CN216572990U - Fluidized bed reactor - Google Patents
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- CN216572990U CN216572990U CN202122445746.1U CN202122445746U CN216572990U CN 216572990 U CN216572990 U CN 216572990U CN 202122445746 U CN202122445746 U CN 202122445746U CN 216572990 U CN216572990 U CN 216572990U
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Abstract
The utility model relates to the technical field of chemical reaction equipment, and discloses a fluidized bed reaction device which comprises a dense-phase region and a dilute-phase region which are sequentially arranged along the vertical direction, wherein a fluidized bed component is arranged in the dense-phase region; the fluidized bed member includes a plurality of vanes intersecting at a common axis that is skewed by a predetermined included angle with respect to a fluidized bed gas flow direction such that a surface of at least one of the vanes is skewed with respect to the fluidized bed gas flow direction. When a plurality of blades which are horizontally intersected are utilized to drive the ultrafine particles to flow through the fluidized bed component, the fluidized bed component can generate certain resistance to the flowing of the fluidized gas, so that turbulence and turbulent flow are generated, and then foaming or particle agglomeration generated by the ultrafine particles is broken under the influence of the turbulence and the turbulent flow, the contact area between the ultrafine particles and the gas is enlarged, and the gas-solid transfer efficiency in the reaction process is improved.
Description
Technical Field
The utility model relates to the technical field of chemical reaction equipment, in particular to a fluidized bed reaction device.
Background
The specific size range of the ultrafine particles has not been determined clearly, and there are different defining methods in different fields. Particles having a particle size of less than 10 μm or 0.1 μm are generally considered to be ultrafine particles. Due to their small size, ultrafine particles have a very specific small size effect. The ultrafine particles have surface and interface effects, small size and large surface, and the atoms on the surface account for a considerable proportion. At present, the ultrafine particles are widely applied to various chemical fields, including the preparation of carbon materials such as graphene and carbon nanotubes, the preparation of silicon powder or various composite materials, and the like.
The C-type particles belong to sticky particles, and the powder material is difficult to form a normal fluidization; in small diameter pipes, such powders are prone to undesirable fluidization phenomena such as slugging, channeling, that is, gas passing through all the interstices from the grid to the surface of the powder. This difficult penetration is due to the fact that the interparticle forces are much greater than the forces exerted by the fluid on the body, which may result from electrostatic forces between the smaller particles, or from the bed material being wet or cohesive. The material mixing and mass and heat transfer in the fluidized bed of the C-type particles are much worse than those of the A-type particles and the B-type particles. Compared with the A-type particles, the C-type particles have smaller average particle size, increased acting force among the particles and stronger particle viscosity, so the flowability in the reactor is poorer, various problems are easily caused in fluidized bed operation, such as phenomena of easy occurrence of slugging and the like, unstable flowing, channeling, easy generation of particle agglomeration and the like, and the gas-solid contact effect is seriously influenced.
To improve fluidization of class C particles, there are generally two methods: one is that the fluidization properties can be changed by external force fields, such as the addition of vibration fields, magnetic and acoustic fields, etc. Another approach is to modify the surface properties of the class C particles or to add coarse particles to improve flow between particles.
For example, document 201811172496.5 discloses a high aeration gas-solid fluidized bed reactor, a method for realizing high aeration rate in a fluidized bed and its application, wherein the reactor comprises a dense phase and a dilute phase, the dense phase comprises gas and solid particles, the aeration rate in the dense phase is as high as 60% -85%, the aeration rate is significantly higher than that of a common fluidized bed reactor, the solid particles are C + type particles, the C + type particles comprise more than 50% of GeldartC type ultrafine powder and a small amount of nano particles, and the nano particles are partially uniformly or non-uniformly, in a single particle or agglomerate form, temporarily or permanently attached to the surface of the GeldartC type ultrafine powder particles, or the C + type particles at least comprise surface-rough GeldartC type ultrafine powder, and the surface roughness of the GeldartC type ultrafine powder is caused by irregular particle shape or micron-sized protrusions on the surface. The concentrated phase in the reactor has extremely high aeration rate and extremely large specific surface area of particles, can obviously improve the contact efficiency of gas-solid two phases, and is beneficial to the gas-solid two-phase reaction and the physical gas-solid contact process.
