CN104096518B - A kind of multi-cell fluidized bed reactor - Google Patents
A kind of multi-cell fluidized bed reactor Download PDFInfo
- Publication number
- CN104096518B CN104096518B CN201310119439.1A CN201310119439A CN104096518B CN 104096518 B CN104096518 B CN 104096518B CN 201310119439 A CN201310119439 A CN 201310119439A CN 104096518 B CN104096518 B CN 104096518B
- Authority
- CN
- China
- Prior art keywords
- goods
- flow
- fluidized bed
- chamber
- bed reactor
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Landscapes
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The present invention relates to a kind of multi-cell fluidized bed reactor, granule materials can be realized by upstream chamber fast, flow to downstream chamber high flux, avoid the granule materials back-mixing between adjacent chamber simultaneously and collaborate.Described multi-cell fluidized bed reactor is made up of air inlet (1), air outlet (2), charging aperture (3), discharging opening (4), air compartment (5), air distribution plate (6), fluidising chamber (7) and n Flow of Goods and Materials controller (8), n >=1, wherein Flow of Goods and Materials controller (8) is made up of dividing plate (9), aperture (10), the descending flow duct of material (11) and bottom baffle (12).Fluidized-bed reactor is divided into n+1 secondary fluidising chamber by dividing plate, and air inlet is connected to air compartment, and air outlet is connected to the top of fluidising chamber, and charging aperture is connected to the 1st secondary fluidising chamber, and discharging opening is connected to the (n+1)th secondary fluidising chamber.
Description
Technical field
The present invention relates to a kind of multicell fluidizing apparatus, particularly, relate to a kind of multi-cell fluidized bed reactor.
Background technology
Fluidizing reactor has heat transfer, mass transfer, feature that momentum transfer efficiency is high, is a kind of heterophase reactor efficiently, has been widely used in the chemical field such as heterogeneous catalysis, powder processing at present.Another principal character of fluidizing reactor is that the material in reative cell is in complete mixed state, and the unreacted material of part can be followed product and is discharged, and therefore the fluidized-bed reactor of single chamber is not suitable for producing highly purified product.
In multi-cell fluidized bed, single reative cell endoparticle material is in complete mixed state, and granule materials sequentially flows between adjacent reaction room.In general, the charge level height of upstream chamber is greater than the charge level height of downstream chamber, and the barometric gradient that difference in height is formed is promoted granule materials and flowed to downstream chamber by mass transport hole.The one-way flow of granule materials between adjacent chamber makes residence time destribution narrow, the conversion profile of granule materials also will narrow, but, pressure oscillation can cause the reverse flow of granule materials, formed " back-mixing ", so, the conversion profile of granule materials will broaden, and be unfavorable for controlling reaction process.Therefore, the back-mixing of granule materials between adjacent chamber is suppressed to be very necessary by design mass transport hole.
BP GB2167679A discloses a series of multichamber type fluid bed reaction apparatus, provide setting and the perforate mode of multiple vertical baffle, comprise bottom perforate, top perforate, up and down dislocation perforate etc., granule materials can be controlled and flow to different directions.But the perforate on the dividing plate that this patent provides is only the intercommunicating pore of simple shape, material is still by intercommunicating pore back-mixing.
Chinese patent CN101947421A discloses a kind of multi-cell fluidized bed be split to form by the vertical baffle of different perforate height, and the baffle plate position of opening of each room sequentially reduces, charge level also sequentially reduces, and has the effect of certain suppression back-mixing.But when charge level drop is less, suppress the effect of back-mixing not obvious; When charge level drop is larger, the pressure drop drop between each room is large, is unfavorable for stable operation on the one hand, and the space availability ratio of fluid bed reduces greatly on the other hand.Such as, when existence 8 rooms, the charge level drop between room is 200mm, and total charge level drop then reaches 1.6m.
