EP3137832B1 - Fluidized-bed evaporation dryer - Google Patents

Description

The invention relates to a device for removing fluids and / or solids from a mixture of particulate materials with a container forming an annular process space with a plurality of cells separated by walls, comprising an inlet cell, intermediate cells and an outlet cell Introducing the mixture to be treated into the inlet chamber of the process chamber, a discharge device for discharging the treated mixture from the outlet cell of the process chamber, a fan device for supplying a first fluidizing agent, in particular in the form of superheated steam, from below into the process chamber through a distributor plate for producing a Fluidized bed in the process chamber, a heating device for processing the first fluidizing agent in the flow direction in front of the fan device, swirl blades for conditioning the flow in the container from the process chamber to the heating gseinrichtung and in part also to a steam outlet, and a dedusting device in the flow path between the process chamber and the heating device, wherein the dedusting dust to the outlet cell is feasible. Such a device is particularly suitable for drying bulk materials and materials from the food and feed industry, but other particulate materials or blends thereof may also be treated with such a device.

From the prior art, a variety of devices of the type mentioned are known, which usually use superheat steam as a fluidizing agent. These so-called fluidized bed evaporators are used to To flow bulk material or particulate materials from below with superheated steam and to fluidize, so that a fluidized bed is formed. The material to be treated is thereby conveyed from an entry cell, in which the material to be treated is introduced into the container and the process space, via subsequent process cells up to a discharge cell. In the discharge cell there is no flow from below, so that at the lower end of the discharge cell the finished treated material can be discharged, for example via a discharge screw. The container is sealed at the discharge end as well as at the entry device via a lock device in order to allow the processing process to proceed under overpressure. Particles entrained by the steam are separated on the way from the process space to a (vapor) discharge using swirl-producing blades and a de-dusting device to then supply the dust-free steam to the process space after re-heating in a heating device via a distributor plate. Such facilities are for example from the EP 1 956 326 B1 . EP 2 146 167 B1 . EP 1 070 223 B1 . US 5,357,686 and the EP 2 457 649 A1 known.

In the known devices may lead to inadmissible accumulation of material or lumps in the field of material entry, which in the worst case can lead to a total failure of the device. To remedy a blockage in the process room namely the device must be turned off, depressurized and cooled, and then manually pick up the blockage with shovels or the like.

Object of the present invention is therefore to further develop the generic device such that it has a higher reliability. In particular, a clumping of material to be dried, ie the mixture of particulate materials, should be substantially avoided. So it should be improved overall flow of the device.

This object is achieved by the features of the characterizing part of claim 1. Claims 2 to 16 describe preferred embodiments of the device according to the invention.

Figur 1a:

eine perspektivische Seitenansicht eines ersten Ausführungsbeispiels einer erfindungsgemäßen Vorrichtung;

Figur 1b:

eine schematische Darstellung der Vorrichtung der Figur 1a;

Figur 2:

eine Längsschnittansicht einer Eintragseinrichtung der Vorrichtung gemäß Figur 1a;

Figuren 3a-3c:

perspektivische Teilansichten des Bodenbereichs der Vorrichtung gemäß Figur 1a;

Figuren 4a und 4b:

perspektivische Teilansichten der Unterseite und Oberseite eines Lochblechs mit Schuppen für die Vorrichtung gemäß Figur 1a und 1b;

Figur 5a:

eine Draufsicht auf einen Bodenreich eines zweiten Ausführungsbeispiels der erfindungsgemäßen Vorrichtung mit einem Nachleitapparat;

Figur 5b:

eine Teilschnittansicht des Bodenbereichs von Figur 5a;

Figur 5c:

eine Ansicht wie Figur 5a mit zusätzlichen, verstellbaren Leitblechen;

Figur 5d:

eine perspektivische Teilansicht des Bodenbereichs der Figur 5c;

Figur 6:

eine perspektivische Ansicht des Bodenbereichs eines dritten Ausführungsbeispiels der erfindungsgemäßen Vorrichtung; und

Figuren 7a und 7b:

Schnittansichten durch einen Anströmboden der Vorrichtung gemäß den Figuren 5a - 5d.

