Patent Publication Number: US-10330385-B2

Title: Fluidized-bed vaporisation dryer

Description:
CROSS-REFERENCE TO RELATED APPLICATIONS 
     This application is a national stage entry of International Patent Application No. PCT/IB2015/051707, filed Mar. 9, 2015, which claims the benefit of German Patent Application No. DE 102014106122.5, filed Apr. 30, 2014, the disclosures of each of which is incorporated herein by reference in their entirety. 
     STATEMENT REGARDING FEDERALLY SPONSORED RESEARCH OR DEVELOPMENT 
     Not applicable. 
     REFERENCE TO COMPACT DISK APPENDIX 
     Not applicable. 
     BACKGROUND OF THE INVENTION 
     1. Field of the Invention 
     The invention relates to a device for removing fluids and/or solid substances from a mixture of particle-shaped materials. For example, the device removes fluids and/or solid substances from a mixture of particle-shaped materials with a container which forms a ring-shaped process chamber with a plurality of cells separated from each other by walls, comprising an inlet cell, intermediate cells and an outlet cell, a feeding installation for conveying the mixture to be treated into the inlet cell of the process chamber, a discharge installation for discharging the mixture treated from the outlet cell of the process chamber, a ventilation installation for feeding in a first fluidisation agent, in particular in the form of overheated vapour, from below into the process chamber through an inflow floor for generating a fluidised bed in the process chamber, a heating installation for preparing the first fluidisation agent in the flow direction before the ventilation installation, swirl impellers for conditioning the flow in the container from the process chamber to the heating installation and which in part also leads to a vapour outlet, and a dust removal installation in the flow path between the process chamber and the heating installation, wherein dust can be guided to the outlet cell via the dust removal installation. A device of this type is in particular suitable for drying bulk products and materials from the food and animal feed industry, although other particle-shaped materials or mixtures from them can also be treated with such a device. 
     2. Description of Related Art 
     A plurality of devices of the above-named type are known from the prior art, which generally use overheated vapour as a fluidisation agent. These so-called “fluidised bed vaporisation dryers” are used to charge overheated vapour through bulk products or particle-shaped materials from below and to fluidise them, so that a fluidised bed is created. The material to be treated is here transported from an entry cell in which the material to be treated is introduced into the container and the process chamber, via subsequent method cells through to a discharge cell. In the discharge cell, no inflow occurs from below, so that on the lower end of the discharge cell, the material that has been fully treated can be discharged, for example via a discharge screw conveyor. The container is sealed on the discharge end and on the feeding installation by means of a threshold installation in order to be able to allow the processing sequence to run under overpressure. Particles which are carried along by the vapour are separated on the path from the process chamber to a (vapour) outlet using impellers which generate a swirl and a dust removal installation, in order to then guide the vapour which has been freed of dust to the process chamber following renewed heating in a heating installation via an inflow floor. Such installations are known e.g. from EP 1 956 326 B  1 , EP 2 146 167 BI, EP 1 070 223 B1, U.S. Pat. No. 5,357,686 and EP 2 457 649 AI. 
     With the known devices, impermissible material accumulations or lumps may occur in the area of the material charge, which in the worst case can lead to a total failure of the device. In order to remedy a blockage in the process chamber, the device must namely be switched off, rendered pressureless, and cooled down in order to then manually remove the blockage with impellers or similar. 
     SUMMARY 
     The object of the invention is thus to further develop the generic device in such a manner that it comprises a higher degree of operational reliability. In particular, the creation of lumps of drying products, i.e. the mixture of particle-shaped materials, is to be fundamentally avoided. The through-flow of the device overall is therefore to be improved. 
     This object is attained according to the invention by means of the fact that in order to support a transportation of the mixture from the inlet cell to the outlet cell and/or a turbulence of the mixture in the process chamber, the inflow floor comprises first unevenness and/or at least at times a second fluidisation agent, in particular in the form of overheated vapour, can be fed at least into the inlet cell essentially parallel to the inflow floor by means of first nozzles, and/or first flow guidance members are provided above the inflow floor and/or second flow guidance members are provided below the inflow floor. 
     Here it can be provided that in the inlet cell, a mixing of dried and damp parts of the mixture takes place according to a type of stirrer tank, in the intermediate cells a flow guidance according to a type of flow pipe is realised in order to avoid the mixing of damp parts with dried parts of the mixture, and no fluidisation agent penetrates into the outlet cell through the inflow floor. 
