EP0141029B1 - Phase distribution container - Google Patents

Phase distribution container Download PDF

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Publication number
EP0141029B1
EP0141029B1 EP84107399A EP84107399A EP0141029B1 EP 0141029 B1 EP0141029 B1 EP 0141029B1 EP 84107399 A EP84107399 A EP 84107399A EP 84107399 A EP84107399 A EP 84107399A EP 0141029 B1 EP0141029 B1 EP 0141029B1
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EP
European Patent Office
Prior art keywords
vessel
chamber
phase
liquid
mixture
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired
Application number
EP84107399A
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German (de)
French (fr)
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EP0141029A2 (en
EP0141029A3 (en
Inventor
Heinz Dr. Juzi
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Trasformazione Societaria sulzer AG
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Gebrueder Sulzer AG
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Publication of EP0141029A2 publication Critical patent/EP0141029A2/en
Publication of EP0141029A3 publication Critical patent/EP0141029A3/en
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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F9/00—Casings; Header boxes; Auxiliary supports for elements; Auxiliary members within casings
    • F28F9/02—Header boxes; End plates
    • F28F9/026—Header boxes; End plates with static flow control means, e.g. with means for uniformly distributing heat exchange media into conduits
    • F28F9/0265—Header boxes; End plates with static flow control means, e.g. with means for uniformly distributing heat exchange media into conduits by using guiding means or impingement means inside the header box
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B37/00—Component parts or details of steam boilers
    • F22B37/02—Component parts or details of steam boilers applicable to more than one kind or type of steam boiler
    • F22B37/22—Drums; Headers; Accessories therefor
    • F22B37/227—Drums and collectors for mixing
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D7/005—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits for only one medium being tubes having bent portions or being assembled from bent tubes or being tubes having a toroidal configuration
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F9/00—Casings; Header boxes; Auxiliary supports for elements; Auxiliary members within casings
    • F28F9/02—Header boxes; End plates
    • F28F9/0202—Header boxes having their inner space divided by partitions
    • F28F9/0204—Header boxes having their inner space divided by partitions for elongated header box, e.g. with transversal and longitudinal partitions
    • F28F9/0214—Header boxes having their inner space divided by partitions for elongated header box, e.g. with transversal and longitudinal partitions having only longitudinal partitions
    • F28F9/0217—Header boxes having their inner space divided by partitions for elongated header box, e.g. with transversal and longitudinal partitions having only longitudinal partitions the partitions being separate elements attached to header boxes