European patent EP 1072855A1 discloses a kind of multicell Splittable fluidized-bed reaction stove, clearly determine the parameters such as the distance between the length of intercommunicating pore and nozzle, the bank lamination inner at intercommunicating pore and two ends formation is thicker, back-mixing between effective suppression adjacent chamber, but this kind of structure limits the transport fluxes (particle transport speed < 500mm/s) of granule materials, when larger transport fluxes need be reached, charge level drop between adjacent chamber is comparatively large, and the space availability ratio of fluidized-bed reactor significantly reduces.
Therefore, need to develop a kind of multi-cell fluidized bed reactor, it can realize granule materials by upstream chamber fast, flow to downstream chamber high flux, can avoid again the granule materials back-mixing between adjacent chamber and collaborate.
Summary of the invention
In view of the technical problem existed in prior art, the object of this invention is to provide a kind of multi-cell fluidized bed reactor, it can realize granule materials by upstream chamber fast, flow to downstream chamber high flux, can avoid again the granule materials back-mixing between adjacent chamber and collaborate.
In order to achieve the above object, the present invention is achieved through the following technical solutions: a kind of multi-cell fluidized bed reactor, be made up of air inlet (1), air outlet (2), charging aperture (3), discharging opening (4), air compartment (5), air distribution plate (6), fluidising chamber (7) and n Flow of Goods and Materials controller (8), wherein n >=1, each Flow of Goods and Materials controller (8) comprises dividing plate (9), aperture (10), the descending flow duct of material (11) and bottom baffle (12); Fluidising chamber (7) is divided into n+1 secondary fluidising chamber by the dividing plate (9) in wherein said n Flow of Goods and Materials controller (8).Air inlet (1) is connected to air compartment, air outlet (2) is connected to the top of fluidising chamber, charging aperture (3) is connected to the 1st secondary fluidising chamber, and discharging opening (4) is connected to the (n+1)th secondary fluidising chamber being positioned at the other end relative with the 1st secondary fluidising chamber.
The shape of multi-cell fluidized bed reactor of the present invention, the quantity of fluidising chamber, the sequence of flow of material between reative cell are unrestricted, and technical staff can select according to treating capacity, technological requirement etc.
Multi-cell fluidized bed reactor provided by the present invention, granule materials sequentially passes through each reative cell under the control of Flow of Goods and Materials controller (8).In the present invention, as shown in Figure 1, in figure, arrow represents flow direction of material to a kind of generalized section of multi-cell fluidized bed reactor of rectangle structure; In the multi-cell fluidized bed of another kind of circular configuration, the dividing method of each secondary chamber and flow direction of material are as shown in Figure 2; The structure of Flow of Goods and Materials controller provided by the present invention as shown in Figure 3.
The shape of the present invention to aperture does not limit, and such as, can adopt semicircle, square.Technical staff can determine the area in aperture according to granule material flow, orifice area should be less than 1/10 of the area of its place dividing plate, preferably, is less than 1/20 of the area of dividing plate.
The shape of the present invention to the descending flow duct of material does not limit, and such as, can adopt semi-circular tube, square tube.Technical staff can according to the sectional area of the descending flow duct of granule material flow determination material and height, and the sectional area of the descending flow duct of material should be less than 1/3 of the sectional area of its place secondary fluidising chamber, preferably, is less than 1/5 of the sectional area of secondary fluidising chamber; The height of the descending flow duct of material should be less than charge level height in secondary fluidising chamber and be greater than 1/5 of charge level height, preferably, is greater than 1/2 of charge level height.
In multi-cell fluidized bed reactor of the present invention, the bottom baffle of Flow of Goods and Materials controller can adopt porous plate or imperforate plate.When adopting porous plate, the percent opening of bottom baffle is less than 5/N, preferably, is less than 2/N, and wherein N is fluidization number, N=U
o/ U
mf, U
osuperficial gas velocity, U
mfit is minimum fluidization velocity.(namely bottom baffle part is in upstream chamber, upstream secondary fluidising chamber), (namely part is in downstream chamber, downstream secondary fluidising chamber), as shown in Figure 3, the area of upper housing portion equals the sectional area of the descending flow duct of material, and the area of downstream chamber's part should be less than 1.5 times of the area of upper housing portion.In the present invention, " upstream " and " downstream " is relative to material moving direction (such as, in Fig. 1 and Fig. 2, arrow is shown).