Further features and advantages of the invention will become apparent from the following description, are explained in the embodiments of the invention with reference to schematic drawings in detail. Showing:

FIG. 1a

a side perspective view of a first embodiment of a device according to the invention;

FIG. 1b

a schematic representation of the device of FIG. 1a ;

FIG. 2:

a longitudinal sectional view of an insertion device of the device according to FIG. 1a ;

FIGS. 3a-3c:

partial perspective views of the bottom portion of the device according to FIG. 1a ;

FIGS. 4a and 4b:

Partial perspective views of the bottom and top of a perforated plate with scales for the device according to FIGS. 1a and 1b ;

FIG. 5a

a plan view of a soil richness of a second embodiment of the device according to the invention with a Nachleitapparat;

FIG. 5b:

a partial sectional view of the bottom portion of FIG. 5a ;

FIG. 5c:

a view like FIG. 5a with additional, adjustable baffles;

FIG. 5d:

a partial perspective view of the bottom portion of FIG. 5c ;

FIG. 6:

a perspective view of the bottom portion of a third embodiment of the device according to the invention; and

FIGS. 7a and 7b:

Sectional views through a distributor plate of the device according to the FIGS. 5a-5d ,

The FIGS. 1a and 1b show a device according to the invention in the form of a fluidized bed evaporator dryer 1000 with an insertion device 1 for introducing material to be dried in the form of pressed pulp in a container 21 which has a process space 23 in the region of its bottom 22. More specifically, the pulp is introduced into the process space 23 in which a fluidized bed 2 can be generated by flowing a superheated steam inflow floor 24 to dry the pulp. Dried pulp can then be discharged from the container 21 by means of a discharge device 3, while particles entrained by the vapor from the process space 23 are separated within the container 21, inter alia by means of a dust collector 4 above the fluidized bed 2. The vapor freed of particles finally passes in part to a steam outlet 5 and partly to a heating device to be reheated by means of a heater 6, so that it again with the interposition of a fan device or a blower 7 the process chamber 23 through the distributor plate 24 can be fed therethrough. As a result, there is a closed circuit of part of the steam.

Above the inflow wall 24, walls 25 are arranged vertically aligned and extend substantially from an outer wall of the heater 6 to a wall of the container 21 to form cells between them in the process space 23. The walls 25 may extend down to the inflow base 24, but then have to have openings or form a space between them and the inflow base 24. The cells formed by the walls 25 are open at the top, so that the steam serving as the fluidizing agent flows through the cells from bottom to top and entrains the material or particles to be treated and optionally transports them to a downstream cell.

There is a first swirl generation between the process chamber 23 and an expansion cone 26 via blades 29 above the walls 25 instead. As a result, the vertical flow of the steam in the process space 23 is deflected in order to lead to a swirl flow in the expansion cone 26. As a result of the swirl impingement, the steam together with the particles entrained therewith is directed onto the wall of the container 21, which causes the particles to decelerate, namely by wall friction, so that the braked particles then fall back along the wall into the process space 23.

In the expansion cone 26, there is a reduction in the flow rate, which leads to a broadening of the flow of steam from the cells. The expansion cone 26 and an upper region 27 adjoining the same have no internals, ie they provide a free space in which, with the separation of particles, the flows spread out of the cells and at least partially intermix. To transfer kinetic energy to improve the mixing of flow layers with different thermal states, superheated steam is blown into the upper region 27 via nozzles 34 and 35. Separated particles are discharged vertically along the wall in the expansion cone 26 via ribs 36, while the rest of the particles enter together with the steam in a central separator in the form of the dust collector 4 in the lid 28 of the container. The ribs 36 thereby ensure a deceleration of the particles, which promotes the deposition. The inner contour of the lid 28 is formed to deflect the flow.

After pre-separation of particles in the free space, the separation of smaller particles takes place by flowing the particle vapor mixture into the dust collector 4. Finally, the separated dust passes through a dust cyclone 33 into an outlet cell 202 in the process space 23.

The entry device 1 introduces the pulp to be treated into a first cell into the process space 23, which is referred to below as the inlet cell 201. The last cell or outlet cell 202 provided with the discharge device 3 is not or only to a small extent flowed through by the fluidizing agent, so that material entering the cell 202 from above or at the inlet bottom 24 reaches the bottom region and via the discharge device 3 , especially as in the EP 2 146 167 B1 described, can be removed. In order to ensure a uniform and continuous fluidization in the fluidized bed 2, a process control according to the EP 2 457 649 A1 be used.