Definitions

  • Fig. 1 shows the known pressure-enthalpy diagram for water / steam, in which some frequently occurring work areas A to E are shown.
  • X means the proportion of steam
  • X 0 for pure water
  • X 1 for pure steam.
  • the water-steam state moves roughly within area A and during a start after approximately eight hours of inactivity, this state runs approximately within area B, area C being common to A and B.
  • the water content in the mixture predominates and the pressure head losses in the pipes therefore predominate. This means that in areas A, B and C there is above all the risk of the flow stagnating through individual pipes.
  • DE-C-882 996 proposes arranging in the tubular container a partition wall which extends in the longitudinal direction and divides the container into two communicating chambers.
  • the dividing wall is flat, leaves the communicating connection for the liquid phase free between its lower edge and the container bottom and has tongue-like extensions on its upper edge, one of which projects into the supply lines opening into the container from above.
  • the discharge lines branch off in the upper area of the container on both sides of the partition.
  • the mixture supplied is divided into two partial streams and fed to the two chambers, from which it is then assigned to the respective chamber neten discharge lines.
  • a liquid level is formed in each sub-chamber which, despite the partition, is still subject to strong fluctuations in the inflowing mixture, which has an unfavorable effect on a uniform distribution of the phases in the discharge lines.
  • the invention is based on the features of the preamble of claim 1 from the known container with a partition according to DE-C-882 996. It is based on the task of further improving the phase distribution container of this type in such a way that the level in it is better kept constant under all circumstances, so that it works optimally with any gas-liquid mixing ratio and at the same time the design and manufacturing costs remain low.
  • the design of the partition as a U-shaped channel divides the container space into an inlet chamber and an outlet chamber, which communicate with one another not only on the liquid side but also on the gas side. In this way it is achieved that level fluctuations in the inlet chamber have only a weak weakening effect on the level in the outlet chamber.
  • the distribution of the two phases of the mixture flowing in the discharge lines is thereby more uniform than in the known containers with a flat partition and without a gas passage opening.
  • An additional advantage of the invention can be seen in the fact that it can be applied to already existing phase distribution containers by subsequently installing the U-shaped channel as a partition. Another advantage is the strengthening of the container by the channel when it is connected to the ends of the container.
  • a phase distributor container for an evaporator is known from US-A-2 220 595.
  • the container is cylindrical and is vertical.
  • a feed line for the two-phase mixture opens tangentially into the container in order to impose a rotational flow on the mixture in the container.
  • a coaxial cylindrical partition is arranged inside the container, which ends at a distance from the container bottom at its lower end and has window-like cutouts at its upper end connected to the container ceiling, which form gas passage openings.
  • several discharge lines for the mixture protrude from above, which dip into the liquid phase with their lower ends and which have axial longitudinal slots in their lower half through which the two-phase mixture can flow into the discharge lines.
  • a partition in the form of a U-shaped channel 15 is arranged in the interior of the phase distributor container 1 and extends along it and is welded to the two end plates 40.
  • the channel 15 divides the interior of the phase distributor container 1 into two chambers: an inlet chamber 2, which is surrounded by the channel 15, and an outlet chamber 3, which surrounds the channel 15.
  • two gas passage openings 11 are provided, via which the inlet chamber 2 and the outlet chamber 3 are connected. Both chambers are further connected by liquid passage openings 12, which are in the form of round holes in the horizontal part of the channel serving as the bottom of the inlet chamber 2.
  • Supply lines 20 run essentially vertically and open into the inlet chamber 2 after they have been bent slightly in the direction of the center of the circular cross section of the phase distributor container 1.
  • Discharge lines 30 likewise run essentially vertically, but are more bent than the feed lines 20 before they also open into the outlet chamber 3, also aimed at the center of the cross section of the phase distributor container 1.
  • the feed and discharge lines 20 and 30 run symmetrically to a vertical plane through the longitudinal axis of the phase distributor container 1, so that all the mouths of the feed lines and all of the mouths of the discharge lines each lie in the same height range.
  • the phase distributor container 1 functions as follows:
  • a mixture of a liquid and a gaseous phase flows through the feed lines 20 and is injected into the inlet chamber 2.
  • the deflection of the irradiated mixture and the different specific weights of the two phases separate them from one another in the inlet chamber 2, with a generally strong swirl prevailing in the inlet chamber 2.
  • the separated gaseous phase escapes through the narrow gas through openings 11 into the outlet chamber 3, as a result of which it flows to the discharge lines 30 in a largely calm manner.
  • the separated liquid phase in turn leaves the on Step chamber 2 through the liquid passage opening 12 and collects in the outlet chamber 3, the extremely limited connection to the inlet chamber 2 and the relatively large liquid mass in the outlet chamber 3 prevent the transmission of turbulence from the inlet chamber 2 to the outlet chamber 3.
  • a stable and uniformly distributed level 31 is thus established in the outlet chamber 3 between the two phases, and the gaseous phase flowing in each mouth to a discharge line 30 entrains a well-dosed amount of liquid.
  • the phase distributor container 1 only functions as a liquid separator.
  • the level 31 rises quickly and closes the mouths to the discharge lines 30 more and more:
  • the amount of gas to be discharged remains approximately constant, it flows faster and faster through the remaining cross-sections of the flow according to the known laws of continuity mentioned mouths, so that the static pressure is always lower and the amount of liquid sucked in is greater.
  • the phase distributor container 1 With a reasonable dimensioning of the various lines and components of the phase distributor container 1, this results in an operating state in which the amount drawn in is equal to the amount of liquid entering through the liquid passage openings 12 and the level 31 remains constant. If the proportion of liquid in the incoming mixture changes, the level 31 shifts and the proportion of liquid in the discharge lines 30 changes accordingly.
  • the actual function of the phase distributor container is fulfilled in all cases because - whether no liquid or pure liquid flows in the discharge lines 30 - the phase distribution is constant for a specific operating state and is the same for all discharge lines 30.
  • phase distributor container 1 according to the invention according to FIGS. 2 and 3 has proven itself better than the phase distributor container according to the prior art, because the steam entering when it passes through the Entry chamber 2 to the exit chamber 3 is very well distributed and has a uniform temperature in the exit chamber.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Feeding, Discharge, Calcimining, Fusing, And Gas-Generation Devices (AREA)
  • Separating Particles In Gases By Inertia (AREA)

Description

Rohrförmige Phasenverteilerbehälter für ein Gas-Flüssigkeitsgemisch sind in Form sogenannter Kollektoren in Dampferzeugern bekannt und in der Einleitung der DE-C-882 996 erwähnt. Sie sind mit einer Anzahl Zufuhrleitungen und mit einer gleich oder verschieden grossen Anzahl Abfuhrleitungen verbunden. Der Zweck dieser Kollektoren ist, die zwei Phasen des Gemisches gleichmässig so zu verteilen, dass in allen Abfuhrleitungen ihre Anteile gleich und für einen konstanten Betriebszustand konstant bleiben, unabhängig davon, ob unterschiedliche Phasenverteilungen zwischen den einzelnen Zufuhrleitungen und/oder in diesen als zeitliche Änderungen vorkommen. Dies geschieht folgendermassen:

  • 1. Im relativ grossen Innenraum des Kollektors sinkt die Geschwindigkeit des Gemisches auf einen relativ niedrigen Wert, die Strömung beruhigt sich und eine Trennung der Gemischphasen, hauptsächlich infolge der verschiedenen spezifischen Gewichte, findet statt.
  • 2. Die Oberfläche der nun verhältnismässig ruhigen flüssigen Phase bildet ein Niveau, das die Mündungsöffnung jeder Abfuhrleitung schneidet. Die schnell fliessende, austretende gasförmige Phase weist im Bereich dieser Mündung einen niedrigeren statischen Druck auf als die sich in Ruhe befindende flüssige Phase, so dass diese von jener teilweise mitgerissen wird. Die Mündungsöffnüng jeder Abfuhrleitung funktioniert also etwa wie eine Strahlpumpe. Bei gleichbleibendem Niveau und gleichbleibenden Druckverhältnissen zwischen dem Inneren des Kollektors und den Abfuhrleitungen ist die Menge an mitgerissener Flüssigkeit konstant und kann durch entsprechende Auslegung der beteiligten Komponenten im voraus bestimmt werden. Es ist auf diese Weise möglich, die Phasenanteile in dem austretenden Gemisch zu steuern und konstant zu halten, selbst wenn die Anzahl der Zufuhrleitungen von der Anzahl der Abfuhrleitungen verschieden ist.
Tubular phase distribution containers for a gas-liquid mixture are known in the form of collectors in steam generators and are mentioned in the introduction to DE-C-882 996. They are connected to a number of supply lines and to an equal or different number of discharge lines. The purpose of these collectors is to evenly distribute the two phases of the mixture so that their proportions remain the same in all discharge lines and remain constant for a constant operating state, regardless of whether different phase distributions between the individual supply lines and / or in these occur as changes over time . This is done as follows:
  • 1. In the relatively large interior of the collector, the speed of the mixture drops to a relatively low value, the flow calms down and a separation of the mixture phases takes place, mainly due to the different specific weights.
  • 2. The surface of the now relatively calm liquid phase forms a level that intersects the mouth of each discharge line. The rapidly flowing, exiting gaseous phase has a lower static pressure in the area of this mouth than the liquid phase which is at rest, so that it is partially entrained by it. The mouth opening of each discharge line works like a jet pump. With a constant level and pressure conditions between the interior of the collector and the discharge lines, the amount of entrained liquid is constant and can be determined in advance by appropriate design of the components involved. In this way it is possible to control the phase components in the emerging mixture and to keep them constant, even if the number of supply lines is different from the number of discharge lines.

Die bekannten Kollektoren weisen jedoch zwei wesentliche Nachteile auf:

  • - Bei hoher Eintrittsgeschwindigkeit des Gemisches entsteht im Bereich der Mündungsöffnung der Zufuhrleitungen eine starke Verwirbelung, die sich auf den ganzen Kollektor auswirkt, so dass das Einhalten eines konstanten Niveaus sowohl zeitlich als auch in Längsrichtung des Kollektors unmöglich ist.
  • - Infolge des relativ hohen Druckes im Bereich der Mündungsöffnung der Zufuhrleitungen und des niedrigeren Druckes im Bereich der Mündungsöffnung der Abfuhrleitungen, ergeben sich unterschiedliche Niveaus in Längsrichtung des Kollektors, selbst bei niedrigen Einströmgeschwindigkeiten des Gemisches. Diese Nachteile verunmöglichen das Einhalten einer gleichen Phasenverteilung in alle Abfuhrleitungen.
However, the known collectors have two major disadvantages:
  • - If the mixture enters at a high speed, there is a strong swirl in the area of the mouth of the feed lines, which affects the entire collector, so that it is impossible to maintain a constant level both in time and in the longitudinal direction of the collector.
  • - Due to the relatively high pressure in the area of the mouth of the supply lines and the lower pressure in the area of the mouth of the discharge lines, there are different levels in the longitudinal direction of the collector, even at low inflow speeds of the mixture. These disadvantages make it impossible to maintain the same phase distribution in all discharge lines.

Die Störung des Niveaus im Bereich der Mündungsöffnung der Abfuhrleitungen beeinträchtigt deshalb die Funktionstüchtigkeit der bekannten Kollektoren. Dazu kommen noch Störungen infolge des Betriebszustandes. Bei Dampferzeugern ist deren Brennkammer vorzugsweise von vertikalen Rohren gebildet, in denen Wasser von unten nach oben strömt, das von den Verbrennungsgasen in der Brennkammer erhitzt wird. Da die Wärmeverteilung innerhalb der Brennkammer nicht ideal ist, ist die Wärmeaufnahme des Wassers in den einzelnen Rohren ungleich und das Wasser- Dampf-Gemisch, das am oberen Ende der Rohre austritt, weist erhebliche Zustandsunterschiede auf. Das Gemisch wird deshalb den Kollektoren zugeführt, aus denen in allen Abfuhrleitungen ein einen gleichen Zustand aufweisendes Wasser- Dampf-Gemisch austreten soll. In der Praxis sind aber oft grosse Abweichungen vom Sollwert feststellbar, was anhand von Fig. 1 erläutert werden soll.The disturbance of the level in the area of the mouth of the discharge lines therefore affects the functionality of the known collectors. There are also malfunctions due to the operating state. In the case of steam generators, their combustion chamber is preferably formed by vertical tubes in which water flows from the bottom upwards, which is heated by the combustion gases in the combustion chamber. Since the heat distribution within the combustion chamber is not ideal, the heat absorption of the water in the individual pipes is uneven and the water-steam mixture that emerges at the upper end of the pipes shows considerable differences in condition. The mixture is therefore fed to the collectors, from which a water-steam mixture with the same state is to emerge in all discharge lines. In practice, however, large deviations from the target value can often be determined, which will be explained with reference to FIG. 1.

