DE3104062A1 - "METHOD FOR MIXING A BLEND OF PULVERIZED INGREDIENTS AND DEVICE FOR CARRYING OUT THE METHOD" - Google Patents

Description

31CK062

Process for mixing a mixture of pulverized components and apparatus for carrying out the process

The invention relates to improvements in mixing UO ₂ and second cohesive powders using a fluidized bed mixer, and more particularly to an improved method and apparatus for converting a heterogeneous mixture of solid UO ₂ powders and second cohesive powders into a homogeneous mixture.

Mixing of particulate solids has heretofore been accomplished in a wide variety of ways. Various types of mechanical mixers such as drum mixers, ribbon mixers and high shear mixers have been used. Bubbling bed mixers and fluid bed mixers were also used. According to the prior art, U0 ₂ ~ powders are mainly mixed with the aid of mechanical mixers of the drum mixer type. This type of mixer has proven to be unsatisfactory for the production of mixed batches which are intended to _{meet certain homogeneity specifications for U0 2} powder. It is believed that

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the inability to meet homogeneity specifications is due to stagnant or dead zones within the fluidized beds of the ingredients to be mixed in the mixer and to segregation problems during discharge. U.S. Patent 4,168,914 describes an improved fluidized bed fluidized bed mixer. This mixer eliminates the large dead zones that occur in the prior art bubble bed / fluidized bed mixers by providing a device for receiving the heterogeneous powder to be mixed, preferably U0 ₂ powder, using a vertically oriented, plate-shaped mixing container comprising a vortex grate arranged at the bottom of the container. The vortex grate constructed in accordance with the teachings of the aforesaid U.S. patent comprises a linear array of generally downwardly directed pyramidal hoppers, each of which has walls converging into a conically shaped opening. A plurality of gas nozzles are provided to direct a stream of fluidizing gas up into the bottom of each funnel. The fluidizing gas is supplied to each of these nozzles at a speed sufficient to cause bubbles of fluidizing gas to rise through the mixture of powders and exit the powders so as to stir the powders until a homogeneous mixture of the powders is achieved. The combination of the linear arrangement of the hoppers and the upward-facing gas nozzles eliminates the dead zones encountered in previous designs of fluidized bed-fluidized bed mixers.

However, none of the known devices have been for mixing fine and cohesive powders in a fluid bed mixer able to meet product homogeneity specifications for mixing UO ^ powders and secondary powder mixes of in high Various physical properties

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to fill. In particular, quite a number of batches of second powders, including those that are hydrophobic, hydrophilic, or hygroscopic, due to their cohesive nature, readily form large agglomerates which provide poor distribution. In addition, certain low density agglomerates will undesirably segregate or separate _{from the primary O 2} powder in a fluidized bed mixer due to the stagnant or dead zones present at the bottom of the fluidized bed. Furthermore, it is known from experience that at certain gas flow rates used when introducing the mixture of the second powder, a discontinuity develops in the mixture of the powders.

The advantages of the present invention are provided by Use of an improved fluidized bed mixer, vortex mill and distributor achieves the are interconnected by a conventional pneumatic conveyor system. The fluidized bed mixer comprises a vertically oriented one Mixing container with a vortex grate arranged on the floor. The vortex grate comprises a linear arrangement of pyramidal shaped funnels, each funnel containing a set of nozzles within the base, those for receiving and straightening jets of vortex gas along in a diverging vortex vortex pattern the walls of each hopper are constructed. Above the linear arrangement of the pyramid-shaped funnels in the vicinity of the base of the fluidized bed in the mixing vessel At least one impact device including a baffle is disposed. A mix of one second powdered ingredient and gas is introduced under pressure into the impingement device in which the baffle the second powdered ingredient evenly

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_{Distributed in the vortex fluidized bed of pulverized UO 2} contained at the beginning of the vertically oriented mixing container. The terms "second material", "second powdered material" or "second powdered ingredient" are to be understood as meaning that the second material, the second powdered material or the second powdered ingredient is either a mixture of hydrophobic, hydrophilic or hygroscopic materials such as they are defined in more detail below, mean and may contain further constituents, such as a binder material and the like. Furthermore, the second material, the second pulverized material or the second pulverized ingredient can be a single additive, such as a hydrophobic, hydrophilic or hygroscopic material, which is to be mixed homogeneously with the UO ^ powder.

