EP3486591B1 - Fluidized bed evaporation drier - Google Patents

Description

The invention relates to a device for removing fluids and / or solids from a mixture of particulate materials with a container which forms an annular process space with a plurality of cells separated by walls, comprising an inlet cell, intermediate cells and an outlet cell, an entry device for Introducing the batch to be treated into the inlet cell of the process space, a discharge device for discharging the treated batch from the outlet cell of the process space, a fan device for supplying a first fluidizing agent, in particular in the form of superheated steam, from below into the process space through an inflow floor to generate a Fluidized bed in the process space, a heating device for processing the first fluidizing agent in the flow direction upstream of the fan device, swirl vanes for conditioning the flow in the container from the process room to the heating device g and in part also leads to a steam outlet, and a dedusting device in the flow path between the process space and the heating device, wherein dust can be guided to the outlet cell via the dedusting device. Such a device is particularly suitable for drying bulk goods and materials from the food and feed industry, but other particulate materials or mixtures thereof can also be treated with such a device.

A large number of devices of the type mentioned are known from the prior art, which generally use superheated steam as a fluidizing agent. These so-called fluidized bed evaporation dryers are used to flow through and fluidize bulk material or particulate materials from below with superheated steam, so that a fluidized bed is created. The material to be treated is 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 to a discharge cell. Takes place in the discharge cell no inflow from below, so that the finished material can be discharged at the lower end of the discharge cell, for example via a discharge screw. The container is sealed at the discharge end as well as at the entry device by means of a lock device in order to allow the machining process to take place under excess pressure. Particles entrained by the steam are separated on the way from the process room to a (steam) discharge using swirl-generating blades and a dedusting device, in order to then feed the dust-free steam to the process room after reheating in a heating device via an inflow floor. Such facilities are from, for example EP 1 956 326 B1 , EP 2 146 167 B1 , EP 1 070 223 B1 , US 5,357,686 A , EP 0 153 704 A2 and the EP 2 457 649 A1 known.

In the known devices, inadmissible accumulations of material or lumps can occur in the area of the material entry, which in the worst case can lead to a total failure of the device. In order to remove a blockage in the process space, the device has to be switched off, depressurized and cooled in order to then manually remove the blockage using shovels or the like.

It is therefore an object of the present invention to further develop the generic device in such a way that it has greater operational reliability. In particular, clumping of the material to be dried, that is to say the mixture of particulate materials, is to be substantially avoided. The overall flow of the device is to be improved.

To achieve the object, a device for removing fluids and / or solids from a mixture of particulate materials with the features of claim 1 is proposed.

This object is achieved according to the invention in that, in order to support a transport of the batch from the inlet cell to the outlet cell and / or a swirling of the batch in the process space of the inflow floor, has first unevenness, and / or at least temporarily a second fluidizing agent, in particular in the form of superheated steam , essentially parallel to the inflow floor by means of first nozzles at least in the Inlet cell can be fed, and / or first flow guide members above the inflow floor and / or second, flow guide members below the inflow floor are provided.

According to the invention, the area of the inflow floor in the inlet cell is larger than, preferably twice as large, the respective area of the inflow floor of the intermediate cells.

It can be provided that in the inlet cell a mixing of dried and moist parts of the mixture takes place in the manner of a stirred tank, in the intermediate cells to avoid mixing of wet parts with dried-on parts of the mixture, flow guidance in the manner of a flow tube is realized, and into the No outlet fluid passes through the inflow floor.

It is also proposed that the feed device for the batch is connected to the container in the region of the inlet cell, preferably in the middle of the height of the inlet cell and / or at the height of the upper extensions of the fluidized bed.

It can be provided that the feed device loosens the batch by mechanical transport, preferably by means of mechanically acting paddles, in particular a screw conveyor, and / or preheated and / or via

Flight transport, preferably by supplying it with a third fluidizing agent, in particular in the form of superheated steam by steam injection into the screw conveyor, which feeds the inlet cell.