The inserter 1 is arranged to introduce the pulp into the center of the inlet cell 201, at the level of the upper extensions of the fluidized bed 2, which is a lower installation than known devices. In addition, it ensures that the pulp loosens and preheated in the inlet cell 201 passes. For this purpose, it comprises a screw conveyor 400 with rotatable paddles 401, as in FIG. 2 shown. In a feed region 402, wet material, that is to say pulp to be dried, is supplied and immediately supplied with steam from a first steam feed 403, and comminution of clumped pulp takes place by mechanical energy input of the rotating paddle 401. By rotating the paddle 401, however, the pulp is also transported and again supplied with steam from second steam feeders 404 and 405 during the transport. By suitable steam supply thus occurs in the feed area 402 and also in the subsequent comminution of clumped pulp during transport not only to warm the pulp under water evaporation, but at the same time in each case to turbulence, which is why there is also a turbulence there. Due to the mechanical transport by means of the mechanically acting paddle 401 and the preheating and the air transport by means of the steam supply 403-405, the pulp comes loose and preheated in the process chamber 23, which counteracts the formation of further clumps of pulp in the process chamber 23. This avoids clogging of openings, crevices and the like in the process space 23 and ensures continuous transport of the pulp from the inlet cell 201 to the outlet cell 202.

The screw conveyor 400 is attached to the container 21 via a docking area 406 and causes the pulp to be preheated and released into the inlet cell 201 along with an excess amount of steam immediately escaping upwardly in the container 21. The inlet cell 201 preferably covers a larger area of the inflow bottom 24 than any of the remaining cells, so that the supplied pulp is brought into contact on an increased bottom area with an increased amount of steam, which again counteracts a clumping. Because in the inlet cell 201, the pulp is still the wettest. Doubling the size of the inlet cell 201 from the rest of the cell has been found to be particularly good.

The flow from the inlet cell 201 to the outlet cell 202 is conditioned via a plurality of flow directors to further counteract agglomeration, as discussed below with reference to FIGS FIGS. 3a to 3c . 4a and 4b is described.

An apron 300 bounds the annular process space 23 inwards. Between the skirt 300 and the heater 6, a steam supply pipe 301 opens above the inflow bottom 24 to supply, via nozzles 302, steam to at least a first quarter of the cells across the inflow tray 24, as in FIG FIG. 3a shown. This leads to a flow from the skirt 300 radially to the wall of the container 21, see flow lines 311. In this case, the steam supply pipe 301 is disposed in the annular portion of the inlet cell 201 to provide there increasingly with transverse steam for loosening, since there also the pulp still carries the largest amount of water. In addition, guide plates 303 are disposed between the nozzles 302 to ensure the cross-flow in each cell. The nozzles 302 and the guide plates 303 thus provide flow directing members, with the addition of steam via the nozzles 302 in addition to heating and water evaporation from the pulp.

The inflow base 24 and the skirt 300 are formed with perforated plates 304a, 304b and 305, respectively, for guiding the flow in a targeted manner. In this case, all the perforated plates 304a, 304b and 305 have holes for the passage of superheated steam, while some of these perforated plates, namely the perforated plates 304b and 305, also have unevennesses for guiding said vapor. Thus, the perforated plates 305 of the skirt 300 support a flow along the skirt 300 down to the inflow base 24, see the flow lines 310, while the perforated plates 304b support a flow along the flow lines 312 as an extension of the flow line 311, so that a circular flow in the fluidized bed 2 in essentially perpendicular to the distributor plate 24, namely from the skirt 300 via the distributor plate 24 back to the skirt 300 is forced. Another circular flow same direction of rotation is not shown by perforated plates with bumps in a direction of the open ends of the cells upwardly inclined floor extension, the one contacting the wall of the container 21 edge 307 according to FIG. 3b is forced, namely along the inflow base 24, the edge 307 and the wall back to the distributor plate 24th

Between the perforated plate 304b and the edge 307 and thus between the two vertical, co-directed circular flows is a transport region 306 which a horizontal circular path from the inlet cell 201 to the outlet 202 to the Promoting the pulp in the process space 23 ensures. According to the invention, therefore, there is a continuous transport path of the pulp in the process space 23 by application of horizontal transport pulses in the direction of the discharge area, see flow lines 313, while at least over the first quarter of the process space 23 a turbulence with 2 vortices circulating in the same direction is forced per cell, which causes the Material flow homogenized in the process chamber 23 and improves the drying.

The nozzles 302, guide plates 303 and perforated plates 304a, 304b and 305 may differ for each cell to account for the progressing drying of the pulp. Thus, the opening ratio of the perforated plates 304a to 305 from the inlet cell 201 to the outlet cell 202 becomes smaller.