Fig. 1 zeigt das bekannte Druck-Enthalpiediagramm für Wasser/Dampf, in dem einige häufig auftretende Arbeitsbereiche A bis E eingezeichnet sind. Der Zweiphasenbereich verläuft zwischen den Linien X = 0 und X = 1, wobei X der Dampfanteil bedeutet, mit X = 0 bei reinem Wasser und X = 1 bei reinem Dampf. Während eines kalten Startes bewegt sich der Wasser-Dampf-Zustand grob innerhalb des Bereiches A und während eines Startes nach ca. acht Stunden Betriebsunterbruch verläuft dieser Zustand etwa innerhalb des Bereiches B, wobei der Bereich C zu A und B gemeinsam ist. In diesen Betriebsbereichen überwiegt der Wasseranteil im Gemisch und dadurch überwiegen in den Rohren die Druckhöhenverluste. Das heisst, dass in den Bereichen A, B und C vor allem die Gefahr einer Stagnation des Durchflusses durch einzelne Rohre besteht. Im Bereich D überwiegt die Dampfmenge und damit überwiegen die Reibungsdruckverluste; das Hauptproblem ist dabei die Verteilung der kleinen Wassermenge. Im Bereich E, wo nur Dampf vorhanden ist, muss dieser so gut verteilt werden, dass eine Vergleichmässigung der Temperatur erfolgt. Der Phasenverteilerbehälter muss also bei allen diesen sehr unterschiedlichen Betriebsbereichen die entsprechend verschiedenartigen Aufgaben erfüllen können. Die bekannten Kollektoren arbeiten jedoch höchstens in einem einzigen dieser Bereiche zufriedenstellend und in den übrigen Bereichen schlechter.Fig. 1 shows the known pressure-enthalpy diagram for water / steam, in which some frequently occurring work areas A to E are shown. The two-phase range runs between the lines X = 0 and X = 1, where X means the proportion of steam, with X = 0 for pure water and X = 1 for pure steam. During a cold start, the water-steam state moves roughly within area A and during a start after approximately eight hours of inactivity, this state runs approximately within area B, area C being common to A and B. In these operating areas, the water content in the mixture predominates and the pressure head losses in the pipes therefore predominate. This means that in areas A, B and C there is above all the risk of the flow stagnating through individual pipes. In area D the amount of steam predominates and thus the friction pressure losses predominate; the main problem is the distribution of the small amount of water. In area E, where there is only steam, it must be distributed so well that the temperature is evened out. The phase distributor container must therefore be able to perform the correspondingly different tasks in all of these very different operating areas. However, the known collectors work satisfactorily in at most one of these areas and worse in the other areas.

Zum Beheben dieser Nachteile wird in der DE-C-882 996 vorgeschlagen, in dem rohrförmigen Behälter eine in dessen Längsrichtung sich erstreckende Trennwand anzuordnen, die den Behälter in zwei kommunizierende Kammern unterteilt. Die Trennwand ist eben, lässt zwischen ihrem unteren Rand und dem Behälterboden die kommunizierende Verbindung für die flüssige Phase frei und weist an ihrem oberen Rand zungenartige Fortsätze auf, von denen jeweils eine in die von oben in den Behälter mündenden Zufuhrleitungen ragt. Im oberen Bereich des Behälters beiderseits der Trennwand zweigen die Abfuhrleitungen ab. Bei dem bekannten Behälter wird also das zugeführte Gemisch in zwei Teilströme unterteilt und den beiden Kammern zugeführt, aus denen es dann in die jeweils der Kammer zugeordneten Abfuhrleitungen gelangt. In jeder Teilkammer bildet sich ein Flüssigkeitsniveau, das trotz der Trennwand noch starken Schwankungen vom zuströmenden Gemisch her unterliegt, was sich auf eine gleichmässige Verteilung der Phasen in den Abfuhrleitungen ungünstig auswirkt.In order to overcome these disadvantages, DE-C-882 996 proposes arranging in the tubular container a partition wall which extends in the longitudinal direction and divides the container into two communicating chambers. The dividing wall is flat, leaves the communicating connection for the liquid phase free between its lower edge and the container bottom and has tongue-like extensions on its upper edge, one of which projects into the supply lines opening into the container from above. The discharge lines branch off in the upper area of the container on both sides of the partition. In the known container, the mixture supplied is divided into two partial streams and fed to the two chambers, from which it is then assigned to the respective chamber neten discharge lines. A liquid level is formed in each sub-chamber which, despite the partition, is still subject to strong fluctuations in the inflowing mixture, which has an unfavorable effect on a uniform distribution of the phases in the discharge lines.