The mixture of the second pulverized ingredient and gas is fed to the impingement device under a predetermined pressure from a vortex mill. In the mix the second powdered ingredient forms relatively large agglomerates [approximately 1200 µm (1200 microns)], and the vortex mill picks up the mixture of the second pulverized component and gas under a predetermined pressure and crushes it the particles of the second powdered ingredient to an average particle size of approximately 10 to approximately 60 microns (approximately 10 to approximately 60 microns) with a preferred average particle size is about 15 ym (15 microns).

The mixture of the second powdered ingredient and gas is vortexed from the mill at a predetermined pressure a manifold having a material inlet port, a gas inlet port for pressurizing the system, and a

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inner mixing chamber owns, supplied. The mixing chamber of the distributor initially and coarsely mixes the constituents of the second pulverized batch by means of turbulence created by the flow of an inert gas introduced into the mixing chamber at a predetermined pressure, and the coarse batch is then pneumatically conveyed under pressure from the distributor to the vortex mill. The particles are then crushed in the vortex mill and mixed further. The mixture is then fed from the mill at a predetermined pressure to the impact device, through which it is introduced into the fluidized bed mixer at a predetermined pressure and divided uniformly _{for homogeneous mixing with the pulverized UO 2 contained therein.}

The invention is explained in more detail by the following description in conjunction with the accompanying drawings, whereby

Figure 1 is a perspective view of one embodiment of the apparatus of the present invention; which includes a fluidized bed mixer, a vortex mill and a distributor.

Figure 2 is an elevation of the fluidized bed mixer showing a number of hoppers and an impingement device, the are constructed in accordance with an embodiment of the present invention.

FIG. 3 is a partial sectional view of the fluidized bed mixer, the section being taken along line 3-3 of FIG and you are looking in the direction of the arrows.

FIG. 4 is an enlarged sectional view of the vortex mill shown in FIG.

Figure 5 is an enlarged sectional view of the impact device; which is shown in FIG.

Figure 6 is a sectional view of the vortex mill, wherein

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the cut is made along the line 6-6 in figure 4 and look in the direction of the arrows.

In Figure 1 an apparatus for mixing powders is shown. The device basically consists of three main parts: An improved fluidized bed mixer 10, an improved vortex mill 11 and a distributor 12.

The mixing of the powdered UO ₂ and the second powdered component, which, as indicated above, may be a powdered hydrophobic, hydrophilic or hygroscopic material, takes place in the improved fluidized bed mixer 10, as shown in FIG. As shown in Figure 2, the fluidized bed mixer 10 includes a vertically oriented mixing vessel 13 with a fluidized grate generally designated 14 at the bottom thereof. The vortex grate 14 includes a linear array of pyramidal hoppers 15, also shown in Figure 2, each containing within the base thereof a set of nozzles 16 as shown in Figure 3 which are used to receive and upwardly direct vortex gas jets in one diverging vortex vortex patterns are provided along the walls of each funnel. The fluidizing gas jets build up a boiling or bubbling bed of the pulverized UO ₂ 9 with which the mixing vessel 13 was initially charged. Above the linear arrangement of the pyramid-shaped funnels 15 there is at least one impact device 20 which allows a deflector plate 21 to be inserted, as shown in FIGS.

Referring to Figures 3 and 5, the impingement device 20 is in the form of a modified, cage-like one Arrangement designed to have a damming effect and a deflection

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kung of a mixture of gas and a second material fed under pressure into the fluidized bed mixer. In particular, the device 20 includes the previously mentioned baffle plate 21 and a top plate 22. These plates are circular and are held in vertically connected connection by four peripherally arranged struts 23. The top plate 22 is perforated centrally and connected in a suitable manner with a line 24. With this arrangement, the aforementioned mixture of pulverized second ingredients and gas is introduced into the mixing vessel and into the fluidized bed of UO- located therein. The pressure causes the second powder to impinge on the baffle to create a damming effect for the powder as it enters the container and to distribute evenly around the perimeter of the impingement device and into the fluidized bed of UO ₂ 9 in the container. In addition, the conduit holds the impingement device in a predetermined position in the fluidized bed adjacent the base of the bed. Of course, while only one impingement device has been illustrated and described, a variety of such devices can be used in a linear arrangement above the funnels 15.

