HU196717B - Apparatus and method for fluidization contacting materials - Google Patents

Abstract

Device for bringing substances, especially dispersed substances and/or solid-liquid dispersions and/or liquid substances into contact with each other and/or with gases with the aid of a rotary fluidisation system, especially for performing drying, granulation and dressing (coating) operations. This device is characterised in that the said layer support 7 comprises, between the vertical geometric axis x of the device and the gap 41 between the bottom of the support 7 and the casing, at least one intermediate annular slot 42, 43 and a conical part 5 concentric with this geometric axis and widening downwards and in that the said layer support 7, or at least its central conical part, can be raised and lowered. <IMAGE>

Description

FIELD OF THE INVENTION The present invention relates to apparatus for rotary fluidizing contact of various materials, such as solid dispersions, materials, liquids, and solid-liquid dispersions, with one another and / or gas, in particular for carrying out drying, granulating and coating of particles with a material layer. The invention also relates to a process for rotating fluidized bed material by means of the apparatus. For solid dispersions, on materials eg. powders, granular left glazes, vegetable (seed) seeds and the like; suspensions, pastes, filter or centrifugal moisturizers, etc. valid.

Solid dispersions of liquids or liquids. There are a number of technico-chemical processes for contacting with gas, namely stationary, mechanically transported layered (e.g., conveyor belt), sliding, mechanical mixing, rolling, vibrating, fluidizing, geyser, floating, pneumatic and fluidized, (Blickle, T., Ormós, Z .: Energy Management 13.49 (1972)).

Közül Among the processes listed above, the fluidization process and / or the fluidization process have been used more and more extensively in recent decades. fluidization apparatus for performing primarily physical operations (e.g., drying, granulating, coating, etc.) in which particulate matter or particles are used to accomplish the task. solid-liquid dispersions and liquids (e.g. solutions) with each other and / or with gas are uniform and intensive.

Solid-liquid dispersions, mainly for removing the moisture content of high-moisture, small-particle, paste-like materials, have been developed by the dry-fluidizing drying process known from U.S. Patent No. 167,659, which comprises dispensing the material to be dried . As a result of the fluidized motion of the charge particles and the mechanical agitation of the layer, the wet material covers the surface of the charge particles and the drying process is predominantly carried out in a thin layer on the surface of the particles. To a lesser extent, the material to be dried forms individual lumps, but these are continuously dispersed as the layers move. After reaching a certain moisture content, small particles of the dried material are detached from the surface of the charge particles and are exited by the gas stream from the fluidized bed. Post-drying one or more of the almost completely dry material leaving the charged fluidized bed. takes place in a vortex layer formed by tangential gas introduction. The dry product is separated from the gas stream by a cyclone and, if necessary, a post-dust remover can be connected to the system. The advantage of this process is that the contact of the material to be dried with the drying medium (air) on the surface of relatively small (in general, 1 mm mean diameter) inert particles in the fluidized bed is very intense, but the disintegration forces due to the relatively small particle size in some cases, they do not reach the degree required for the dry powder to scrub off the surface of the inert particle and to escape from the layer by a gas stream.

Hungarian Patent No. 174,030 also discloses a geyser-type apparatus and method of operation in the form of powdery, particulate, particulate materials, solutions, suspensions, paste-like materials. contact with gas or. which consists of a vertical shaft conveyor screw and a vertical axis insertion tube and, if necessary, a vertical axis mixer. The bottom of the tank is perforated and air is introduced into the tank. the container has a lateral air supply. This apparatus and method can be advantageously used for solving certain drying tasks, such as ground paprika, fodder corn, cubes of vegetables (e.g. carrots, celery) and the like. However, such geyser systems generally have the disadvantage that, on the one hand, gas distribution is not nearly as smooth as in fluidized systems, and, on the other hand, due to the relatively low particle movement in the annular sliding layer, there is a risk of adhesion application options. Thus, for example, the use of geyser-based equipment is often out of the question for granulation or coating applications.

Fluid For more than two decades, fluidization-spraying techniques have been used more and more extensively to carry out the granulation and coating process (Ormós, Z: Fluidized Granulation, Journal of Hungarian Chemists, 5, 511/1 975). The essence of this is to spray a liquid, solution, suspension or molten liquid containing a solid which is suitable for the operation to the gas-fluidized layer of the solid base materials. In the production of granules, the bt spray liquid generally contains a binder: - and the solid particles moistened with the liquid gradually form agglomerates held together by the liquid binding bridges. After evaporation of the solvent content of the granulating fluid, agglomerates form solid particles with solid bonds. In the case of film coating or scaling coatings, the coating material is generally contained in the atomised liquid or in suspension, and the solid coating on the surface of the particles or cores fluidized with the warm air is the solvent or solvent. is formed by evaporation of the suspending agent e.

Fluidization-spray granulation and coating can be carried out in both batch and continuous modes (Hungarian Patent Nos. 168,255 and 168,675).

In a fluidized bed, very good snow transfer between the particle set and the gas can be achieved, and thus devices of this type can generally be operated efficiently, with high performance, but in other respects have their drawbacks.

One of the basic conditions for granulation and coating, intensive particle movement in this process, is provided by the gas flowing through the layer. In case of inappropriate particle movement, uncontrolled particle growth and clot formation occurs in the layer, which in some cases can lead to malfunction. For materials that are poorly fluidizable, mechanical mixing or vibration is often required as an auxiliary process.

It is also a disadvantage that the process, even if the particles are properly moved, is characterized by loose contact between the solid particles in the fluidized bed.

coatings have a loose, porous structure and generally have less strength than required for catalysts, adsorbents or coated plant seeds. A further disadvantage is that the particle shape is quite different from the generally favorable spherical shape.

For the production of particulate solids and coated products, the so-called "solids" is widely used. rolling machine, the most commonly used apparatus of which is a turntable, a turntable and a rotating pan (P. J. Sherrington, R. Oliver, Granulation, HEYDEN, London (1981), 60-86).

Coated dragees, e.g. in a rotating cauldron, they are prepared by alternately moistening (eg with water) the granules of the rolling stock and dipping or dipping. they melt or suspend on their surface. Here, the particulate layer is not relaxed by a gas stream, and thus, due to the compacting effect of the weight of the layer and the rolling motion, the solid particles deposited on the surface of the particles are stratified into approximately spherical compact agglomerates.

U.S. Pat. No. 3,141,792 also discloses a method for controlling or controlling the moisture of the granules. however, the heat transfer efficiency of such solutions is generally inadequate relative to the volume of the cauldron because the contact surface of the particles in the cauldron with the drying air is so small that the moisture introduced can only be removed over a relatively long period of time.