It is further preferred that the inflow floor has first openings in the inlet cell and the intermediate cells, the opening ratio of which preferably decreases from the inlet cell in the direction of the outlet cell.

Devices according to the invention can be characterized in that the inflow floor has the first unevenness in the form of recessed recesses and / or at least over the first quarter of the process space.

It is also proposed that the inflow base be inclined upward at its edge facing the container and otherwise be essentially horizontal, the edge preferably being provided with first openings and / or first unevenness at least over the first quarter of the process space.

It can also be provided that the second fluidizing agent can be fed in at a pressure of at least 2 bar above the mean pressure in the container and / or in the first quarter of the process space.

A shielding of the heating device can be provided, the shielding preferably expanding conically in the process space from top to bottom, the first nozzles extending between the shielding and the inflow floor, and / or the shielding second openings and / or second bumps, preferably in the form of recessed recesses.

It is also suggested that the wall between the outlet cell and the inlet cell extends down to the level of the inflow floor, and / or the walls between the inlet cell and a first intermediate cell, between the intermediate cells and between the last intermediate cell and the outlet cell a vertical Have a distance to the inflow floor, in particular to the edge of the inflow floor.

It is preferred that the first flow guide members are provided and / or adjustable between the first nozzles.

The invention also proposes that first second flow guide members are provided in a dished end as part of a follow-up device of the fan device, the fan device preferably comprising a blower within the follow-up device.

Preferred devices according to the invention are characterized in that second second flow guide members are provided in a dished end and / or are attached and / or adjustable on the guide apparatus, preferably each being rotatable about an axis of rotation that extends essentially perpendicular to the inflow floor or vertically.

It is also preferred that third second flow guide members are attached to and / or adjustable on the inflow floor support members, preferably in each case rotatable about an axis of rotation extending essentially parallel to the inflow floor or horizontally.

According to the invention, it is also proposed that the number, orientation and / or arrangement of the first and / or second openings, the first and / or second bumps, the first nozzles and / or the first and / or second flow guide members for the targeted application of horizontal to the batch Transport pulses in the direction of the outlet cell and / or vertical swirling pulses is determined or can be changed.

It can be provided that the orientation, in particular the second second and / or third second flow guide members, and / or the supply from the second fluidization means to the first nozzles can be changed via an adjustment device that can be operated from outside the container.

Figur la:

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 la 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 result from the following description, in which exemplary embodiments of the invention are explained in detail on the basis of schematic drawings. It shows:

Figure la:

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

Figure 1b:

a schematic representation of the device of the Figure 1a ;

Figure 2:

a longitudinal sectional view of an entry device of the device according to Figure 1a ;

Figures 3a-3c:

perspective partial views of the bottom region of the device according to Figure 1a ;

Figures 4a and 4b:

perspective partial views of the underside and top of a perforated plate with scales for the device according to Figures la and 1b;

Figure 5a:

a plan view of a floor area of a second embodiment of the device according to the invention with a Nachleitapparat;

Figure 5b:

a partial sectional view of the bottom portion of Figure 5a ;

Figure 5c:

a view like Figure 5a with additional, adjustable baffles;

Figure 5d:

a partial perspective view of the bottom portion of the Figure 5c ;

Figure 6:

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

Figures 7a and 7b:

Sectional views through an inflow floor of the device according to the Figures 5a - 5d .

The Figures 1a and 1b show a device according to the invention in the form of a fluidized bed evaporation dryer 1000 with an entry device 1 for introducing material to be dried in the form of pressed pulp into a container 21 which has a process space 23 in the region of its bottom 22. More precisely, the pulp is introduced into the process space 23, in which a fluidized bed 2 can be produced by flowing an inflow base 24 with superheated steam to dry the pulp. Dried pulp can then be discharged from the container 21 by means of a discharge device 3, while particles entrained in the steam from the process space 23 within the container 21 are separated off, inter alia by means of a dust collector 4 above the fluidized bed 2. The particle-freed steam finally arrives in part to a steam outlet 5 and partly to a heating device in order to be overheated again by means of a heater 6, so that it can be fed again to the process space 23 through the inflow floor 24 with the interposition of a fan device or a blower 7. This results in a closed circuit of part of the steam.

