WO1994021964A1 - Lit fluidise - Google Patents

Lit fluidise Download PDF

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Publication number
WO1994021964A1
WO1994021964A1 PCT/CH1994/000050 CH9400050W WO9421964A1 WO 1994021964 A1 WO1994021964 A1 WO 1994021964A1 CH 9400050 W CH9400050 W CH 9400050W WO 9421964 A1 WO9421964 A1 WO 9421964A1
Authority
WO
WIPO (PCT)
Prior art keywords
cyclone
fluidized bed
gas
outlet
solid particles
Prior art date
Application number
PCT/CH1994/000050
Other languages
German (de)
English (en)
Inventor
Arthur Ruf
Hans Geissbuehler
Edgar Muschelknautz
Original Assignee
Buehler 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 Buehler Ag filed Critical Buehler Ag
Publication of WO1994021964A1 publication Critical patent/WO1994021964A1/fr

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
    • F23J15/022—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material for removing solid particulate material from the gasflow
    • F23J15/027—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material for removing solid particulate material from the gasflow using cyclone separators
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/005—Separating solid material from the gas/liquid stream
    • B01J8/0055—Separating solid material from the gas/liquid stream using cyclones
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
    • B04C3/00—Apparatus in which the axial direction of the vortex flow following a screw-thread type line remains unchanged ; Devices in which one of the two discharge ducts returns centrally through the vortex chamber, a reverse-flow vortex being prevented by bulkheads in the central discharge duct
    • B04C3/04—Multiple arrangement thereof
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
    • B04C3/00—Apparatus in which the axial direction of the vortex flow following a screw-thread type line remains unchanged ; Devices in which one of the two discharge ducts returns centrally through the vortex chamber, a reverse-flow vortex being prevented by bulkheads in the central discharge duct
    • B04C3/06—Construction of inlets or outlets to the vortex chamber
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/02—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed
    • F23C10/04—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone
    • F23C10/08—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases
    • F23C10/10—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases the separation apparatus being located outside the combustion chamber
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2900/00—Special arrangements for conducting or purifying combustion fumes; Treatment of fumes or ashes
    • F23J2900/15026—Cyclone separators with horizontal axis