A further disadvantage is that the magnitude of the particle movement in the rolling device and hence the magnitude of the forces preventing the agglomerates from sticking together can only be varied within a narrow range of particles. Above a given speed (critical speed), the particles rise to such height in the device that they no longer return to the original circular path, like the discarded bodies, with the desired drop-down movement. At even higher speeds, the centrifugal force acting on the agglomerates can be so large that they rotate along a circular path with the device without being agitated relative to one another. Because there is only very limited scope for varying the shear forces that allow agglomerates to separate, smaller unit particles or more viscous wetting fluid will significantly reduce the performance of the device, since at higher speeds, unwanted agglomeration may be avoided by feeding the wetting fluid at a higher rate.

A process for coating granules, especially dragee cores and tablets, is known in the prior art, which comprises spraying a fluid containing coating material onto a set of granules forced to circulate rolling motion in a device formed by a solid disk rotated by a vertical axis and a body above it. , while warm air is introduced into the layer through the gap between the stationary and rotor parts or by means of a pipe from above. on the layer to dry the coated particles. The apparatus is in fact reminiscent of a draining pan or chalice whose axis is vertical, cut at its lower part and secured at its upper part. The embossed (internally concave) rotating disc provides centrifugal rolling motion for the material to be coated.

U.S. Pat. No. 3,711,319 discloses a method for coating particulate and dusty materials, wherein the material to be coated is a vertical, cylindrical, extending upper portion of a device mounted horizontally on a vertical axis, flat or upwardly curved (saucer). is formed by circulating the disk, partly by rotating the disk, partly by introducing air through a narrow annular slot between the periphery of the circular disk and the wall of the cylindrical body, and spraying the coating solution from the top downwards from the apparatus. it is removed through an aperture approximately in the same plane as the rotating disk.

The last two procedures respectively. thus, the advantages of the rolling layer (turntable, turntable) and fluidization solutions can be partially combined by using a device, since the particle to be coated performs a centrifugal rolling motion, while the space between the stationary device body and the rotating disk can be contacted with gas (air) . The disadvantage of this type of equipment, however, is that the contact between the air introduced in the narrow annular gap and the particle stack is not nearly as uniform and intense as that obtained with fluidization equipment. In addition, the problem is that once the air passage in the gap is stopped, the powdery particulate material will fall into the space below the disc, which can cause a lot of inconvenience and there is no reference in U.S. Patent No. 3,671,296 to remove the finished product. It is likely that the coated dragee core or the coated dragee nucleus. tablets are removed from the body of the dragee-like pan by either manual force or by a suction-powered pneumatic conveyor. In U.S. Patent No. 3,711,319, the complete removal of particulate particulate matter, in particular, when discharging to the side of the device in the plane of the rotating disk, does not appear to be clearly ensured.

SUMMARY OF THE INVENTION It is an object of the present invention to provide a rotary fluidization apparatus for contacting various dispersions, in particular solid-liquid dispersions, and liquids with one another and / or with a gas, which provides a uniform or substantially uniform fluidizing gas transferring through a rotating material. and thus provides good heat and material transfer conditions with relatively low ventilation energy input. It is a further object of the present invention to provide a variety of different materials, particularly for drying, granulating, coating, etc., for the purpose of contacting the aries. The removal of the final product resulting from the operations, the grain aggregate, shall be simple and complete. Finally, it is an object of the present invention to provide a method that enables the optimization of material contact operations performed in the apparatus, both in terms of technology and economy (energy use).

The present invention is based on the discovery that if, in addition to the gap between the rotating bed support and the device body wall, the washer has a further annular slot (s) and a central conical insert which is movable up and down, on the other hand, removal of the finished product can be accomplished in the most favorable way by eliminating it at the bottom.

Based on these findings, the object of the present invention has been solved by an apparatus having a housing, a rotatable layer support washer therein, a gas flow gap between the inner surface of the housing wall and the layer support, a gas supply arrow and a feed material; a device for removing the end product, the apparatus having the layer support having at least one intermediate ring gap between the vertical central geometric axis of the device and the peripheral slot and a concentric top-down, preferably tapered body with this geometric axis and that the retaining pad, or at least its central body, can be raised and lowered. Preferably, the liner is at least partially housed in a downwardly tapered chamber of the housing, and the housing has a cylindrical chamber beneath the liner, into which a gas inlet port terminates, and a downwardly opening cross-sectional flow within the cylindrical chamber. furthermore, if the lower part of the housing is formed as a desiccating chamber having a descending downward cross-section, preferably a tapered material discharge port. Generally, a vibrator is attached to the wall of the material discharge chamber, preferably outside. According to a further feature of the invention, one or more, preferably two to four, gas inlet ports are provided in the housing above the bed support, in which it is formed by a fluidized roller-rotating material assembly, preferably a cylindrical chamber, in this case. it is expedient that the inlet stumps extend into the chamber in the direction of the inlet of the gas, preferably their longitudinal geometric central axis is at an angle of approximately 120-150 ° with the drawn radius. The device has a liquid feed device located above the layer in the housing, preferably a two-fluid liquid atomiser, and a screw feeding device for feeding the powder into the housing, preferably a powder, granular material or paste.

Another preferred embodiment of the device is that the bed support washer or at least its central conical body is connected to a rotatable vertical axis having a lifting device at its lower end, preferably a hydraulic cylinder. In this case, it is preferable that the shaft is driven by a fixed sprocket, a motor-connected sprocket, a spring-mounted intermediate auxiliary sprocket and a chain mechanism.

In a further embodiment, the liner is provided with horizontal or substantially horizontal, orifice discs spaced apart from each other and spaced apart from each other, and spaced apart, between the discs and the conical body to form intermittent annular gas-fed gaps. the diameter of the motherboard is smaller than the diameter of the disk below and the diameter of the bottom disk is larger than the diameter of the disk above each. Typically, there is a peripheral gas-permeable gap between the outer rim of the lowest disc and the inner wall surface of the conical chamber of the housing. In each of the discs, the through-openings are distributed on a dividing circle, the dividing circuits above each other being offset relative to one another, and spacer rings are provided between the discs and the conical body.