In a preferred embodiment of multi-cell fluidized bed reactor of the present invention, in each Flow of Goods and Materials controller, gas speed is less than or equal to the minimum fluidization velocity of material, and the granule materials in the descending flow duct of material is in close phase stacking states, forms the unidirectional two-phase transportation stream of granule materials.The porosity of the descending flow duct of material, lower than the porosity of its place secondary fluidising chamber, thus produces higher Flow of Goods and Materials motive force, granule materials can be delivered to high pressure secondary fluidising chamber by low-pressure secondary fluidising chamber.
In a preferred embodiment of multi-cell fluidized bed reactor of the present invention, the material reserve in the descending flow duct of material in each Flow of Goods and Materials controller and Flow of Goods and Materials motive force be reinforcement with granule material flow reinforcement.
In a preferred embodiment of multi-cell fluidized bed reactor of the present invention, by changing the charge level height of the Altitude control fluidising chamber of the descending flow duct of material in Flow of Goods and Materials controller.Because the Flow of Goods and Materials controller in the present invention has higher Flow of Goods and Materials motive force, when charge level height higher than upstream chamber of the height of the descending flow duct of material in downstream chamber, also continuous print, high-throughout mass transport can be realized, now, downstream chamber's charge level height is by the Altitude control of the descending flow duct of material wherein, by higher than the height equaling the descending flow duct of material, also simultaneously higher than upstream chamber.Schematic diagram as shown in Figure 4.
Multi-cell fluidized bed reactor of the present invention is applicable to the powder processing in the industry such as chemical industry, metallurgy, such as, for the production of high-purity powder product; Multi-cell fluidized bed reactor of the present invention is also applicable to catalytic industries, such as, for the reaction of making charcoal of decaying catalyst, significantly can reduce the probability that the lower catalyst granules of the rate of making charcoal is admitted to reactor, improves overall efficiency of making charcoal.
Compared with prior art scheme, the present invention has following beneficial effect:
1, the gas speed in the descending flow duct of material in multi-cell fluidized bed reactor of the present invention is less than or equal to the minimum fluidization velocity of granule materials, therefore granule materials is in close phase stacking states, define the unidirectional two-phase transportation stream of granule materials, avoid the material back-mixing between adjacent chamber, inhibit the string wind between adjacent chamber.
2, multi-cell fluidized bed reactor of the present invention, the Flow of Goods and Materials motive force produced by granule materials pressure in the descending flow duct of material increases with granule material flow and increases, there is self-regulating function, stable granule materials two-phase transportation stream can be obtained adaptively.
3, multi-cell fluidized bed reactor of the present invention, can by the charge level height of its place fluidising chamber of Altitude control of the descending flow duct of material, therefore, when the descending flow duct height of the material in downstream chamber is higher than upstream chamber charge level height, downstream chamber's charge level height will higher than upstream chamber.
Accompanying drawing explanation
Fig. 1 is the schematic diagram of an embodiment of the multi-cell fluidized bed reactor of rectangle structure of the present invention, and wherein top is the longitudinal sectional view of multi-cell fluidized bed, and below is the top view along A-A line;
Fig. 2 is the schematic top plan view of an embodiment of the multi-cell fluidized bed reactor of circular configuration of the present invention;
Fig. 3 is the schematic diagram of an embodiment of Flow of Goods and Materials controller in multi-cell fluidized bed reactor of the present invention, and wherein left is longitudinal sectional view, and right is the top view along B-B line;
Fig. 4 is the schematic diagram that Flow of Goods and Materials controller of the present invention controls an embodiment of fluidising chamber's charge level height.
