EP2352959B1 - Indirectly heated fluidized bed dryer - Google Patents

Indirectly heated fluidized bed dryer Download PDF

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Publication number
EP2352959B1
EP2352959B1 EP08875030.2A EP08875030A EP2352959B1 EP 2352959 B1 EP2352959 B1 EP 2352959B1 EP 08875030 A EP08875030 A EP 08875030A EP 2352959 B1 EP2352959 B1 EP 2352959B1
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EP
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Prior art keywords
fluidized bed
bed dryer
heat exchanger
flow
dryer according
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EP08875030.2A
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German (de)
French (fr)
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EP2352959A1 (en
Inventor
Hans-Joachim Klutz
Claus Moser
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RWE Power AG
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RWE Power AG
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    • 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
    • F28D13/00—Heat-exchange apparatus using a fluidised bed
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B3/00—Drying solid materials or objects by processes involving the application of heat
    • F26B3/02—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air
    • F26B3/06—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour flowing through the materials or objects to be dried
    • F26B3/08—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour flowing through the materials or objects to be dried so as to loosen them, e.g. to form a fluidised bed
    • F26B3/084—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour flowing through the materials or objects to be dried so as to loosen them, e.g. to form a fluidised bed with heat exchange taking place in the fluidised bed, e.g. combined direct and indirect heat exchange

Definitions

  • the invention relates to an indirectly heated fluidized bed dryer for drying moist, fine-grained bulk materials, such as lignite, comprising a housing with a gassing, with above the gassing floor extending heat exchanger installations and at least one provided below the gassing floor discharge device for the dried bulk material, said usable flow cross section of the housing increases in the region of the heat exchanger installations over the entire height of the heat exchanger installations in the flow direction of the fluidizing gas.
  • Such a fluidized bed contact dryer is for example from EP 0 341 347 A1 known.
  • the vapor mass flow increases in the flow direction, which causes a corresponding increase in the flow velocity of the gas or the vapors within the dryer.
  • the maximum of the heat transfer is associated with a certain expansion state of the fluidized bed or a certain speed in the fluidized bed.
  • excessive expansion of the fluidized bed degrades the operation of the heat exchanger.
  • coarsening of the bed material by fine discharge also worsens the operation of the dryer.
  • the housing is formed by at least one trough, in each of which a steam flowed through by condensed heat exchanger in the form of a Geradrohrbündels in several steam passes with significantly reducing the number of tubes or steam cross section is arranged.
  • the tubes are arranged in the troughs of the contact dryer so as to give a uniform pitch of the heater.
  • the invention is therefore based on the object to improve a fluidized bed dryer of the type mentioned in terms of the best possible heat transfer.
  • an indirectly heated fluidized-bed dryer for drying moist, fine-grained bulk materials comprising a housing with a gassing bottom with heat exchanger installations extending above the gassing floor and at least one discharge device for the dried bulk material provided below the gassing floor, the usable flow cross-section
  • the fluidized bed dryer according to the invention is characterized in that the cross section of the housing is constant and decreases the packing density of the heat exchanger internals in the flow direction of the fluidizing gas of the housing in the region of the heat exchanger units over the entire height of the heat exchanger installations in the flow direction of the fluidizing gas.
  • the housing of the fluidized bed dryer according to the invention has a rectangular, preferably a square cross-section.
  • the housing has a circular cross-section.
  • tube bundles and / or plate packs are provided as heat exchangers, which are combined into segments of different pipe pitch and / or different plate spacings.
  • a heat exchanger tube bundle may be provided as a heat exchanger tube bundle, which are arranged in segments with different pipe diameters and / or different distances to each other. Expediently, the pipe diameters decrease in the flow direction of the fluidizing gas or their distances become larger in the direction of flow.
  • At least two or preferably three heat exchanger segments for example in the form of heating registers in the flow direction of the fluidizing gas, can be arranged one behind the other or connected in series.
  • all heat exchanger segments have an approximately equal heat exchange surface, so that an average falling speed level is established in the heat exchanger tubes.
  • the heat exchanger installations can be designed to be more continuous, preferably the heat exchanger installations are of three-flighted design, with each passage being connected to a condensate collector. By the latter measure name pressure losses are avoided due to entrained condensate.
  • the multi-pass arrangement of the heat exchanger tubes the heat transfer is increased on the inside of the steam-heated tubes, which contributes to the fact that the heat transfer coefficient and thus the efficiency of heat transfer is improved in total.
  • a variant of the fluidized-bed dryer according to the invention is characterized in that a funnel-shaped outlet is provided, which is geometrically designed so that sets mass flow when deducting bulk material. This means that all the contents of the spout are in motion when the material is removed. There are no or at most minimal dead zones or resting bulk zones. The opposite of this is generally referred to as a so-called Kempound, which may possibly cause a disturbance of the fluidization of the fluidized bed. This can occur, for example, when deposits accumulate on the fixed bed below the gassing soil, which are not moved when material is removed.
  • the steepness of the enclosing walls of the outlet is chosen so that sets mass flow when deducting bulk material, that is, when material removal, the entire fixed bed is in motion at each point.
  • the in FIG. 1 shown fluidized bed dryer (1) has a housing (2) with a rectangular cross-section.
  • a Rohbraunkohleneintrag a filler pipe (4) with a rotary valve (5).
  • a funnel-shaped outlet (7) is provided below a gassing floor (6), at the lower end of which a mechanical discharge, for example in the form of a rotary valve (5, FIG. ) is provided.
  • a mechanical discharge for example in the form of a rotary valve (5, FIG. ) is provided.
  • a mechanical discharge for example in the form of a rotary valve (5, FIG. ) is provided.
  • a mechanical discharge for example in the form of a rotary valve (5, FIG. ) is provided.
  • a mechanical discharge and a screw conveyor or the like there could be provided as a mechanical discharge and a screw conveyor or the like.
  • the fluidized-bed dryer (1) according to the embodiment is primarily intended for drying lignite and will be described with reference to a process for drying lignite, but the
  • the gassing bottom (6) is provided on its side facing away from the material take-off (7) with nozzles (8) for introducing a fluidizing gas.
  • a fluidizing gas or fluidizing medium is steam into consideration.
  • a partial flow from the fluidized bed dryer leaving vapors are diverted behind an electrostatic precipitator.
  • gassing floor (6) extend transversely to the gas flow and optionally slightly inclined heat exchanger installations in the form of tube bundles (9) or in the form of plates, which are traversed by steam as the heating medium.
  • the lignites introduced, for example, with a particle size of 0 to 2 mm and a water content of up to 65% by weight into the fluidized-bed dryer (1) are held above the gasification base (6) by means of the fluidizing medium in a quasi-stationary fluidized bed, the fluidized bed level in the fluidized-bed dryer (1) by the reference numeral (10).
  • the lignite grains in the fluidized bed come into contact with the tube bundle heat exchangers transversely across the housing (9), which are arranged in three segments 11 a, 11 b and 11 c in the flow direction one behind the other.
  • At temperatures of about 105 to 120 ° C more than 50% of the original weight of the coal to be dried is evaporated as water.
  • the vapor mass flow continuously increases in the region of the tube bundle heat exchanger (9) installed in the fluidized bed.
  • the speed of the vapors increases accordingly.
  • the stationary fluidized bed comes in an unstable area and the dust discharge of the fine coal content of the fluidized bed increases sharply. This essentially affects the particle size of less than 300 ⁇ m. This causes a coarsening of the bed material of the fluidized bed, which has a negative effect on the fluid mechanics and heat transfer in the fluidized bed.
  • the heat exchanger installations in the form of shell and tube heat exchanger in the described embodiments are designed with increasing pitch in the flow direction, thereby resulting in an increase in the useful cross-section of the housing (2) with the same cross section or diameter of the housing over the entire height of the heat exchanger installations.
  • the greater distance between the tubes of the tube bundle heat exchanger (9) to each other can be achieved either in that fewer tubes are arranged at a greater distance in a segment or that the tubes are designed in the flow direction with a reduced diameter.
  • the distance of the tubes from each other in the gassing bottom (6) nearest segment 11a is smaller than in the subsequent segment 11 b.
  • the distance of the tubes of the tube bundle heat exchanger (9) is greatest, so that there the fluidic usable cross section of the housing (2) is greatest, which counteracts an increase in velocity of the vapor mass flow in the flow direction.
  • the heat exchanger internals in the housing (2) are designed as a three-pass shell-and-tube heat exchanger with a total of three condensate collectors (13a, b, c).
  • the hot steam as the heating medium is introduced into the first, upper segment 11 a via the steam inlet designated by (14) into the tube bundle heat exchanger (9) which passes completely through the housing (2).
  • the transversely and optionally slightly inclined to the flow direction of the fluidizing medium passing tubes are flowed through by the heating medium, which flows on the opposite side of the steam inlet (14) into the condensate collector (13a).
  • the resulting condensate is removed separately.
  • the heating medium flows back into the condensate collector (13b) provided on the side of the steam inlet (14) and from there into the lowest condensate collector 13c.
  • the segments 11a, b, c or the heating registers 11a, b, c are designed such that their heat exchange surface is approximately the same, so that sets in the individual courses an average falling speed level.
  • the dried lignite collects in the funnel-shaped spout (7).
  • Funnel-shaped in the sense of the invention does not necessarily mean that the cross section of the outlet is annular.
  • the inclination of the enclosing walls of the outlet (7) is chosen so that adjusts mass flow in material removal, for example with the rotary valve.
  • mass flow means that the entire funnel contents are in motion, so that the fixed bed below the aeration bottom (6) evenly lowers when material is withdrawn. There are no or at most minimal dead zones, ie dormant bulk zones. The bulk material surface or the fixed bed sinks almost uniformly.