Document 03816550.3 discloses a fluidization additive useful for improving the flow properties of fine powders, and the powder formulation to which the fluidization additive is added may be any powder formulation including paint spray powders or pharmaceutical powder compositions. The method can improve the flow property and the conveying property of the superfine powder.
Although a great deal of research has been conducted by many scholars on improvement of fluidization properties of fine particles and adhesive particles, the operation and equipment for improving fluidization properties by mechanical and physical methods are complicated, and there is a lot of controversy.
SUMMERY OF THE UTILITY MODEL
The utility model aims to solve the problem that ultrafine micro-nano particles are difficult to fluidize in a fluidized bed and further cause low gas-solid transmission efficiency in the prior art, and provides a fluidized bed reaction device.
In order to achieve the above object, the present invention provides a fluidized bed reactor, which comprises a dense phase zone and a dilute phase zone sequentially arranged along a vertical direction, wherein a fluidized bed member is arranged in the dense phase zone; the fluidized bed member includes a plurality of vanes intersecting at a common axis that is skewed by a predetermined included angle with respect to a fluidized bed gas flow direction such that a surface of at least one of the vanes is skewed with respect to the fluidized bed gas flow direction.
Optionally, the vanes have straight sides extending along the axis, a plurality of the vanes being connected by the straight sides; and/or the included angle between the adjacent blades is 45-90 degrees.
Optionally, the surface of the vane is inclined at an angle of from 0 ° to 45 ° relative to the direction of flow of the fluidised bed gas.
Optionally, the width of the vanes increases in the direction of gas flow.
Optionally, the blade is one of an inverted trapezoid, an inverted triangle, and a rectangle.
Optionally, two of the fluidized bed components arranged in a mirror image in the horizontal direction form a group of the fluidized bed components, and the fluidized bed reaction device comprises a plurality of groups of the fluidized bed components arranged at intervals.
Optionally, each set of said fluid bed members is spaced apart a minimum distance of 0.2-1.5 times the height of said fluid bed member 7; and/or the maximum distance between the farthest ends of each group of the fluidized bed members is 1-3 times the height of the fluidized bed members 7.
Optionally, the fluidized bed reactor further comprises a tail vane spaced from the fluidized bed member in the direction of gas flow of the fluidized bed; and/or a tail wing included angle is formed between the main flow surface of the tail wing plate and the gas flow direction of the fluidized bed, and the tail wing included angle is 5-45 degrees.
Optionally, the tail plate is spaced from the fluidized bed member by a distance of 0.5-2 times the height of the fluidized bed member 7.
Optionally, the superficial gas velocity in the fluidized bed reaction device is 0.03-0.8 m/s.
Through the technical scheme, when the fluidized gas drives the ultrafine particles to flow through the fluidized bed component by utilizing the blades intersected in the plurality of levels, because a certain included angle is formed between the fluidized bed component and the fluidized gas flowing direction, the fluidized bed component generates certain resistance to the flowing of the fluidized gas, so that turbulence and turbulence are generated, and then foaming or particle agglomeration generated by the ultrafine particles is broken under the influence of the turbulence and the turbulence, the contact area between the ultrafine particles and gas is increased, and the gas-solid transfer efficiency in the reaction process is improved.
Drawings
FIG. 1 is a schematic structural view of one embodiment of a fluidized bed reactor according to the present invention;
FIG. 2 is a schematic structural view of one embodiment of a fluidized bed unit according to the present invention;
FIG. 3 is a schematic structural view of another embodiment of a fluidized bed unit according to the present invention;
FIG. 4 is a schematic structural view of one embodiment of a set of fluidized bed components according to the present invention;
fig. 5 is a schematic mechanical view of an embodiment of the tail vane of the present invention.
Description of the reference numerals
1-gas distributor, 2-dense phase zone, 3-dilute phase zone, 4-gas collection chamber, 5-outflow pipeline, 6-heat exchange tube, 7-fluidized bed component, 71-blade, 72-axis, 8-shell, 9-cyclone separator, 10-gas chamber and 20-tail wing plate.
Detailed Description
The following detailed description of embodiments of the utility model refers to the accompanying drawings. It should be understood that the detailed description and specific examples, while indicating the present invention, are given by way of illustration and explanation only, not limitation.
In the present invention, unless otherwise specified, terms of orientation such as "upper", "lower", "top" and "bottom" are generally used to refer to an orientation of a device or apparatus in a use state. It should be noted that this is only for the convenience of describing the present invention and should not be construed as limiting the present invention.