The FIGS. 4a and 4b For example, a perforated plate 304b having a plurality of holes 341 and flakes 342 is shown. More specifically shows FIG. 4a an underside 343 on which the perforated plate 403b in the region of the flakes 342 each have a large opening for superheated steam, resulting in a bump on the top 344, the in FIG. 4b is shown, leads and thus can provide the superheated steam with a directional pulse. Many different geometric designs are conceivable; It is also conceivable that the in the FIGS. 3b and 3c shown flow lines 312 are not exactly radial, but are inclined in the direction of the flow lines 313, so as to serve a transport of the pulp.

The fan 7, according to FIG. 1a is provided within a dished bottom 22 a of the bottom 22, serves to convey superheated steam from the heater 6, which is often referred to as the vapor stream and which allows fluidization in the fluidized bed 2. The need for vapors or drying vapors in the individual cells of the process space 23 is different, since the pulp to be dried from the inlet cell 201 in the direction of the outlet cell 202 loses moisture. Since the vapor stream enters the individual cells via the distributor plate 24 substantially in parallel via the fan 7, the vapor is distributed in accordance with the pressure loss which arises when the individual cells flow. This pressure loss is primarily influenced by the pressure loss of the inflow base 24 and the overlying mass of the fluidized bed 2.

Not only does the pulp have to be dried in the process space 23, but at the same time it has to be transported from the inlet cell 201 to the outlet cell 202 for drying. In the embodiment of the FIGS. 3a-3d can be influenced by targeted selection of the number, orientation and / or arrangement of the holes 341, the shed 342, the nozzles 302 and the guide plates 303, both the transport and the turbulence and thus drying. The holes 341 and flakes 342 in the perforated plates 304a, 304b, and 305 as well as the guide plates 303 are fixedly installed in the fluidized bed dryer 1000. In the following, an alternative construction will be described with reference to FIGS FIGS. 5a-5d described.

FIG. 5a shows a plan view of a dished bottom 22'a of a second embodiment of a fluidized bed evaporator according to the invention, in addition to a fan 7 'a plurality of baffles 501 of a Nachleitapparats 500 are arranged, which serve the conditioning of the flow in the dished bottom 22'a, namely for guiding said flow radially outward as through the flow paths A in FIG. 5a shown. The Nachleitapparat 500 includes further baffles 502 and 503 with different orientations, as best in FIG. 5b which shows a partial perspective of the area below an inflow bottom 24 'within a bottom 22' with the dished bottom 22'a. In FIG. 5b is also a Anströmmbodenstützglied 24'a shown, along which the conditioned by the Nachleitapparat 500 flow according to the flow path B rises, and either through openings in the substantially horizontally extending distributor plate 24 'or to the wall of the bottom 22' inclined edge 240 ' to get into the process room or in the area of the bottom 22 'below the inflow base 24' is circulated.

It has surprisingly been found that the swirl flow in the process space forced through the secondary flow apparatus 500 below the inflow base 24 'has a considerable influence on the transport of solids. In order to be able to influence this transport of solids in a targeted manner, the invention proposes adjustable baffles 600 in the region of the bottom 22 ', in particular into the dished bottom 22'a into, as in the FIGS. 5c and 5d shown. Each adjustable guide plate 600 is rotatable about an axis of rotation 601 via an adjusting device 602. The adjusting device 602 can be adjusted either manually in the case of the opening of the fluidized bed evaporator dryer according to the invention, or else from outside the fluidized bed evaporator, even in the drying operation thereof.

As an alternative to the adjustable baffles 600 or even cumulatively thereto, further adjustable baffles 700 can be arranged directly underneath the baffle bottom. This is in FIG. 6 in a perspective view, according to which are arranged substantially parallel to the distributor plate 24 "the adjustable baffles 700 in the area of Anströmmbodenstützgliedern 24" b, namely about an axis of rotation 701 rotatable, as indicated by the arrow F. The inflow base support members 24 "b are in turn supported by the inflow base support members 24" a, which are secured to the wall of the floor.

Based on FIGS. 7a and 7b Subsequently, the mode of action of the adjustable baffles 600 and 700 will be explained. The FIGS. 7a and 7b namely, the flow path G or G 'through the individual openings in a distributor plate 24''' removable, which has an influence on the solids transport path H or H 'within the fluidized bed 2''' has. Depending on the orientation of the flow path G or G 'there are different effects. Thus, a flow path G performs according to Figure 7a due to its lower inclination to the inflow base 24 '''to increased transport within the fluidized bed 2''', while a flow path G 'according to FIG. 7b steeper passes through the inlet plate 24 '''and thus provides for an increased turbulence in the fluidized bed 2'".