Referring to Figures 1 and 4, it can be seen that the line 24 is connected to an output 25 on the above-mentioned vortex mill 11 and in this way the Mixture of gas and second pulverized material fed from the mill to line 24. The vortex mill -11 receives the second material and the gas mixture from the manifold through a regulated inlet 26. In the vortex mill 11 are the particles of the mixture of a mixture of large agglomerates I approximately 1200 µm (1200 microns)] to one Mixture with an average particle size in the range

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from approximately 10 to approximately 60 μπι (LO to approximately 60 Microns) with a particle size of 15 µm (15 microns) preferred.

After the mixture of the second powdered ingredient has been crushed to a preferred particle size, the mixture of the second powdered constituent under pressure from the vortex mill 11 through a line 36 in the impactor 20 is conveyed as shown in FIGS.

The mixture of the second powdered ingredient is pneumatically under pressure from the distributor 12 of the vortex mill supplied as shown in FIG.

The mixture of the second powdered component is drawn under vacuum into the manifold through an opening 34 due to the action of the gas entering the manifold through an inlet opening 33. The gas entering the manifold is an inert gas such as N ₂ and can be supplied by a gas source 37 as shown in FIG. The mixture of the second pulverized constituent is pneumatically fed into the vortex mill 11 from the distributor 12.

Referring to Figure 3, one of the many hoppers included within the fluidized bed mixer is connected with the impact device arranged within the mixing chamber 20 shown. The fluidized bed mixer used in accordance with the present invention is one of ordinary skill in the art known type and comprises a vertically-oriented mixing vessel 13 with a vortex grate 14 attached to the bottom of the container 10 is arranged. The vortex grate 14 includes

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a linoarc arrangement of generally directed unton, pyramidal funnels 15, each of which is too having conically shaped openings converging walls. A plurality of valves 17 are used for discharge the mixed powder, such as UCU powder and a second one powdered mixture, used by the funnels, with such a valve 17 at the bottom of each funnel is arranged. A set of nozzles 16 is located at the base of each funnel, and the nozzle set is provided with one Gas inlet 18 for a source of fluidizing gas connected by means of a manifold and connecting lines.

A general discussion of the prior art for constructing an air-jet-fluidized bed mixer necessary considerations including the consideration of particle properties, particle size, particle distribution , Container geometry, surface gas velocity and circulation schemes is described in Fluidization and Particel Fluid Systems by Frederick A. Zenz and Donald F. Othmer, Reinhold Chemical Engineering Series, Reinhold Publishing Corporation, New York, 1960 found.

The fluidized bed mixer of the present invention differs from the fluidized bed mixers of the prior art by the incorporation of at least one impact device 20 in the vicinity of the vortex grid, as shown in FIG Figures 2 and 3 is shown. Although only a single impact device is shown, it should be noted that a variety of impact devices may be used in practicing the present invention can. The impact device as shown in Figures 3 and 5 is of cage-like construction with a Input line 24, a circular baffle 21,

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an upper circular plate 22, and supporting members or braces 23 which connect the upper and lower plates of the impact device in a vertically arranged position. The particular construction of the impingement device makes it suitable for effectively damming and deflecting the pressurized batch of second powder entering through conduit 24 and results in a reduced velocity and inlet pressure of the batch of second powder introduced into the mixing chamber of the fluidized bed. When the comminuted mixture of the second powder is fed into the fluidized bed mixer from the vortox mill, the effect of the impact device enables a wide distribution of the mixture of the second powder within the U0 ₉ powder, and a homogeneous powder mixture is achieved.