In the present invention, "a plurality" means at least two, e.g., two, three, etc., unless specifically limited otherwise.
The utility model provides a fluidized bed reaction device, which comprises a dense-phase zone 2 and a dilute-phase zone 3 which are sequentially arranged along the vertical direction, wherein a fluidized bed component 7 is arranged in the dense-phase zone 2, the fluidized bed component 7 comprises a plurality of blades 71, the plurality of blades 71 are intersected on the same axis 72, and the axis 72 is inclined at a preset included angle relative to the gas flow direction of a fluidized bed, so that the surface of at least one blade 71 is inclined relative to the gas flow direction of the fluidized bed.
The fluidized bed reactor (referred to simply as a fluidized bed) described in the present application is a reactor in which solid particles are in a state of suspension motion by passing a gas or a liquid through a granular solid layer, and a gas-solid phase reaction process or a liquid-solid phase reaction process is performed. When the speed of fluid passing through the bed is gradually increased to a certain value, the particles in the fluid are loosened, the gaps among the particles are increased, and the volume of the bed is expanded. If the fluid velocity is increased still further, the bed will not remain stationary. At this point, the particles were all suspended in the fluid and showed fairly irregular motion. As the flow rate increases, the movement of the particles becomes more vigorous and the expansion of the bed increases, but the particles remain in the bed and are not carried away by the fluid. This state of the bed is referred to as a fluidized bed, similar to a liquid.
The fluidization of fluidized bed and the solid phase material of reaction in this application mainly refer to superfine granule, especially C class granule, because C class granule belongs to a stickness granule, this kind of powder material is difficult to form a "normal" fluidization, because the effort of intergranular is far greater than the power that fluid acted on the components of a whole that can function independently, and these power probably come from the electrostatic force between the less granule, or the bed material is wet or the bonding leads to, make the gas be difficult to normally pass the clearance between the gas, lead to the area of contact greatly reduced between superfine granule and the gas, and then influence the reaction and take place.
The gas flow direction of the fluidized bed means a gas in the fluidized bed which moves solid particles in the fluidized bed, and generally, the gas flows from bottom to top along the fluidized bed.
Generally, the total height of the fluidized bed is divided into a dense phase zone 2 and a dilute phase zone 3. The region below the fluidized bed interface is referred to as the dense phase zone 2 and the region above the interface is referred to as the dilute phase zone 3. The total height of the fluidized bed is the sum of the heights of the dense phase zone 2 and the dilute phase zone 3. More specifically, as shown in fig. 1, a housing 8 is provided at the outside, the fluidized bed reactor may include a gas distributor 1 for distributing fluidizing gas in the fluidized bed, a plenum chamber 4 provided at the top, and an outflow pipe 5 connected to the top of the plenum chamber 4, so that the material in the plenum chamber 4 can flow to a collection device or other processes through the outflow pipe 5, a cyclone 9 is provided at the lower part of the plenum chamber 4, and a gas chamber 10 is provided at the bottom of the housing 8.
As more ultrafine particles are in the dense-phase zone 2 and are the main reaction area, the ultrafine particles in the dense-phase zone 2 are bonded and agglomerated and bubbles are broken through the fluidized bed member 7 arranged in the dense-phase zone 2, so that the contact area between the ultrafine particles and gas is enlarged, and the gas-solid transfer efficiency in the reaction process is improved.
When utilizing the blade 71 that a plurality of levels intersect to make the fluidization gas drive ultrafine particle to flow through fluidized bed component 7 among the above-mentioned technical scheme, certain contained angle has between the flow direction of blade 71 at least partial surface and fluidization gas to make fluidized bed component 7 produce certain resistance to the flow of fluidization gas, and then produce turbulence and vortex, and then make the foaming or the granule reunion that ultrafine particle produced broken under the influence of turbulence and vortex, increase the area of contact of ultrafine particle and gas, thereby improve the gas-solid transfer efficiency among the reaction process.
The blades 71 may be plate-like structures that intersect along a boundary, may intersect at some point on a surface, may have a completely contiguous boundary, or may only partially intersect. The plurality of blades 71 may be of identical shape or may have different intersecting shapes.
For better gas flow turbulence, as shown in fig. 2 and 3, fig. 2 shows a fluidized bed member 7 consisting of two vanes 71, fig. 3 shows a fluidized bed member 7 consisting of 4 vanes together, said vanes 71 having straight sides extending along said axis 72, a plurality of said vanes being connected by said straight sides, more specifically, the angle α between adjacent said vanes 71 is 45-90 degrees, preferably 65 degrees.
