geschieht im Allgemeinen intermittierend. Falls gewünscht, kann ein Teil des Kopfgases auch direkt als gasförmiges Kopfprodukt abgezogen werden (nicht dargestellt).A first part of the condensate formed in the
Das Ausführungsbeispiel der
Die beiden Ausführungsbeispiele eignen sich insbesondere für die Rein-KryptonGewinnung. In diesem Fall wird als Einsatzfluid flüssiges, fast reines Krypton in die Trennsäule 2 eingeleitet, die als Rein-Krypton-Säule betrieben wird. Das Einsatzfluid stammt aus einer Krypton-Xenon-Säule zur Auftrennung von Krypton und Xenon (oder aus einer Kryptonsäule zur Abtrennung leichterflüchtiger Komponenten). Es enthält noch geringe Mengen schwererflüchtigen Verunreinigungen, insbesondere in Form von halogenierten Kohlenwasserstoffen oder Kohlenstoffen wie CF4. Die Rein-Krypton-Säule kann unmittelbar an die vorgeschaltete Krypton-Xenon- oder Krypton-Säule angeschlossen werden. Alternativ wird das fast reine Krypton aus einer oder mehreren vorgeschalteten Anlagen gesammelt und von Zeit zu Zeit in der Rein-Krypton-Säule weiterverarbeitet.The two embodiments are particularly suitable for pure KryptonGewinnung. In this case, liquid, almost pure krypton is introduced as the feed fluid into the
Claims (8)
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EP11003607A EP2390604A1 (en) | 2010-05-27 | 2011-05-03 | Method and device for separating a fluid mixture using deep temperature distillation, in particular for acquiring pure krypton |
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DE201010021797 DE102010021797A1 (en) | 2010-05-27 | 2010-05-27 | Process and apparatus for separating a fluid mixture by cryogenic distillation, in particular for pure krypton recovery |
EP10007531 | 2010-07-20 | ||
EP11003607A EP2390604A1 (en) | 2010-05-27 | 2011-05-03 | Method and device for separating a fluid mixture using deep temperature distillation, in particular for acquiring pure krypton |
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EP11003607A Withdrawn EP2390604A1 (en) | 2010-05-27 | 2011-05-03 | Method and device for separating a fluid mixture using deep temperature distillation, in particular for acquiring pure krypton |
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Cited By (1)
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CN109999748A (en) * | 2019-04-25 | 2019-07-12 | 中冶焦耐(大连)工程技术有限公司 | One kind, which efficiently connects, washes knockout tower and sodium phenolate solution and dephenolize fraction seperation method |
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DE2133465A1 (en) * | 1971-07-06 | 1973-01-25 | Linde Ag | Liquid nitrogen prodn - by single-column fractional distillation of air at 6 to 9 bar pressure |
JPS5342758B1 (en) * | 1966-09-19 | 1978-11-14 | ||
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JPH0268475A (en) * | 1988-08-31 | 1990-03-07 | Nippon Sanso Kk | Condensation vaporizer and operation thereof |
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2011
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JPS5342758B1 (en) * | 1966-09-19 | 1978-11-14 | ||
DE2133465A1 (en) * | 1971-07-06 | 1973-01-25 | Linde Ag | Liquid nitrogen prodn - by single-column fractional distillation of air at 6 to 9 bar pressure |
DE2814464A1 (en) * | 1978-04-04 | 1979-10-18 | Linde Ag | Separator for gaseous components from carrier gas - utilises compression and removes contaminants before entering low temp. rectification zone |
DE3732363A1 (en) * | 1987-09-25 | 1989-04-06 | Linde Ag | Method and device for restarting a gas fractionation plant |
JPH0268475A (en) * | 1988-08-31 | 1990-03-07 | Nippon Sanso Kk | Condensation vaporizer and operation thereof |
JPH03186182A (en) * | 1989-12-13 | 1991-08-14 | Nippon Sanso Kk | Air liquefying separator and pouring method for liquefied gas |
US5437160A (en) * | 1993-04-29 | 1995-08-01 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and installation for the separation of air |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN109999748A (en) * | 2019-04-25 | 2019-07-12 | 中冶焦耐(大连)工程技术有限公司 | One kind, which efficiently connects, washes knockout tower and sodium phenolate solution and dephenolize fraction seperation method |
CN109999748B (en) * | 2019-04-25 | 2023-09-15 | 中冶焦耐(大连)工程技术有限公司 | High-efficiency continuous washing separation tower and sodium phenolate solution and dephenolized fraction separation method |
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