Referring to FIGS. 1 and 4, the mixture of the second powder is fed into the vortex mill 11 through a vortex mill inlet 26 and reaches the interior through a feed hopper 27. The storage system for the vortex mill is adapted to high pressure operation |> 17O2.7 mbar (> 10 psig)] to ensure a pressure-tight introduction of the gas and the second pulverized material into the lower regions of the fluidized bed mixer. In particular, it is possible to adapt the storage system of the vortex mill to operation at high pressure a high velocity flow within the pneumatic Conveyor system which is an agglomeration of trapped second material after grinding decreases when the gas and the second pulverized material to the Fluidized bed mixer is promoted.

When the mixture of the second powder passes through the feed

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funnel 27 of the vortex mill 11 passes., arrives; e ;; in contact with a spreader 30 at the base of a gyro wheel assembly. When the mixture of the second powder comes into contact with the surface of the spreader, the particles are moved by the centrifugal movement of the rotor, which is operated at approximately 20,000 revolutions per minute, is accelerated to approximately 213 m / s. The particles are driven radially outward through channels 28, formed by the lower expansion distributor and the upper rotor plate, and violently collide with tungsten carbide impact blocks 32, mostly on the circumference of the lower spreading distributor 30 are arranged. Upon contact with the tungsten carbide impact blocks the particles of the mixture of the second powder are comminuted, then under pressure from the vortex mill conveyed out through the pressure-tight line system 36 and into the fluidized bed mixer 10. It can be seen that comminuting the particles of the second powder by any suitable comminuting mill or grinder suitable devices can be effected, and it is the present invention not to the use of a vortex mill limited.

The manifold 12, as shown in Figure 1, is of conventional construction and has a material inlet port 34, a gas inlet port 33 and an internal mixing chamber which initially contains the constituents of the mixture of the second powder due to the turbulence created by the flow of the inert gas is generated in the mixing chamber from a gas source 3 7, mixes. As mentioned earlier, the particle size of the second batch is on the order of approximately 1200 ] µm (1200 microns). The distributor also provides pressure ventilation of the line system 36, which is required for the operation of the entire mixing device. The distributor-

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ausyariy 35 is directly connected to the line system 36 to the Vortex mill input 26 connected such that the initial mixture of the mixture of the second powder in the Vortex mill is introduced, as shown schematically in Figure. The details of the distributor discussed above do not form part of the present invention and it can be used for the initial introduction of the secondary materials a manifold of any suitable type can be inserted into the mixing device, such as, for example a Type 264 as used in the practical apparatus of the present invention and available from AMETK Inc., Cornwells Heights, PA. 19020 is produced.

The mixing apparatus of the present invention is effective for homogeneously mixing powders having widely diverse physical properties with UO ₂ powder in a fluidized bed mixer. During operation, the mixing container 13 of the bubbling bed-fluidized bed mixer is _{filled with U0 2} powder through an inlet opening at the top of the same with a valve, such as a throttle valve (not shown), the attached valve serving to prevent powder from escaping during the To prevent mixing process. The throttle valve does not form part of the present invention and any suitable type of valve can be used. The mixing container 13 is initially filled to about half its height with a mixture of heterogeneous or unmixed powder. In this way, the lower part of the mixing container 13 serves as a mixing chamber for the container, while the upper part serves as a gas space in which powder entrained within the fluidizing gas can settle.

The mixing of the particles in this type of mixer is done by

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from the nozzle set 16 attached to the base Blowing fluidizing gas and maintaining an internal pressure in the container of approximately 1082.2 mbar (1 psig) to approximately 1358.0 mbar (5 psig). The gas bubbles rise from the nozzles through the bed to the top up the bed in sweeping zigzag movements. Once a bubble forms, neighboring ones begin to flow Particles around their top and down to their lower cavity so that the bubble rises. The particles directly above the bubble are forced upwards, while others are pushed aside and some flow down into the lower part of the bladder and fill in their trail. In this way an ascending spread Blow the particles radially in all directions. When a given bubble rises, the particles which fill their lower cavity, packed a little more densely than particles just outside the lane the bladder. The next rising bubble in this general area becomes a trail through the less closely packed particles follow immediately on the side of the path of the first bubble. That way, each will subsequent bubbles show the tendency to rise at a different point, causing other particles to join the previously mixed particles are mixed. As more and more bubbles rise up through the particle bed, will small neighboring bubbles combine to form larger bubbles. This effect, along with that The bubbles flow to areas of low pressure, causing and creating a sweeping zigzag motion a horizontal as well as vertical convection mixing process. Those escaping from the top of the particle bed Bubbles scatter some UO ^ powder into the gas space on the upper part of the mixing container 13. However, the compressible