Description

Die Erfindung betrifft einen indirekt beheizten Wirbelschicht-Trockner zur Trocknung von feuchten, feinkörnigen Schüttgütern, wie beispielsweise Braunkohle, umfassend ein Gehäuse mit einem Begasungsboden, mit sich oberhalb des Begasungsbodens erstreckenden Wärmetauschereinbauten und wenigstens einer unterhalb des Begasungsbodens vorgesehenen Austragseinrichtung für das getrocknete Schüttgut, wobei der nutzbare Strömungsquerschnitt des Gehäuses im Bereich der Wärmetauschereinbauten über die gesamte Höhe der Wärmetauschereinbauten in Strömungsrichtung des Fluidisierungsgases zunimmt.The invention relates to an indirectly heated fluidized bed dryer for drying moist, fine-grained bulk materials, such as lignite, comprising a housing with a gassing, with above the gassing floor extending heat exchanger installations and at least one provided below the gassing floor discharge device for the dried bulk material, said usable flow cross section of the housing increases in the region of the heat exchanger installations over the entire height of the heat exchanger installations in the flow direction of the fluidizing gas.

Ein solcher Wirbelschicht-Kontakttrockner ist beispielsweise aus der EP 0 341 347 A1 bekannt.Such a fluidized bed contact dryer is for example from EP 0 341 347 A1 known.