Definitions

  • the invention relates to a fluidized bed with a lying cyclone, which extends approximately over the length of the fluidized bed, according to the preamble of claim 1.
  • a fluidized bed is formed when a bed of solid particles flows through an upward gas stream, the solid particles being raised so that they float in the gas stream.
  • Such fluidized beds are advantageously used for a wide variety of applications due to their thermal properties. Only if the fill layer consists of approximately uniform grains, i.e. made of grains with almost the same sinking velocity, the fluidized bed has a defined surface, corresponding to a liquid surface, after the gas flow velocity assigned to the vortex point has been exceeded. With different grain sizes, however, segregation takes place, whereby smaller and smallest grains accumulate in the vicinity of the fluidized bed surface and are discharged at inflow velocities which exceed their sinking velocity.
  • the solids treated in fluidized beds generally have particle collectives of different distribution spectra, owing to the variety of possible forms in the course of different processes, such as grinding, pre-crystallizing or condensing - to name just a few.
  • Plastic granules for example, which are subjected to drying in a fluidized bed, can be of very different sizes, and the smallest particles, such as dust or abrasion, can also penetrate them.
  • a fluidized bed in itself shows a classifying behavior, which is useful for the treatment of particle collectives with a narrow particle diameter distribution.
  • tion which is only permeated with abrasion or dust, proves to be advantageous since - with a correspondingly selected flow velocity of the fluidizing gas - only the latter is discharged from the fluidized bed and drawn off in a known manner.
  • solid particles are discharged in an undesirable manner, which, if discharged and reclassified, are on the one hand of inferior quality due to uncontrollable dwell times, or on the other hand if discharged and deducted, the Reduce productivity.
  • Known systems such as that described in WO 86/03986, therefore provide cyclone separators arranged parallel to the fluidized bed, into which the fluidizing gas carrying the entrained solid particles is passed. Particles entrained are discharged in the usual way at the lower end of the conically tapering cyclone and introduced back into the fluidized bed via a return line.
  • a parallel suction line also allows the return of smaller solid particles that would otherwise be entrained by the gas emerging from the cyclone from an immersion tube.
  • a disadvantage of such an arrangement is the relatively large amount of space required for the two components, fluid bed and cyclone, which are arranged next to one another, and it is also difficult to check the actual dwell times; insufficient duration or intensity of treatment due to the relatively long distances through the fluidized bed, cyclone and return line may have to be accepted.
  • WO 88/06924 describes a cyclone separator which is arranged lying above a fluidized bed. Solid particles which are entrained with the fluidizing gas are to be separated from the gas due to the special arrangement and configuration of the gas outlet from the cyclone and - due to centrifugal force - are brought back in via a solid outlet provided over the entire cyclone length and tangentially leading away from the cyclone the fluidized bed is returned to the treatment.
  • a disadvantage of this arrangement it turns out, however, that - also due to the special design of the gas outlet with its guide tubes or guide slots which cause a reversal of the flow direction of the gas into the axial gas outlet pipe - there is no ideal formation of the rotational flow.
  • the present invention has the object of providing a device which eliminates the disadvantages listed above and which permits problem-free treatment of solid particles introduced into a fluidized bed, with a lying cyclone assigned to the fluidized bed ensuring the rapid and complete return of causes solid particles to be treated in the fluidized bed, and at the same time undesired small particles such as abrasion or dust are discharged through the gas outlet of the cyclone.
  • the fluidizing gas flowing through the fluidized bed carries with it solid particles whose rate of descent is lower than the flow rate of the gas and flows tangentially into the cyclone. Since - in contrast to the centrifuge, in which the particles rotate at the same angular velocity - the angular velocity increases sharply inwards in the cyclone, there is turbulence due to the wall friction and a wave-like distribution of the solid particles on the inner walls of the cyclone. However, if secondary gas is allowed to flow tangentially into the cyclone, this waveform "pulls out", the strand of solid particles formed on the inner wall of the cyclone is thrown up, the solid particles are returned to the fluidized bed via a solid outlet.
  • the thrown-up solid particles are preferably fed back to the fluidized bed through a solid outlet arranged close to the secondary inlet with respect to the axial extent of the cyclone or fluidized bed, preferably opposite, whereby this arrangement increases the effect of the secondary gas supply becomes.
  • the secondary gas inlet can be provided either in the area of the transition between the first and second cyclones or also on a side of the first cyclone opposite this transition, viewed in the axial direction, this depending in particular on the shape of the first cyclone becomes.
  • the secondary gas inlet will preferably be assigned to the side of the first cyclone opposite the transition between the two cyclones.
  • the diameter of the second cyclone is preferably also dimensioned such that it increases in the direction of the first cyclone, so that the regions of the largest diameters for both cyclones are adjacent to one another.
  • the secondary inlet will preferably be arranged next to the transition between the two cyclones.
  • FIG. 1 shows a longitudinal section through a fluidized bed with a first cyclone arranged horizontally above it and a second cyclone adjoining it;
  • Fig. 2 is a section along A-B of Fig. 1;
  • Fig. 3 is a section along C-D of Fig. 1;
  • Fig. 4 is a longitudinal section E-F-G of Fig. 1;