     It is also recommended that the feeding installation for the mixture is connected with the container in the area of the outlet cell, preferably in the centre of the height of the inlet cell and/or at the level of the upper outlets of the fluidised bed. 
     Here it can be provided that the feeding installation guides the loosened mixture to the inlet cell via a mechanical transport means, preferably by means of mechanically acting paddles, in particular of a screw conveyor, and/or pre-warmed and/or via air transport, preferably by adding a third fluidisation agent, in particular in the form of overheated vapour through vapour injection into the screw conveyor. 
     It is preferred that the area of the inflow floor is larger in the inlet cell, preferably doubly the size, of the respective area of the inflow floor of the intermediate cells. 
     It is further preferred that the inflow floor comprises first openings in the inlet cell and in the intermediate cells, the opening relationship of which preferably decreases from the inlet cell in the direction of the outlet cell. 
     Devices according to the invention can be characterized by the fact that the inflow floor comprises the first unevenness in the form of deeper lying recesses and/or at least over the first quarter of the process chamber. 
     It is additionally recommended that the inflow floor points upwards on its edge facing towards the container, and otherwise runs essentially horizontally, wherein the edge is preferably equipped with first openings and/or first unevenness at least over the first quarter of the process chamber. 
     It can also be provided that the second fluidisation agent can be fed in with a pressure of at least 2 bar above the average pressure in the container and/or in the first quarter of the process chamber. 
     A screen for the heating installation can be provided, wherein preferably, the screen widens conically in the process chamber from top to bottom, the first nozzles extend between the screen and the inflow floor, and/or the screen comprises two openings and/or second unevenness, preferably in the form of deeper lying recesses. 
     It is also recommended that the wall between the outlet cell and the inlet cell extends up to the height of the inflow floor, and/or the walls between the inlet cell and a first intermediate cell, between the intermediate cells and between the first intermediate cell and the outlet cell, comprise a vertical distance to the inflow floor, in particular to the edge of the inflow floor. 
     It is preferred that the first flow guidance members are provided and/or adjustable between the first nozzles. 
     With the invention, it is further recommended that first second flow guidance members are provided in a torospherical head as part of a discharge guide vane of the ventilation installation, wherein preferably, the ventilation installation comprises a bellows within the discharge guide vane. 
     Preferred devices according to the invention are characterized by the fact that second second flow guidance members are provided in a torospherical head and/or are attached and/or adjustable on the discharge guide vane, preferably in each case pivoted around a pivot axis which is essentially vertical to the inflow floor or which extends vertically. 
     It is equally preferred that third second flow guidance members are attached and/or adjustable on inflow floor supporting members, preferably in each case pivoted around a pivot axis which is essentially parallel to the inflow floor or which extends horizontally. 
     According to the invention, it is also recommended that the number, alignment and/or arrangement of the first and/or second openings, the first and/or second unevenness, the first nozzles and/or the first and/or second flow guidance members is or are determined or changeable for the targeted appliance to the mixture with horizontal transport impulses in the direction of the outlet cell and/or turbulence impulses. 
     Here it can be provided that the alignment, in particular of the second second and/or third second flow guidance members, and/or the infeed from the second fluidisation agent to the first nozzles via an adjustment installation which can be operated from outside of the container, is changeable. 
    
    
     
       BRIEF DESCRIPTION OF THE SEVERAL VIEWS OF THE DRAWINGS 
       Further features and advantages of the invention arise from the following description, in which exemplary embodiments of the invention are explained in detail with reference to schematic drawings, in which: 
         FIG. 1 a    shows a perspective side view of a first exemplary embodiment of a device according to the invention; 
         FIG. 1 b    shows a schematic view of the device as shown in  FIG. 1   a;    
         FIG. 2  shows a longitudinal profile view of a feeding installation of the device as shown in  FIG. 1   a;    
         FIGS. 3 a , 3 b , and 3 c    show perspective partial views of the floor area of the device as shown in  FIG. 1   a;    
         FIGS. 4 a  and 4 b    show perspective partial views of the underside and upper side of a perforated sheet with scales for the device as shown in  FIGS. 1 a    and  1   b;    
         FIG. 5 a    shows a top view onto a floor area of a second exemplary embodiment of the device according to the invention with a discharge guide vane; 
         FIG. 5 b    shows a partial profile view of the floor area as shown in  FIG. 5   a;    
         FIG. 5 c    shows a view as shown in  FIG. 5 a    with additional, adjustable guide plates; 
         FIG. 5 d    shows a perspective partial view of the floor area as shown in  FIG. 5   c;    
         FIG. 6  shows a perspective view of the floor area of a third exemplary embodiment of the device according to the invention; and 
         FIGS. 7 a  and 7 b    show profile views through an inflow floor of the device as shown in  FIGS. 5 a   - 5   d.    