Bei der Aufbereitung von Braunkohle als Kesselkohle zur Verbrennung in einem Dampferzeuger ist es bekannt, diese in Schlagrad- und Hammermühlen, die ein Teil des Kraftwerkskessels sind, gleichzeitig zu zerkleinem und zu vermahlen (Mahltrocknung), wobei die für die Trocknung erforderliche Trocknungsenergie durch einen abgezweigten Rauchgasstrom aufgebracht wird.In the treatment of lignite as boiler coal for combustion in a steam generator, it is known to crush and mill in Schlagrad- and hammer mills, which are part of the power plant boiler (grinding drying), the drying energy required for the drying by a branched Flue gas flow is applied.

Wie dies bereits im Stand der Technik beschrieben ist, kann die Trocknung von grubenfeuchter Rohbraunkohle in einem Wirbelschicht-Trockner energetisch günstiger sein. Wirbelschicht-Kontakttrockner sind allerdings konstruktiv aufwendige Apparate. Es gibt deshalb Bemühungen, das Wirbelschichtverfahren so zu gestalten, dass die Investitionskosten für den Trockner möglichst niedrig gehalten werden können. Beispielsweise in der DE 196 20 047 A1 wird hierzu vorgeschlagen, das Verfahren so zu gestalten, dass in dem Wirbelschicht-Trockner mit verhältnismäßig hohen Strömungsgeschwindigkeiten gearbeitet werden kann, so dass der Trockner eine verhältnismäßig kleine Querschnitts- und damit Grundfläche aufweisen kann.As has already been described in the prior art, the drying of pit-wet raw lignite in a fluidized-bed dryer can be more favorable in terms of energy. However, fluidized bed contact dryers are structurally complex apparatuses. There are therefore efforts to make the fluidized bed process so that the investment costs for the dryer can be kept as low as possible. For example, in the DE 196 20 047 A1 For this purpose, it is proposed to design the method so that it is possible to work with relatively high flow velocities in the fluidized-bed dryer so that the dryer can have a relatively small cross-sectional area and therefore base area.

Für den Wärmeübergang im Wirbelbett bzw. in der Wirbelschicht ist allerdings eine allzu hohe Strömungsgeschwindigkeit des den Trockner durchströmenden Gases nicht wünschenswert. Ab einer kritischen Geschwindigkeit kommt die stationäre Wirbelschicht in einen instabilen Bereich, weil der Austrag an feinstkörnigem Material aus der Wirbelschicht ansteigt. Hierdurch stellt sich eine Vergröberung des Bettmaterials der Wirbelschicht ein, was sich negativ auf die Strömungsmechanik und die Wärmeübertragung in der Wirbelschicht auswirkt.For the heat transfer in the fluidized bed or in the fluidized bed, however, an excessively high flow velocity of the dryer flowing through Gas not desirable. From a critical speed, the stationary fluidized bed comes in an unstable area, because the output of fine-grained material from the fluidized bed increases. This causes a coarsening of the bed material of the fluidized bed, which has a negative effect on the fluid mechanics and heat transfer in the fluidized bed.

Durch die Verdampfung von Wasser innerhalb des Trockners nimmt der Brüdenmassenstrom in Strömungsrichtung zu, was einen entsprechenden Anstieg der Strömungsgeschwindigkeit des Gases bzw. der Brüden innerhalb des Trockners bewirkt.Due to the evaporation of water within the dryer, the vapor mass flow increases in the flow direction, which causes a corresponding increase in the flow velocity of the gas or the vapors within the dryer.

In der CH 575 075 wird ein Wirbelschicht-Kontakttrockner beschrieben, wobei die wärmeübertragenden Wände sich je mindestens über 70% der Höhe des Wirbelbettes erstrecken. Einer vergrößerten Strömungsgeschwindigkeit wird durch eine Querschnittsabnahme im obersten Bereich der wärmeübertragenden Wände entgegengewirkt. In diesem Bereich wird so eine Beruhigungszone geschaffen.In the CH 575 075 a fluidized bed contact dryer is described, wherein the heat transferring walls each extend at least over 70% of the height of the fluidized bed. An increased flow rate is counteracted by a decrease in cross-section in the uppermost region of the heat-transferring walls. In this area, a calming zone is created.

Gemäß der Theorie der Wärmeübertragung in Wirbelschichten ist das Maximum des Wärmeüberganges einem bestimmten Expansionszustand der Wirbelschicht bzw. einer bestimmten Geschwindigkeit in der Wirbelschicht zugeordnet. Daraus resultiert, dass eine übermäßige Expansion der Wirbelschicht die Wirkungsweise des Wärmetauschers verschlechtert. Darüber hinaus verschlechtert eine Vergröbung des Bettmaterials durch Feinkomaustrag ebenfalls die Wirkungsweise des Trockners.According to the theory of heat transfer in fluidized beds, the maximum of the heat transfer is associated with a certain expansion state of the fluidized bed or a certain speed in the fluidized bed. As a result, excessive expansion of the fluidized bed degrades the operation of the heat exchanger. In addition, coarsening of the bed material by fine discharge also worsens the operation of the dryer.

In der EP 0 341 347 A1 ist ein Wirbelschicht-Kontakttrockner gemäß dem Oberbegriff des Anspruchs 1 beschrieben, dessen Gehäuse von mindestens einem Trog gebildet wird, in dem jeweils ein von kondensiertem Dampf durchströmter Wärmetauscher in Form eines Geradrohrbündels in mehreren Dampfgängen mit sich erheblich verringender Rohranzahl bzw. Dampfquerschnitt angeordnet ist. Die Rohre sind in den Trögen des Kontakt-Trockners so angeordnet, dass sich eine gleichmäßige Teilung des Heizregisters ergibt.In the EP 0 341 347 A1 is a fluidized bed contact dryer according to the preamble of claim 1 described, the housing is formed by at least one trough, in each of which a steam flowed through by condensed heat exchanger in the form of a Geradrohrbündels in several steam passes with significantly reducing the number of tubes or steam cross section is arranged. The tubes are arranged in the troughs of the contact dryer so as to give a uniform pitch of the heater.