Reference numeral in accompanying drawing is as follows:
1-air inlet; 2-air outlet; 3-charging aperture; 4-discharging opening; 5-air compartment; 6-air distribution plate; 7-fluidising chamber; 8-Flow of Goods and Materials controller; 9-dividing plate; 10-aperture; The descending flow duct of 11-material; 12-bottom baffle; 12a-bottom baffle upper housing portion; 12b-bottom baffle downstream chamber part; 13-charge level height schematic lines.
The present invention is described in more detail below.But following example is only simple and easy example of the present invention, does not represent or limits the scope of the present invention, and interest field of the present invention is as the criterion with claims.
Detailed description of the invention
Fig. 1 is the generalized section of an embodiment of multi-cell fluidized bed reactor of the present invention, and this multi-cell fluidized bed reactor is rectangle structure, and wherein granule materials sequentially presses arrow direction indication by each reative cell under the effect of Flow of Goods and Materials controller; Fig. 2 is the generalized section of another embodiment of multi-cell fluidized bed reactor of the present invention, and this multi-cell fluidized bed reactor is circular configuration, and wherein granule materials sequentially presses arrow direction indication by each reative cell under the effect of Flow of Goods and Materials controller.As shown in Figure 3, Flow of Goods and Materials controller is made up of dividing plate, aperture, the descending flow duct of material and bottom baffle the generalized section of Flow of Goods and Materials controller of the present invention.In Fig. 3, B-B sectional view shows the schematic top plan view of an embodiment of bottom baffle, and this bottom baffle is porous plate.
For better the present invention being described, be convenient to understand technical scheme of the present invention, typical but non-limiting embodiment of the present invention is as follows:
Embodiment 1
A kind of rectangle multi-cell fluidized bed reactor, be made up of air inlet, air outlet, charging aperture, discharging opening, air compartment, air distribution plate, fluidising chamber and 4 wherein built-in Flow of Goods and Materials controllers, 4 pieces of dividing plates are arranged in parallel, fluidized-bed reactor is divided into from left to right 5 secondary chamber, air inlet is connected to air compartment, and air outlet is connected to the top of fluidising chamber, and charging aperture is connected to the 1st secondary fluidising chamber, discharging opening is connected to the 5th secondary fluidising chamber, and material sequentially flows from left to right.Flow of Goods and Materials controller is made up of dividing plate, aperture, the descending flow duct of material and bottom baffle.Aperture on dividing plate is square, and orifice area is 1/20 of dividing plate area.The descending flow duct of material is semi-circular tube, and sectional area equals the area in aperture, and height is 1/2 of charge level height in secondary fluidising chamber.Bottom baffle is porous plate, and percent opening is 1/N, and the area of downstream chamber's part equals the area of upper housing portion.
Embodiment 2
A kind of rectangle multi-cell fluidized bed reactor, be made up of air inlet, air outlet, charging aperture, discharging opening, air compartment, air distribution plate, fluidising chamber and 3 pieces of wherein built-in dividing plates, 3 pieces of dividing plates are arranged in parallel, fluidized-bed reactor is divided into from left to right 4 secondary chamber, air inlet is connected to air compartment, and air outlet is connected to the top of fluidising chamber, and charging aperture is connected to the 1st secondary fluidising chamber, discharging opening is connected to the 4th secondary fluidising chamber, and material sequentially flows from left to right.Flow of Goods and Materials controller is made up of dividing plate, aperture, the descending flow duct of material and bottom baffle.Aperture on dividing plate is square, and orifice area is 1/10 of dividing plate area.The descending flow duct of material is square tube, and sectional area is 1/5 of its place secondary fluidising chamber sectional area, is highly slightly less than charge level height in secondary fluidising chamber.Bottom baffle is imperforate plate, and the area of downstream chamber's part is 1/2 of upper housing portion.