     
    
    
     DETAILED DESCRIPTION OF THE INVENTION 
       FIGS. 1 a  and 1 b    show a device according to the invention in the form of a fluidised bed vaporisation dryer  1000  with a feeding installation  1  for feeding products to be dried in the form of pressed pulp into a container  21 , which comprises a process chamber  23  in the area of its floor  22 . More precisely, the pulp is introduced into the process chamber  23  in which a fluidised bed  2  can be generated by charging overheated vapour through an inflow floor  24  in order to dry the pulp. Dried pulp can then be discharged from the container  21  by means of a discharge installation  3 , while particles which are carried along by the vapour from the process chamber  23  are separated within the container  21 , e.g. by means of a dust collector  4  above the fluidised bed  2 . The vapour freed of particles then partially reaches a vapour outlet  5  and partially a heating installation, in order to again be heated by means of a heater  6 , so that it can again be guided to the process chamber  23  through the inflow floor  24  with the interposition of a ventilation installation or a bellows  7 . As a result, a closed circuit for part of the vapour is provided. 
     Above the inflow floor  24 , walls  25  are arranged in a vertical alignment and essentially extend 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 chamber  23 . The walls  25  can reach down to the inflow floor  24 , but must then comprise openings or form an empty space between themselves and the inflow floor  24 . The cells formed by the walls  25  are open above, so that the vapour which serves as a first or second fluidisation agents  20   a ,  20   b  flow from bottom to top through the cells and carry material or particles to be treated, and if necessary transport them to a subordinate cell. 
     A first swirl is generated between the process chamber  23  and an extension cone  26  using impellers  29  above the walls  25 . As a result, the vertical flow of the vapour is deflected in the process chamber  23  in order to lead to a swirl flow in the extension cone  26 . Through the application of the swirl, the vapour together with the particles carried along with it is thus directed onto the wall of the container  21 , as a result of which the particles are decelerated, namely through wall friction, so that the decelerated particles then fall back along the wall into the process chamber  23 . 
     In the extension cone  26 , a reduction of the flow velocity occurs, which leads to an expansion of the vapour flow out of the cells. The extension cone  26  and an upper area  27  which is adjacent to said cone comprise no fixtures, and are thus an empty space in which while separating the particles the flows from the cells split and at least partially mix with each other. In order to transmit kinetic energy for the purpose of improving the mixture of flow layers with different thermal states, overheated vapour is blown into the upper area  27  via nozzles  34  and  35 . Separated particles are vertically conducted away along the wall in the extension cone  26  via ribs  36 , while the remainder of the particles together with the vapour enters a central separator in the form of a dust collector  4  in the lid  28  of the container. The ribs  36  here ensure a deceleration of the particles, which facilitates separation. The inner contour of the lid  28  is formed to deflect the flow. 
     Following the preliminary separation of particles in the empty space, smaller particles are separated by the inflow of the particle-vapour mixture into the dust collector  4 . The separated dust then enters an outlet cell  202  in the process chamber  23  via a dust cyclone  33 . 
     The feeding installation  1  enters the pulp to be treated into a first cell in the process chamber  23 , which is referred to below as the inlet cell  201 . The first or second fluidisation agents  20   a ,  20   b  do not, or only to a low degree, flow through the last cell equipped with the discharge installation  3  or outlet cell  202 , so that material entering into this cell  202  from above or on the inflow floor  24  lands in the floor area and can be removed via the discharge installation  3 , in particular such as that described in EP 2 146 167 B1. One or more intermediate cells  203  are positioned between the inlet cell  201  and the outlet cell  202 . In order to guarantee an even and constant fluidisation in the fluidised bed  2 , a process control can be used in accordance with EP 2 457 649 A1. 