Durch die Maßnahme gemäß EP 0 341 347 wird eine im Wesentlichen konstante Strömungsgeschwindigkeit des Heizdampfes innerhalb des Rohrbündelwärmetauschers erzielt. Die Lösung gemäß EP 0 341 347 A1 ist allerdings mit dem Nachteil behaftet, dass die Querschnittsfläche des Trocknergehäuses nicht über dessen Höhe im Bereich der Wärmetauschereinbauten konstant ist. Dies führt zu strömungsmechanischen Störungen im Wirbelbett, was schon aus Gründen einer Leistungsoptimierung nicht wünschenswert ist.By the measure according to EP 0 341 347 a substantially constant flow rate of the heating steam within the shell and tube heat exchanger is achieved. The solution according to EP 0 341 347 A1 However, there is the disadvantage that the cross-sectional area of the dryer housing is not constant over its height in the area of the heat exchanger installations. This leads to flow-mechanical disturbances in the fluidized bed, which is undesirable for reasons of performance optimization.

Der Erfindung liegt daher die Aufgabe zugrunde, einen Wirbelschicht-Trockner der eingangs genannten Art im Hinblick auf einen möglichst optimalen Wärmeübergang zu verbessern.The invention is therefore based on the object to improve a fluidized bed dryer of the type mentioned in terms of the best possible heat transfer.

Die Aufgabe wird gelöst durch einen indirekt beheizten Wirbelschicht-Trockner zur Trocknung von feuchten, feinkörnigen Schüttgütern, umfassend ein Gehäuse mit einem Begasungsboden mit sich oberhalb des Begasungsbodens erstreckenden Wärmetauschereinbauten und mit wenigstens einer unterhalb des Begasungsbodens vorgesehenen Austragseinrichtung für das getrocknete Schüttgut, wobei der nutzbare Strömungsquerschnitt des Gehäuses im Bereich der Wärmetauschereinheiten über die gesamte Höhe der Wärmetauscher-einbauten in Strömungsrichtung des Fluidisierungsgases zunimmt Dabei zeichnet sich der Wirbelschicht-Trockner gemäß der Erfindung dadurch aus, dass der Querschnitt des Gehäuses konstant ist und die Packungsdichte der Wärmetauschereinbauten in Strömungsrichtung des Fluidisierungsgases abnimmt.The object is achieved by an indirectly heated fluidized-bed dryer for drying moist, fine-grained bulk materials, comprising a housing with a gassing bottom with heat exchanger installations extending above the gassing floor and at least one discharge device for the dried bulk material provided below the gassing floor, the usable flow cross-section The fluidized bed dryer according to the invention is characterized in that the cross section of the housing is constant and decreases the packing density of the heat exchanger internals in the flow direction of the fluidizing gas of the housing in the region of the heat exchanger units over the entire height of the heat exchanger installations in the flow direction of the fluidizing gas.

Bevorzugt besitzt das Gehäuse des Wirbelschicht-Trockners gemäß der Erfindung einen rechteckigen, vorzugsweise einen quadratischen Querschnitt.Preferably, the housing of the fluidized bed dryer according to the invention has a rectangular, preferably a square cross-section.

Es ist selbstverständlich auch möglich, dass das Gehäuse einen kreisförmigen Querschnitt aufweist.It is of course also possible that the housing has a circular cross-section.

So wird in vorteilhafter Art und Weise eine übermäßige Zunahme der Strömungsgeschwindigkeit des Gases bzw. des Brüdens über die Höhe des Gehäuses vermieden. Dadurch reduziert sich der Staubaustrag des Feinkornanteils der Wirbelschicht, wodurch sich der Wärmeübergang an den Kontaktflächen der Wärmetauschereinbauten verbessert.Thus, an excessive increase in the flow rate of the gas or the vapor over the height of the housing is avoided in an advantageous manner. This reduces the dust discharge of the fine grain fraction of the fluidized bed, which improves the heat transfer at the contact surfaces of the heat exchanger installations.

Durch die abnehmende Packungsdichte ist es ohne zusätzliche Einbauten möglich, bei konstantem Querschnitt des Gehäuses über die Höhe der Wärmetauscher den nutzbaren Strömungsquerschnitt des Gehäuses zu vergrößern mit der Folge einer Verringerung der Geschwindigkeitszunahme bei zunehmendem Brüdenmassenstrom.Due to the decreasing packing density, it is possible without additional installations to increase the usable flow cross-section of the housing at a constant cross-section of the housing over the height of the heat exchanger with the result of a reduction in the increase in velocity with increasing vapor mass flow.

Bei einer bevorzugten Variante des Wirbelschicht-Trockners gemäß der Erfindung ist vorgesehen, dass als Wärmetauscher Rohrbündel und/oder Plattenpakete vorgesehen sind, die zu Segmenten unterschiedlicher Rohrteilung und/oder unterschiedlicher Plattenabstände zusammengefasst sind.In a preferred variant of the fluidized-bed dryer according to the invention it is provided that tube bundles and / or plate packs are provided as heat exchangers, which are combined into segments of different pipe pitch and / or different plate spacings.