In order to further enhance the turbulent flow effect, the blades 71 of the blades 71 have a width that is increased along the gas flow direction as shown in fig. 2 and 3, and such a structure shape can make the fluidized bed member 7 have a flow resistance that is reduced as much as possible to the fluidized gas flowing therethrough and the ultrafine solid particles entrained by the fluidized gas. As a specific embodiment, the blade 71 may have a plate-like structure formed by a regular straight edge such as a rectangle or a trapezoid, or may have a plate-like structure with curved sides; at the same time, in order to further prevent the blades 71 from generating too much resistance to the flow of fluidized gas, the offset angle β of the surface of the blades 71 with respect to the flow direction of the fluidized bed gas may be set to 0-45 degrees, preferably to 45 degrees.
As a specific embodiment, the blade 71 has one of an inverted trapezoid shape, an inverted triangle shape, and a rectangular shape.
In order to enhance the crushing effect of the foaming or particle agglomeration generated on the ultrafine particles, as a specific embodiment, as shown in fig. 1, 4 and 5, two fluidized bed members 7 arranged in a mirror image in the horizontal direction form a group of the fluidized bed members 7, and the fluidized bed reaction apparatus includes a plurality of groups of the fluidized bed members arranged at intervals. Because the ultrafine particles are driven by the fluidizing gas and generate a flowing effect under the mutual collision action, but the flowing direction does not completely move according to the direction of the fluidizing gas, in order to enhance the disturbance effect of the fluidized bed component 7 on the fluidizing gas, the fluidized bed component 7 arranged in a mirror image mode can enable the orientation of the blades 71 to be more various, and therefore the disturbance effect is enhanced.
In order to prevent the fluidized bed members 7 from generating too much resistance to the fluidizing gas, as a specific embodiment, each group of said fluidized bed members 7 is spaced apart from each other by a minimum distance of 0.2 to 1.5 times the height of said fluidized bed members 7, preferably, set to 1; the maximum distance between the most distal ends of each set of said fluid bed members 7 is 1-3 times, preferably 2.5 times the height of said fluid bed members 7.
In order to further enhance the disturbance effect on the fluidized gas, the fluidized bed reaction device further comprises a tail wing plate 20 which is arranged at a distance from the fluidized bed component 7 along the gas flow direction of the fluidized bed; the tail wing plate 20 may be configured in a regular plate-shaped structure, such as a trapezoid, a rectangle, a circle, and the like, and is preferably configured in a rectangle. The main flow surface of the tail wing plate 20 and the gas flow direction of the fluidized bed form a tail wing included angle therebetween, and the tail wing included angle γ is 5-45 degrees, preferably 30 degrees.
As a specific embodiment, as shown in fig. 5, the distance between the tail plate 20 and the fluidized bed member 7 is 0.5 to 2 times, preferably 0.7 times, the height of the fluidized bed member 7.
In order to achieve better gas-solid transfer efficiency, the apparent linear speed of gas in the fluidized bed reaction device is set to be 0.03-0.8 m/s.
The following provides a preferred embodiment of the present application as an example:
[ example 1 ]
The fluidized bed reaction device shown in figure 1 is adopted, the raw material is a carbon-containing gas source, the catalyst/template particles take nickel or/and copper as main active components, and the average particle size of the catalyst is 500 nm. The reaction conditions are as follows: the average reaction temperature is controlled to be 600-750 ℃, and the reaction pressure is normal pressure.
The angle α between two adjacent blades 71 in the fluid bed unit 7 is 65 °, the blades of the fluid bed unit 7 are inverted trapezoidal, and the ratio of the length of the bottom edge of the blade 71 to the length of the top edge of the blade 71, viewed in the vertical direction, is 0.45. The device is characterized in that 4 groups of fluidized bed components 7 are arranged in the dense-phase region 2 of the fluidized bed, and each group of two fluidized bed components 7 are arranged in a mirror image mode in the horizontal direction. The distance between the most proximal of the two fluid bed members 7 in each set of fluid bed members 7 is 1.0 times the height of the fluid bed members 7 and the distance between the most distal of the two fluid bed members 7 in said set of fluid bed members 7 is 2.5 times the height of the fluid bed members 7. The offset angle β between the axis 72 and the gas flow direction is 45 °. A tail wing plate 20 is arranged above the fluidized bed component 7, the shape of the tail wing plate 20 is rectangular, and the included angle gamma of the tail wing is 30 degrees. The distance between the tail plate 20 and the fluidized bed member 7 is 0.7 times of the height of the fluidized bed member 7.