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

A first swirl is generated between the process space 23 and an expansion cone 26 via blades 29 above the walls 25. The vertical flow of the steam in the process space 23 is thereby deflected in order to lead to a swirl flow in the expansion cone 26. Due to the swirl the steam together with the entrained particles are thus directed onto the wall of the container 21, which causes the particles to slow down, 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 decrease in the flow speed, which leads to a broadening of the steam flow out of the cells. The expansion cone 26 and an upper region 27 adjoining the same have no internals, that is to say represent a free space in which, with the separation of particles, the flows from the cells spread apart and at least partially mix. To transfer kinetic energy in order 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 together with the steam enter a central separator in the form of the dust collector 4 in the lid 28 of the container. The ribs 36 ensure that the particles are decelerated, which promotes separation. The inner contour of the cover 28 is shaped to deflect the flow.

After pre-separation of particles in the free space, smaller particles are separated by inflowing the particle-vapor mixture into the dust collector 4. Finally, the separated dust arrives in an outlet cell 202 in the process space 23 via a dust cyclone 33.

The entry device 1 enters the pulp to be treated into a first cell in the process space 23, which is referred to below as the inlet cell 201. The fluidizing agent does not flow through the last cell or outlet cell 202 provided with the discharge device 3 or only to a small extent, so that material entering this cell 202 from above or along the inflow floor 24 reaches the bottom area and via the discharge device 3 , especially as in the EP 2 146 167 B1 described, can be removed. To be even and steady To ensure fluidization in the fluidized bed 2, a process control according to the EP 2 457 649 A1 be used.

The feed device 1 is arranged in such a way that it brings the pulp into the middle of the inlet cell 201, at the level of the upper extensions of the fluidized bed 2, which represents a lower installation than known devices. In addition, it ensures that the pulp is loosened and preheated into the inlet cell 201. For this purpose, it comprises a screw conveyor 400 with rotatable paddles 401, as in FIG Figure 2 shown. In a feed area 402, wet material, that is to say pulp to be dried, is fed in and steam is applied directly from a first steam feed 403, and clumped pulp is comminuted by mechanical energy input from the rotating paddles 401. By rotating the paddles 401, however, the pulp is also transported and, during the transport, steam is supplied again from second steam supplies 404 and 405. A suitable supply of steam therefore not only heats up the pulp under water evaporation in the supply area 402 and also during the subsequent comminution of clumped pulp, but at the same time in each case creates turbulence, which is why there is in fact turbulence there. Due to the mechanical transport by means of the mechanically acting paddles 401 and the preheating and the air transport by means of the steam supply 403-405, the pulp is loosened and preheated in the process space 23, which counteracts the formation of further clumps of pulp in the process space 23. This prevents clogging of openings, gaps and the like in the process space 23 and ensures a 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 ensures that the pulp is preheated and loosened together with an excess amount of steam that immediately escapes upwards in the container 21 into the inlet cell 201. The inlet cell 201 preferably covers a larger area of the inflow base 24 than each of the remaining cells, so that the supplied pulp is brought into contact with an increased amount of steam on an enlarged floor area, which also counteracts clumping works. Because in the inlet cell 201, the pulp is still the wettest. A doubling of the size of the inlet cell 201 compared to the rest of the cell has proven 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 clumping, as described below with respect to FIG Figures 3a to 3c , 4a and 4b is described.

