Efficient spiral-flow type circulating fluidized bed reactor

Abstract

The utility model discloses an efficient spiral-flow type circulating fluidized bed reactor which comprises a fluidized bed and a cyclone separator, the fluidized bed is respectively communicated with the cyclone separator through a feed pipe and a return pipe, and the fluidized bed is provided with a fluidized bed feed port used for feeding heat exchange media and a fluidized bed discharge port used for discharging the heat exchange media. The fluidized bed comprises an air inlet cavity arranged in the fluidized bed and an air inlet pipe communicated with the air inlet cavity, a rotational flow air distribution plate is arranged in the air inlet cavity, and a plurality of rotational flow air ejector pipes are arranged on the outer wall of the fluidized bed and evenly arranged in the circumferential direction of the outer side of the fluidized bed. The included angle between the axis of the rotational flow gas ejector pipe and the axis of the outer wall face of the fluidized bed ranges from 30 degrees to 85 degrees, and the included angle between the axis of the rotational flow gas ejector pipe and the tangent line of the outer wall face of the fluidized bed ranges from 0 degree to 40 degrees. The efficient spiral-flow type circulating fluidized bed reactor provided by the utility model can shorten the fluidization time and improve the fluidization effect.

Description

Technical Field

[0001] The utility model relates to a fluidized bed reactor, in particular to a high-efficiency cyclone-type circulating fluidized bed reactor. Background Art

[0002] Fluidized bed technology plays an important role in many industries such as energy, chemical and pharmaceutical due to its excellent mass and heat transfer efficiency, stable temperature distribution and uniform contact between gas and solid phases.

[0003] According to Geldart's particle classification theory, C-type particles are also called sticky particles or agglomerated particles. The fluidization of sticky particles in a fluidized bed is a complex process. Due to their small particle size, large specific surface area, and relatively strong attraction between particles (such as van der Waals force), their fluidization behavior in a fluidized bed is different from that of other types of particles. They are prone to agglomeration, resulting in poor fluidization effect.

[0004] Adding an external force field can effectively reduce the fluidization agglomeration of particles, but there are many problems in the actual application process, such as the high cost and small range of action of the acoustic field equipment; the use of a stirring device can effectively break up the particle agglomeration, but ultrafine particles can easily enter the gap of the stirring shaft, causing abnormal noise in the stirring device or even jamming; the vibration device has poor equipment stability and is difficult to apply on a large scale. Utility Model Content

[0005] In view of the above-mentioned shortcomings currently existing, the utility model provides a high-efficiency cyclone circulating fluidized bed reactor, which can shorten the fluidization time and improve the fluidization effect.

[0006] In order to achieve the above object, the embodiment of the utility model adopts the following technical solution:

[0007] A high-efficiency cyclone circulating fluidized bed reactor comprises a fluidized bed and a cyclone separator, wherein the fluidized bed is connected to the cyclone separator through a feed pipe and a return pipe respectively, and a fluidized bed feed port for introducing a heat exchange medium and a fluidized bed discharge port for discharging the heat exchange medium are arranged on the fluidized bed, the fluidized bed comprises an air inlet cavity arranged inside the fluidized bed and an air inlet pipe connected to the air inlet cavity, a cyclone air distribution plate is arranged in the air inlet cavity, a plurality of cyclone air injection pipes are arranged on the outer wall of the fluidized bed, the cyclone air injection pipes are evenly arranged along the outer circumferential direction of the fluidized bed, the angle between the axis of the cyclone air injection pipe and the axis of the outer wall of the fluidized bed is in the range of 30° to 85°, and the angle between the axis of the cyclone air injection pipe and the tangent of the outer wall of the fluidized bed is in the range of 0° to 40°.

[0008] According to one aspect of the utility model, the swirl jet pipes are arranged in a vertical direction along the outside of the fluidized bed.

[0009] According to one aspect of the utility model, a plurality of guide vanes are provided on the swirl air distribution plate.

[0010] According to one aspect of the utility model, the guide blades are evenly distributed along the circumferential direction of the swirl air distribution plate.

