AU2006212416A2 - Method and apparatus for fluidizing a fluidized bed - Google Patents
Method and apparatus for fluidizing a fluidized bed Download PDFInfo
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- AU2006212416A2 AU2006212416A2 AU2006212416A AU2006212416A AU2006212416A2 AU 2006212416 A2 AU2006212416 A2 AU 2006212416A2 AU 2006212416 A AU2006212416 A AU 2006212416A AU 2006212416 A AU2006212416 A AU 2006212416A AU 2006212416 A2 AU2006212416 A2 AU 2006212416A2
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- Australia
- Prior art keywords
- pipeline
- vessel
- gas
- fluidized bed
- fluidizing
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J4/00—Feed or outlet devices; Feed or outlet control devices
- B01J4/001—Feed or outlet devices as such, e.g. feeding tubes
- B01J4/002—Nozzle-type elements
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/26—Nozzle-type reactors, i.e. the distribution of the initial reactants within the reactor is effected by their introduction or injection through nozzles
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1818—Feeding of the fluidising gas
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1872—Details of the fluidised bed reactor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/36—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed through which there is an essentially horizontal flow of particles
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Feeding, Discharge, Calcimining, Fusing, And Gas-Generation Devices (AREA)
- Polymerisation Methods In General (AREA)
Description
WO 2006/084682 PCT/EP2006/001113 Method and apparatus for fluidizing a fluidized bed The invention relates to a method for fluidizing a fluidized bed, which forms a fluidized bed of solid particles, in a vessel with a base by feeding a fluidizing gas into the fluidized bed via at least one pipe, and to an apparatus for carrying out this method.
Hitherto, fluidized beds have been fluidized by gas being supplied from below via open vertical holes, nozzle tubes with lateral holes with or without caps or porous plates (cf. "Handbook of Fluidization and Fluid-Particle Systems", Chapter 6: Gas Distributor and Plenum Design in Fluidized Beds pages 155-176, Ed. W.C. Yang, Dekker, New York, 2003).
In the case of cap type nozzles, even fluidizing is achieved by virtue of the fact that each cap nozzle is equipped with a high pressure loss by virtue of small cross sections of flow. The high velocities and multiple diverting of the gas flow makes it difficult for solids to penetrate backwards into the gas supply. Nevertheless, when the gas supply is switched off, residual fluidization often causes solids to penetrate into the cap, and these solids are not generally flushed out again when the apparatus is started up again, which can even cause the cap to become blocked.
Drainage measures then have to be undertaken, which represent an occupational safety problem in the case of processes carried out at a high temperature.
Porous plates or fabrics produce a very uniform fluidization but have the drawback that the porous medium becomes clogged over the course of time and cannot be fully cleaned again, or that the porous medium loses pressure loss over the course of time as a result of erosion. As in the case of the distributor equipped with caps or nozzles, it is necessary to provide for the possibility of emptying the space through which the gas flows at least for the eventuality of the fabric breaking. Moreover, the use temperature of the porous plates and in particular of the fabrics is limited.
It is known from DE 33 40 099 for gas to be introduced laterally upwards into the fluidized bed. However, in particular in this case the penetration of the solids occurs to an increased extent.
O Alternatively, the gas may be fed into the fluidized bed for example through pipes from the side (DE 40 07 835 C2). Even fluidizing requires a plurality of pipes, the ends of which are distributed evenly over the cross-sectional area. In addition, it Sis necessary to ensure that approximately the same volumetric flow of gas flows through each pipe. This is then achieved by each pipe being provided with a IDpressure loss which ensures that the gas is evenly distributed. In the case of nozzles which have hitherto been used for this purpose, the pressure loss is c achieved by a significant narrowing in the nozzle tip. This has the drawback of Shigh flow velocity in direct contact with solids, which generates turbulence, leads to erosion at the nozzle tip and mechanically stresses the particles in the fluidized 0bed.
It is also known to introduce a further medium with the aid of a gas stream designed as a jet nozzle (DE 102 37 124). In this case, however, the nozzle is not used for fluidization.
Therefore, it is an object of the invention to allow the uniform fluidizing of a fluidized bed without the possibility for parts of the gas feed to become blocked by the solids. In addition, it is intended to prevent erosion and/or particle fragmentation.