An apron 300 delimits the annular process space 23 to the inside. A steam supply pipe 301 opens above the inflow base 24 between the apron 300 and the heater 6 in order to supply steam via nozzles 302 to at least a first quarter of the cells across the inflow base 24, as in FIG Figure 3a shown. This leads to a flow from the apron 300 radially to the wall of the container 21, see flow lines 311. The steam supply pipe 301 is arranged in the ring section of the inlet cell 201 in order to loosen up there increasingly with transverse steam, since the pulp there too still carries the largest amount of water. In addition, guide plates 303 are arranged between the nozzles 302 to ensure the cross flow in each cell. The nozzles 302 and the guide plates 303 thus represent flow directors, the steam supply via the nozzles 302 additionally leading to heating and water evaporation from the pulp.

The inflow base 24 and the apron 300 are formed with perforated plates 304a, 304b and 305 in order to guide the flow in a targeted manner. All perforated plates 304a, 304b and 305 have holes for the passage of superheated steam, while some of these perforated plates, namely perforated plates 304b and 305, also have unevenness for guiding said steam. Thereby, the perforated plates 305 of the apron 300 support a flow along the apron 300 down to the inflow floor 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 im substantially perpendicular to the inflow floor 24, namely from the apron 300 via the inflow floor 24 back to the apron 300 is enforced. A further circular flow of the same direction of rotation is caused by perforated plates (not shown) with unevenness in a base extension which is inclined upward in the direction of the open ends of the cells and which corresponds to an edge 307 contacting the wall of the container 21 Figure 3b represents, namely, along the inflow floor 24, the edge 307 and the wall back to the inflow floor 24.

A transport area 306 runs between the perforated plate 304b and the edge 307 and thus between the two vertical, same-directional circular flows, which ensures a horizontal circular path from the inlet cell 201 to the outlet cell 202 for conveying the pulp in the process space 23. According to the invention, there is therefore a continuous transport path of the pulp in the process space 23 through the 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, swirling with 2 vortices circulating in the same direction per cell is forced, which means that Material flow in process room 23 homogenized and drying improved.

The nozzles 302, guide plates 303 and perforated plates 304a, 304b and 305 can differ for each cell in order to take into account the progressive 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 Figures 4a and 4b show, by way of example, a perforated plate 304b which has a multiplicity of holes 341 and scales 342. Specifically shows Figure 4a a lower side 343, on which the perforated plate 403b in the area of the scales 342 each has a large opening for superheated steam, which is in an unevenness on the upper side 344, the in Figure 4b is shown, leads and can thus provide the superheated steam with a directional pulse. Many different geometrical designs are conceivable; it is also conceivable that the in the Figures 3b and 3c The flow lines 312 shown do not run exactly radially, but are inclined in the direction of the flow lines 313 so as to serve to transport the pulp.

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

The pulp not only has to be dried in the process space 23, but at the same time as drying it has to be transported from the inlet cell 201 to the outlet cell 202. In the embodiment of the Figures 3a - 3d Both the transport and the swirling and thus drying can be influenced by a targeted selection of the number, orientation and / or arrangement of the holes 341, the scales 342, the nozzles 302 and the guide plates 303. The holes 341 and scales 342 in the perforated plates 304a, 304b and 305 as well as the guide plates 303 are permanently installed in the fluidized bed evaporation dryer 1000. The following is an alternative structure for this with reference to the Figures 5a - 5d described.

Figure 5a shows a top view of a dished end 22'a of a second exemplary embodiment of a fluidized bed evaporation dryer according to the invention, in which, in addition to a blower 7 ', a plurality of baffles 501 of a secondary diverter 500 are arranged, which are used to condition the flow in the dished end 22'a, namely for guiding said flow radially outward, as through the flow paths A in Figure 5a shown. The guide apparatus 500 comprises further baffles 502 and 503 with different orientations, as best shown in FIG Figure 5b shown, which is a partial perspective of the area below a Inflow floor 24 'within a floor 22' with the dished bottom 22'a. In Figure 5b An inflow base support member 24'a is also shown, along which the flow conditioned by the after-directing apparatus 500 rises in accordance with the flow path B, and either through openings in the essentially horizontally extending inflow base 24 'or an edge 240' inclined towards the wall of the base 22 '. for this purpose enters the process space or is circulated in the area of the floor 22 'below the inflow floor 24'.