Another embodiment of the device according to the invention is characterized in that the laminate washer has a funnel-like body formed by a series of overlapping and spaced apart, downwardly tapered, annular conical plates that reduce the central conical body from below to below. - surrounded, formed with and rotatably connected thereto, with a removable connection thereto, the widest - external - gas inlet gap being the upper annular plate and the inner surface of the housing wall, the intermediate annular plate and the bottom of the housing * the inner surface, the intermediate annular gas inlet slots being formed between the frustoconical plates. The conical annular plates are secured to each other by spacer screws, preferably to allow adjustment of the spacing between them. This device has a shoulder formed by an annular plate for supporting the funnel body inside the housing, and only the central conical body is rigidly connected to the lift-lower rotary axis. It is expedient to have outwardly projecting ribs in the lower region of the outer surface of the central conical body, on which the funnel body fits into the lower edge of the lowest conical annular plate, and if the conical plates of the conical body except for the uppermost plate: They are shaped like a labyrinth and form a labyrinthine gas outlet.

In all of the embodiments, it may be advantageous for the gentle particle movement to have a central conical body tip curved and / or a convex external surface.

The apparatus method of the present invention consists in reducing the amount of gas resulting from the product of the minimum fluidization gas velocity of the material in the layer through the joints of the rotating bed liner and, where appropriate, through the nipples over the liner. into the layer. As a result of this action, the granules roll over each other in a layer, creating an intense rotary-rolling motion state that greatly enhances the efficiency of material contact. It is advisable to inject up to 30% of the total amount of gas fed from side to side, and, if a solid dispersion material forming a movable layer is preferably dispersed in a liquid, in particular solvent and / or solution, in the form of droplets having an average droplet size of 0.02-0.10 mm for carrying out a semi-granulation and / or coating and / or adsorbing operation; / or a suspension is administered.

The process is a preferred embodiment! In order to carry out a stuffed drying operation in accordance with the method of this invention, the layer in rotary fluidizing motion is formed of inert particles having an average diameter of 3 µm, e.g., spherical or spherical, or liquid balls to be dried. solids-liquid dispersions, pastes or the like and other materials to be dried are preferably fed to the layer by means of a screw feeder, while in the layer, in order to pneumatically remove the dry product, an amount of gas, usually air, is it should be less than the minimum fluidization gas velocity of the inert fill, but greater than the floating or falling velocity of the dried material particles.

The procedure is another implementation! is characterized by the fact that - especially powdery and / or granular material (s) - spherical or close-spherical granules or multilayer granules or coated granular materials, e.g. for the production of cores, the step of forming or / and increasing the particle size by layering is carried out in several, preferably three, sub-operations and is performed sequentially over time, periodically as necessary in three work stages, preferably in a first step providing optimum conditions for the sub-processes. applying powdered material and / or dispersed granulating fluid to the layer, preferably by spraying, while maintaining an amount and temperature of gas, usually air, through the layer to ensure that the theoretically usable amount of heat introduced by the desiccant is less than the amount of heat needed to evaporate it, in the second step without the intake of dust and liquid in the intense rotating-rolling layer 1, up to the side fed, preferably at room temperature, by spheronizing and compacting the wet granules and, in a third step, reintroducing hot gas from below into the layer through a rotating bed liner, thereby drying and compacting the wet layer onto the surface of the granules.

This most recent embodiment of the process thus relates to the production of spherical or near-spherical shaped particles of powdery material (s), where appropriate high-strength molded materials and coated granular products, the process of which is to interrupt the process of layering the granules. and providing optimum conditions for the subprocesses in a well-controllable rotary fluidization moving bed by heat transfer through the gas passing through the bed and by controlling the magnitude of the forces acting on the particles (gas flow through the chamber wall and centrifugal force). In accordance with the sub-processes of pelletization, the powder to be processed is layered on the particles in the fluidized bed in three successive and periodically repeating stages.

In the first phase, the material to be processed is applied to the surface of the granules at a moisture content (meaning the outer surface of the granules) large enough to be practically lossless (without powder application) but less than the moisture content the particles would stick together. Since the magnitude of the shear forces to ensure the granules separation variable supply flow of gas over a wide range through the washer rotational speed and the chamber wall, and therefore is small even in case of eye lenses, or viscous dampening / 'possibility of grain growth in terms ked- ³ · ve2Ő relatively high to maintain moisture. The humidity is controlled via the rotating washer and the hot gas (preferably air) introduced between the washer and the chamber wall.

In order to ensure proper strength and shape, the second stage is emphasized, during which the applied and not yet solidified wet layer is formed and compacted by maintaining the intense rotary-rolling motion of the granules. The third stage is drying the product.

Thus, in the first of the periodically repeated steps, in the implementation of the process detailed above, powder and / or liquid is added to the rotating fluidization layer of the granules, with rotation of the washer and introduction of drying air, to achieve a varying moisture content. Due to the intense particle movement, the solid particles introduced into the device are evenly distributed over the surface of the particles of the fluorinated layer without adhering. In this phase, the amount of heat introduced by the drying air is less than that required to evaporate the total amount of moisture introduced by the spray liquid, i.e., the application of the solid particles to the surface of the granules is carried out in a wetted layer.

In the second stage, the layered materials are compacted. During this process, the addition of powder and / or wetting fluid and the introduction of the drying air are stopped while rotating the washer and guiding the gas flow through the wall of the can to force the particles into a rotating spiral path in the apparatus. In the method, the wet particles contact the rotating washer over a relatively large surface area and thus obtain a very good forming and compacting effect in the device.

In the third step, hot air is reintroduced through the washer, and between the fluidization chamber wall and the washer, and the wet layer applied and compacted to the surface of the granules is fixed by drying.

The invention will now be described in more detail with reference to the accompanying drawings, which show some preferred embodiments of the apparatus. 1 is a schematic vertical sectional view of an embodiment of the apparatus, FIGS. Figures 1 to 5 show further preferred embodiments of the layer retaining pad according to the invention, also in schematic vertical axis view.

The apparatus according to the invention has a housing I with a vertical geometric center axis, the interior of which is divided into two spacer sections by the layer-bearing washer, which is designated by reference numeral 7. The house is partly cylindrical and partly conical. The washer 7, rigidly connected to the rotatable vertical axis 7, is located in an upwardly expanding truncated conical chamber 1. In this embodiment, the washer 7 comprises two gas discs 3, 4 spaced apart by spaced -51 apart by gas-perforated openings 9 and 10, and a conical body 5 over which the lower surface is spaced b from the upper surface of the upper disk 4 stretches. The spacings a, b are secured by spacer rings 6 between the discs 3 and 4 and between the disc 4 and the conical body 5. The disc 3D, a larger diameter than the disk 4 d ₂ is the diameter of the seven pad base sheet _d3 diameter but lower than the dial 4 d ₂ is the diameter, i.e. the wheels and conical body geometric conditions gives ₃ <d ₂ <dj context It features. There is a gap 41 between the disc 3 and the conical wall of the chamber 1, but as a result of the structural and geometrical construction described above, two further concentric annular slots 42, 43 are formed in the liner 7 having diameters of the aforementioned d ₂ -d ₃ diameters, or substantially the same.