According to the present invention there is provided a method for fluidizing a fluidized bed of solid particles, in a vessel with a base by feeding a fluidizing gas into the fluidized bed via at least one pipeline, wherein the fluidizing gas is introduced into the vessel via the pipeline in the vicinity of the vessel base, characterized in that the gas flow in the pipeline is directed substantially continuously downwards and that a pressure loss is generated in the pipeline at a part of said pipeline above the maximum height up to which the solids could rise in the pipe.
According to the present invention there is also provided an apparatus for fluidizing a fluidized bed, having a vessel, to which solids are fed via a feed line and from which solids are removed via a discharge line, having a line system for feeding a fluidizing gas into the fluidized bed, and having an off-gas line for discharging the off-gas, characterized in that at least one pipeline for supplying N\Melboune\Cae\Patent\72000-72999\P72440.AU\Specia\P72440.AU GHSPEC first.doc 26/07/07 0 the fluidizing gas is introduced substantially continuously downwards into the vessel and in the vicinity of the vessel base has an opening for the outlet of the fluidizing gas, and in that a flow resistance which is arranged above the fluidized I bed is provided in the at least one pipeline.
I Advantageous embodiments of the invention are evident form the dependent claims.
cThe new form of fluidization is distinguished by the fact that the gas stream is S 10 guided continuously downwards from a distributor above the fluidized bed and Semerges from the pipe in the vicinity of the vessel base. According to a preferred configuration of the invention the pipe does not have any narrowings in the direction of flow below the maximum height up to which the solids could rise in the pipe, i.e. the pipe has a cross section which remains constant or widens downwards below this height.
The pressure loss required to make the fluidizing more uniform is in each pipe brought about by a flow resistance an orifice) which, however, in any event N\Melbourne\Caea\Patent\72000-72999\P72440.AU\Specia\P72440.AU GHSPEC first.doc 26/07/07 WO 2006/084682 PCT/EP2006/00I113 3 lies in a part of the individual pipe which remains free of solids. It is preferable for the flow resistance to be located outside the fluidizing space, so that it is readily accessible. According to the invention, the pressure loss in the flow resistance should amount to between 10 and 1500 mbar, preferably between 20 and 200 mbar.
The outlet velocity of the gas from the bottom end of the pipe depends on the sensitivity of the solids in the fluidized bed and its permissible stressing. If it is a sensitive, for example brittle, solid and fragmentation is undesirable, the velocity must be selected to be as low as possible. The outlet velocity should generally be between 2 and 50 m/s, preferably between 5 and 30 m/s.
To set the gas streams in all the pipes to be absolutely even, the pressure ratio across the orificecan be set to more than 2 to 1, i.e. the absolute pressure upstream of the orificeis at least double the absolute pressure downstream of the orifice. Consequently, sonic flow is reached in the narrowest cross section of the orifice. The sonic flow means that the volumetric flow in the pipe is accurately defined irrespective of the operating fluctuations and the outlet velocity at the bottom end of the pipe. The volumetric flows in the pipes may optionally also be determined in such a way that even a desired defined uneven distribution is achieved.
The pipes may be introduced vertically or at an angle to the horizontal. The angle is in this case more than 1' with respect to the horizontal, preferably more than 30' with respect to the horizontal. This makes it possible to prevent the pipes from becoming blocked, or else solids which have penetrated are easy to blow out again when the fluidizing is started up.
Irrespective of their introduction angle, the pipes are preferably cut off horizontally at the end, in order to enable the gas to flow out as far down as possible, i.e.
close to the base of the fluidized bed, generally at a distance of less than 250 mm, preferably a distance of less than 150 mm, from it.
To further improve the flow at the pipe outlet, the pipe end can be provided with a "detachment lug" on the top side, which reduces the erosion to the pipe caused by the flow. To reduce wear to the pipes, it is possible to select a wear-resistant material, e.g. stainless steel. Furthermore, it is possible to prevent wear to the WO 2006/084682 PCT/EP2006/001113 4 pipe end by means of a build-up weld.
This new design allows the gas distributor of the fluidized bed to be simple and inexpensive in form. Furthermore, the design prevents solids through-fall through the distributor.
To make it easy to optimize the operating performance of the fluidized bed, it is possible to configure the flow resistance as an exchangeable apertured orifice between two flanges. To further improve the ease of maintenance, it is additionally possible for the nozzle tubes themselves to be introduced into the vessel through connection pieces with flanges, in order to facilitate their replacement.