It has surprisingly been found that the swirl flow in the process space, which is forced by the after-guide apparatus 500 below the inflow base 24 ′, has a considerable influence on the solids transport. In order to be able to influence this solids transport in a targeted manner, it is proposed according to the invention to provide adjustable guide plates 600 in the region of the bottom 22 ', in particular up to the dished bottom 22'a, as in Figures 5c and 5d shown. Each adjustable baffle 600 can be rotated about an axis of rotation 601 via an adjusting device 602. The adjusting device 602 can either be adjusted manually when the fluidized bed evaporation dryer according to the invention is opened, or else from outside the fluidized bed evaporation dryer, even in the drying operation of the same.

As an alternative to the adjustable guide plates 600 or even cumulatively, further adjustable guide plates 700 can be arranged directly below the inflow floor. This is in Figure 6 Shown in a perspective view, according to which the adjustable guide plates 700 are arranged substantially parallel to the inflow base 24 ″ in the region of the inflow floor support members 24 ″ b, and can be rotated about an axis of rotation 701, as indicated by the arrow F. The inflow floor support members 24 "b are in turn supported by the inflow floor support members 24" a, which are attached to the wall of the floor.

Based on Figures 7a and 7b the mode of operation of the adjustable guide plates 600 and 700 is explained below. The Figures 7a and 7b namely, the flow path G or G 'can be removed through the individual openings in an inflow base 24'" has an influence on the solids transport path H or H 'within the fluidized bed 2'". Depending on the orientation of the flow path G or G ', different effects occur Figure 7a due to its lower tendency towards the inflow floor 24 ′ ″ for increased transport within the fluidized bed 2 ″ ′, while a flow path G ′ according to FIG Figure 7b steeper through the inflow floor 24 "'and thus ensures increased turbulence in the fluidized bed 2'".

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

The features disclosed in the above description, in the drawings and in the claims can be essential both individually and in any combination for the implementation of the invention in its various embodiments.

Reference symbol list

1

Entry facility

2, 2 '"

fluidized bed

3rd

Discharge device

4th

Dust collector

5

Steam outlet

6

Heater

7, 7 '

fan

21st

container

22.22 '

ground

22a, 22'a

Dished bottom

23

Process room

24, 24 ', 24 ", 24'"

Inflow floor

24'a, 24 "a, 24" b

Inflow floor support member

25th

wall

26

Extension cone

27th

upper area

28

cover

29

shovel

33

Dust cyclone

34

jet

35

jet

36

rib

201

Inlet cell

202

Exhaust 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 area

307

edge

310-313

Flow line

341

hole

342

Dandruff

343

bottom

344

Top

400

Screw conveyor

401

paddle

402

Feed area

403-405

Steam supply

406

Docking area

500

Guide device

501-503

Baffle

600

Adjustable baffle

601

Axis of rotation

602

Adjustment device

700

Adjustable baffle

701

Axis of rotation

1000

Fluidized bed evaporation 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 '

Solids transport path

Claims (16)

1. A device (1000) for removing fluids and/or solid substances from a mixture of particulate materials, including

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

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

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

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

   • a heating means (6) for processing the first fluidizing agent in the flow direction in front of the ventilator means (7, 7'),

   • swirl impellers (29) for conditioning the flow (110 - 160) leading within the container (21) from the process chamber (23) to the heating means (6) and in part to a steam outlet (5), and

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

   characterized in that
   for supporting a transport of the mixture from the inlet cell (201) to the outlet cell (202) and/or a turbulence of the mixture within the process chamber (23):