[0011] According to one aspect of the utility model, the cross section of the guide vane is arc-shaped.

[0012] According to one aspect of the utility model, the cross section of the guide vane is an airfoil.

[0013] According to one aspect of the utility model, the number of the swirl jet pipes arranged in the circumferential direction of the outer side of the fluidized bed is 4 to 30.

[0014] According to one aspect of the utility model, the number of layers of the swirl jet pipes arranged in the axial direction of the fluidized bed is 1 to 10.

[0015] The advantages of the implementation of the utility model are as follows: by adopting a swirl air distribution plate and a swirl air injection pipe, the gas forms a swirl effect in the fluidized bed on the one hand, further strengthening the fluidization effect of the particles; on the other hand, it can blow to the wall surface, and will not react on the reactor wall surface during vapor deposition, thereby ensuring the long-term stable operation of the fluidized bed; the gas-solid mixture discharged from the fluidized bed outlet is separated into gas and solid by a cyclone separator, and the cyclone airflow brings the particles back into the fluidized bed, thereby improving the utilization rate of the particles. BRIEF DESCRIPTION OF THE DRAWINGS

[0016] In order to more clearly illustrate the technical solutions in the embodiments of the present invention, the following briefly introduces the drawings required for use in the embodiments. Obviously, the drawings described below are only some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without creative work.

[0017] Figure 1 It is a schematic diagram of the structure of the utility model;

[0018] Figure 2 It is a cross-sectional view of the utility model along the AA line;

[0019] Figure 3 It is a cross-sectional view of the utility model along the BB line;

[0020] Figure 4 It is a schematic diagram of the swirl air distribution plate of the utility model;

[0021] Figure 5 It is a schematic diagram of the cyclone separator described in the utility model.

[0022] 1. Fluidized bed; 11. Fluidized bed feed port; 12. Fluidized bed air outlet; 13. Cyclone jet pipe; 14. Fluidized bed return port; 15. Fluidized bed discharge port; 16. Air inlet cavity; 17. Air inlet pipe; 2. Cyclone separator; 21. Separator air outlet; 22. Feed pipe; 23. Return pipe; 3. Cyclone air distribution plate; 31. Guide vane. DETAILED DESCRIPTION

[0023] The following will be combined with the drawings in the embodiments of the utility model to clearly and completely describe the technical solutions in the embodiments of the utility model. Obviously, the described embodiments are only part of the embodiments of the utility model, not all of the embodiments. Based on the embodiments in the utility model, all other embodiments obtained by ordinary technicians in the field without making creative work are within the scope of protection of the utility model. In the description of the utility model, it should be noted that the orientation or position relationship indicated by the terms "top", "bottom", "one side", "the other side", "front", "back", "middle part", "inside", "top", "bottom" and the like is based on the orientation or position relationship shown in the drawings, which is only for the convenience of describing the utility model and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be understood as a limitation on the utility model.

[0024] Embodiment 1:

[0025] like Figures 1 to 4 As shown, a high-efficiency cyclone circulating fluidized bed reactor comprises a fluidized bed 1 and a cyclone separator 2, the fluidized bed 1 is connected with the cyclone separator 2 through a feed pipe 22 and a return pipe 23 respectively, the fluidized bed 1 is provided with a fluidized bed feed port 11 for introducing a heat exchange medium and a fluidized bed discharge port 15 for passing out the heat exchange medium, the fluidized bed 1 comprises an air inlet cavity 16 arranged inside the fluidized bed 1 and an air inlet pipe 17 connected with the air inlet cavity 16, a cyclone air distribution plate 3 is arranged in the air inlet cavity 16, a plurality of cyclone air injection pipes 13 are arranged on the outer wall of the fluidized bed 1, the cyclone air injection pipes 13 are evenly arranged along the outer circumferential direction of the fluidized bed 1, the angle between the axis of the cyclone air injection pipe 13 and the axis of the outer wall of the fluidized bed 1 is in the range of 30°~85°, and the angle between the axis of the cyclone air injection pipe 13 and the tangent of the outer wall of the fluidized bed 1 is in the range of 0°~40°. The swirl jet pipes 13 are evenly arranged along the circumferential direction of the outer side of the fluidized bed 1 body, and maintain a certain angle with the fluidized bed 1 body to promote the swirl movement of the material and enhance the mixing effect; the swirl jet pipes 13 are used to optimize the circulation and distribution of the material.