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ie gas from the particle bed in intermittent gas pulses. These intermittent bursts of gas give the particles that would normally be entrained in the gas stream an opportunity to falling back into the particle bed rather than being carried away and expelled with the fluidizing gas. It it should be emphasized that in the bubble bed-fluidized bed mixer described here there is in fact no mass movement of the particle bed takes place, as is the case in a bubble bed mixer, although here the aforementioned mixing is in the circuit is present.

After the mixture of the second powder is initially mixed in the distributor, that is carried over in the inert gas Mixture conveyed under pressure to inlet 26 of vortex mill 11 and into the interior of the vortex mill through the feed hopper. When the mixture of the second powder flows through the feed hopper of the vortex mill, it strikes the surface of a spreading distributor 30 with a pyramidal, nipple-like, convex central part that gradually falls outwards. The spreading distributor surface works in coordination with an upper one Rotor plate through which the feed hopper passes. The rotor plate surface is a mirror image to the expansion manifold surface, thereby forming radial channels 28 which gradually expand to create a Circumferential exit in the vicinity of the circular impact blocks 32 at the circumference of the radial channels, formed by the expansion distributor surface and the rotor plate, narrow. The spreader rotates at approximately 20,000 revolutions per minute, and this force works in unison the inlet pressure of the line system to the effect, the mixture of the second particles entrained in the inert gas to force through the radial channel and to the tungsten carbide

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Impact blocks at approximately 213 m / s, thereby causing the particle size of the batch of the second powder of approximately 1200 ym (1200 microns) to particles having an average size in the range of approximately 5 to approximately 60 µm (approximately 5 to approximately 60 microns) in diameter, preferably to approximately 15 pim (15 microns) in diameter.

After the mixture of the second powder has been brought to a preferred diameter by crushing in the improved vortex mill, it is now in a form in which it can be mixed with the _{U0 2 powder contained in the improved fluidized bed mixer 10.}

The mixture of the second powder entrained in the inert gas leaves the vortex mill through a generally shown in FIG Discharge opening 25 shown and is through the line system 36 led to the entrance 24 of the impact device. The mixture of the second powdered ingredient occurs into the fluidized bed mixer via the impingement device, which is near the base of the fluidized bed, and preferably approximately 61 cm (2 feet) above the vortex grid 14 or the tops of the downwardly directed pyramidal shape Funnel 15, is arranged.

The mixture of the second powder is at a pressure in the range of approximately 1220.1 mbar (3 psig) to approximately 1358.0 mbar (5 psig), and preferably at a pressure of about 1254.6 mbar (3.5 psig) into the input line 24 to the Impact plate is inserted and comes into contact with the deflector plate 21. The cage-like construction of the impact device provides a damming effect and in conjunction with the baffle it causes a reduction in force, thereby

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the mixture of the second powder enters the fluidized bed mixer at a rate of approximately 1151.2 mbar (2 psig). The impact plate causes a uniform distribution or dispersion of the mixture of the second powder within the Fluidizing the first powdered ingredient in the fluidized bed mixer.

That for mixing the second cohesive powder with the UO _? The method used for powder is started by activating the distributor 12, whereby the piping system for the batch of the second powder and the vortex mill are pressurized. Almost simultaneously, the fluidized bed mixer 10 is activated so that the UO ^ powder contained within the fluidized bed mixer circulates in a random manner. The manifold is initially started to prevent any leakage of the UO _{? Contained in the fluidized bed mixer.} -Powder in the pneumatic line system 36 via the impact device 20 to prevent.

After activation of the manifold by introducing an inert gas such as N _2, to the gas inlet at a pressure of approximately 2131, O, is the pre-cooled batch of the second powdered material introduced mbar (25 psig) at the same time in the distributor at the material inlet opening 34 wherein it is drawn into the internal mixing chamber and mixed roughly under the turbulence created by the incoming gas and at a pressure therein of less than about 1358.0 mbar (5 psig).