The method according to the invention is suitable for all fluidized beds, but in particular for those in which what is known as nozzle through-fall can very easily occur, for example if the particles are very small or remain in the fluidized state for a very long time after the fluidizing has been stopped.
The invention is explained in more detail below on the basis of exemplary embodiments and with reference to the drawing, in which all the features described and/or illustrated in figures form the subject matter of the invention, irrespective of the way in which they are combined in the claims or the way in which the claims are referred back. In the drawing: Fig. 1 shows an apparatus according to the invention for fluidizing a fluidized bed, Fig. 2a, b show alternative configurations of the pipe ends which open out above the vessel base, and Fig. 3 shows another embodiment of an apparatus according to the invention.
The apparatus for fluidizing a fluidized bed which is diagrammatically depicted in Fig. 1 comprises a vessel 1 into which solid particles are introduced via a feed line 2. The solid particles are, for example, heat-treated in the vessel 1 in a fluidized bed 3 and then discharged again from the vessel 1 via a discharge line 4. The off-gas produced is discharged via an off-gas line WO 2006/084682 PCT/EP2006/001113 The fluidized bed 3 is fluidized by supplying a fluidizing gas, the composition and properties, in particular temperature, of which depend on the desired treatment of the solid particles. The fluidizing gas is supplied via a line system 14 which divides the fluidizing gas, via a gas distributor (header) 6, between a plurality of pipes 7 distributed for example in the shape of a circle. In the embodiment illustrated in Fig. 1, the pipes 7 extend substantially vertically from above into the fluidized bed formed by the fluidized bed 3, and their respective outlet openings 8, which are cut off horizontally, open out into the fluidized bed 3 just above the base 9 of the vessel 1. The distance between the outlet openings 8 and the vessel base 9 is, for example, 100 or 200 mm.
In the pipes 7, an apertured orifice 10 is in each case provided as a flow resistance above the region which can be reached by the solid particles of the fluidized bed 3. The apertured orifice 10 is, for example, secured between two flanges 11, so that it can easily be replaced in order to optimize the operating properties and/or for maintenance or repair work. The passage opening of the apertured orifice 10 may be variable, in order to set the pressure loss and therefore the quality of even distribution of the gas. Given a sufficiently high admission pressure, the diameter of the apertured orifice 10 can alternatively be set in such a way that a pressure ratio of at least 2:1 is produced at the orifice, and sonic flow is achieved at the smallest cross section.
In the embodiment illustrated, the apertured orifices 10 lie outside the vessel 1.
However, they may also be arranged inside it, provided that it is ensured that the solid particles cannot rise up as far as the flow resistance and block it and/or cause wear to it.
Instead of the vertical arrangement of the pipes 7 illustrated in Fig. 1, the pipes 7 may also be inclined. Fig. 2a and 2b illustrate examples of an inclined pipe arrangement of this type, in which the pipes 7a and 7b are at an angle of approx.
with respect to the horizontal.
To increase the resistance to erosion with regard to the gas flow, the pipe cross section is thickened in the region of the outlet opening 8a or 8b. In the embodiment shown in Fig. 2a, in this case a material thickening produced for example by a build-up weld 12 is provided around the opening region of the pipe 7a.
WO 2006/084682 PCT/EP2006/001113 6 By contrast, in the variant shown in Fig. 2b, there is merely a "detachment lug" 13 provided at the top side, since the gas in any case rises upwards and is guided away from the pipe 7b by the detachment lug 13.
When using the apparatus shown in Fig. 1 (or the variants shown in Fig. 2a or 2b), fluidizing gas is introduced into the fluidized bed 3 through the pipes 7 and fluidizes the solid particles. The pressure loss brought about by the flow resistance produces even fluidizing, while it is ensured that the solid particles cannot rise up as far as the flow resistance and block the pipe 7.
Fig. 3 shows another example of the use of the fluidizing method according to the invention for solid conveying in what are known as "airlift sending pots". An airlift system is used for the pneumatic conveying of 100 t/h of aluminium hydrate with grain diameters of between 30 and 170 im over a height of approx. 60m. The airlift sending pot 20 shown in Fig. 3 is for this purpose used to feed the conveying. The vessel 21 has a diameter of 1200 mm with a centrally arranged conveying pipe 22 with a diameter of 400 mm. A conveying air stream of approx.