Embodiment 3
A kind of rectangle multi-cell fluidized bed reactor, be made up of air inlet, air outlet, charging aperture, discharging opening, air compartment, air distribution plate, fluidising chamber and 2 pieces of wherein built-in dividing plates, 2 pieces of dividing plates are arranged in parallel, fluidized-bed reactor is divided into from left to right 3 secondary chamber, air inlet is connected to air compartment, and air outlet is connected to the top of fluidising chamber, and charging aperture is connected to the 1st secondary fluidising chamber, discharging opening is connected to the 3rd secondary fluidising chamber, and material sequentially flows from left to right.Flow of Goods and Materials controller is made up of dividing plate, aperture, the descending flow duct of material and bottom baffle.Aperture on dividing plate is semicircle, and orifice area is 1/10 of dividing plate area.The descending flow duct of material is semi-circular tube, and sectional area is 1/3 of its place secondary fluidising chamber sectional area.In 2nd secondary fluidising chamber, the height of the descending flow duct of material is about 200mm higher than the 1st secondary fluidising chamber charge level, and the 2nd secondary fluidising chamber charge level is about 200mm higher than the 1st secondary fluidising chamber, and the 3rd secondary fluidising chamber charge level height is suitable with the 2nd secondary fluidising chamber.Bottom baffle is porous plate, and percent opening is 5/N, and the area of downstream chamber's part is 1/2 of upper housing portion.
Embodiment 4
A kind of circular multi-cell fluidized bed reactor, be made up of air inlet, air outlet, charging aperture, discharging opening, air compartment, air distribution plate, fluidising chamber and 3 Flow of Goods and Materials controllers wherein (containing 3 pieces of dividing plates), 1 piece of dividing plate, 4 pieces of dividing plate segmentation fluid beds form 4 secondary chamber, air inlet is connected to air compartment, air outlet is connected to the top of fluidising chamber, charging aperture is connected to the 1st secondary fluidising chamber, and discharging opening is connected to the 4th secondary fluidising chamber, and material is along sequentially flowing counterclockwise.Flow of Goods and Materials controller is made up of dividing plate, aperture, the descending flow duct of material and bottom baffle.Aperture on dividing plate is semicircle, and orifice area is 1/10 of dividing plate area.The descending flow duct of material is semi-circular tube, and sectional area equals the area in aperture, is highly slightly less than the charge level height of secondary fluidising chamber.Bottom baffle is porous plate, and percent opening is 2/N, and the area of downstream chamber's part is 1.5 times of upper housing portion.
Embodiment 5
A kind of circular multi-cell fluidized bed reactor, be made up of air inlet, air outlet, charging aperture, discharging opening, air compartment, air distribution plate, fluidising chamber and 3 Flow of Goods and Materials controllers wherein (containing 3 pieces of dividing plates), 1 piece of dividing plate, 4 pieces of dividing plate segmentation fluid beds form 4 secondary chamber, air inlet is connected to air compartment, air outlet is connected to the top of fluidising chamber, charging aperture is connected to the 1st secondary fluidising chamber, and discharging opening is connected to the 4th secondary fluidising chamber, and material is along sequentially flowing counterclockwise.Flow of Goods and Materials controller is made up of dividing plate, aperture, the descending flow duct of material and bottom baffle.Aperture on dividing plate is semicircle, and orifice area is 1/25 of dividing plate area.The descending flow duct of material is square tube, and sectional area is 1/7 of its place secondary fluidising chamber sectional area, and height is 1/4 of the charge level height of secondary fluidising chamber.Bottom baffle is porous plate, and percent opening is 1/2N, and the area of downstream chamber's part is 1/3 of upper housing portion.
The present invention illustrates detailed construction feature of the present invention by above-described embodiment, but the present invention is not limited to above-mentioned detailed construction feature, does not namely mean that the present invention must rely on above-mentioned detailed construction feature and could implement.Person of ordinary skill in the field should understand, any improvement in the present invention, to equivalence replacement and the increase of accessory, the concrete way choice etc. of parts selected by the present invention, all drops within protection scope of the present invention and open scope.