The second materials to be mixed are usually called described as hydrophobic, hydrophilic or hygroscopic. Because of their cohesive nature, they can easily form large agglomerates

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that provide poor distribution.

Hydrophobic materials such as zinc stearate, oils, fats and waxes do not dissolve in water, but they adhere to one another. Accordingly, the agglomerates for mixing this type of material must be reduced in size before a adequate distribution can be achieved.

Hydrophilic materials tend to absorb water and combine with one another. Fall into this category such materials as carbohydrates (starches, vegetable gums, and the like) and complex proteins. These Materials must also be scaled down before adequate mixing is achieved.

Inorganic materials including ammonium bicarbonate, ammonium oxalate, calcium chloride and zinc chloride form one third category described as hygroscopic. These substances absorb moisture from the air. In particular dissolvable materials are hygroscopic powders of water-soluble chemical salts that dissolve in water absorbed from the air. These materials are difficult to handle and have to be fed in when dry.

The mixture of the second pulverized material roughly mixed in the distributor is pneumatically pressurized from approximately 1082.2 to 1220.1 mbar (1 psig to 3 psig), and preferably under a pressure of about 1151.2 mbar (2 psig) fed to the vortex mill for grinding to a preferred particle size. The effect of the vortex mill adds a pressure of about 1151.2 mbar (2 psig), which results in the slightly higher pressure at which the mixture

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is conveyed from the vortex mill to the mixing container. Then, as discussed above, this comminuted mixture of the second pulverized material is pneumatically transported under pressure to the impact device within the fluidized bed mixer, which in cooperation with the bubble bed of the mixture of the primary or first pulverized material, in this case UO ₂ powder, causes a homogeneous mixture of the mixture of the first and second pulverized material.

As soon as a homogeneous mixture of the mixture of OO ₂ powder and the second powder has been achieved, the homogeneous mixture is discharged from the funnels by means of a plurality of valves, such a valve being arranged at the opening of each funnel. These valves serve as drainage openings for the mixing container as soon as a homogeneous mixture of the powders has been achieved. When the mixing process is completed, the mixed powder is quickly and efficiently discharged according to a method described in U.S. Patent 4,182,383. Other embodiments and uses of the present invention will be readily apparent to those skilled in the art, and it is intended that the appended claims cover all such modifications.

In summary, the present application relates to a method for introducing second cohesive powders into an improved fluidized bed mixer containing RO powder, and for mixing such second cohesive powders with the RO ^ powder in the fluidized bed mixer, and devices to carry out the procedure. The apparatus includes a manifold, an improved one that operates under pressure Vortex mill, a pneumatic conveyor system used in

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turbulent flow works, and an improved fluidized bed mixer. The method and the device enable the introduction and the even distribution of a second, cohesive, powdered component or such components with hydrophobic, hydrophilic or hygroscopic Properties in the fluidized bed mixer in the vicinity of the bottom of the fluidized bed in it while the mixing operation, whereby the entrainment of the mixture of the second powder is minimized and a homogeneous one Mixture of powders is obtained.

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Claims (15)