The shaft 2 can be raised / lowered vertically by means of a lifting device 8 connected to its lower end, such as a hydraulic cylinder, thereby adjusting the size of the annular gap 41 between the disc rim 3 and the inner surface of the chamber wall. It is possible to change the size of the slots 42.43 by adjusting the thickness of the spacer rings 6. The apertures 9 and 10 are disposed in a circular fashion, that is, along a dividing circle, and each row of apertures disposed off relative to one another in the discs 3 and 4.

Beneath the layer support washer 7 is a cylindrical chamber 11 of the housing I into which a gas inlet pipe 12 extends, the geometric longitudinal axis of which may be perpendicular to the vertical central geometric axis x of the apparatus. Inside the cylindrical chamber 11, a downwardly tapered flow-modifying insert 13 is disposed in the form of a tapered truncated cone, the function of which will be returned to.

A cylindrical chamber 14 is located above the conical chamber 1 containing the layer-bearing washer 7, the lower part of which, directly above the washer 7, penetrates the gas supply pipe nozzles 15. The insertion direction of the nozzles 15 preferably forms an angle of about 120-150 ° with the radius of this insertion point. Preferably, two to four pipe fittings 15 are used through which, e.g. in order to control the movement of the layer, the gas, which is guided in several directions, can be introduced into the material set 17, e.g. For discharge of gas from the apparatus (arrow f) is provided a manifold 16 which protrudes from the conical cover 24.

Between the aforesaid lifting device 8 for moving the shaft 2 and the shaft 2, a sole bearing 18 is mounted, and the shaft 2 is also embedded in further bearings 19, 20 and guided by the bearings 18-20. A motor (not shown), which is connected to the shaft 2 by means of the sprockets 21 and 22, the chain 44 and the spring-mounted auxiliary sprocket 23, can be used to rotate the shaft 2 and thus the washer 7. This connection makes it relatively easy to adjust to the vertical movements of the axis 2 (arrow c), which are otherwise relatively small, in practice generally not exceeding 10 ein.

In order to feed liquid substances such as solutions, suspensions into the layer 17, the chamber 14 is fitted with a two-fluid atomiser 25 mounted above the layer, through which the liquid can be sprayed onto the surface of the layer 17 when sprayed with gas. Fluidization also flows into the cylindrical chamber 14 above the layer 17! materials to be treated (contact), eg. solid dispersions such as dusts, etc., or e.g. a 26-screw dispenser for feeding paste-like solid-liquid dispersions in the present embodiment.

Connected to the lower part of the cylindrical chamber 11 is a downwardly tapered chamber 27, the lower end of which has a lateral outlet 28 for discharging the treated material, i.e. the end product, into which a container 29 is integrated. A vibrator 30 is connected to the outside of the conical wall of the chamber 27, which may facilitate the operation of material supply if necessary.

The operation of the device of Figure 1 is as follows:

the dispenser 26 feeds the solid disperse material into the chamber, the shaft 2 and thereby the bed support 7, and consequently the material 17 thereon, in a rotating and rolling motion, and the layer is fed to the nozzle 12 by a main gas stream; maintaining the fluid in a fluid state through the nozzles 15 via auxiliary gas streams fed as required by these arrows. In Figure 1, the path of the main gas flow is indicated by arrows g. It is well appreciated that the main gas stream through the nozzle 12 collides with the conical wall of the flow baffle 13, forcing the gas, usually air, to circulate, so that the gas flows upwardly across the lower edge of the flow modifier 13 and it passes through the annular gaps, on the other hand, through the openings 9, 10 and the annular gaps 42, 43 into the material set 17. The gas introduced through the nozzles (these arrows) flows into the layer 17 with a momentum. The total amount of gas introduced into the rotary rolling stock 17 is preferably selected to be less than the product of the minimum fluidization gas velocity multiplied by the maximum equipment cross-section corresponding to the diameter D _max , preferably up to 30% flow through the stubs 15 from the side, the rest from below through the layer 17. As described above, the main gas stream is distributed through the three slits 41, 42 and 43 into three ring-shaped streams, the proportion of which can be varied within wide limits by varying the size of the slits and the openings 9, 10.

The fluidized bed 17 in the rotating rolling motion is fed with the liquid by means of the two-fluid atomizer 25.

After the required processes (drying, coating, etc.) in the layer 17 have been carried out, the material is emptied by moving the still rotating layer support 7 fixed to the shaft 2 by means of the lifting mechanism 8, as a result of which the disc 3 and the gap 41 between the conical walls of chamber 1 must expand to such an extent that the vast majority of the material is discharged through this gap into the lower conical chamber 27, so that the extent of raising the washer 7 should be selected in consideration of this aspect. by rotating the shaft 2 for a short period of time, centrifugation 61 causes the rifugal force to drop into and pass through the gap 41. The granular end product can be removed from the chamber 27 via the orifice 28 by opening the closure member 29, which operation by operating Incidentally, the method of material removal is illustrated by the d arrowed h arrows.

Fig. 2 shows a preferred embodiment of the plywood carrier 7, which differs from that of Fig. 1 in that it has only a disc 3 and in that the tip of the conical body 31 is rounded, and the outside is slightly concave on the outside. In Figure 2, reference numerals and symbols already used in Figure 1 are used as appropriate.