Claims (14)
1. a multi-cell fluidized bed reactor, it is characterized in that, described multi-cell fluidized bed reactor comprises air inlet (1), air outlet (2), charging aperture (3), discharging opening (4), air compartment (5), air distribution plate (6), fluidising chamber (7) and n Flow of Goods and Materials controller (8), wherein n >=1; Each Flow of Goods and Materials controller (8) comprises dividing plate (9), aperture (10), the descending flow duct of material (11) and bottom baffle (12); Fluidising chamber (7) is divided into n+1 secondary fluidising chamber by the dividing plate (9) in wherein said n Flow of Goods and Materials controller (8), granule materials sequentially via each Flow of Goods and Materials controller (8) by each secondary fluidising chamber; Air inlet (1) is connected to air compartment (5), air outlet (2) is connected to the top of fluidising chamber (7), charging aperture (3) is connected to the 1st secondary fluidising chamber, and discharging opening (4) is connected to the (n+1)th secondary fluidising chamber.
2. multi-cell fluidized bed reactor as claimed in claim 1, it is characterized in that, the area in the aperture (10) in each Flow of Goods and Materials controller (8) is less than or equal to 1/10 of place, described aperture dividing plate (9) area.
3. multi-cell fluidized bed reactor as claimed in claim 1, it is characterized in that, the area in the aperture (10) in each Flow of Goods and Materials controller (8) is less than or equal to 1/20 of place, described aperture dividing plate (9) area.
4. multi-cell fluidized bed reactor as claimed in claim 1, it is characterized in that, the sectional area of the descending flow duct of material (11) in each Flow of Goods and Materials controller (8) is less than or equal to 1/3 of described material descending flow duct place secondary fluidising chamber sectional area.
5. multi-cell fluidized bed reactor as claimed in claim 1, it is characterized in that, the sectional area of the descending flow duct of material (11) in each Flow of Goods and Materials controller (8) is less than or equal to 1/5 of described material descending flow duct place secondary fluidising chamber sectional area.
6. multi-cell fluidized bed reactor as claimed in claim 1, it is characterized in that, the height of the descending flow duct of material (11) in each Flow of Goods and Materials controller (8) should be less than or equal to the charge level height of described material descending flow duct place secondary fluidising chamber and be more than or equal to 1/5 of the charge level height of the descending flow duct place secondary fluidising chamber of described material.
7. multi-cell fluidized bed reactor as claimed in claim 1, it is characterized in that, the height of the descending flow duct of material (11) in each Flow of Goods and Materials controller (8) should be less than or equal to the charge level height of described material descending flow duct place secondary fluidising chamber and be more than or equal to 1/2 of the charge level height of the descending flow duct place secondary fluidising chamber of described material.
8. multi-cell fluidized bed reactor as claimed in claim 1, it is characterized in that, the bottom baffle (12) in each Flow of Goods and Materials controller (8) is imperforate plate.
9. multi-cell fluidized bed reactor as claimed in claim 1, it is characterized in that, the bottom baffle (12) in each Flow of Goods and Materials controller (8) is porous plate, and the percent opening of bottom baffle (12) is less than or equal to 5/N, wherein N is fluidization number, N=U
o/ U
mf, U
osuperficial gas velocity, U
mfit is minimum fluidization velocity.
10. multi-cell fluidized bed reactor as claimed in claim 1, it is characterized in that, the bottom baffle (12) in each Flow of Goods and Materials controller (8) is porous plate, and the percent opening of bottom baffle (12) is less than or equal to 2/N, wherein N is fluidization number, N=U
o/ U
mf, U
osuperficial gas velocity, U
mfit is minimum fluidization velocity.
11. multi-cell fluidized bed reactors as claimed in claim 1, is characterized in that, bottom baffle (12) part in each Flow of Goods and Materials controller (8) is in upstream chamber, and part is in downstream chamber.