Of course, the adjustable baffles 600 and 700 can be combined with special perforated plate designs as well as guide plates above the inflow floor. Such a combination provides a precise adjustment of the flow needed for the particular pulp to optimize drying from an inlet cell to an outlet cell.

LIST OF REFERENCE NUMBERS

1

charge device

2, 2 '"

fluidized bed

3

discharge

4

dust collector

5

steam outlet

6

heaters

7, 7 '

fan

21

container

22, 22 '

ground

22a, 22'a

torospherical

23

process space

24, 24 ', 24 ", 24' ''

Inlet floor

24'a, 24 "a, 24" b

Anströmbodenstützglied

25

wall

26

flare cone

27

upper area

28

cover

29

shovel

33

dust cyclone

34

jet

35

jet

36

rib

201

inlet cell

202

outlet cell

240 '

edge

300

apron

301

Steam supply pipe

302

jet

303

guide plate

304a

perforated sheet

304b

perforated sheet

305

perforated sheet

306

transport sector

307

edge

310-313

streamline

341

hole

342

scale

343

bottom

344

top

400

screw conveyor

401

paddle

402

feed area

403-405

steam supply

406

docking

500

guide vane

501 - 503

baffle

600

Adjustable baffle

601

axis of rotation

602

adjustment

700

Adjustable baffle

701

axis of rotation

1000

Fluidized bed steam dryer

A

flow path

B

flow path

C

flow path

D

flow path

e

direction of rotation

F

direction of rotation

G, G '

flow path

H, H '

Solid transport path

Claims (16)

1. An apparatus (1000) for removing fluids and/or solids from a mixture of particulate materials, with

   • a container (21) forming an annular process chamber (23) with a plurality of cells separated from one another by walls (25) comprising an inlet cell (201), intermediate cells and an outlet cell (202),

   • an introduction device (1) for introducing the mixture to be treated into the inlet cell (201) of the process chamber (23),

   • a discharge device (3) for discharging the treated mixture from the outlet cell (202) of the process chamber (23),

   • a fan device (7, 7') for supplying a first fluidizing agent, in particular in the form of superheated steam, from below into the process chamber (23) through an inflow bottom (24, 24', 24", 24''') for generating a fluidized bed (2) in the process chamber (23),

   • a heating device (6) for preparing the first fluidizing agent in flow direction upstream of the fan device (7, 7'),

   • swirl vanes (29) for conditioning the flow in the container (21) from the process chamber (23) to the heating device (6) and partly to a steam outlet (5), and

   • a dust removal device (4) in the flow path between the process chamber (23) and the heating device (6), wherein dust can be guided to the outlet cell (202) via the dust removal device (4),

   wherein for supporting a transport of the mixture from the inlet cell (201) to the outlet cell (202) and/or a swirling of the mixture in the process chamber (23)

   • the inflow bottom (24) has first irregularities (342), and/or

   • at least temporarily a second fluidizing agent, in particular in the form of superheated steam, can be injected substantially parallel to the inflow bottom (24) by means of first nozzles (302) at least into the inlet cell (201), and/or

   • first flow guiding members (303) are provided above the inflow bottom (24) and/or second flow guiding members (501, 502, 503, 600, 700) are provided below the inflow bottom (24', 24", 24'''),

   characterized in that the introduction device (1) for the mixture is connected to the container (21) in the area of the inlet cell (201),
   the introduction device (1) supplies the mixture in a loosened state to the inlet cell (201) by a mechanical transport by means of mechanically acting paddles (401) of a screw conveyor (400), and preheated by applying a third fluidizing agent, in particular in the form of superheated steam by steam injection (403-405), into the screw conveyor (400),
   wherein the surface of the inflow bottom (24) in the inlet cell (201) is greater than, preferably twice as large as, the respective surface of the inflow bottom (24) of the intermediate cells, and
   for supporting a transport of the mixture from the inlet cell (201) to the outlet cell (202) and/or a swirling of the mixture in the process chamber (23) first flow guiding members (303) are provided above the inflow bottom (24) and/or second flow guiding members (501, 502, 503, 600, 700) are provided below the inflow bottom (24', 24", 24''').
2. The apparatus according to claim 1, characterized in that a mixing of dried and moist parts of the mixture takes place in the manner of a stirred tank in the inlet cell (201), in order to avoid a mixing of moist parts with dried parts of the mixture a flow guide is implemented in the manner of a flow pipe in the intermediate cells, and no fluidizing agent gets through the inflow bottom (24) into the outlet cell (202).
3. The apparatus according to claim 1 or 2, characterized in that the introduction device (1) for the mixture is connected to the container (21) in the area of the inlet cell (201) in the middle of the height of the inlet cell (201) and/or at the height of the upper extension of the fluidized bed (2).
4. The apparatus according to any one of the preceding claims, characterized in that for supporting a transport of the mixture from the inlet cell (201) to the outlet cell (202) and/or a swirling of the mixture in the process chamber (23)