Beispielsweise können als Wärmetauscher Rohrbündel vorgesehen sein, die segmentweise mit unterschiedlichen Rohrdurchmessem und /oder unterschiedlichen Abständen zueinander angeordnet sind. Zweckmäßigerweise nehmen die Rohrdurchmesser in Strömungsrichtung des Fluidisierungsgases ab oder deren Abstände werden in Strömungsrichtung größer.For example, may be provided as a heat exchanger tube bundle, which are arranged in segments with different pipe diameters and / or different distances to each other. Expediently, the pipe diameters decrease in the flow direction of the fluidizing gas or their distances become larger in the direction of flow.

Es können wenigstens zwei oder vorzugsweise drei Wärmetauschersegmente beispielsweise in Form von Heizregistern in Strömungsrichtung des Fluidisierungsgases hintereinander angeordnet sein bzw. hintereinander geschaltet sein.At least two or preferably three heat exchanger segments, for example in the form of heating registers in the flow direction of the fluidizing gas, can be arranged one behind the other or connected in series.

Bei einer bevorzugten Variante des Wirbelschicht-Trockners gemäß der Erfindung ist vorgesehen, dass alle Wärmetauschersegmente eine etwa gleiche Wärmetauschfläche aufweisen, so dass sich in den Wärmetauscherrohren ein im Mittel fallendes Geschwindigkeitsniveau einstellt.In a preferred variant of the fluidized-bed dryer according to the invention, it is provided that all heat exchanger segments have an approximately equal heat exchange surface, so that an average falling speed level is established in the heat exchanger tubes.

Die Wärmetauschereinbauten können mehrgängig ausgebildet sein, vorzugsweise sind die Wärmetauschereinbauten dreigängig ausgebildet, wobei jeder Gang an einen Kondensatsammler angeschlossen ist. Durch letztere Maßname werden Druckverluste aufgrund von mitgeschlepptem Kondensat vermieden. Durch die mehrgängige Anordnung der Wärmetauscherrohre wird der Wärmeübergang auf der Innenseite der dampfbeheizten Rohre erhöht, was dazu beiträgt, dass der Wärmedurchgangskoeffizient und damit die Effizienz der Wärmeübertragung in Summe verbessert wird.The heat exchanger installations can be designed to be more continuous, preferably the heat exchanger installations are of three-flighted design, with each passage being connected to a condensate collector. By the latter measure name pressure losses are avoided due to entrained condensate. The multi-pass arrangement of the heat exchanger tubes, the heat transfer is increased on the inside of the steam-heated tubes, which contributes to the fact that the heat transfer coefficient and thus the efficiency of heat transfer is improved in total.

Insbesondere durch die Erweiterung der Rohrteilung in Strömungsrichtung oder durch die Verringerung der Rohrdurchmesser in Strömungsrichtung werden die für das Strömungsverhalten entscheidenden freien Flächen zwischen den Rohren vergrößert. Dadurch wird der Anstieg der Geschwindigkeit durch den nach oben zunehmenden Dampfmassenstrom verringert. Hierdurch wird der Staubaustrag reduziert, eine Vergröberung des Wirbelbetts wird wirksam vermieden. Die Wärmeübertragung wird durch Annäherung der Zwischenrohrgeschwindigkeit an das für die Wärmübertragung theoretische Optimum verbessert. Darüber hinaus wird die spezifische Verdampfungsleistung in kg/m2 h bis zum Erreichen der kritischen Geschwindigkeit erhöht.In particular, by the extension of the pipe pitch in the flow direction or by reducing the pipe diameter in the flow direction, the decisive for the flow behavior of free surfaces between the pipes increased. This reduces the increase in speed due to the increasing steam mass flow. As a result, the dust discharge is reduced, a coarsening of the fluidized bed is effectively avoided. The heat transfer is improved by approaching the intermediate tube speed to the theoretical optimum for heat transfer. In addition, the specific evaporation capacity is increased in kg / m 2 h until reaching the critical speed.

Eine Variante des Wirbelschicht-Trockners gemäß der Erfindung zeichnet sich dadurch aus, dass ein trichterförmiger Auslauf vorgesehen ist, der geometrisch so gestaltet ist, dass sich bei Abzug von Schüttgut Massenfluss einstellt. Das bedeutet, dass sich der gesamte Inhalt des Auslaufs bei Materialabzug in Bewegung befindet. Es existieren keine oder allenfalls minimale Totzonen bzw. ruhende Schüttgutzonen. Das Gegenteil hiervon wird im Allgemeinen als so genannter Kemfluss bezeichnet, der unter Umständen eine Störung der Fluidisierung der Wirbelschicht verursachen kann. Dies kann beispielsweise dann eintreten, wenn sich auf dem Festbett unterhalb des Begasungsbodens Ablagerungen kumulieren, die bei Materialabzug nicht bewegt werden.A variant of the fluidized-bed dryer according to the invention is characterized in that a funnel-shaped outlet is provided, which is geometrically designed so that sets mass flow when deducting bulk material. This means that all the contents of the spout are in motion when the material is removed. There are no or at most minimal dead zones or resting bulk zones. The opposite of this is generally referred to as a so-called Kemfluss, which may possibly cause a disturbance of the fluidization of the fluidized bed. This can occur, for example, when deposits accumulate on the fixed bed below the gassing soil, which are not moved when material is removed.

Bevorzugt ist die Steilheit der Umfassungswände des Auslaufs so gewählt, dass sich bei Abzug von Schüttgut Massenfluss einstellt, das heißt, dass bei Materialabzug das gesamte Festbett an jeder Stelle in Bewegung ist.Preferably, the steepness of the enclosing walls of the outlet is chosen so that sets mass flow when deducting bulk material, that is, when material removal, the entire fixed bed is in motion at each point.