A raw material carbon source is uniformly distributed in a gas chamber 10 through a gas distributor 1 and then flows into a dense-phase region 2 of a fluidized bed, particles in the dense-phase region 2 of the fluidized bed are pushed to fluidize, particle clusters and bubbles are formed and are gradually crushed and dispersed after being crushed and disturbed through a fluidized bed component 7, violent reaction is carried out in the dense-phase region, part of the particles carried by the reacted gas enter a dilute-phase region 3, the particles are separated through a cyclone separator 9 and then return to the dense-phase region 2 of the fluidized bed through a dipleg of the cyclone separator 9, and the gas flows into a gas collection chamber 4 and then enters a subsequent unit.
The expansion coefficient (the expansion coefficient is the ratio of the height of a bed layer to the height of a static bed in normal reaction) in the fluidized bed reaction device is 1.94, the standard deviation of bed layer pressure pulsation is 105Pa, the number of layers of the produced powder graphene is less than 3, and the specific surface area is 1000-2000 m 2/g.
[ example 2 ]
A fluidized bed reaction device shown in figure 1 is adopted, a gas phase raw material is a carbon-containing gas source and is one or more of methane, ethane, acetylene, ethylene, propane, propylene, benzene or toluene, a certain proportion of inert gas is doped, the inert gas is one or a mixture of nitrogen and argon, particles are silicon or oxides thereof, and the average particle size is 30-200 nm. The reaction conditions are as follows: the average reaction temperature is controlled to be 600-750 ℃, and the reaction pressure is normal pressure.
The included angle alpha between two adjacent blades 71 in the fluidized bed component 7 is 90 degrees, the blades of the fluidized bed component 7 are inverted trapezoids, and the ratio of the length of the bottom edge of the blade 71 to the length of the top edge of the blade 71 is 0.5 when viewed in the vertical direction. The device is characterized in that 4 groups of fluidized bed components 7 are arranged in the dense-phase region 2 of the fluidized bed, and each group of two fluidized bed components 7 are arranged in a mirror image mode in the horizontal direction. The distance between the most proximal of the two fluid bed members 7 in each set of fluid bed members 7 is 1.1 times the height of the fluid bed members 7 and the distance between the most distal of the two fluid bed members 7 in said set of fluid bed members 7 is 1.5 times the height of the fluid bed members 7. The offset angle beta between the axis 72 and the gas flow direction is 30 deg.. A tail wing plate 20 is arranged above the fluidized bed component 7, the shape of the tail wing plate 20 is rectangular, and the included angle gamma of the tail wing is 15 degrees. The distance between the tail plate 20 and the fluidized bed member 7 is 0.5 times of the height of the fluidized bed member 7.
A raw material carbon source is uniformly distributed in a gas chamber 10 through a gas distributor 1 and then flows into a dense-phase region 2 of a fluidized bed, particles in the dense-phase region 2 of the fluidized bed are pushed to fluidize, particle clusters and bubbles are formed and are gradually crushed and dispersed after being crushed and disturbed through a fluidized bed component 7, violent reaction is carried out in the dense-phase region, part of the particles carried by the reacted gas enter a dilute-phase region 3, the particles are separated through a cyclone separator 9 and then return to the dense-phase region 2 of the fluidized bed through a dipleg of the cyclone separator 9, and the gas flows into a gas collection chamber 4 and then enters a subsequent unit.
The expansion coefficient (the expansion coefficient is the ratio of the height of a bed layer to the height of a static bed in normal reaction) in the fluidized bed reaction device is 1.78, the standard deviation of the pressure pulsation of the bed layer is 113Pa, and in the produced silicon-carbon composite material, the particle surface has an obvious graphene coating structure under a transmission electron microscope, the number of graphene layers is less than 5, and the carbon coating amount is 5-7%.