   • the inflow bottom (24) has first irregularities (342), and/or

   • at least temporarily a second fluidizing agent, in particular in the form of superheated steam, can be injected substantially parallel to the inflow bottom (24) by means of first nozzles (302) at least into the inlet cell (201).
5. The apparatus according to any one of the preceding claims, characterized in that the inflow bottom (24) has first openings (341) in the inlet cell (201) and the intermediate cells, the opening ratio of which preferably decreases from the inlet cell (201) in the direction of the outlet cell (202).
6. The apparatus according to any one of the preceding claims, characterized in that the inflow bottom (24) has the first irregularities (342) in the form of recessed recesses and/or at least over the first quarter of the process chamber (23).
7. The apparatus according to any one of the preceding claims, characterized in that the inflow bottom (24) is inclined upward at its edge (307) facing the container (21) and otherwise extends substantially horizontally, wherein the edge (307) is preferably provided with first openings (341) and/or first irregularities (342) at least over the first quarter of the process chamber (23).
8. The apparatus according to any one of the preceding claims, characterized in that second fluidizing agent can be injected at a pressure of at least 2 bar above the mean pressure in the container (21) and/or in the first quarter of the process chamber (23).
9. The apparatus according to any one of the preceding claims, characterized by a shield (300) of the heating device (6), wherein preferably the shield (300) widens conically from top to bottom in the process chamber (23), the first nozzles (302) extend between the shield (300) and the inflow bottom (24), and/or the shield (300) has second openings (341) and/or second irregularities (342), preferably in the form of recessed recesses.
10. The apparatus according to any one of the preceding claims, characterized in that the wall (25) between the outlet cell (202) and the inlet cell (201) extends downward to the level of the inflow bottom (24), and/or the walls (25) between the inlet cell (201) and a first intermediate cell, between the intermediate cells and between the last intermediate cell and the outlet cell (202) have a vertical distance to the inflow bottom (24), in particular to the edge (307) of the inflow bottom (24).
11. The apparatus according to any one of the preceding claims, characterized in that the first flow guiding members (303) are provided and/or are adjustable between the first nozzles (302).
12. The apparatus according to any one of the preceding claims, characterized in that first second flow guiding members (501, 502, 503) are provided in a Klopper head (22' a) as part of a downstream guiding apparatus (500) of the fan device (7'), wherein preferably the fan device (7') comprises a blower inside of the downstream guiding apparatus (500).
13. The apparatus according to any one of the preceding claims, characterized in that second second flow guiding members (600) are provided in a Klopper head (22' a) and/or are attached to the downstream guiding apparatus (500) and/or are rotatable in each case about an axis of rotation (601) extending substantially perpendicular to the inflow bottom (24') or vertically.
14. The apparatus according to any one of the preceding claims, characterized in that third second flow guiding members (700) are arranged at inflow bottom supporting members (24"b) and/or are rotatable in each case about an axis of rotation (701) extending substantially parallel to the inflow bottom (24") or horizontally.
15. The apparatus according to any one of the preceding claims, characterized in that the number, orientation and/or arrangement

    • of the first and/or second openings (341),

    • of the first and/or second irregularities (342),

    • of the first nozzles (302) and/or

    • of the first and/or second flow guiding members (303, 501, 502, 503, 600, 700)

    is or are determined or variable for targeted application of the mixture with horizontal transport pulses in the direction of the outlet cell (202) and/or vertical swirling pulses.
16. The apparatus according to claim 15, characterized in that the orientation, in particular of the second second and/or third second flow guiding members (600, 700), and/or the supply of the second fluidizing agent to the first nozzles (302) is variable via an adjusting device (602) which can be operated from outside of the container (21).

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