12. multi-cell fluidized bed reactors as claimed in claim 1, it is characterized in that, the area of bottom baffle (12) upper housing portion in each Flow of Goods and Materials controller (8) equals the sectional area of the descending flow duct of material (11), and the area of downstream chamber's part is less than or equal to 1.5 times of the area of upper housing portion.
13. multi-cell fluidized bed reactors as claimed in claim 1, it is characterized in that, in the descending flow duct of material (11), gas speed is less than or equal to minimum fluidization velocity, granule materials is in close phase stacking states, forms the unidirectional two-phase transportation stream of granule materials.
14. multi-cell fluidized bed reactors as claimed in claim 1, is characterized in that, by the charge level height of the Altitude control secondary fluidising chamber of the descending flow duct of material (11) in Flow of Goods and Materials controller (8).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310119439.1A CN104096518B (en) | 2013-04-08 | 2013-04-08 | A kind of multi-cell fluidized bed reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310119439.1A CN104096518B (en) | 2013-04-08 | 2013-04-08 | A kind of multi-cell fluidized bed reactor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104096518A CN104096518A (en) | 2014-10-15 |
| CN104096518B true CN104096518B (en) | 2016-01-20 |
Family
ID=51665292
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310119439.1A Active CN104096518B (en) | 2013-04-08 | 2013-04-08 | A kind of multi-cell fluidized bed reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104096518B (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107185447A (en) * | 2017-06-23 | 2017-09-22 | 福建南方路面机械有限公司 | A kind of method and granule materials mixer of the granule materials that tile |
| CN109045947B (en) * | 2018-09-03 | 2021-08-17 | 青岛科技大学 | Fluidized bed cluster reactor |
| CN109499262B (en) * | 2018-12-14 | 2021-08-13 | 青岛科技大学 | Novel longitudinal parallel bed adsorber |
| CN110079346B (en) * | 2019-05-29 | 2021-02-12 | 青岛科技大学 | Biomass thermal cracking reactor of multi-chamber fluidized bed |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2911290A (en) * | 1957-04-18 | 1959-11-03 | Albert A Jonke | Multistage fluidized bed reactor |
| CN85108482A (en) * | 1984-10-15 | 1986-06-10 | 三菱金属株式会社 | Multichamber type fluid bed reaction apparatus |
| JPS62117626A (en) * | 1985-11-19 | 1987-05-29 | Mitsubishi Metal Corp | Multichamber type fluidized bed reactor |
| DE69103743T2 (en) * | 1989-10-10 | 1994-12-22 | Ici Plc | Liquid phase reaction method. |
| CN1276861A (en) * | 1998-02-20 | 2000-12-13 | 川崎重工业株式会社 | Multichamber division type fluidized bed furnace |
| CA2297712A1 (en) * | 1999-06-16 | 2000-12-16 | Mitsubishi Materials Corporation | Multi-chamber fluidized bed equipment |
| CN2725287Y (en) * | 2004-08-31 | 2005-09-14 | 湖南省爱普环境工程有限公司 | Anaerobic deflecting plate reactor |
| CN101947421A (en) * | 2010-07-09 | 2011-01-19 | 清华大学 | Fluidized bed reactor for preparing high-purity Mg2Si |
| CN102659243A (en) * | 2012-05-21 | 2012-09-12 | 苏州苏水环境工程有限公司 | Separated anaerobic baffled reactor and work method of separated anaerobic baffled reactor |
-
2013
- 2013-04-08 CN CN201310119439.1A patent/CN104096518B/en active Active
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2911290A (en) * | 1957-04-18 | 1959-11-03 | Albert A Jonke | Multistage fluidized bed reactor |
| CN85108482A (en) * | 1984-10-15 | 1986-06-10 | 三菱金属株式会社 | Multichamber type fluid bed reaction apparatus |