Die Erfindung wird nachstehend anhand eines in den Zeichnungen dargestellten Ausführungsbeispiels erläutert.The invention will be explained below with reference to an embodiment shown in the drawings.

Es zeigen:

  • Figur 1 eine schematische Ansicht eines Wirbelschicht-Trockners gemäß der Erfindung und
  • Figur 2 einen Schnitt durch den Wirbelschicht-Behälter aus Figur 1 um 90° versetzt.
Show it:
  • FIG. 1 a schematic view of a fluidized bed dryer according to the invention and
  • FIG. 2 a section through the fluidized bed container FIG. 1 offset by 90 °.

Der in Figur 1 dargestellte Wirbelschicht-Trockner (1) weist ein Gehäuse (2) mit einem rechteckigen Querschnitt auf. An der oberen Stirnseite (3) des Wirbelschicht-Trockners (1) ist als Rohbraunkohleneintrag ein Einfüllrohr (4) mit einer Zellenradschleuse (5) vorgesehen. An dem von der oberen Stirnseite (3) abliegenden unteren Ende des Wirbelschicht-Trockners (1) ist unterhalb eines Begasungsbodens (6) ein trichterförmiger Auslauf (7) vorgesehen, an dessen unterem Ende ein mechanischer Austrag, beispielsweise in Form einer Zellenradschleuse (5,) vorgesehen ist. Anstelle dessen könnte dort als mechanischer Austrag auch ein Schneckenförderer oder dergleichen vorgesehen sein. Der Wirbelschicht-Trockner (1) gemäß Ausführungsbeispiel ist vorwiegend zur Trocknung von Braunkohle vorgesehen und wird unter Bezugnahme auf ein Verfahren zur Trocknung von Braunkohle beschrieben, die Erfindung ist jedoch so zu verstehen, dass der Trockner auch zur Trocknung anderer körniger Stoffe Anwendung finden kann.The in FIG. 1 shown fluidized bed dryer (1) has a housing (2) with a rectangular cross-section. At the upper end face (3) of the fluidized-bed dryer (1) is provided as a Rohbraunkohleneintrag a filler pipe (4) with a rotary valve (5). At the lower end of the fluidized-bed dryer (1) remote from the upper end face (3), a funnel-shaped outlet (7) is provided below a gassing floor (6), at the lower end of which a mechanical discharge, for example in the form of a rotary valve (5, FIG. ) is provided. Instead, there could be provided as a mechanical discharge and a screw conveyor or the like. The fluidized-bed dryer (1) according to the embodiment is primarily intended for drying lignite and will be described with reference to a process for drying lignite, but the invention is to be understood so that the dryer can also be used for drying other granular materials.

Der Begasungsboden (6) ist auf seiner dem Materialabzug (7) abgekehrten Seite mit Düsen (8) zum Einbringen eines Fluidisierungsgases vorgesehen. Als Fluidisierungsgas bzw. Wirbelmedium kommt Wasserdampf in Betracht. Zur Fluidisierung der Braunkohle in dem Wirbelschicht-Trockner (1) kann beispielsweise ein Teilstrom aus dem den Wirbelschicht-Trockner verlassenen Brüden hinter einem Elektrofilter abgezweigt werden.The gassing bottom (6) is provided on its side facing away from the material take-off (7) with nozzles (8) for introducing a fluidizing gas. As a fluidizing gas or fluidizing medium is steam into consideration. To fluidize the lignite in the fluidized bed dryer (1), for example, a partial flow from the fluidized bed dryer leaving vapors are diverted behind an electrostatic precipitator.

Oberhalb des Begasungsbodens (6) erstrecken sich quer zum Gasstrom und gegebenenfalls leicht geneigt Wärmetauschereinbauten in Form von Rohrbündeln (9) oder in Form von Platten, die von Dampf als Heizmedium durchströmt werden.Above the gassing floor (6) extend transversely to the gas flow and optionally slightly inclined heat exchanger installations in the form of tube bundles (9) or in the form of plates, which are traversed by steam as the heating medium.

Die beispielsweise mit einer Körnung von 0 bis 2 mm und einem Wassergehalt von bis zu 65 Gew.% in den Wirbelschicht-Trockner (1) eingebrachten Braunkohlen werden oberhalb des Begasungsbodens (6) mittels des Wirbelmediums in einer quasi stationären Wirbelschicht gehalten, wobei das Wirbelschichtniveau in dem Wirbelschicht-Trockner (1) mit dem Bezugszeichen (10) gekennzeichnet ist. Die Braunkohlenkörner in der Wirbelschicht gelangen dabei in Kontakt mit den das Gehäuse quer durchsetzenden Rohrbündelwärmetauschern (9), die in drei Segmenten 11a, 11b und 11c in Strömungsrichtung hintereinander angeordnet sind. Bei Temperaturen von etwa 105 bis 120°C werden mehr als 50% des ursprünglichen Gewichts der zu trocknenden Kohle als Wasser verdampft. Durch die Verdampfung des Kohlenwassers nimmt der Brüdenmassenstrom im Bereich der in der Wirbelschicht eingebauten Rohrbündelwärmetauscher (9) nach oben hin kontinuierlich zu. Damit steigt auch die Geschwindigkeit der Brüden entsprechend an.The lignites introduced, for example, with a particle size of 0 to 2 mm and a water content of up to 65% by weight into the fluidized-bed dryer (1) are held above the gasification base (6) by means of the fluidizing medium in a quasi-stationary fluidized bed, the fluidized bed level in the fluidized-bed dryer (1) by the reference numeral (10). The lignite grains in the fluidized bed come into contact with the tube bundle heat exchangers transversely across the housing (9), which are arranged in three segments 11 a, 11 b and 11 c in the flow direction one behind the other. At temperatures of about 105 to 120 ° C, more than 50% of the original weight of the coal to be dried is evaporated as water. As a result of the evaporation of the hydrocarbon, the vapor mass flow continuously increases in the region of the tube bundle heat exchanger (9) installed in the fluidized bed. Thus, the speed of the vapors increases accordingly.