Πγ rer not Horct ^ rhnUr 6000 Frankfurt / Main 1, 5 · Febr · 1 98Ί Dr. rer. nat. Morst student Koiserstraße 4i Dr.s «h /» M / Da. PATENTANWALT phone (0611) 235555 Telex: 04-16759 mapat d 3104062 postal check account. 282420-602 Frankfurt M. Bank account: 225/0389 Deutsche Bank AG, Frankfurt / M. 8581-24NF-O4388 GENERAL ELECTRIC COMPANY 1 River Road Schenectady, N.Y./U.S.A. Claims 1. Method of mixing a mixture of powdered Components, characterized in that one (a) introduces a first powdered ingredient into a pressure-tight container, (b) building a fluidized bed of the first powdered ingredient in the container, and (c) into the container a second powdered ingredient under pressure by impacting the second powdered one Component on one, within the fluidized bed for evenly distributing the second component therein arranged baffle, introduces. 2. A method for mixing a mixture of pulverized ingredients according to claim 1, characterized , that he (a) crushing the second powdered ingredient in a powder mill, (b) the crushed mixture of the second powdered ingredient from the powder mill in the pressure-tight Container conveyed under pressure, and (c) the mixture of the crushed, second, pulverized 130061/043 4 Component on a baffle located within the fluidized bed of the first powdered component lets bounce and the mixture of the second powdered ingredient evenly in the one in the container contained mixture of the first pulverized component evenly distributed and thereby the mixture from mixes the first and second powdered ingredients homogeneously, 3. A method for mixing a mixture of powdered ingredients according to claim 1, characterized in that that he (a) introduces a gas into a manifold to initiate pressurization, (b) then feeds a mixture of a second powdered ingredient to the distributor, (c) the gas and the mixture of the second powdered ingredient mixes under pressure in the manifold, (d) the gas and the mixture of the second powdered ingredient conveyed under pressure into a powder mill and the mixture of the second powdered ingredient therein crushed, (e) the gas and the mixture of the crushed, second, pulverized Component transferred from the powder mill into the pressure-tight container, and (f) the mixture of the comminuted, second, pulverized ingredient on one, within the fluidized bed the first pulverized component arranged baffle can impact and the mixture of the second pulverized Ingredient in the mixture contained in the container of the first powdered ingredient evenly distributed and thereby the Gemenqe of the first and the second pulverized constituent mixes homogeneously. 130061/0434 4. The method according to any one of claims 1 to 3, characterized in that the powders are UO ₂ and a second pulverized component has hydrophobic, hydrophilic or hygroscopic properties, in which one (a) a powdered UO ^ component into a pressure-tight one Introduces container, (b) a fluidized bed of the powdered RO ^ component builds up in the pressure-tight container, and (c) the second powdered ingredient in the fluidized bed by introducing the second powdered ingredient evenly distributed under pressure in the container by placing the second powdered ingredient on a, baffle disposed within the fluidized bed, with the second powdered component selected from the group consisting of hydrophobic, hydrophilic and hygroscopic powdered materials is. 5. The method according to claim 4, characterized in that that the second powdered ingredient has an average particle size when introduced into the fluidized bed in the range from approximately 10 μm to approximately 60 μm (approximately 10 to approximately 60 microns). 6. The method according to any one of claims 4 and 5, characterized in that the second pulverized component when introduced into the fluidized bed an average particle size of approximately 15 μπ \ (15 microns). 7. The method according to any one of claims 1 to 6, characterized in that one 130061/0434 (a) builds a fluidized bed of a first powdered component in the pressure-tight container, the pressure in the container is in the range of approximately 1082.2 mbar (1 psig) to approximately 1358.0 mbar (5 psig); (b) a second powdered ingredient at a pressure in the range of approximately 1220.1 mbar (3 psig) to approximately 1358.0 mbar (5 psig) into the container upon impact of the second powdered ingredient introduces a baffle located within the fluidized bed, and (c) the pressure of the second powdered component due to the throttling and dividing action of the impact plate, which evenly distributes the second powdered ingredient in the fluidized bed, to 1151.2 mbar (2 psig) decreased, 8. The method according to any one of claims 1 to 7, characterized in that one (a) the mixture of the second pulverized component is comminuted in a vortex mill, (b) the ground, second, pulverized component from the vortex mill at a pressure of approximately 1254.6 mbar (3.5 psig) transported into the pressure-tight container, and (c) the mixture of the comminuted, second, powdered ingredient on one, within the fluidized bed of the first pulverized component arranged deflector plate can impact and the mixture of the second pulverized Ingredient in the mixture of the first powdered ingredient contained in the container uniformly distributed for homogeneous mixing of the mixture of the first and second pulverized ingredients. 