Die Erfindung geht gemäss den Merkmalen des Oberbegriffs des Anspruchs 1 von dem bekannten Behälter mit Trennwand nach der DE-C-882 996 aus. Ihr liegt die Aufgabe zugrunde, den Phasenverteilerbehälter dieser Art dahingehend weiter zu verbessern, dass in ihm das Niveau unter allen Umständen besser konstant gehalten wird, so dass er bei jedem Gas-Flüssigkeits-Mischverhältnis optimal arbeitet und gleichzeitig der konstruktive und herstellungsmässige Aufwand gering bleibt.The invention is based on the features of the preamble of claim 1 from the known container with a partition according to DE-C-882 996. It is based on the task of further improving the phase distribution container of this type in such a way that the level in it is better kept constant under all circumstances, so that it works optimally with any gas-liquid mixing ratio and at the same time the design and manufacturing costs remain low.

Diese Aufgabe wird erfindungsgemäss durch die kennzeichnenden Merkmale des Anspruchs 1 gelöst.According to the invention, this object is achieved by the characterizing features of claim 1.

Durch die Ausbildung der Trennwand als U-förmige Rinne wird eine Unterteilung des Behälterraumes in eine Eintrittskammer und eine Austrittskammer bewirkt, die nicht nur flüssigkeitsseitig, sondern auch gasseitig miteinander kommunizieren. Auf diese Weise wird erreicht, dass Niveauschwankungen in der Eintrittskammer sich nur stark abgeschwächt auf das Niveau in der Austrittskammer auswirken. Die Verteilung der beiden Phasen des in den Abfuhrleitungen strömenden Gemisches wird dadurch gleichmässiger als bei den bekannten Behältern mit ebener Trennwand und ohne Gasdurchtrittsöffnung.The design of the partition as a U-shaped channel divides the container space into an inlet chamber and an outlet chamber, which communicate with one another not only on the liquid side but also on the gas side. In this way it is achieved that level fluctuations in the inlet chamber have only a weak weakening effect on the level in the outlet chamber. The distribution of the two phases of the mixture flowing in the discharge lines is thereby more uniform than in the known containers with a flat partition and without a gas passage opening.

Ein zusätzlicher Vorteil der Erfindung ist darin zu sehen, dass sie auf schon bestehende Phasenverteilerbehälter angewendet werden kann, indem nachträglich die U-förmige Rinne als Trennwand eingebaut wird. Ein weiterer Vorteil besteht in der festigkeitsmässigen Verstärkung des Behälters durch die Rinne, wenn diese an den Enden des Behälters mit diesem verbunden wird.An additional advantage of the invention can be seen in the fact that it can be applied to already existing phase distribution containers by subsequently installing the U-shaped channel as a partition. Another advantage is the strengthening of the container by the channel when it is connected to the ends of the container.

Aus der US-A-2 220 595 ist ein Phasenverteilerbehälter für einen Verdampfer bekannt. Der Behälter ist zylindrisch und steht vertikal. Eine Zufuhrleitung für das Zweiphasengemisch mündet tangential in den Behälter, um dem Gemisch im Behälter eine Rotationsströmung aufzuzwingen. Innerhalb des Behälters ist eine koaxiale zylindrische Trennwand angeordnet, die an ihrem unteren Ende mit Abstand vom Behälterboden endet und an ihrem oberen, mit der Behälterdecke verbundenen Ende fensterartige Ausschnitte aufweist, die Gasdurchtrittsöffnungen bilden. In den Innenraum der zylindrischen Trennwand ragen von oben mehrere Abfuhrleitungen für das Gemisch, die mit ihren unteren Enden in die flüssige Phase tauchen und die in ihrer unteren Hälfte axiale Längsschlitze aufweisen, über die das Zweiphasengemisch in die Abfuhrleitungen einströmen kann.A phase distributor container for an evaporator is known from US-A-2 220 595. The container is cylindrical and is vertical. A feed line for the two-phase mixture opens tangentially into the container in order to impose a rotational flow on the mixture in the container. A coaxial cylindrical partition is arranged inside the container, which ends at a distance from the container bottom at its lower end and has window-like cutouts at its upper end connected to the container ceiling, which form gas passage openings. In the interior of the cylindrical partition, several discharge lines for the mixture protrude from above, which dip into the liquid phase with their lower ends and which have axial longitudinal slots in their lower half through which the two-phase mixture can flow into the discharge lines.

Einige bevorzugte Ausführungsbeispiele der Erfindung sind in der folgenden Beschreibung anhand der Zeichnung näher erläutert. Es zeigen:

  • Fig. 1 ein Druck-Enthalpie-Diagramm für Wasser/Dampf, in dem einige häufig auftretende Arbeitsbereiche eingezeichnet sind; wurde bereits besprochen.
  • Fig. 2 und 3 einen kollektorartigen Phasenverteilerbehälter nach der Erfindung, mit gleichvielen Zufuhr- und Abfuhrleitungen, wobei Fig. 2 ein Schnitt gemäss der Ebene 111-111 in Fig. 3 ist.
  • Fig. 4 und 5 einen abgewandelten Phasenverteilerbehälter mit zehn Abfuhrleitungen auf eine Zufuhrleitung, wobei Fig. 4 einen Schnitt gemäss Ebene V-V in Fig. 5 darstellt.
Some preferred exemplary embodiments of the invention are explained in more detail in the following description with reference to the drawing. Show it:
  • Figure 1 is a pressure-enthalpy diagram for water / steam, in which some frequently occurring work areas are shown. has already been discussed.
  • 2 and 3 a collector-like phase distributor container according to the invention, with the same number of supply and discharge lines, FIG. 2 being a section according to plane 111-111 in FIG. 3.
  • 4 and 5 a modified phase distribution container with ten discharge lines to a supply line, FIG. 4 showing a section along plane VV in FIG. 5.