Ab einer kritischen Geschwindigkeit kommt die stationäre Wirbelschicht in einen instabilen Bereich und der Staubaustrag des Feinkohlenanteils der Wirbelschicht steigt stark an. Hiervon sind im Wesentlichen die Partikelgröße von kleiner 300µm betroffen. Hierdurch stellt sich eine Vergröberung des Bettmaterials der Wirbelschicht ein, was sich negativ auf die Strömungsmechanik und die Wärmeübertragung in der Wirbelschicht auswirkt.From a critical speed, the stationary fluidized bed comes in an unstable area and the dust discharge of the fine coal content of the fluidized bed increases sharply. This essentially affects the particle size of less than 300 μm. This causes a coarsening of the bed material of the fluidized bed, which has a negative effect on the fluid mechanics and heat transfer in the fluidized bed.

Aus diesem Grund sind die Wärmetauschereinbauten in Form der Rohrbündelwärmetauscher bei den beschriebenen Ausführungsbeispielen mit in Strömungsrichtung zunehmender Teilung ausgeführt, so dass sich hierdurch bei gleichbleibendem Querschnitt bzw. Durchmesser des Gehäuses über die gesamte Höhe der Wärmetauschereinbauten eine Vergrößerung des Nutzquerschnitts des Gehäuses (2) ergibt.For this reason, the heat exchanger installations in the form of shell and tube heat exchanger in the described embodiments are designed with increasing pitch in the flow direction, thereby resulting in an increase in the useful cross-section of the housing (2) with the same cross section or diameter of the housing over the entire height of the heat exchanger installations.

Der größere Abstand der Rohre der Rohrbündelwärmetauscher (9) zueinander kann entweder dadurch erreicht werden, dass weniger Rohre mit größerem Abstand in einem Segment angeordnet werden oder dass die Rohre in Strömungsrichtung mit einem verringerten Durchmesser ausgeführt sind.The greater distance between the tubes of the tube bundle heat exchanger (9) to each other can be achieved either in that fewer tubes are arranged at a greater distance in a segment or that the tubes are designed in the flow direction with a reduced diameter.

Bei dem vorliegenden Ausführungsbeispiel ist vorgesehen, dass der Abstand der Rohre zueinander in dem dem Begasungsboden (6) nächstliegenden Segment 11a kleiner ist als in dem darauffolgenden Segment 11 b. In dem oberen Segment 11 c ist der Abstand der Rohre des Rohrbündelwärmetauschers (9) am größten, so dass dort der strömungstechnisch nutzbare Querschnitt des Gehäuses (2) am größten ist, was einer Geschwindigkeitszunahme des Brüdenmassenstroms in Strömungsrichtung entgegenwirkt.In the present embodiment, it is provided that the distance of the tubes from each other in the gassing bottom (6) nearest segment 11a is smaller than in the subsequent segment 11 b. In the upper segment 11 c, the distance of the tubes of the tube bundle heat exchanger (9) is greatest, so that there the fluidic usable cross section of the housing (2) is greatest, which counteracts an increase in velocity of the vapor mass flow in the flow direction.

Über die Brüdenabgänge (12) wird der Brüden aus dem Wirbelschicht-Trockner (1) abgeführt.About the Brüdenabgänge (12) the vapor is removed from the fluidized bed dryer (1).

Die Wärmetauscheinbauten im Gehäuse (2) sind als dreigängiger Rohrbündelwärmetauscher mit insgesamt drei Kondensatsammlern (13a, b, c) ausgeführt. Der heiße Dampf als Heizmedium wird über den mit (14) bezeichneten Dampfeintritt in den das Gehäuse (2) vollständig durchsetzenden Rohrbündelwärmtauscher (9) in dem ersten, oberen Segment 11 a eingeleitet. Die quer und gegebenenfalls leicht geneigt zur Strömungsrichtung des Wirbelmediums laufenden Rohre werden von dem Heizmedium durchströmt, welches auf der gegenüberliegenden Seite des Dampfeintritts (14) in den Kondensatsammler (13a) strömt. Das dort anfallende Kondensat wird separat abgezogen. Über den Kondensatsammler (13a) strömt das Heizmedium zurück in den auf der Seite des Dampfeintritts (14) vorgesehenen Kondensatsammler (13b) und von dort in den untersten Kondensatsammler 13c. Die Segmente 11a, b, c bzw. die Heizregister 11a, b, c sind so ausgestaltet, dass deren Wärmetauschfläche etwa gleich ist, so das sich in den einzelnen Gängen ein im Mittel fallendes Geschwindigkeitsniveau einstellt.The heat exchanger internals in the housing (2) are designed as a three-pass shell-and-tube heat exchanger with a total of three condensate collectors (13a, b, c). The hot steam as the heating medium is introduced into the first, upper segment 11 a via the steam inlet designated by (14) into the tube bundle heat exchanger (9) which passes completely through the housing (2). The transversely and optionally slightly inclined to the flow direction of the fluidizing medium passing tubes are flowed through by the heating medium, which flows on the opposite side of the steam inlet (14) into the condensate collector (13a). The resulting condensate is removed separately. Via the condensate collector (13a), the heating medium flows back into the condensate collector (13b) provided on the side of the steam inlet (14) and from there into the lowest condensate collector 13c. The segments 11a, b, c or the heating registers 11a, b, c are designed such that their heat exchange surface is approximately the same, so that sets in the individual courses an average falling speed level.