130 0 81/0434 9. The method according to any one of claims 1 to 8, characterized in that one (a) a gas into a manifold to initiate pressurization the manifold at a pressure of approximately 2737.0 mbar (25 psig) (b) introducing a mixture of a second powdered ingredient into the manifold, (c) the gas and the mixture of the second powdered ingredient under a pressure of less than about Mixes 1358.0 mbar (5 psig) in the manifold, (d) the gas and the mixture of the second pulverized Component from the manifold at a pressure of approximately 1082.2 mbar (1 psig) to approximately 1220.1 mbar (3 psig) conveyed to the vortex mill and therein crushed the mixture of the second powdered ingredient, (e) the gas and the mixture of the crushed, second, pulverized component from the vortex mill into the pressure-tight container at a pressure in the range of approximately 1220.1 mbar (3 psig) to approximately 1358.0 mbar (5 psig) promotes, and (f) the mixture of the crushed, second, pulverized Component on a baffle positioned within the fluidized bed of the first powdered component can impact, and thereby the pressure at which it is contained in the mixture of in the container first powdered ingredient is distributed, for homogeneous mixing of the mixture of the first and second Constituent lowered to approximately 1151.2 mbar (2 psig). 10. The method according to claim 9, characterized in that one (a) the gas and the mixture of the second powdered ingredient 130061/0434 partly conveyed from the manifold into the vortex mill at a pressure of approximately 1151.2 mbar (2 psig) and in this the mixture of the second powdered component is crushed, and (b) the gas and the mixture of the crushed, second, pulverized Component from the vortex mill into the pressure-tight container at a pressure of approximately 1254.6 mbar (3.5 psig) transferred. 11. fluidized bed mixing device, characterized in that that they (a) a vertically oriented, pressure-tight mixing container (13), (b) means for introducing a first powdered ingredient into the mixing vessel, (c) a fluidized grate (14) for building up a fluidized bed in the mixing container, (d) at least one impact device (20) arranged above the vortex grate and including a deflector plate (21), and (e) means for introducing a second powdered ingredient into the impingement device under pressure and Directing the same onto a baffle, causing the second powdered ingredient in the fluidized bed of the the first powdered ingredient is divided evenly in the mixing container, contains. 12. The device according to claim 11, characterized in that that the impact device (20) spatially separated, upper (22) and lower (21) circular plates connected by a plurality of spatially separated, peripherally arranged struts (23) and the lower circular plate forms the baffle plate (21). - / 7 - 130061/0434 13. Device according to one of claims 11 and 12, characterized in that it (a) Conduit means for introducing the second pulverized one Component into the impact device (20) and directing the same onto the upper central surface of the Baffle (21), and (b) Support devices which move the impact device a predetermined distance above the grate (14) put in position, contains. 14. Device according to one of claims 11 to 13, characterized in that it has a lower Pressurized crusher to contain a mixture of gas and powdered ingredients Pressure effective to crush and mix the powdered ingredients and means for conducting the mixture of gas and components under pressure from the crushing device into the impact device, contains. 15. The device according to claim 14, characterized in that it (a) a distributor (12), (b) means (33) for introducing a gas under pressure into the manifold, (c) means (34) for introducing a powdered material into the manifold, (d) an internal mixing chamber for mixing the gas and pulverized material, and (e) outlet devices (35) for discharging the gas and the pulverized material into the comminution device, contains. 130061/0 434 J 6. Device according to one of claims 11 to 15, characterized in that it (A) a vertically oriented mixing container (13) with a vortex grate (14) arranged on the bottom thereof, (b) and containing a cage-like impact device (20) mounted within the vertically-oriented mixing vessel an inlet (26) for the supply of a mixture of a gas-fed pulverized material under pressure in the impact device, (c) conduit means (24) for conveying a gas and a mixture of a pulverized material below Pressure in the entrance of the impact device, (d) a vortex mill (11) effective for high pressure operation an outlet (25) for conveying a gas and a mixture of pulverized material under pressure from the Vortex mill to the line devices (36) which connect the vortex mill to the entrance of the impact device and an inlet for receiving a mixture of gas-pulverized material under pressure and devices for mixing and crushing (32) the pulverized material introduced therein, (e) a distributor (12) with a material feed inlet (34), a gas inlet (33), an inert mixing chamber for initially mixing a gas and a pulverized mixture of materials therein, and an outlet (35), (f) conduit means (36), which the entrance of the vortex mill with the distributor outlet for conveying the gas and the pulverized material mixture under pressure from the Connect the distributor to the vortex mill, and (g) means for a predetermined pressurization of the device, cmholds. 130061/0434