Der Phasenverteilerbehälter 1 nach Fig. 2 und 3 besteht im wesentlichen aus einem horizontalen Rohr, das an beiden Enden mittels dicht verschweisster kreisrunder Abschlussplatten 40 geschlossen ist. Eine Trennwand in Form einer U-förmigen Rinne 15 ist im Innern des Phasenverteilerbehälters 1 diesem entlang verlaufend angeordnet und an den beiden Abschlussplatten 40 fest angeschweisst. Durch die Rinne 15 ist das Innere des Phasenverteilerbehälters 1 in zwei Kammern unterteilt: eine Eintrittskammer 2, die von der Rinne 15 umgeben ist, und eine Austrittskammer 3, die die Rinne 15 umgibt. Zwischen dem Phasenverteilerbehälter 1 und entlang den oberen Kanten der vertikalen Rinnenteile sind zwei Gasdurchtrittsöffnungen 11 vorgesehen, über die die Eintrittskammer 2 und die Austrittskammer 3 verbunden sind. Beide Kammern sind ferner durch Flüssigkeitsdurchtrittsöffnungen 12 verbunden, die sich in Form von runden Löchern im horizontalen als Boden der Eintrittskammer 2 dienenden Teil der Rinne befinden.2 and 3 consists essentially of a horizontal tube which is closed at both ends by means of tightly welded circular end plates 40. A partition in the form of a U-shaped channel 15 is arranged in the interior of the phase distributor container 1 and extends along it and is welded to the two end plates 40. The channel 15 divides the interior of the phase distributor container 1 into two chambers: an inlet chamber 2, which is surrounded by the channel 15, and an outlet chamber 3, which surrounds the channel 15. Between the phase distributor container 1 and along the upper edges of the vertical channel parts, two gas passage openings 11 are provided, via which the inlet chamber 2 and the outlet chamber 3 are connected. Both chambers are further connected by liquid passage openings 12, which are in the form of round holes in the horizontal part of the channel serving as the bottom of the inlet chamber 2.

Zufuhrleitungen 20 verlaufen im wesentlichen vertikal und münden in die Eintrittskammer 2, nachdem sie in Richtung auf das Zentrum des kreisrunden Querschnittes des Phasenverteilerbehälters 1 leicht gebogen sind. Ebenfalls im wesentlichen vertikal, verlaufen Abfuhrleitungen 30, welche jedoch stärker als die Zufuhrleitungen 20 gebogen sind, bevor sie, auch auf das Zentrum des Querschnittes des Phasenverteilerbehälters 1 zielend, in die Austrittskammer 3 münden. Die Zu-und Abfuhrleitungen 20 bzw. 30 verlaufen symmetrisch zu einer vertikalen Ebene durch die Längsachse des Phasenverteilerbehälters 1, so dass sämtliche Mündungen der Zufuhrleitungen und sämtliche Mündungen der Abfuhrleitungen jeweils im gleichen Höhenbereich liegen.Supply lines 20 run essentially vertically and open into the inlet chamber 2 after they have been bent slightly in the direction of the center of the circular cross section of the phase distributor container 1. Discharge lines 30 likewise run essentially vertically, but are more bent than the feed lines 20 before they also open into the outlet chamber 3, also aimed at the center of the cross section of the phase distributor container 1. The feed and discharge lines 20 and 30 run symmetrically to a vertical plane through the longitudinal axis of the phase distributor container 1, so that all the mouths of the feed lines and all of the mouths of the discharge lines each lie in the same height range.

Der Phasenverteilerbehälter 1 nach den Fig. 2 und 3 funktioniert wie folgt:The phase distributor container 1 according to FIGS. 2 and 3 functions as follows:

Durch die Zufuhrleitungen 20 fliesst ein Gemisch aus einer flüssigen und einer gasförmigen Phase, welches in die Eintrittskammer 2 eingestrahlt wird. Durch die Umlenkung des eingestrahlten Gemisches und durch die unterschiedlichen spezifischen Gewichte der zwei Phasen werden diese in der Eintrittskammer 2 voneinander getrennt, wobei in der Eintrittskammer 2 eine allgemein starke Verwirbelung herrscht. Die abgetrennte gasförmige Phase entweicht durch die schmalen Gasdurchtrittsöffnungen 11 in die Austrittskammer 3, wodurch sie weitgehend beruhigt zu den Abfuhrleitungen 30 hin fliesst. Die abgetrennte flüssige Phase verlässt ihrerseits die Eintrittskammer 2 durch die Flüssigkeitsdurchtrittsöffnung 12 und sammelt sich in der Austrittskammer 3, wobei die äusserst begrenzte Verbindung zu der Eintrittskammer 2 und die relativ grosse Flüssigkeitsmasse in der Austrittskammer 3 die Übertragung der Verwirbelungen von der Eintrittskammer 2 zu der Austrittskammer 3 verhindern. In der Austrittskammer 3 stellt sich also ein stabiles und gleichmässig verteiltes Niveau 31 zwischen die beiden Phasen ein und die in jeder Mündung zu einer Abfuhrleitung 30 fliessende gasförmige Phase reisst eine gut dosierte Flüssigkeitsmenge mit. Während kurzer Zeit, am Anfang des Betriebes, bis genügend Flüssigkeit sich in der Austrittskammer 3 angesammelt hat, um die Mündungen zu den Abfuhrleitungen 30 zu erreichen, fliesst natürlich nur gasförmige Phase aus dem Phasenverteilerbehälter 1 heraus. Diese Zeit ist meistens sehr kurz. Ist die Menge an flüssiger Phase jedoch so klein, dass die Höhe der Mündungen zu den Abfuhrleitungen 30 nicht erreicht wird, so funktioniert der Phasenverteilerbehälter 1 lediglich als Flüssigkeitsabscheider. Ist dagegen die Flüssigkeitsmenge sehr gross, steigt das Niveau 31 rasch an und sperrt die Mündungen zu den Abfuhrleitungen 30 immer mehr zu: da aber die abzuführende Gasmenge etwa kontant bleibt, fliesst sie nach den bekannten Gesetzen der Kontinuität immer schneller durch die ihr verbleibenden Durchtrittsquerschnitte der erwähnten Mündungen hindurch, so dass der statische Druck immer geringer und die angesaugte Flüssigkeitsmenge immer grösser wird. Es ergibt sich also bei einer vernünftigen Dimensionierung der verschiedenen Leitungen und Komponenten des Phasenverteilerbehälters 1 ein Betriebszustand, bei dem die angesaugte gleich der durch die Flüssigkeitsdurchtrittsöffnungen 12 eintretenden Flüssigkeitsmenge ist, und das Niveau 31 konstant bleibt. Bei Änderungen des Flüssigkeitsanteils im eintretenden Gemisch verschiebt sich das Niveau 31 und der Flüssigkeitsanteil in den Abfuhrleitungen 30 verändert sich entsprechend. Die eigentliche Funktion des Phasenverteilerbehälters wird auf alle Fälle erfüllt, weil - ob keine Flüssigkeit oder reine Flüssigkeit in den Abfuhrleitungen 30 fliesst - die Phasenverteilung für einen bestimmten Betriebszustand konstant und für alle Abfuhrleitungen 30 gleich ist.A mixture of a liquid and a gaseous phase flows through the feed lines 20 and is injected into the inlet chamber 2. The deflection of the irradiated mixture and the different specific weights of the two phases separate them from one another in the inlet chamber 2, with a generally strong swirl prevailing in the inlet chamber 2. The separated gaseous phase escapes through the narrow gas through openings 11 into the outlet chamber 3, as a result of which it flows to the discharge lines 30 in a largely calm manner. The separated liquid phase in turn leaves the on Step chamber 2 through the liquid passage opening 12 and collects in the outlet chamber 3, the extremely limited connection to the inlet chamber 2 and the relatively large liquid mass in the outlet chamber 3 prevent the transmission of turbulence from the inlet chamber 2 to the outlet chamber 3. A stable and uniformly distributed level 31 is thus established in the outlet chamber 3 between the two phases, and the gaseous phase flowing in each mouth to a discharge line 30 entrains a well-dosed amount of liquid. During a short time, at the beginning of the operation, until sufficient liquid has accumulated in the outlet chamber 3 in order to reach the outlets to the discharge lines 30, only gaseous phase naturally flows out of the phase distributor container 1. This time is usually very short. However, if the amount of liquid phase is so small that the height of the mouths to the discharge lines 30 is not reached, the phase distributor container 1 only functions as a liquid separator. If, on the other hand, the amount of liquid is very large, the level 31 rises quickly and closes the mouths to the discharge lines 30 more and more: However, since the amount of gas to be discharged remains approximately constant, it flows faster and faster through the remaining cross-sections of the flow according to the known laws of continuity mentioned mouths, so that the static pressure is always lower and the amount of liquid sucked in is greater. With a reasonable dimensioning of the various lines and components of the phase distributor container 1, this results in an operating state in which the amount drawn in is equal to the amount of liquid entering through the liquid passage openings 12 and the level 31 remains constant. If the proportion of liquid in the incoming mixture changes, the level 31 shifts and the proportion of liquid in the discharge lines 30 changes accordingly. The actual function of the phase distributor container is fulfilled in all cases because - whether no liquid or pure liquid flows in the discharge lines 30 - the phase distribution is constant for a specific operating state and is the same for all discharge lines 30.