Die getrocknete Braunkohle sammelt sich in dem trichterförmigen Auslauf (7). Trichterförmig im Sinne der Erfindung bedeutet nicht notwendigerweise, dass der Querschnitt des Auslaufs kreisringförmig ausgebildet ist. Die Neigung der Umfassungswände des Auslaufs (7) ist so gewählt, dass sich bei Materialabzug, beispielsweise mit der Zellenradschleuse Massenfluss einstellt. Massenfluss bedeutet im Gegensatz zum Kernfluss, dass der gesamte Trichterinhalt in Bewegung ist, so dass sich das Festbett unterhalb des Begasungsbodens (6) bei Materialabzug gleichmäßig absenkt. Es existieren keine oder allenfalls minimale Totzonen, d. h. ruhende Schüttgutzonen. Die Schüttgutoberfläche bzw. das Festbett senkt sich nahezu gleichmäßig ab.The dried lignite collects in the funnel-shaped spout (7). Funnel-shaped in the sense of the invention does not necessarily mean that the cross section of the outlet is annular. The inclination of the enclosing walls of the outlet (7) is chosen so that adjusts mass flow in material removal, for example with the rotary valve. In contrast to the core flow, mass flow means that the entire funnel contents are in motion, so that the fixed bed below the aeration bottom (6) evenly lowers when material is withdrawn. There are no or at most minimal dead zones, ie dormant bulk zones. The bulk material surface or the fixed bed sinks almost uniformly.

Bezugszeichenliste:LIST OF REFERENCE NUMBERS

1.1.
Wirbelschicht-TrocknerFluidized bed dryer
2.Second
Gehäusecasing
3.Third
Stirnseitefront
4.4th
Einfüllrohrfiller pipe
5.5th
Zellenradschleuserotary
6.6th
BegasungsbodenBegasungsboden
7.7th
Auslaufoutlet
8.8th.
Düsenjet
9.9th
RohrbündelwärmetauscherTube heat exchanger
10.10th
WirbelschichtniveauFluidized bed level
11a, b,11a, b,
c Segmentec segments
1212
Brüdenabgangvapor outlet
13a, b, c13a, b, c
Kondensatsammlercondensate collector
1414
Dampfeintrittsteam inlet

Claims (9)

  1. Indirectly heated fluidized bed dryer (1) for drying moist, fine-grained bulk materials comprising a housing (2) with a gas-injection bottom (6), with built-in heat exchanger parts extending above the gas-injection bottom (6) and with at least one discharge device, provided below the gas-injection bottom (6), for the dried bulk material, wherein the usable flow cross section of the housing increases in the region of the built-in heat exchanger parts over the entire height of the built-in heat exchanger parts in the direction of flow of the fluidization gas, characterized in that the cross section of the housing (2) is constant in the direction of flow and the packing density of the built-in heat exchanger parts decreases in the direction of flow of the fluidization gas.
  2. Fluidized bed dryer according to Claim 1, characterized in that the housing (2) has a rectangular, preferably square cross section.
  3. Fluidized bed dryer according to Claim 1, characterized in that the heat exchangers provided are in the form of bundles of tubes and/or packs of plates which are combined to form segments (11a, b, c) of differing tube division and/or differing plate spacings.
  4. Fluidized bed dryer according to one of Claims 1 to 3, characterized in that the heat exchangers provided are in the form of tube bundle heat exchangers (9), segments of which are arranged with differing tube diameters and/or differing spacings from one another.
  5. Fluidized bed dryer according to one of Claims 1 to 4, characterized in that at least two, preferably three heat exchanger segments are arranged in series in the direction of flow of the fluidization gas.
  6. Fluidized bed dryer according to Claim 5, characterized in that all the heat exchanger segments have approximately the same heat exchanging area.
  7. Fluidized bed dryer according to one of Claims 1 to 6, characterized in that the built-in heat exchanger parts are embodied so as to have multiple channels, preferably three channels, each segment being connected to a condensate collector (13a, b, c).
  8. Fluidized bed dryer according to one of Claims 1 to 7, characterized in that a funnel-shaped outlet (7) is provided, which is geometrically configured in such a way that mass flow is set on withdrawal of bulk material.
  9. Fluidized bed dryer according to Claim 8, characterized in that the steepness of the enclosing walls of the outlet (7) is selected in such a way that mass flow is set on withdrawal of bulk material.
EP08875030.2A 2008-11-24 2008-11-24 Indirectly heated fluidized bed dryer Not-in-force EP2352959B1 (en)

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DE102013104032A1 (en) 2013-04-22 2014-10-23 Rwe Power Ag Process for the milling drying of coal
CN105255519B (en) * 2015-09-30 2017-08-29 中科合成油工程股份有限公司 A kind of feed coal is predrying, the method and its dedicated processes system of powder processed and conveying

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CN102224388A (en) 2011-10-19
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AU2008364234B2 (en) 2013-01-24
EP2352959A1 (en) 2011-08-10
RU2474777C1 (en) 2013-02-10
WO2010057509A1 (en) 2010-05-27
CA2742929A1 (en) 2010-05-27
RU2011125916A (en) 2012-12-27
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AU2008364234A1 (en) 2011-06-30
US20110283555A1 (en) 2011-11-24

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