The embodiment of Fig. 3 differs from that of Figs. 1 and 2, among other things, in that it is not only the cone body 36 that can be lifted-lowered in one member according to the double arrow c. The remainder of the washer 7 is comprised of inwardly inclined, overlapping, downwardly inclined, conical plates 32, 33 and 34 disposed spaced from each other and tapered together toward the lower portion of the upper, rounded conical body. They form a funnel-like body comprising annular slots 47, 48 and 53 located level above and below each other. These slots are formed by each of said plate members 32-34 and by the inner surface of the chamber 1 wall. The truncated conical ring members 32-34, which are of decreasing diameter from above to below, are secured to one another by means of spacer screws 35, and these spacers are also adjustable by means of these screws. An annular support shoulder 46 extends inwardly from the upper edge of the cylindrical chamber 11, on which a substantially tapered, conical body 51 formed by the discs 32-34 is supported, with its lowest plate 34 supported. This truncated conical bottom plate 34 has recesses of low depth forming grooves below which extend into the peripheral ribs 37 extending from the surface in the lower end region of the conical body 36, thereby forming a funnel 51 formed by the conical body 36 and the plates 32-34. a soluble connection can be established between the bodies, allowing them to be rotated together. In all other respects, the apparatus of Fig. 3 is the same as that of Fig. 1, therefore, the reference numerals and symbols used therein have been used mutatis mutandis in Fig. 3: The operation of the latter apparatus is essentially the same as that of Fig. the gas feeds into the rotary-rolling charge 17 in accordance with the arrows g through the annular concentric slots 47-49 and, additionally, through the stubs 15 (these arrows), and the final product is discharged through the enlarged slots 49 in accordance with the dotted arrow h. The deviation is essentially in the way of changing the size of the lowest slot 49. In Figure 3, the full line drawn state corresponds to the inoperative position of the apparatus, with plate 34 resting on shoulder 46, no slot at shoulder 46 and lowest frustoconical 34 the gap between the latter and the lateral surface of the conical body 36 having an opposite conical angle is also closed. The apparatus is operated by slightly raising the conical body 36 so that it also carries the funnel body 51 so that a gap 50 is formed between the plate 34 and the inner rim of the shoulder 46. This raised position of the conical body 36 is represented by a dashed line (omitting the funnel-like body 51 for the sake of clarity). Then, the gas fed to the nozzle 12 may enter the annular space 52, according to the arrow arrows, from which it flows through the slots 47, 48, and 53 to the material 17, thereby fluidizing while the conical body 36 engages with the funnel body 51 via ribs 37. as a result, it spins together. The operation will now be as described with reference to Figure 1. To discharge the finished product, the conical body 36 is lowered until the funnel body 51 rests on the shoulder 46, and the lowering operation is continued until the gap 49 between the lower edge of the conical body 51 and the outer periphery of the conical body 36 is reached. does not reach the value required to ensure that the granular end product is dead. For the conical body 36, this lower (end) position is indicated by a dotted line.

The use of the apparatus of Fig. 3 is only possible if the gas inlet (arrows g) is constant during rotation of the washer 7 through the slots 47 and 43 during the material contact operation, otherwise the slits are smaller than their width due to centrifugal force the particles would leave the layer 17 during the operation. However, this problem can be overcome by the solution of FIG. 4, which differs from that of FIG. 3 in that two of the plate elements 32, 38 and 39, which are otherwise substantially frustoconical in shape of the funnel body 51, are essentially Z salts. cross-section and the lower edge of these discs 38, 39 extends below the upper edge thereof, thereby making the gaps 47, 48 labyrinth-like and preventing the fall of material particles by centrifugal force into the lower space. In Fig. 4, the drawing of the screw conveyor 40 illustrates the possibility in all embodiments that a portion of material may be removed from the moving layer 17 during operation, such as drying. In this case, too, the total amount of finished product is removed by lowering the conical body 36, and in all other respects the structure and function are as in Figure 3, and the reference numerals and symbols therein are applied mutatis mutandis to Figure 4.

The invention will now be described by way of example only.

Example 1

A coated sugar beet seed dragee with a weight of 0.42 kg and a water content of 33.6% was dried in a 0.184 m diameter rotary washer. The total drying air flow rate was 45 Nm ³ / h and the washer speed was 180 rpm. 35 Nin ³ / h (about 78%) of the desiccant was passed through the washer and 10 Nm ³ / h of air in the upper third of the layer through the side stumps to be dried. In order to preserve the seed's original germination properties, drying was carried out with relatively low air temperature (45 ° C).

The temperature and water content of the dragee varied as a function of drying time, as shown below, which indicates that the apparatus can achieve very rapid and gentle drying (see Table 1).

Slovak). t (ynyl) Table 1 temperature of dragees (° C) humidity 0 24.0 33.5 3 18.5 27.3 5 20.5 24.0 10 28.0 14.7 15 35.0 10.0 20 39.5 7.9

Example 2

A zinc carbonate dryer having a moisture content of 50% was continuously added to a rotary bottom fluidization apparatus of the invention having a diameter of 0.184 m. 1.3 kg, with an average particle size of A1 ₂ O ₃ , d = 3 mm, was used as the filler. The material to be dried was continuously fed through a screw feeder at a rate of 1 kg / h into a vigorously moving layer of the inert fill.

The rotor speed was 170 L / ml, the drying air flow rate was 20 Nm ³ / h, and the temperature was 115 ° C (15 Nm ³ / h air was introduced through the washer, while 5 Nm '/ h was introduced through the side joints). The product was separated from the air stream leaving the unit by cyclones. From the cyclones, a product having a moisture content of 4.5-5% and a mass flow rate of 0.52 kg / h was removed.

After prolonged operation, the equilibrium mass of the rotating-rolling fluidized bed is approx. 1.5 kg, ie approx. It was 15% greater than the weight of the inert filler in the layer.

Example 3

A 2: 1 mixture of 0.3 kg of lactose-corn starch was granulated with a 60 g / l aqueous gelatin solution in a 0.184 m diameter rotary washer fluidizer. The fluidization air temperature was 70 ° C and the flow rate was 13 m ³ / h. At the rate of 12.7 g / min, 51 g of granulating fluid was sprayed onto the fluidized bed with constant rotation of the washer. The washer speed was set to 1801 / min. After the addition of the granulating liquid, the granules were dried for ten minutes. At the end of the experiment, the product of Table 2 was obtained. for comparison, Table 2 also shows the properties of the product obtained with the same amount of granulating fluid in a conventional fluidization apparatus.

Table 2 particle size roto-fluid conventional (mm) fluidization rails weight ratio (m%)

1.0-2.0 0.25 0.35 0.6-1.0 6.03 5.42 0.4-0.6 29.66 25.16 0.2-0.4 30.31 29.08 0.1-0.2 23,24 26.61 Below 0.1 10.49 13.27

filling bulk density: 435 kg / m ³ 385 kg / m ³ average porosity: 42.3% 50.3%

Example 4

In a rotary bottom fluidization apparatus of 0.184 m diameter, 45% thiamin hydrogen fumarate and 55% lactose granules were prepared. The apparatus was charged with 0.265 milk sugars having the following particle size distribution (see Table 3).

Table 3

particle size (mm) the weight ratio (wt%) 0.4 0.5 1.47 0.3-0.4 21.96 0.2 -0.3 55.39 0.16 to 0.2 14.64 0.10 to 0.16 3.65 0.06 to 0.10 1.88 Below 0.06 1.01

The rotating-rolling fluidized bed maintained by rotating the rotor and passing air at 24 ° C was sprayed with distilled water. powdered tiamulin hydrogen fumarate was added. Granulation was carried out with the following parameters:

- air volume flow through the unit »today: 2 Nm ³ / h,

- speed of the washer; 3001 / min,

- weight of tiamulin hydrogen fumarate added: 0,22 kg,

- weight of the wetting liquid (distilled water): 64 g,

- granulation time: 24 min.