  • FIG. 5 shows an alternative embodiment to FIG. 1 of a fluidized bed with a first cyclone arranged horizontally above it and a second cyclone adjoining it, the two cyclones each having a conical design, and
  • FIG. 6 shows a section along A-B of FIG. 5.
  • FIG. 1 shows a longitudinal section through a fluidized bed 1, into which bulk material has been introduced, optionally via a screw conveyor, not shown.
  • This bulk material which contains solid particles of different sizes and also very fine particles, such as abrasion and dust, is flowed through from bottom to top by fluidizing gas which flows through an inflow base 10 provided with openings. From a certain flow velocity of the fluidizing gas, the so-called vortex point, a fluidized bed 3 is formed, the surface of which only looks like a liquid surface when the bulk material introduced is composed of approximately uniform solid particles. Solid particles, the sink rate of which is lower than the inflow speed of the gas, as well as that caused, among other things, by the strong turbulence dust is discharged with the gas flowing out of the fluidized bed 3.
  • a lying, first cyclone 2 is arranged above the fluidized bed 3 and extends over the entire length of the fluidized bed 3. This cyclone 2 has a cylindrical diameter which corresponds to the width of the fluidized bed 1.
  • the cylindrical jacket of the cyclone 2 has on one side a slot 12 lying against a side wall 11 of the fluidized bed 1, through which the gas emerging from the fluidized bed 3 flows into the cyclone 2 (arrows 13), whereby it carries with it the solid particles 14 discharged from the fluidized bed 3.
  • the slot 12 extends approximately over the entire length of the fluidized bed 1 and thus also approximately over the entire length of the cyclone 2.
  • the gas loaded with solid particles 14 enters the first cyclone 2 through the slot 12; a swirl flow arises due to the tangential inflow, the larger solid particles being thrown against the wall of the cyclone 2 by centrifugal force and moving in a streak-like fashion against the second cyclone 7 . Since the speeds of the solid particles increase towards the cyclone axis and the solid particles adjacent to the cyclone wall are braked due to the effects of friction, a wave-shaped profile of the strand of the solid particles is formed.
  • solid-free secondary gas is blown tangentially into the first cyclone via an inlet 6, which is provided between the first cyclone 2 and the second cyclone 7, then this detects the strand of solid particles 16 arriving there and throws it up so that the larger solid particles are fed back to the fluidized bed 3 via a first solid outlet 4.
  • the secondary inlet 6 and the first solids outlet 4 are arranged on mutually opposite sides of the first cyclone 2, the secondary gas being supplied tangentially via the secondary gas inlet 6, while the larger ones at the Particles of solid separated from the cyclone are tangentially discharged via the first solids outlet 4.
  • This solid outlet 4 which may have a square cross section, extends over approximately half the circumference of the inner wall of the cyclone 2, but this will depend on the inflow rate of the secondary gas and the maximum sink rate of the solid particles deposited in the cyclone 2.
  • tubular secondary gas inlet 6 which is arranged along the side wall 11 of the fluidized bed 1, will be connected to the pressure chamber for the fluidizing gas flowing through the inflow floor 10, or may be designed to stand directly on the inflow floor 10.
  • the first solids outlet 4 protrudes into the fluidized bed 3 and ends somewhat above the inflow floor 10, which is closed in this area 17 in order not to whirl up the solid particles to be reintroduced into the fluidized bed 3.
  • a suitable dimensioning of the cyclone 2, in particular by a suitable choice of the size of the inlet slot 12, has the effect, in a known manner, that dust and abrasion are not yet separated in the first cyclone 2 and thus not returned to the Fluidized bed.
  • This fine fraction is entrained with the gas into the second cyclone 7 and introduced there into a dust collecting space 19 through a slit-shaped, second solid outlet 8.
  • the cleaned gas leaves the cyclone arrangement through the immersion tube 15, cleaned of larger and finer solid particles, and can, if necessary, return to the pressure chamber for the fluidizing gas flowing through the inflow floor 10 are supplied.
  • the fine particles obtained in the dust collecting space 19 can be emptied via a discharge lock 20.
  • FIG. 5 An alternative embodiment can be seen in FIG. 5, in which the two cyclones 2a and 7a are each conical, the regions with the largest diameter being adjacent to one another.
  • a helical swirl flow runs along the inner wall of the two cyclones 2a and 7a to the areas with the smallest diameter, the solid particles being thrown outwards.
  • a strand of solid particles 16a is formed on the inner wall, which contains the larger solid particles, while the fine particles are entrained into the second cyclone 7a via the secondary vortex near the axis and are discharged there into the dust collecting space 19a via the second solid outlet 8a.
  • the secondary gas supporting the discharge of the larger solid particles into the fluidized bed 3a is advantageously allowed to flow in tangentially in the region of the smallest diameter of the first cyclone 2a.
  • Secondary gas inlet 6a and first solids outlet 4a are therefore arranged on the side of the first cyclone 7a opposite the transition region of the two cyclones 2a and 7a.
  • the gas loaded with larger, smaller and finest solid particles and rising from the fluidized bed 3 has to pass this pre-separator 9, the sluggish, larger solid particles being pushed against the zigzag-shaped deflection plates, braked and back in the fluidized bed 3 fall back.
  • This achieves a pre-classification of the solid particles, thus increasing the effectiveness of the separation in the subsequent two cyclones 2 and 7, in particular since this increases the risk of formation a "surf wave" is reduced.
  • Such a preliminary separator is advantageously arranged in the manner shown essentially over the entire, preferably undiminished, width of the fluidized bed and in particular has a plurality of separate classifier channels.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Combustion & Propulsion (AREA)
  • Cyclones (AREA)