6000 m3/h is passed through the central nozzle 23 and carries the solids with it. To achieve even conveying, the surrounding solids have to be fluidized, so that they can always flow sufficiently into the region of the central nozzle 23. This requires a fluidizing gas flow of 300 m 3 /h The vessel is fluidized via pipe nozzles 24 (nominal width the bottom ends of which are arranged in two concentric rings of different diameters, so that the annular space between conveying pipe 22 and vessel wall 25 is uniformly supplied with air. The fluidizing pipes 24 are supplied with air from a common distributor 26 which lies above the region which can be loaded with solids. In each pipe 24, there is an orifice 27 just below the distributor 26, which with a pressure loss of 150 mbar is designed in such a way that each pipe 24 receives virtually the same volumetric flow of air.
Surprisingly, it has been found that this form of fluidizing is superior to standard bottom fluidization with a porous fabric in terms of the evenness of solids conveying. It is virtually impossible for the fluidizing pipes to become blocked. There is no need for the standard emptying measures.
WO 2006/084682 PCT/EP2006/001113 -7- List of reference numbers 1 Vessel 2 Introduction line for solids 3 Fluidized bed 4 Discharge line for solids Off-gas line 6 Gas distributor 7 Pipe 8 Outlet opening 9 Vessel base Apertured orifice 11 Flange 12 Build-up weld 13 Detachment lug 14 Line system Airlift sending pot 21 Vessel 22 Conveying pipe 23 Central nozzle 24 Fluidizing pipe Vessel wall 26 Distributor 27 Orifice
Claims (22)
1. Method for fluidizing a fluidized bed of solid particles, in a vessel with a O base by feeding a fluidizing gas into the fluidized bed via at least one pipeline, (N wherein the fluidizing gas is introduced into the vessel via the pipeline in the \N vicinity of the vessel base, characterized in that the gas flow in the pipeline is directed substantially continuously downwards and that a pressure loss is c generated in the pipeline at a part of said pipeline above the maximum height up Sto which the solids could rise in the pipe. \O
2. Method according to Claim 1, characterized in that a pressure loss is (,i generated in the pipeline above the fluidized bed in which the solid is fluidized in the vessel.
3. Method according to Claim 2, characterized in that the pressure loss can be selected according to the demands imposed on the quality of even distribution of the gas between the pipelines.
4. Method according to Claim 2 or 3, characterized in that the pressure loss in the pipeline amounts to between 10 and 1500 mbar.
Method according to Claim 4, characterized in that the pressure loss in the pipeline is between 20 and 200 mbar.
6. Method according to any one of Claims 2 to 5, characterized in that the pressure loss in the pipeline is generated by a flow resistance, and in that the flow velocity in the narrowest cross section of the pipeline is equal to the speed of sound.
7. Method according to any one of Claims 2 to 6, characterized in that the pressure loss in the pipeline is generated by a flow resistance, and in that the pressure ratio at the flow resistance is 2:1, based on the absolute pressures upstream and downstream of the flow resistance.
8. Method according to any one of the preceding claims, characterized in that the volumetric flows in the pipes are set in such a way that a defined uneven N:\Melbourne\Cases\Patent\72000-72999\P7240.AU\SpeciS\P72440.AU GHSPEC firsidoc 26/07/07 0 distribution of the fluidizing gas introduced into the vessel is produced. N
9. Method according to any one of the preceding claims, characterized in I that the outlet velocity of the fluidizing gas from the pipeline is between 2 and 50 m/s. Method according to Claim 9, characterized in that the outlet velocity of N the fluidizing gas from the pipeline is between 5 and 30 m/s.
S 10
11. Apparatus for fluidizing a fluidized bed, having a vessel, to which solids are 0 fed via a feed line and from which solids are removed via a discharge line, having a line system for feeding a fluidizing gas into the fluidized bed, and having an off-gas line for discharging the off-gas, in particular for carrying out a method according to any one of the preceding claims, characterized in that at least one pipeline for supplying the fluidizing gas is introduced substantially continuously downwards into the vessel and in the vicinity of the vessel base has an opening for the outlet of the fluidizing gas, and in that a flow resistance which is arranged above the fluidized bed is provided in the at least one pipeline.
12. Apparatus according to Claim 11, characterized in that the flow resistance is attached by means of a flanged connection in the pipeline.