     The feeding installation  1  is arranged in such a manner that it enters the pulp into the centre of the inlet cell  201 , at the level of the upper extensions of the fluidised bed  2 , which provides a lower installation site than with known devices. Additionally, it ensures that the pulp reaches the inlet cell  201  in a loosened and pre-heated state. For this purpose, it comprises a screw conveyor  400  with rotatable paddles  401 , as is shown in  FIG. 2 . In a feed area  402 , wet product, i.e. pulp to be dried, is added and directly treated with vapour from a first vapour feed  403 , and lumpy pulp is shredded by the mechanical energy input of the rotating paddles  401 . By rotating the paddles  401 , the pulp is also transported, however, and during transport is again treated with vapour from the second vapour feeds  404  and  405 . Through a suitable feed of steam, in the feed area  402  and during the subsequent shredding of lumpy pulp during transport, not only a heating of the pulp under water vapour occurs, but also at the same time turbulences are created, which is why a swirl is indeed also present there. Through the mechanical transportation by means of the mechanically acting paddles  401  and the pre-heating and air transport by means of the vapour feed  403 - 405 , the pulp reaches the process chamber  23  in a loosened and pre-heated state, which counteracts the formation of further lumps of pulp in the process chamber  23 . This enables a blockage of openings, gaps and similar to be avoided in the process chamber  23 , and secures a continuous transport of 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 introduced into the inlet cell  201  in a pre-heated and loosened state together with an excess quantity of steam, which immediately escapes upwards in the container  21 . The inlet cell  201  preferably covers over a larger area of the inflow floor  24  than each of the remaining cells, so that the pulp which has been fed in is brought into contact with an enlarged floor area with an enlarge quantity of steam, which also again counteracts the formation of lumps. In the inlet cell  201 , the pulp is namely still in its dampest state. A doubling of the size of the inlet cell  201  as opposed to the remaining cells has been shown to be particularly advantageous. 
     The flow from the inlet cell  201  to the outlet cell  202  is conditioned via a plurality of flow guidance members in order to further counteract the formation of lumps, as is described below with reference to  FIGS. 3 a  to 3 c , 4 a    and  4   b.    
     A screen  300 , also referred to hereinafter as an apron  300 , limits the ring-shaped process chamber  23  inwards. Between the apron  300  and the heater  6 , a vapour feed pipe  301  opens out above the inflow floor  24 , in order to guide vapour in a transverse direction across the inflow floor  24  via first nozzles  302  to at least one first quarter of the cells, as is shown in  FIG. 3 a   . This leads to a flow from the apron  300  radially to the wall of the container  21 , see flow lines  311 . Here, the vapour feed pipe  301  is arranged in the ring section of the inlet cell  201 , in order to ensure additional loosening with transverse directed steam, since there, the pulp also still carries the largest water quantity with it. Additionally, guide plates  303  are arranged between the first nozzles  302  in order to guarantee the transverse flow in each cell. The first nozzles  302  and the guide plates  303  are thus flow guidance members, wherein the vapour feed via the first nozzles  302  additionally leads to a heating and water evaporation from the pulp. 
     The inflow floor  24  and the apron  300  are designed with perforated sheets  304   a ,  304   b  and  305 , in order to guide the flow in a targeted way. All perforated sheets  304   a ,  304   b  and  305  here comprise holes for a penetration of overheated steam, while some of these perforated sheets, namely perforated sheets  304   b  and  305 , also comprise unevenness to guide said steam. As a result, the perforated sheets  305  of the apron  300  support a flow along the apron down to the inflow floor  24 , see the flow lines  310 , while the perforated sheets  304   b  support a flow along the flow lines  312  as an extension of the flow line  311 , so that a circular flow is enforced in the fluidised bed  2  essentially vertical to the inflow floor  24 , namely from the apron  300  via the inflow floor  24  back to the apron  300 . A further circular flow of the same rotational direction is enforced by perforated sheets (not shown) with unevenness in a floor extension which inclines upwards in the direction of the open ends of the cells, which represents an edge  307  which is in contact with the wall of the container  21  as shown in  FIG. 3 b   , namely along the inflow floor  24 , the edge  307  and the wall back to the inflow floor  24 . 