In order to embody the advantages of the present technical solution, two reaction conditions in the fluidized bed reaction apparatus without the fluidized bed member 7 are also proposed as comparative examples:
comparative example 1
A conventional fluidized bed reaction device is adopted, raw materials are carbon-containing gas sources, catalyst/template particles take nickel or/and copper as main active components, and the average particle size of the catalyst is 500 nm. The reaction conditions are as follows: the average reaction temperature is controlled to be 600-750 ℃, and the reaction pressure is normal pressure.
The flow in the fluidized bed reaction device is relatively disordered, mainly by channeling, the height is almost not obviously expanded during the reaction, the expansion coefficient is lower than 1.1, and only 10 percent of the produced powder carbon-containing product is graphene.
Comparative example 2
A conventional fluidized bed reaction device is adopted, a gas-phase raw material is a carbon-containing gas source and is one or more of methane, ethane, acetylene, ethylene, propane, propylene, benzene or toluene, a certain proportion of inert gas is doped, the gas-phase raw material is one or a mixture of nitrogen and argon, particles are silicon or oxides thereof, and the average particle size is 30-200 nm. The reaction conditions are as follows: the average reaction temperature is controlled to be 600-750 ℃, and the reaction pressure is normal pressure.
The flow in the fluidized bed reaction device is disordered, the channeling is taken as a main part, the height is almost not obviously expanded during the reaction, the expansion coefficient is lower than 1.1, in the produced silicon-carbon composite material, only a small part of particles have an obvious graphene coating structure on the surface under a transmission electron microscope, and the carbon coating amount is unevenly distributed to be 0-13%.
The preferred embodiments of the present invention have been described in detail above with reference to the accompanying drawings, but the present invention is not limited thereto. Within the scope of the technical idea of the utility model, many simple modifications can be made to the technical solution of the utility model. Including each of the specific features, are combined in any suitable manner. The utility model is not described in detail in order to avoid unnecessary repetition. Such simple modifications and combinations should be considered within the scope of the present disclosure as well.
Claims (10)
1. A fluidized bed reaction device is characterized by comprising a dense-phase zone (2) and a dilute-phase zone (3) which are sequentially arranged along the vertical direction, wherein a fluidized bed component (7) is arranged in the dense-phase zone (2);
the fluidized bed member (7) comprises a plurality of vanes (71), a plurality of the vanes (71) intersecting on the same axis (72), the axis (72) being inclined by a predetermined angle with respect to the fluidized bed gas flow direction such that the surface of at least one of the vanes (71) is inclined with respect to the fluidized bed gas flow direction.
2. The fluidized bed reactor according to claim 1, wherein the vanes (71) have straight sides extending along the axis (72), a plurality of the vanes being connected by the straight sides; and/or (c) and/or,
the included angle between the adjacent blades (71) is 45-90 degrees.
3. The fluidized bed reactor as set forth in claim 1, wherein the surface of the vane (71) is inclined at an angle of 0 ° to 45 ° with respect to the flow direction of the fluidized bed gas.
4. The fluidized bed reactor according to claim 1, wherein the width of the vane (71) increases in the gas flow direction.
5. The fluidized bed reactor according to claim 4, wherein the vanes (71) are one of inverted trapezoidal, inverted triangular, and rectangular.
6. The fluidized bed reactor according to claim 1, characterized in that two of said fluidized bed members (7) arranged in a mirror image in a horizontal direction form a group of said fluidized bed members (7), and said fluidized bed reactor comprises a plurality of groups of said fluidized bed members (7) arranged at a distance from each other.
7. The fluidized bed reaction apparatus according to claim 6, characterized in that each group of the fluidized bed members (7) is spaced apart by a minimum distance of 0.2-1.5 times the height of the fluidized bed members (7); and/or (c) and/or,
the maximum distance between the furthest ends of each set of said fluid bed members (7) is 1-3 times the height of said fluid bed members (7).
8. The fluidized bed reactor according to claim 5, further comprising a tail vane (20) spaced from the fluidized bed member (7) in the fluidized bed gas flow direction; and/or (c) and/or,
and a tail wing included angle is formed between the main flow surface of the tail wing plate (20) and the gas flow direction of the fluidized bed, and the tail wing included angle is 5-45 degrees.
9. The fluidized bed reaction apparatus according to claim 8, characterized in that the distance between the tail flap (20) and the fluidized bed member (7) is 0.5-2 times the height of the fluidized bed member (7).
10. The fluidized bed reactor as claimed in claim 5, wherein the superficial linear velocity of the gas in the fluidized bed reactor is 0.03-0.8 m/s.
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