| JPS62117626A (en) * | 1985-11-19 | 1987-05-29 | Mitsubishi Metal Corp | Multichamber type fluidized bed reactor |
| DE69103743T2 (en) * | 1989-10-10 | 1994-12-22 | Ici Plc | Liquid phase reaction method. |
| CN1276861A (en) * | 1998-02-20 | 2000-12-13 | 川崎重工业株式会社 | Multichamber division type fluidized bed furnace |
| CA2297712A1 (en) * | 1999-06-16 | 2000-12-16 | Mitsubishi Materials Corporation | Multi-chamber fluidized bed equipment |
| CN2725287Y (en) * | 2004-08-31 | 2005-09-14 | 湖南省爱普环境工程有限公司 | Anaerobic deflecting plate reactor |
| CN101947421A (en) * | 2010-07-09 | 2011-01-19 | 清华大学 | Fluidized bed reactor for preparing high-purity Mg2Si |
| CN102659243A (en) * | 2012-05-21 | 2012-09-12 | 苏州苏水环境工程有限公司 | Separated anaerobic baffled reactor and work method of separated anaerobic baffled reactor |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104096518A (en) | 2014-10-15 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104096518B (en) | A kind of multi-cell fluidized bed reactor | |
| US11560309B2 (en) | Process and reactor comprising a plurality of catalyst receptacles | |
| CN101460239A (en) | Reactor for the production of C2 to C8 olefins from an oxygenate, water vapor, and one or more material flows containing hydrocarbon | |
| CN103864021B (en) | A kind of device and method utilizing chemical chain air separation to prepare oxygen | |
| CN102686308A (en) | Reactor with gas distribution system in bottom | |
| CN102441350A (en) | Radial bed vessels having uniform flow distribution | |
| CN102858447A (en) | Process for the synthesis of methanol | |
| CN201912927U (en) | Low-temperature boiling chlorination furnace | |
| CN105765664A (en) | Series-coupled fluidized bed reactor units including cyclonic plenum assemblies and related methods of hydrofluorination | |
| CN101690867B (en) | Tangential-flow and direct-flow composite air intake desulfurizing tower of half dry type circulating fluidized bed (CFB) | |
| CN104524922A (en) | Method for designing radial bed with high-efficiency airflow distribution and designed radial bed | |
| CN101746830A (en) | Device for safely producing potassium manganate | |
| CN104229798B (en) | Device and the method for work thereof of separating carbon dioxide are worked in coordination with in chain circulation reaction hydrogen manufacturing | |
| CN101574636B (en) | Tubular membrane reactor | |
| CN203379869U (en) | Slurry bed reactor | |
| CN203231297U (en) | Chemical-looping combustion reactor device | |
| CN102482082A (en) | Method for producing chlorine by gas phase oxidation of hydrogen chloride in a fluidized-bed reactor | |
| US9146055B2 (en) | Gas-particle processor | |
| CN103508417A (en) | Method and apparatus for producing hydrogen from bio-oil in chained mode and separating CO2 | |
| EP4182611A1 (en) | Fluidized-bed heat exchanger for conversion of thermal energy to electricity | |
| CN203540507U (en) | Efficient fluidized bed reactor | |
| CN106540637A (en) | A kind of circulation flow reactor and application process | |
| CN202506374U (en) | Uniform moving bed radial reactor | |
| CN114247395A (en) | Hollow fiber membrane type micro-channel reactor and application | |
| US12097489B1 (en) | Expanded bed direct-contact system and heat exchanger and chemical reactor using the same |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20230420 Address after: 116318 Xingang village, Changxing Island Economic Zone, Dalian, Liaoning Patentee after: Zhongke New Catalytic Technology (Dalian) Co.,Ltd. Address before: 116023 No. 457, Zhongshan Road, Liaoning, Dalian Patentee before: DALIAN INSTITUTE OF CHEMICAL PHYSICS, CHINESE ACADEMY OF SCIENCES |