     Between the perforated sheet  304   b  and the edge  307  and thus between the two vertical circular flows in the same direction, a transportation area  306  runs which secures a horizontal circular path from the inlet cell  201  to the outlet cell  202  to convey the pulp in the process chamber  23 . According to the invention, therefore, an uninterrupted transportation path of the pulp in the process chamber  23  is provided by applying horizontal transport impulses in the direction of the discharge area, see flow lines  313 , while at least via the first quarter of the process chamber  23  a swirl is enforced with  2  swirls per cell circulating in the same direction, which homogenises the material flow in the process chamber  23  and improves the drying. 
     The nozzles  302 , guide plates  303  and perforated sheets  304   a ,  304   b  and  305 , can differ for each cell in order to take into account the progressive drying of the pulp. Thus the opening relationship of the perforated sheets  304   a  to  305  decreases in size from the inlet cell  201  to the outlet cell  202 . 
       FIGS. 4 a  and 4 b    show as an example a perforated sheet  304   b  which comprises a plurality of second openings  341 , also referred to hereinafter as holes  341 , and second unevenness  342 , also referred to hereinafter as scales  342 . More precisely,  FIG. 4 a    shows an underside  343  on which the perforated sheet  403   b  comprises one large opening for overheated vapour respectively in the area of the scales  342 , which leads into an unevenness on the upper side  304 , which is shown in  FIG. 4 b   , and thus can apply a direction impulse to the overheated steam. Many different geometric designs are possible; equally, it is possible that the flow lines  312  shown in  FIGS. 3 b  and 3 c    do not run precisely radially, but instead are inclined in the direction of the flow lines  313  in order to thus serve a transportation of the pulp. 
     The ventilator  7 , which as shown in  FIG. 1 a    is provided within a torospherical head  22   a  of the floor  22 , serves to convey overheated vapour current from the heater  6 , which is frequently also described as exhaust vapour, and which enables the fluidisation of the fluidised bed  2 . The need for exhaust vapour current or drying exhaust vapour in the individual cells of the process chamber  23  differs, since the pulp to be dried loses humidity from the inlet cell  201  in the direction of the outlet cell  202 . Since via the bellows  7  the exhaust vapour current enters the individual cells via the inflow floor  24  essentially parallel, the exhaust vapours are distributed according to the pressure loss which arises when the individual cells are subjected to the flow. This pressure loss is predominantly influenced by the pressure loss of the inflow floor  24  and the mass of the fluidised bed  2  located above it. 
     The pulp must not only be dried in the process chamber  21 , but for drying purposes, it must at the same time also be transported from the inlet cell  201  to the outlet cell  202 . With the exemplary embodiment shown in  FIGS. 3 a -3 d   , through targeted selection of the number, alignment and/or arrangement of the holes  341 , the scales  342 , the nozzles  302  and the guide plates  303 , both the transportation and the swirl, and thus the drying, can be influenced here. The holes  341  and scales  342  in the perforated sheets  304   a ,  304   b  and  305 , as well as the guide plates  303 , are firmly installed in the fluidised bed vaporisation dryer  1000 . An alternative structure in this regard is now described below with reference to  FIGS. 5 a   - 5   d.    
       FIG. 5 a    shows a top view onto a torospherical head  22 ′ a  of a second exemplary embodiment of a fluidised bed vaporisation dryer according to the invention, in which in addition to a bellows  7 ′, a plurality of guide plates  501  of a discharge guide vane  500  are arranged, which serve to condition the flow in the torospherical head  22 ′ a , namely to guide said flow radially outwards, as is shown by the flow paths A in  FIG. 5 a   . The discharge guide vane  500  comprises additional guide plates  502  and  503  with different orientations, as is best shown in  FIG. 5 b   , which shows a partial perspective of the area below an inflow floor  24 ′ within a floor  22 ′ with the torospherical head  22 ′ a . The guide plates  501 ,  502 ,  503  may also be referred to as the first second flow guidance members  501 ,  502 ,  503 . In  FIG. 5 b   , an inflow floor supporting member  24 ′ a  is also shown here, along which the flow conditioned by the  500  rises according to the flow path B, and either through openings in the essentially horizontally running inflow floor  24 ′ or in an edge  240 ′ which is inclined towards the wall of the floor  22 ′ also reaches the process chamber, or is circulated in the area of the floor  22 ′ below the inflow floor  24 ′. 
