EP2352959B1 - Sechoir en lit fluidise a chauffage indirect - Google Patents

Sechoir en lit fluidise a chauffage indirect 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
Authority
EP
European Patent Office
Prior art keywords
fluidized bed
bed dryer
heat exchanger
flow
dryer according
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.)
Not-in-force
Application number
EP08875030.2A
Other languages
German (de)
English (en)
Other versions
EP2352959A1 (fr
Inventor
Hans-Joachim Klutz
Claus Moser
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.)
RWE Power AG
Original Assignee
RWE Power AG
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by RWE Power AG filed Critical RWE Power AG
Priority to PL08875030T priority Critical patent/PL2352959T3/pl
Publication of EP2352959A1 publication Critical patent/EP2352959A1/fr
Application granted granted Critical
Publication of EP2352959B1 publication Critical patent/EP2352959B1/fr
Not-in-force legal-status Critical Current
Anticipated expiration legal-status Critical

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Classifications

    • 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.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Microbiology (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Drying Of Solid Materials (AREA)

Claims (9)

  1. Séchoir en lit fluidisé à chauffage indirect (1) pour le séchage de matières en vrac humides à grain fin, comprenant une enceinte (2) avec un fond de gazage (6), avec des éléments rapportés d'échangeur de chaleur s'étendant au-dessus du fond de gazage (6) et avec au moins un dispositif d'extraction prévu en dessous du fond de gazage (6) pour les matières en vrac séchées, dans lequel la section transversale d'écoulement utile de l'enceinte dans la région des éléments rapportés d'échangeur de chaleur augmente sur toute la hauteur des éléments rapportés d'échangeur de chaleur dans la direction d'écoulement du gaz de fluidisation, caractérisé en ce que la section transversale de l'enceinte (2) est constante dans la direction d'écoulement et la densité de garnissage des éléments rapportés d'échangeur de chaleur diminue dans la direction d'écoulement du gaz de fluidisation.
  2. Séchoir en lit fluidisé selon la revendication 1, caractérisé en ce que l'enceinte (2) présente une section transversale rectangulaire, de préférence carrée.
  3. Séchoir en lit fluidisé selon la revendication 1, caractérisé en ce qu'il est prévu comme échangeurs de chaleur des faisceaux de tubes et/ou des paquets de plaques, qui sont rassemblés en segments (11a, b, c) présentant des pas de tubes différents et/ou des distances de plaques différentes.
  4. Séchoir en lit fluidisé selon l'une quelconque des revendications 1 à 3, caractérisé en ce qu'il est prévu comme échangeurs de chaleur des échangeurs de chaleur à faisceaux de tubes, qui sont disposés par segments avec des diamètres de tubes différents et/ou des distances différentes les uns des autres.
  5. Séchoir en lit fluidisé selon l'une quelconque des revendications 1 à 4, caractérisé en ce qu'au moins deux, de préférence trois segments d'échangeur de chaleur sont disposés l'un derrière l'autre dans la direction d'écoulement du gaz de fluidisation.
  6. Séchoir en lit fluidisé selon la revendication 5, caractérisé en ce que tous les segments d'échangeur de chaleur présentent une surface d'échange de chaleur sensiblement égale.
  7. Séchoir en lit fluidisé selon l'une quelconque des revendications 1 à 6, caractérisé en ce que les éléments rapportés d'échangeur de chaleur sont réalisés à plusieurs entrées, de préférence à trois entrées, dans lequel chaque segment est raccordé à un collecteur de condensat (13a, b, c).
  8. Séchoir en lit fluidisé selon l'une quelconque des revendications 1 à 7, caractérisé en ce qu'il est prévu une sortie en forme d'entonnoir (7), qui est configurée géométriquement de telle manière qu'il s'établisse un flux de masse lors du soutirage de matières en vrac.
  9. Séchoir en lit fluidisé selon la revendication 8, caractérisé en ce que la pente des parois entourant la sortie (7) est choisie de telle manière qu'il s'établisse un flux de masse lors du soutirage de matières en vrac.
EP08875030.2A 2008-11-24 2008-11-24 Sechoir en lit fluidise a chauffage indirect Not-in-force EP2352959B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
PL08875030T PL2352959T3 (pl) 2008-11-24 2008-11-24 Ogrzewana pośrednio suszarka ze złożem fluidalnym

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/EP2008/009922 WO2010057509A1 (fr) 2008-11-24 2008-11-24 Séchoir en lit fluidisé à chauffage indirect

Publications (2)

Publication Number Publication Date
EP2352959A1 EP2352959A1 (fr) 2011-08-10
EP2352959B1 true EP2352959B1 (fr) 2015-09-02

Family

ID=40886516

Family Applications (1)

Application Number Title Priority Date Filing Date
EP08875030.2A Not-in-force EP2352959B1 (fr) 2008-11-24 2008-11-24 Sechoir en lit fluidise a chauffage indirect

Country Status (9)

Country Link
US (1) US20110283555A1 (fr)
EP (1) EP2352959B1 (fr)
CN (1) CN102224388B (fr)
AU (1) AU2008364234B2 (fr)
CA (1) CA2742929C (fr)
PL (1) PL2352959T3 (fr)
RU (1) RU2474777C1 (fr)
UA (1) UA100932C2 (fr)
WO (1) WO2010057509A1 (fr)

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102011009903A1 (de) 2011-01-31 2012-08-02 Rwe Technology Gmbh Verfahren und System zur Herstellung von Braunkohlenkoks
DE102013104032A1 (de) 2013-04-22 2014-10-23 Rwe Power Ag Verfahren zur Mahltrocknung von Kohle
CN105255519B (zh) * 2015-09-30 2017-08-29 中科合成油工程股份有限公司 一种原料煤预干燥、制粉和输送的方法及其专用处理系统

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Also Published As

Publication number Publication date
EP2352959A1 (fr) 2011-08-10
CN102224388A (zh) 2011-10-19
AU2008364234B2 (en) 2013-01-24
RU2011125916A (ru) 2012-12-27
CA2742929C (fr) 2016-10-11
CN102224388B (zh) 2013-10-02
US20110283555A1 (en) 2011-11-24
AU2008364234A1 (en) 2011-06-30
RU2474777C1 (ru) 2013-02-10
WO2010057509A1 (fr) 2010-05-27
CA2742929A1 (fr) 2010-05-27
PL2352959T3 (pl) 2016-01-29
UA100932C2 (ru) 2013-02-11

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