The wet pellets thus obtained were dried with air at a flow rate of 17 Nm '/ h at 65 ° C for 15 minutes in the same apparatus. The final product obtained is a set of granules having the following properties (see Table 4).

Table 4 particle size (mm) weight ratio (m%)

Above 1.0, 0.71

0.5-1.0 7.13

0.125-0.5 87.31

Below -125 4.85 filling bulk density (kg / m ³ ) 602 moisture content (m%) 0.37

The active substance content (thiariulin hydrogen fumarate) was 44.8% by weight in the particle size group of uniformly spherical granules.

Example 5

Choline iodide, nicotinic acid amide, and various vitamins were deposited on 0.2 to 0.4 mm granules of vitamin C, with a protective layer of cetyl alcohol between each layer. During the experiment, 183.1 g of vitamin C were charged to a rotary washer device of 0.184 m internal diameter, and then a solution of 34.86 h of 15% cetyl alcohol in a fluidized particle was sprayed from the guild coating. Subsequently, 366.2 g of kaolin iodide was deposited on the surface of the granules in powder form, to which 50.0 g of a 6.5% gelatin solution in ethyl alcohol was applied as a wetting liquid. This was followed again by an ethanol coating. The weight of the introduced chloroform side was 124.5 g. Nicotinic acid anhydride (54.9 g) was added as a powder while 23 g of a 29% PVP solution in ethyl alcohol was sprayed onto the fluidized bed. After Cetilalkoholos coating (mass of the coating liquid was 124.5 g), 0.92 g of B, vitamin _E, 0.022 g vitamin B _{I 2,} 0.007 g of vitamin D ₂ and

9.2 g of vitamin K were applied to the surface of the granules from a suspension in 10% PVP solution.

During the layering of the powdered kaolin iodide and nicotinic acid amide, air at 25 ° C and a flow rate of 3 Nin ³ / h was passed through the apparatus and the rotor speed was adjusted to 3001 / mjn. The powder feed rate was 3.7 g / min.

During the coating of cetyl alcohol and the application of vitamins from the suspension, the temperature is 35 ° C and approx. Air flow rate of 14 Nm ³ / h was passed through the particulate layer. In this case, the washer speed was 300 rpm. Total duration of the experiment: 142 min.

99.1% of the granules produced are in the range of 0.2 to 1.0 mm and the particles are approximately spherical. The product is good] encapsulated.

Example 6

A catalytically active layer of 2.0-2.5 mm in size on a-Al ₂ O ₃ spherical support containing 15% NiO and 85% γ-Α _{1 2} Ο _{2 was} formed in a 0.184 m diameter underlay fluidizing device.

200 g of carrier was charged into the cylindrical cell of the apparatus and the washer was rotated at 210 rpm and the air flow rate was adjusted to 2 Nm ² (h). For the a-Al ₂ O ₃ balls in vigorous motion, 100 g of active substance (powder) ) was added by spraying 80 g of wetting fluid (water), powder 2.9 g / min, water

It was added at a rate of 2.3 g / min. After application of the active layer, the catalyst was cured in a sealed vessel for 18 h and then dried in an oven.

At the end of the experiment, spherical particles of uniform size with high mechanical stability were obtained. The catalyst had a compressive strength of 150 N and an average thickness of the applied catalytically active layer of 0.14 mm.

Example 7

A rotary fluidized bed apparatus of the invention having a cell diameter of 0.184 m was loaded with 100 g of beet seed having a grain size of d = 3.5-4.5 mm.

Λ The volume of air flowing through the unit at 25 ° C was set at 3 Nm ³ / h and the rotor speed was set at 310 rpm.

Subsequently, water (at a total of 157 g) was sprayed onto the surface of the intensive rotating-rolling cores using a two-fluid atomizer. a powder mixture containing 56% kaolin, 14% gypsum and 30 nt% furfural bran was added via a vibration feeder. The coating powder (220 g) was deposited on the core surface in 50 min. The water content of the wet dragees is approx. It was 33%.

Thereafter, the coated tablets were dried at a temperature of air flow 46 Nm ³ / h ° in the same apparatus. During drying, the rotor speed was reduced to 180 rpm. After drying for 20 minutes, uniformly sized machine-seeded spherical drops were obtained with an average water content of approx. It was 8%. The weight of the dragee (94%) was within the size range of 4-5 mm and the seeding capacity of the seed did not deteriorate during the drageing.

Example 8

In a rotary disk fluidization apparatus according to the invention having a diameter of 0.184 m, an coated granulated sugar beet core having a mean particle size of G = 250 g, d = 4.5 mm was tested using a coating liquid having the following composition:

-Polivinyl-alkoliol 2.6 m%

Carboxymethyl cellulose sodium 0.9%

- Kaolin 13.7 tn% distilled water 82.8 m% (colored with water soluble red ink)

At a flow rate of 180 rpm, the inlet air flow rate is 60 to 70 Nnr '/ h, the temperature is 45 to 50 ° C, the outlet air temperature is 37 ° C, the coating liquid delivery rate w = 4 ml / min, the spray time is 27 ntin volt.

The relative amount of coating material applied to the grain surface was 0.18 kg / m ² , which resulted in a mass increase of almost 8 m%.

The purpose of the film coating applied to the seeded sugar beet seeds is on the one hand to control coloring, to distinguish well, to control large-scale sowing. the insecticide (organic phosphate ester) previously applied to the dragee corozote from the organic solvent solution was covered, which requirements are well met by the final homogenous product.

Example 9

In a rotary disk fluidization apparatus of the invention of 0.184 m diameter, a film coating experiment was carried out with G = 350 g (d = 10 mm, h = 5.9 mm, thousands of weight 448.1 g) of potassium and magnesium asparaginate as described below.

Composition of the coating liquid:

- Eudragit L 5.0 m% - Triacetin 0.5 m% - Talc 0.9 m% - Mg stearate 0.1 m% - Isopropanol 93.5 m% n = 1801 / min plate inlet air flow rate of 100-110 m ³ / h, temperature 50 C, 55 ^D, the exhaust air temperature 45 ° C, the coating liquid feed rate of w '= 10 ml / min, the poilasztás time was approximately 15 min.

After application of the coating liquid, the dragee cores were polished in 22.5 mL of a 10% PEG 6000 solution (1: 1 acetone-water).

The coating was successfully applied to the surface with an 80% application efficiency. The relative amount of coating material actually applied to the surface is 25 g / m ² (about 20 g / m ² per filmmaker).