Abstract

Un premier cyclone (2) s'étendant approximativement sur la longueur du lit fluidisé (1) et comportant une sortie de gaz axiale (15) est monté en position horizontale au-dessus dudit lit fluidisé (1). Le gaz s'écoulant à travers la couche fluidisée (3) peut être amené à ce cyclone (2) sensiblement tangentiellement sur la longueur du lit fluidisé (1). Au moins une partie des solides séparés dans le premier cyclone (2) sont ramenés dans le lit fluidisé par l'intermédiaire d'une première sortie de solides (4). Du gaz secondaire est amené tangentiellement dans le premier cyclone (2) par l'intermédiaire d'un entrée secondaire (6) qui est située à l'opposé de la première sortie de solides (4) dans le sens axial. Un deuxième cyclone (7) positionné également horizontalement et présentant un diamètre inférieur au premier cyclone (2) est relié à ce dernier. Le deuxième cyclone (7) possède une deuxième sortie de solides (8).
PCT/CH1994/000050 1993-03-15 1994-03-09 Lit fluidise WO1994021964A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DEP4308103.7 1993-03-15
DE19934308103 DE4308103A1 (de) 1993-03-15 1993-03-15 Wirbelbett

Publications (1)

Publication Number Publication Date
WO1994021964A1 true WO1994021964A1 (fr) 1994-09-29

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1997039278A1 (fr) * 1996-04-12 1997-10-23 Abb Carbon Ab Procede et installation de combustion pour une combustion a lit fluidise sous pression avec recyclage des matieres solides

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE29501148U1 (de) * 1995-01-25 1995-07-20 Bielefeldt, Ernst-August, 24582 Bordesholm Einrichtung zur Stofftrennung mittels Fliehkraft
FR2871554A1 (fr) 2004-06-11 2005-12-16 Alstom Technology Ltd Procede de conversion energetique de combustibles solides minimisant la consommation d'oxygene

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1985004117A1 (fr) * 1984-03-20 1985-09-26 Rauma-Repola Oy Reacteur a deux ou plusieurs composants
GB2159726A (en) * 1984-06-01 1985-12-11 Ahlstroem Oy Apparatus for separating solid material in a circulating fluidized bed reactor
EP0216677A1 (fr) * 1985-09-09 1987-04-01 Framatome Chaudière à lit fluidisé circulant
US4854249A (en) * 1987-08-03 1989-08-08 Institute Of Gas Technology Two stage combustion
EP0438169A2 (fr) * 1990-01-19 1991-07-24 Nkk Corporation Appareil à combustion à lit fluidisé circulant

Family Cites Families (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE605026C (de) * 1934-11-02 I G Farbenindustrie Akt Ges Vorrichtung zum Schwelen von Brennstoffen
DE686367C (de) * 1937-09-24 1940-01-08 Theodor Froehlich A G Kombinierte Saugzug- und Entstaubungsanlage
GB720465A (en) * 1949-12-07 1954-12-22 Svenska Maskinverken Ab Improvements in dust separators
DE958170C (de) * 1952-06-21 1957-02-14 Babcock & Wilcox Dampfkessel W Fliehkraftstaubabscheider
DE1096173B (de) * 1956-04-26 1960-12-29 Alpine Ag Maschinenfabrik Und Spiralwindsichter
DE2342091A1 (de) * 1973-08-21 1975-03-06 Kloeckner Humboldt Deutz Ag Verfahren und vorrichtung zur abtrennung von feuchten staubfoermigen bestandteilen in der rohwaschkohle
DE2538664C2 (de) * 1975-08-30 1983-11-17 Messerschmitt-Bölkow-Blohm GmbH, 8000 München Einrichtung zum Abtrennen des spezifisch leichteren Anteils aus einem Strom eines mit suspendierten Stoffen beladenen Mediums
DE7606402U1 (de) * 1976-03-03 1977-06-08 Ventilatorenfabrik Oelde Gmbh, 4740 Oelde Vorrichtung zur trennung eines gemisches aus schrott und schutt
GB1580655A (en) * 1977-07-09 1980-12-03 Lappeenrannan Konepaja Oy Method and apparatus for pneumatic fine classification
US4672918A (en) * 1984-05-25 1987-06-16 A. Ahlstrom Corporation Circulating fluidized bed reactor temperature control
FI75505C (fi) * 1985-01-11 1988-07-11 Ahlstroem Oy Foerfarande och anordning foer avskiljning av fast material ur roekgaserna fraon en reaktor med cirkulerande baedd.
US4732113A (en) * 1987-03-09 1988-03-22 A. Ahlstrom Corporation Particle separator

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1985004117A1 (fr) * 1984-03-20 1985-09-26 Rauma-Repola Oy Reacteur a deux ou plusieurs composants
GB2159726A (en) * 1984-06-01 1985-12-11 Ahlstroem Oy Apparatus for separating solid material in a circulating fluidized bed reactor
EP0216677A1 (fr) * 1985-09-09 1987-04-01 Framatome Chaudière à lit fluidisé circulant
US4854249A (en) * 1987-08-03 1989-08-08 Institute Of Gas Technology Two stage combustion
EP0438169A2 (fr) * 1990-01-19 1991-07-24 Nkk Corporation Appareil à combustion à lit fluidisé circulant

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1997039278A1 (fr) * 1996-04-12 1997-10-23 Abb Carbon Ab Procede et installation de combustion pour une combustion a lit fluidise sous pression avec recyclage des matieres solides

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Publication number Publication date
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