   • the inflow bottom (24) has first uneven surfaces, and/or

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

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

   wherein the surface of the inflow bottom (24) within the inlet cell (201) is larger than, preferably twice as large as, the respective surface of the inflow bottom (24) of the intermediate cells.
2. The device according to claim 1, characterized in that
   the introduction means (1) comprises a screw conveyor (400) having rotatable vanes (401), which is configured to realize a mixing of dried and humid parts of the mixture in the manner of a stirrer tank,
   within the intermediate cells, a flow guidance is realized in the manner of a flow tube for avoiding humid parts to be mixed with dried parts of the mixture, and
   the outlet cell (202) is configured such that no fluidizing agent gets through the inflow bottom (24).
3. The device according to claim 1 or 2, characterized in that
   the introduction means (1) for the mixture is connected to the container (21) in the area of the inlet cell (201),
   preferably in the middle of the height of the inlet cell (201) and/or at the level of the upper tails of the fluidized bed (2).
4. The device according to claim 3, characterized in that
   the introduction means (1) supplies the mixture in a loosened manner to the inlet cell (201)

   • by mechanical transportation, preferably by means of mechanically acting vanes (401), in particular of a screw conveyor (400), and/or

   • in a preheated manner and/or via transportation by air, preferably by applying a third fluidizing agent, in particular in the form of overheated steam, by steam injection (403 - 405) into the screw conveyor (400).
5. The device 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 thereof preferably decreasing from the inlet cell (201) toward the outlet cell (202).
6. The device according to any one of the preceding claims, characterized in that the inflow bottom (24) includes the first uneven surfaces (342) in the form of recesses situated deepened and/or at least over the first quarter of the process chamber (23).
7. The device according to any one of the preceding claims, characterized in that at its edge (307) facing the container (21), the inflow bottom (24) is upwardly inclined and otherwise substantially horizontally extending, wherein the edge (307) preferably is provided with first openings (341) and/or first uneven surfaces (342) at least over the first quarter of the process chamber (23).
8. The device according to any one of the preceding claims, characterized in that the first nozzles (302) are designed to feed in the second fluidizing agent at a pressure of at least 2 bars above the average pressure in the container (21) and/or in the first quarter of the process chamber (23).
9. The device according to any one of the preceding claims, characterized by a shielding (300) of the heating means (6), the shielding (300) preferably conically flaring in the process chamber (23) from the top to the bottom, the first nozzles (302) extending between the shielding (300) and the inflow bottom (24), and/or
   the shielding (300) including second openings (341) and/or second uneven surfaces (342) preferably in the form of recesses situated deepened.
10. The device according to any one of the preceding claims, characterized in that the wall (25) between the outlet cell (201) and the inlet cell (202) 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 from the inflow bottom (24), in particular from the edge (307) of the inflow bottom (24).
11. The device according to any one of the preceding claims, characterized in that the first flow guidance members (303) are provided and/or adjustable between the first nozzles (302).
12. The device according to any one of the preceding claims, characterized in that first second flow guidance members (501, 502, 503) are provided in a torispherical head (22'a) as a part of a post-guidance apparatus (500) of the ventilator means (7'), wherein preferably the ventilator means (7') comprises a fan within the post-guidance apparatus (500).
13. The device according to any one of the preceding claims, characterized in that second second flow guidance members (600) are provided in a torispherical head (22'a) and/or are attached to the post-guidance apparatus (500) and/or are adjustable each preferably about an axis of rotation (601) extending substantially perpendicular or vertically to the inflow bottom (24').
14. The device according to any one of the preceding claims, characterized in that third second flow guidance members (700) are attached to inflow bottom support members (24"b) and/or are adjustable each preferably about an axis of rotation (601) extending substantially in parallel or horizontally to the inflow bottom (24").
15. The device according to any one of the preceding claims, characterized in that the number, orientation and/or arrangement

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

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

    • the first nozzles (302), and/or

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

    is or are determined or modifiable for selectively applying the mixture with horizontal transportation pulses in the direction of the outlet cell (202) and/or vertical turbulence pulses.
16. The device according to claim 15, characterized in that
    the orientation, in particular of the second second and/or third second flow guidance members (600, 700), and/or the supply of the second fluidizing agent to the first nozzles (302) is modifiable via an adjusting means (602) that is operable from outside the container (21).

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