13. Apparatus according to Claim 11 or 12, characterized in that the flow resistance is formed by an orifice.
14. Apparatus according to any one of Claims 11 to 13, characterized in that the pipeline has an angle of inclination with respect to the horizontal of from 1 to or is greater than or equal to approx.
15. Apparatus according to any one of Claims 11 to 14, characterized in that the pipeline does not have any narrowing below the region which can be reached by the solids.
16. Apparatus according to any one of Claims 11 to 15, characterized in that the pipeline has a horizontal outlet opening at its open end. N.\Melbourne\Casea\Patent\72000-72999\P72440.AU\Specia\P72440.AU CHSPEC firot.doc 26/07/07
17. Apparatus according to any one of Claims 11 to 16, characterized in that the outlet opening of the pipeline is arranged 250 mm, or less than 150 mm, Sabove the vessel base. (N
18. Apparatus according to any one of Claims 11 to 17, characterized in that I the pipeline, in the region of its outlet opening, has an outer material thickening, in particular a build-up weld. c
19. Apparatus according to any one of Claims 11 to 18, characterized in that S 10 in the region of its outlet opening the pipeline has an in particular upwardly directed detachment lug.
Apparatus according to any one of Claims 11 to 19, characterized in that the pipeline is attached to the vessel by means of flange connection pieces provided on the vessel.
21. Apparatus according to any one of Claims 11 to 20, characterized in that a plurality of pipelines are provided in the vessel, distributed in the shape of a circle.
22. Apparatus according to Claim 21, characterized in that the pipelines are provided distributed on a plurality of preferably concentric circles within the vessel. N,\Melbourne\Cases\Patelfl\7200-72999\P72440.AU\Speci8\P72440.AU GHSPEC first.doc 26/07/07
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE102005006570.8A DE102005006570B4 (en) | 2005-02-11 | 2005-02-11 | Method and device for fluidizing a fluidized bed |
| DE102005006570.8 | 2005-02-11 | ||
| PCT/EP2006/001113 WO2006084682A1 (en) | 2005-02-11 | 2006-02-08 | Method and apparatus for fluidizing a fluidized bed |
Publications (4)
| Publication Number | Publication Date |
|---|---|
| AU2006212416A2 true AU2006212416A2 (en) | 2006-08-17 |
| AU2006212416A1 AU2006212416A1 (en) | 2006-08-17 |
| AU2006212416A8 AU2006212416A8 (en) | 2006-08-17 |
| AU2006212416B2 AU2006212416B2 (en) | 2011-03-17 |
Family
ID=36021845
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| AU2006212416A Active AU2006212416B2 (en) | 2005-02-11 | 2006-02-08 | Method and apparatus for fluidizing a fluidized bed |
Country Status (7)
| Country | Link |
|---|---|
| CN (1) | CN101115552B (en) |
| AU (1) | AU2006212416B2 (en) |
| BR (1) | BRPI0608239B8 (en) |
| DE (1) | DE102005006570B4 (en) |
| MY (1) | MY146065A (en) |
| RU (1) | RU2410154C2 (en) |
| WO (1) | WO2006084682A1 (en) |
Families Citing this family (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102268559A (en) | 2007-05-21 | 2011-12-07 | 奥贝特勘探Vspa有限公司 | Processes for extracting aluminum and iron from aluminous ores |
| CN101920177A (en) * | 2010-08-31 | 2010-12-22 | 北京矿冶研究总院 | Aerating device and reactor comprising same |
| AU2012231686B2 (en) | 2011-03-18 | 2015-08-27 | Aem Technologies Inc. | Processes for recovering rare earth elements from aluminum-bearing materials |
| US9410227B2 (en) | 2011-05-04 | 2016-08-09 | Orbite Technologies Inc. | Processes for recovering rare earth elements from various ores |
| WO2012162817A1 (en) | 2011-06-03 | 2012-12-06 | Orbite Aluminae Inc. | Methods for preparing hematite |