     It was discovered in a surprising way that the swirl flow enforced by the discharge guide vane  500  below the inflow floor  24 ′ in the process chamber has a considerable influence on the transportation of solid materials. In order to be able to influence this transportation of solid materials in a targeted manner, it is recommended according to the invention that adjustable guide plates  600  be provided in the area of the floor  22 ′, in particular through into the torospherical head  22 ′ a , as shown in  FIGS. 5 c  and 5 d   . Each adjustable guide plate  600  is here pivotable around a pivot axis  601  via and adjustment installation  602 . The adjustable guide plates  600  may also be referred to as the second flow guidance members  600 . The adjustment installation  602  can be either manually adjusted in cases when the fluidised bed vaporization dryer according to the invention is opened, or also from outside the fluidised bed vaporization dryer, even when in drying mode. 
     As an alternative to the adjustable guide plates  600 , or even in addition to these, further adjustable guide plates  700  can be arranged directly below the inflow floor. This is shown in  FIG. 6  in a perspective view, according to which the adjustable guide plates  700  in the area of the inflow floor supporting members  24 ″ b  are essentially arranged in parallel to the inflow floor  24 ″, such that they are pivotable around a pivot axis  701 , as is shown by the arrow F. The inflow floor supporting members  24 ″ b  are for their part supported by the inflow floor supporting members  24 ″ a , which are affixed to the wall of the floor. 
     The method of functioning of the adjustable guide plates  600  and  700  will now be explained with reference to  FIGS. 7 a  and 7 b   . In  FIGS. 7 a  and 7 b   , the flow path G and G′ can namely be seen through the individual openings in an inflow floor  24 ′″, which has an influence on the solid materials transportation path H or H′ within the fluidised bed  2 ′″. Depending on the orientation of the flow path G and G′, different effects occur. Thus, a flow path G as shown in  FIG. 7 a    leads to increased transportation within the fluidised bed  2 ′″ due to its lesser inclination to the inflow floor  24 ′″, while a flow path G′ as shown in  FIG. 7 b    penetrates the inflow floor  24 ′″ more steeply, and thus ensures an increased swirl in the fluidised bed  2 ′″. 
     Naturally, the adjustable guide plates  600  and  700  can be combined with special perforated sheet designs, as well as guide plates above the inflow floor. Such a combination enables a precise adjustment of the flow required for the respective pulp for the purpose of optimising the 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 required for the realisation of the invention in its different embodiments. 
     LIST OF REFERENCE NUMERALS 
     
         
           1  Feeding installation 
           2 ,  2 ′″ Fluidised bed 
           3  Discharge installation 
           4  Dust collector 
           5  Vapour outlet 
           6  Heater 
           7 ,  7 ′ Bellows 
           21  Container 
           22 ,  22 ′ Floor 
           22   a ,  22 ′ a  Torospherical head 
           23  Process chamber 
           24 ,  24 ′,  24 ″,  24 ′″ Inflow floor 
           24 ′ a ,  24 ″ a ,  24 ″ b  Inflow floor supporting member 
           25  Wall 
           26  Extension cone 
           27  Upper area 
           28  Lid 
           29  Impeller 
           33  Dust cyclone 
           34  Nozzle 
           35  Nozzle 
           36  Rib 
           201  Inlet cell 
           202  Outlet cell 
           240 ′ Edge 
           300  Apron 
           302  Nozzle 
           303  Guide plate 
           304   a  Perforated sheet 
           304   b  Perforated sheet 
           305  Perforated sheet 
           306  Transportation area 
           307  Edge 
           310 - 313  Flow line 
           341  Hole 
           342  Scale 
           343  Underside 
           344  Upper side 
           400  Screw conveyor 
           401  Paddle 
           402  Feed area 
           403 - 405  Vapour feed 
           406  Docking area 
           500  Discharge guide vane 
           501 - 503  Guide plate 
           600  Adjustable guide plate 
           601  Pivot axis 
           602  Adjustment installation 
           700  Adjustable guide plate 
           701  Pivot axis 
           1000  Fluidised bed vaporisation dryer 
         A Flow path 
         B Flow path 
         C Flow path 
         D Flow path 
         E Pivot direction 
         F Pivot direction 
         G. G′ Flow path 
         H. H′ Solid material flow path