Auch im Einphasenbetrieb, wie beispielsweise beim Betrieb mit reinem Dampf im Bereich E der Fig. 1, bewährt sich ein erfindungsgemässer Phasenverteilerbehälter 1 nach den Fig. 2 und 3 besser als der Phasenverteilerbehälter nach dem Stande der Technik, weil der eintretende Dampf beim Durchtritt von der Eintrittskammer 2 zur Austrittskammer 3 sehr gut verteilt wird und in der Austrittskammer eine vergleichmässigte Temperatur aufweist.Also in single-phase operation, such as when operating with pure steam in area E of FIG. 1, a phase distributor container 1 according to the invention according to FIGS. 2 and 3 has proven itself better than the phase distributor container according to the prior art, because the steam entering when it passes through the Entry chamber 2 to the exit chamber 3 is very well distributed and has a uniform temperature in the exit chamber.

Beim ähnlichen Ausführungsbeispiel nach den Fig. 4 und 5, sind zehn Abfuhrleitungen 30 für jede Zufuhrleitung 21 vorhanden, die Funktionsweise bleibt aber genau gleich wie im Falle der Fig. 2 und 3.In the similar embodiment according to FIGS. 4 and 5, ten discharge lines 30 are provided for each feed line 21, but the mode of operation remains exactly the same as in the case of FIGS. 2 and 3.

Claims (3)

1. Tube shaped phase distributor vessel (1) for a gas-liquid mixture with a generally horizontal longitudinal axis and with several mixture supply lines (20) leading into the vessel (1) and several delivery lines (30) branching off from the vessel (1), and in the vessel a separator wall extending in the longitudinal direction the wall dividing the vessel into two communicating chambers, characterised in thatthe separator wall forms a U-shaped channel (15) which surrounds the one chamber as inlet chamber (2) and which is surrounded by the other chamber as outlet chamber, the supply lines (20) leading into the inlet chamber (2) and the delivery lines (30) branching off from the outer chamber (3), and in that for the gas phase of the mixture there is provided at least one gas through-flow opening (11) in the upper region of the channel (15) while the communicating connection for the liquid phase of the mixture is formed by a least one liquid through-flow opening (12) in the lower region of the channel (15), the gas- and liquid- through-flow openings (11 and 12) being so arranged that any turbulence in the inlet chamber (2) does not generally affect the surface in the outlet chamber (3).
2. Phase distributor vessel according to Claim 1, characterised in that the supply lines (20) lead into the upper region of the vessel (1) in two rows parallel to the length direction and directed towards the longitudinal axis.
3. Phase distributor vessel according to Claim 2 in which the delivery lines (30) are also arranged in the upper region of the vessel in rows parallel to the length direction, characterised in that the inlet and delivery lines (20 and 30) - viewed in the length direction of the vessel (1) - include an angle greater than 29° and less than 86°.
EP84107399A 1983-09-22 1984-06-27 Phase distribution container Expired EP0141029B1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CH5149/83 1983-09-22
CH514983 1983-09-22

Publications (3)

Publication Number Publication Date
EP0141029A2 EP0141029A2 (en) 1985-05-15
EP0141029A3 EP0141029A3 (en) 1986-01-02
EP0141029B1 true EP0141029B1 (en) 1988-08-24

Family

ID=4288752

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EP84107399A Expired EP0141029B1 (en) 1983-09-22 1984-06-27 Phase distribution container

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US (1) US4650503A (en)
EP (1) EP0141029B1 (en)
JP (1) JPS6073201A (en)
AU (1) AU562508B2 (en)
CA (1) CA1249527A (en)
DE (1) DE3473638D1 (en)
IN (1) IN160977B (en)
PL (1) PL142950B1 (en)

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GB2209286B (en) * 1987-09-02 1991-05-01 Shell Int Research Apparatus for separating dispersed phases from fluid mixtures
US4902404A (en) * 1988-07-05 1990-02-20 Exxon Research And Engineering Company Hydrotreating process with catalyst staging
US6694999B2 (en) * 2001-12-07 2004-02-24 Hettinger Welding, Inc. Systems for well gas collection and processing
JP2006234347A (en) * 2005-02-28 2006-09-07 Daikin Ind Ltd Refrigerant flow divider and refrigerating device using the same
FR2963417B1 (en) * 2010-08-02 2014-03-28 Air Liquide U-SHAPED TUBE VAPORIZER
US20130220238A1 (en) * 2012-02-28 2013-08-29 Hrst, Inc. Dual Chemistry Steam Drum
KR101464556B1 (en) * 2014-05-07 2014-11-24 (주)코스모테크놀로지 Safety control system of automatic shutoff device and range hood and safty control method using the same

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Also Published As

Publication number Publication date
DE3473638D1 (en) 1988-09-29
JPS6073201A (en) 1985-04-25
US4650503A (en) 1987-03-17
CA1249527A (en) 1989-01-31
AU3335884A (en) 1985-03-28
EP0141029A2 (en) 1985-05-15
AU562508B2 (en) 1987-06-11
EP0141029A3 (en) 1986-01-02
JPH0541884B2 (en) 1993-06-24
IN160977B (en) 1987-08-22
PL249686A1 (en) 1985-05-07
PL142950B1 (en) 1987-12-31

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