The purpose of the film-coating operation in this case is to protect the dragee core containing moisture-sensitive material from the damaging effect of moisture in the environment. The final product of the experiment is an aesthetically pleasing, shiny, smooth-surfaced dragee, which provides sufficient protection against moisture, the so-called active ingredient. quick wetting! it does not interfere with the absorption of the active substance in the stomach.

Example 10

In a rotary plate fluidization apparatus of 0.184 m diameter, a film coating experiment was carried out with a dragee core containing G = 35O g of potassium and inagnesium asparaginate (d = 10 mm, h = 5.9 mm, thousand weight 448.1 g) as detailed below .

Composition of the coating liquid:

- Mowilith DH (507?) 10% - Troy 1% - Talkum 11%

Distilled water At 78 m% η = 180 -200 L / min plate speed, the inlet air flow rate is 110 Nm ³ / h, the average temperature 48-50 ° C, the outlet 'Air' temperature 40-42 ° C, the 22 m The rate of addition of the coating liquid (aqueous dispersion) with% solids was w '= = 3.5 ntl / y, and the spraying time was 17 min.

The drops were polished with 10% aqueous PEG-6000 after application of the coating liquid.

The coating was applied to the surface with an application efficiency of 88.5%. Relative amount 44 g / m ² (almost 22 g / m ^{2 for} film-maker).

The final product of the experiment is an aesthetically pleasing film coated with moisture protection film. According to this example, a dragee containing a moisture sensitive active ingredient may also be provided with a moisture barrier coating from an aqueous system in the apparatus described. The product obtained meets drug technology requirements for both disintegration test and rapid wetting test.

The advantages of the apparatus and method according to the invention may be summarized as follows.

Using the apparatus, solid dispersions (e.g., particle assemblies, cores, powders, etc.), solid-liquid dispersions (e.g. suspensions), and liquids (e.g. solutions) can be contacted with each other and / or in a gas-rotating fluidized system. The linear gas velocity relative to the total cross-section is preferably lower than the minimum fluidization rate of the bed material, however, due to the uniform distribution of gas, various operations (e.g. drying, granulation, etc.) can be performed under good heat and material transfer conditions.

The annular slots on the bed support and moving rotary pads on the gas distributor, as well as the stumps on the side of the chamber, allow intake / etcse and uniform distribution of the gas (s) with relatively low air resistance, i.e. low rotational energy - can be solved without disturbing its rolling state.

The rotating washer and / or the gas distribution design of the present invention does not interfere with the flow of the particles, nor does it break or abrasion the particles. It should be noted that it is precisely because of these adverse phenomena that it is not advisable to simply distribute the air by perforating the washer. The centrifugal force generated by the foam barrier of the washer and, in some embodiments, the gas entering the annular slits forces the particles from the inside of the fluidization space to the wall of the device and forces the entire particle mass to rotate about the center. At the wall of the device, the particles move upward and their speed decreases due to friction. These particles, rolling down the lower layers at higher speeds, retaining the washer 7, retaining the inside of the device. A spiral-like flow is formed in the chamber, which can be made more intense and controllable by injecting a high-speed, directed gas stream through the chamber wall at several points into the upper third of the fluidized bed, i.e., the lower velocity particle region.

Λ Solid dispersions (eg cores, grain assemblies) can be simply and practically completely removed from the equipment after completion of operations on material contact, or, if necessary, can be removed during operation or even continuously.

In the rotary roller fluidized system, inert particles of significantly larger size and density can be deposited in layer 17 during drying of solid-liquid dispersions (e.g., suspensions, or paste-like materials) and maintained under intense motion during wet drying, the risk of adhesion and clogging of parts of the material is significantly reduced and it is also possible to dry materials which cannot be removed by gas flow from conventional fluidization equipment because they do not peel off or wear off the inert charge.

Since the intense rotary-rolling motion of the material in the layer 17 is not primarily and exclusively determined by the velocity of the gas stream passed through, the present invention also provides granulation and / or coating tasks that substantially differ in size from solid dispersions such as larger particles. or contact between seeds and powders and liquid (s) and a drying medium (such as air) are required.

The apparatus implementable processes combine the advantages of conventional fluidization and rolling layer processes, thereby providing fluidization and fluidization. In addition to high heat and material transfer conditions achieved by fluidization-spraying equipment and high productivity, granular and / or coated products with near spherical shape, relatively low porosity (solid), and sufficient strength and mechanical stability can be produced. The starting particles are a. The material to be processed, its own granules produced in a manner known per se (e.g., by extrusion), may be non-volatile foreign matter. Thus, by the same process, particulate materials (e.g. coated plants) having the same composition (e.g., catalysts, catalyst supports, adsorbents, etc.) or having a layered structure different from the inner core may be obtained.

The developed rotary fluidization equipment and operating procedures are suitable for the various, mainly physical, operations in the pharmaceutical, pesticide manufacturing, organic and inorganic chemical, building materials, food and agricultural production, and other industries.

-101 perception and involvement),

The invention is, of course, not limited to the Vi described above. and the method of implementation listed above, but may be practiced in many ways within the scope of the claims.

Claims (27)