| WO2013037054A1 (en) | 2011-09-16 | 2013-03-21 | Orbite Aluminae Inc. | Processes for preparing alumina and various other products |
| RU2016104423A (en) | 2012-01-10 | 2018-11-22 | Орбит Текнолоджис Инк. | METHODS FOR PROCESSING RED SLUR |
| CA2862307C (en) | 2012-03-29 | 2015-12-01 | Orbite Aluminae Inc. | Processes for treating fly ashes |
| BR112015000626A2 (en) | 2012-07-12 | 2017-06-27 | Orbite Aluminae Inc | processes for preparing titanium oxide and other miscellaneous products |
| US9353425B2 (en) | 2012-09-26 | 2016-05-31 | Orbite Technologies Inc. | Processes for preparing alumina and magnesium chloride by HCl leaching of various materials |
| CA2891427C (en) | 2012-11-14 | 2016-09-20 | Orbite Aluminae Inc. | Methods for purifying aluminium ions |
| DE102013005921A1 (en) * | 2013-04-03 | 2014-10-09 | Glatt Ingenieurtechnik Gmbh | Fluidisierungsapparat |
Family Cites Families (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3298793A (en) * | 1963-04-04 | 1967-01-17 | Badger Co | Fluid bed diffusion |
| US3451784A (en) * | 1965-10-28 | 1969-06-24 | Lummus Co | Fluidized bed reactor |
| US3933445A (en) * | 1973-10-15 | 1976-01-20 | Exxon Research And Engineering Company | Process and apparatus for preventing deposits on a gas inlet nozzle |
| DE2658371C2 (en) * | 1976-12-23 | 1983-03-03 | Carl Robert Eckelmann AG, 2000 Hamburg | Process for pyrolyzing old tires |
| NL185896C (en) * | 1979-01-08 | 1990-08-16 | Bpb Industries Ltd | DEVICE FOR HEAT TREATMENT OF A GRANULAR MATERIAL. |
| DE3234911A1 (en) * | 1982-09-21 | 1984-03-22 | Herbert 7853 Steinen Hüttlin | FLUID BED APPARATUS |
| US5017536A (en) * | 1984-02-03 | 1991-05-21 | Phillips Petroleum Company | Catalyst regeneration including method of introducing oxygen into fluidized bed |
| DE3523653A1 (en) * | 1985-07-02 | 1987-02-12 | Bbc Brown Boveri & Cie | FLUIDIZED LAYER REACTOR |
| JPH07104105B2 (en) * | 1987-03-17 | 1995-11-13 | 株式会社小松製作所 | Flow homogenization method for long-axis fluidized bed furnace |
| GB8810390D0 (en) * | 1988-05-03 | 1988-06-08 | Shell Int Research | Apparatus & process for exchanging heat between solid particles & heat exchange medium |
| US5549815A (en) * | 1994-05-20 | 1996-08-27 | Exxon Research And Engineering Company | Method for fluidizing a dense phase bed of solids |
| US6991767B1 (en) * | 2000-09-18 | 2006-01-31 | Procedyne Corp. | Fluidized bed gas distributor system for elevated temperature operation |
| DE10232789A1 (en) * | 2002-07-18 | 2004-02-05 | Vinnolit Technologie Gmbh & Co.Kg Werk Gendorf | Device for introducing gas into a fluid bed and method therefor |
-
2005
- 2005-02-11 DE DE102005006570.8A patent/DE102005006570B4/en active Active
-
2006
- 2006-02-08 WO PCT/EP2006/001113 patent/WO2006084682A1/en not_active Application Discontinuation
- 2006-02-08 BR BRPI0608239A patent/BRPI0608239B8/en active IP Right Grant
- 2006-02-08 CN CN2006800045203A patent/CN101115552B/en active Active
- 2006-02-08 RU RU2007133826/05A patent/RU2410154C2/en active
- 2006-02-08 AU AU2006212416A patent/AU2006212416B2/en active Active
- 2006-02-09 MY MYPI20060565A patent/MY146065A/en unknown
Also Published As
| Publication number | Publication date |
|---|---|
| BRPI0608239A2 (en) | 2009-11-24 |
| BRPI0608239B8 (en) | 2023-03-28 |
| DE102005006570B4 (en) | 2014-07-10 |
| AU2006212416B2 (en) | 2011-03-17 |
| DE102005006570A1 (en) | 2006-08-24 |
| RU2007133826A (en) | 2009-03-20 |
| AU2006212416A1 (en) | 2006-08-17 |
| BRPI0608239B1 (en) | 2016-03-08 |
| CN101115552A (en) | 2008-01-30 |
| CN101115552B (en) | 2010-09-08 |
| RU2410154C2 (en) | 2011-01-27 |
| WO2006084682A1 (en) | 2006-08-17 |
| AU2006212416A8 (en) | 2006-08-17 |
| MY146065A (en) | 2012-06-29 |
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