Patent claims Apparatus for fluidizing contact of materials, in particular of solid dispersions or / and solids-liquid dispersions or / and liquids in contact with each other and / or gas in a rotary fluidization system, in particular for drying, granulating and coating operations, the housing thereof being rotatable therein a layer support, a gas flow gap between the inner surface of the housing wall and the layer support, a gas feed aperture, and a structure for feeding contact materials and removing the final product, characterized in that the layer support (7) has at least one an intermediate annular gap (42,43,47,47,48) between the vertical geometric center axis (x) of the device and the peripheral slot (41,53) and concentric to the top downward with an egeometric center axis (x) , Preferably conical body (5, 31.36), and in that the layer support washer (7), or at least the central body emlehtő-recessed (36). Apparatus according to claim 1, characterized in that the layer retaining washer (7) is located at least partially in a downwardly tapered chamber (1) of the housing (I). Apparatus according to claim 1 or 2, characterized in that the housing (I) has a cylindrical chamber (11) beneath the layer support (7) into which the gas inlet (12) extends and the cylindrical chamber (11) an open flow modifying insert (13) having a downwardly decreasing cross-section is located inside. 4. Apparatus according to any one of claims 1 to 3, characterized in that the lower part of the housing (I) is formed as a downwardly decreasing cross-sectional chamber (27), preferably conical, from which a preferably oblique discharge outlet (28) is provided (Fig. 1). . Apparatus according to claim 4, characterized in that a vibrator (30) is attached to the wall of the thickening chamber (27), preferably outside. (Figure I) Apparatus according to any one of claims 1 to 5, characterized in that the housing (I) preferably has a cylindrical layer (17) above the layer support (7) in fluidized rolling-rotary motion during operation. one or more, preferably two to four, gas inlets (15) extend into the portion of the chamber (14). Apparatus according to Claim 6, characterized in that the gas inlets (15) extend into the chamber (14) in a direction leading to a perpendicular gas supply, preferably at an angle of approximately 120 ° to 150 ° with a radius drawn to the point of collapse. . 8. Apparatus according to any one of claims 1 to 3, characterized in that the housing (1) has a liquid feeding device, preferably a two-fluid liquid atomiser (25) located above the layer (17) (Fig. 1). 9. Apparatus according to any one of claims 1 to 5, characterized in that the housing (I) has a screw feeder (26) suitable for feeding powder, particulate material or paste (26) over the layer (17) (Fig. 1). 10. Apparatus according to any one of claims 1 to 3, characterized in that the layer support washer (7) or at least its central conical body (36) is connected to a rotatable vertical axis (2) having a lower end (8), preferably a hydraulic cylinder. . figure). Device according to Claim 10, characterized in that the shaft (2) is a mechanism formed by a sprocket (22) attached to it, a sprocket connected to an engine, such as a spring-mounted intermediate auxiliary sprocket (23) and a chain (44). drive 'an (Figure 1). 12. The method of any one of claims 111; endezés, characterized in that during the layer carrier of the washer (7) of the conical body (5) from one another and - preferably variable - spacings (a, b) in the horizontal or substantially víszin ^T and, with openings (9, 10) pierced discs (3 , 4), and these discs (3, 4) and the conical body (5) form intermediate annular gas supply slots (42, 43) with the base plate (d ₃ ) having a diameter smaller than the diameter (d ₂ ) of the disc (4) below and the diameter (d ^) of the lowest (3) is greater than the diameter (d ₂ ) of the disc (4) above it (Figure 1). Apparatus according to claim 12, characterized in that the outermost gas passage (41) is located between the outer rim of the lowest disc (3) and the inner wall surface of the conical chamber (1) of the housing (I). (Figure 1) Apparatus according to claim 12 or 13, characterized in that the through openings (9, 10) in each of the discs (3, 4) are distributed on a dividing circle and the dividing circuits above each other are offset with respect to each other. arranged. (Figure 1). 15. A 12-14. Device according to any one of claims 1 to 3, characterized in that spacers (6) are provided between the discs (3, 4) and the conical body (5) (Fig. 1). 16. Apparatus according to any one of claims 1 to 3, characterized in that the layer support (7) has a funnel-like body (51) formed by annular conical plates (32-34) which are partly overlapping and spaced apart (a) and which are fixed to one another. surrounded by a central conical body (36) having a downwardly decreasing cross-section, it is formed with it but rotatable but connected by a releasable connection, with the outermost-outer gas-inlet (53) being formed by the uppermost annular plate (32) and the inner surface of the housing (I) wall, the intermediate annular gas inlet slots (47,48) being formed between the frustoconical plates (32-34) (Fig. 3), The apparatus of claim 16, further comprising -111 196.717, characterized in that the conical annular plates (32-34) are secured to one another by means of spacer screws (35), preferably in order to control the distance between the spacers (a) (Fig. 3). Apparatus according to claim 16 or 17, characterized by a shoulder (46) formed in the form of an annular plate extending inside the gas (I) to support the funnel body (51). (Figures 3 and 4) 19. Apparatus according to any one of claims 1 to 4, characterized in that only the centrifugal conical body (36) is rigidly connected to the liftable-lowering rotary shaft (2). 20. A 16 -19. Apparatus according to any one of claims 1 to 3, characterized in that there are outwardly extending forming ribs (37) in the lower region of the outer surface of the central conical body (36) to which the funnel body (51) fits into the lower edge of the lower conical (Figure 3). 21. Apparatus according to any one of claims 1 to 4, characterized in that the annular conical plates (38, 39) of the funnel-like body (51) are Z-shaped in cross-section and overlapping the labyrinthine gas outlet slots (47, 48). each other (Figure 4). 22. Apparatus according to any one of claims 1 to 3, characterized in that the apex of the central conical body (31,36) is spherical and / or its side surface is concave (convex), (Figures 2-4). 23. A method of contacting materials by fluidization, in particular by contacting a solid dispersion material and / or solid-liquid dispersions or / and liquids with a rotary fluidization system 7 and / or gas. Apparatus according to any one of claims 1 to 4, in particular for performing drying, granulating and coating operations, characterized in that the total amount of material in the layer (17) through the joints of the rotating layer washer (7) and, if appropriate, less than the amount of gas resulting from the product of its fluidization gas velocity and the largest equipment cross-sectional volume is introduced into the layer (17). A method according to claim 23, characterized in that up to 30% of the total amount of gas fed is introduced sideways in a swinging manner, the remainder being passed through the layer (17) from below. Method according to claim 23 or 24, characterized in that the solid dispersion material constituting the movable layer (17) is preferably a liquid, in particular a solvent and / or solution, in a dispersed state with an average droplet size of 0.02-0.10. and / or administering a suspension. A method according to any one of claims 23 or 24, characterized in that the rotary-rolling fluidized bed (17) - Preferably, 1 θ is formed from inert granules having a mean diameter of 3 to 6 mm, such as spherical or near-spherical cores and / or balls, liquid solid-liquid dispersions to be dried, paste or the like and other materials to be dried. preferably fed to the layer (17) by means of a screw feeder (26) while passing through the layer an amount of gas, usually air, such that the linear gas relative to the largest cross-section of the apparatus is less than the minimum fluidization gas velocity of the should be greater than the velocity of falling or falling particles of the dried material. 27. A 23-25. Process according to any one of claims 1 to 3, characterized in that - for preparing granules of particulate material and / or particulate material (s), or / and multilayer granules or / and coated granules, for example cores, pelleting or / and pelleting. is carried out in several, preferably three, sub-operations and is performed sequentially over time, periodically in three working phases as necessary, preferably in the form of powdered material and dispersed granulating fluid, preferably pulverulent, preferably in powder form. while providing an amount and temperature of needle gas, air is generally passed through the layer to ensure that the theoretically usable heat input by the desiccant is less than the amount of heat required to evaporate the total amount of moisture, preferably by spraying, In a 4Q intensive rotary-rolling moving layer, the wet particles are spheronized and compacted without the addition of a powdery liquid without addition of powdered liquid, up to a side feed, preferably at room temperature, and again in a third step through the rotating x-plate pad. 45, and the wet layer applied and compacted to the surface of the granules is then fixed by drying.