[0026] In this embodiment, a fluidized bed return port 14 is provided on the fluidized bed 1 , and the fluidized bed return port 14 is connected to a return pipe 23 .

[0027] In this embodiment, a fluidized bed gas outlet 12 is provided on the fluidized bed 1 , and the fluidized bed gas outlet 12 is connected to the feed pipe 22 .

[0028] When in use, the gas enters from the air inlet pipe 17, and after being held in pressure by the air inlet cavity 16, the airflow is stabilized to ensure that the gas enters the fluidized bed 1 at an appropriate pressure and speed; then it rises to the cyclone air distribution plate 3, and the gas forms a spiral upward airflow when passing through, which helps the uniform suspension and mixing of particles; the particles are put into the fluidized bed 1 through the feed port; the airflow blows the particles, causing them to spirally rise in the fluidized bed 1 to form a good fluidized state. This movement helps the mixing and mass transfer between particles; the gas ejected from the cyclone jet pipe 13 forms a cyclone in the fluidized bed 1, which can break up the agglomerated materials, prevent the particles from agglomerating in the bed layer, and further enhance the fluidization effect of the particles; when the airflow carries the particles upward to the outlet of the fluidized bed 1, the gas-solid mixture enters the cyclone separator 2. Here, due to the action of centrifugal force, the particles are separated and settled from the airflow; the particles separated by the cyclone separator 2 re-enter the fluidized bed 1 through the return pipe 23 to form a closed loop. This ensures the continuous reaction and treatment of the particles in the reactor.

[0029] In this embodiment, the cyclone separator 2 is provided with a feed pipe 22 and a separator outlet 21. The feed pipe 22 is connected to the outlet of the fluidized bed 1 for receiving the rising mixture of gas and solid particles; the separator outlet 21 is used to discharge the separated gas, and the return pipe 23 is used to guide the solid particles back to the lower part of the fluidized bed 1 through the return pipe 23 to achieve circulation.

[0030] In practical applications, the angle between the axis of the swirl jet pipe 13 and the axis of the outer wall of the fluidized bed 1 is in the range of 30° to 85°.

[0031] like Figure 5 As shown, the angle between the axis of the swirl jet pipe 13 and the tangent line of the outer wall of the fluidized bed 1 is in the range of 0° to 40°.

[0032] In practical applications, the swirl jet pipes 13 are arranged in the vertical direction outside the fluidized bed 1 to further enhance the fluidization effect of the particles.

[0033] In practical applications, a plurality of guide vanes 31 are provided on the swirl air distribution plate 3. The guide vanes 31 improve the separation effect.

[0034] The guide vanes 31 can determine a suitable inclination angle according to actual conditions to optimize gas flow and promote the swirl motion of the material.

[0035] In practical applications, the guide vanes 31 are evenly distributed along the circumferential direction of the swirl air distribution plate 3 .

[0036] In practical applications, the cross section of the guide vane 31 is arc-shaped, which can further reduce the fluid dynamics resistance.

[0037] In practical applications, the cross section of the guide vane 31 is an airfoil, which can further reduce the fluid dynamics resistance.

[0038] In practical applications, the number of swirl jet pipes 13 arranged in the circumferential direction of the outer side of the fluidized bed 1 is 4 to 30.

[0039] In practical applications, the number of layers of the swirl jet pipes 13 arranged in the axial direction of the fluidized bed 1 is 1 to 10.

[0040] The beneficial effects of this embodiment are:

[0041] 1. The swirl air distribution plate 3 and the swirl air injection pipe 13 are used. On the one hand, the gas forms a swirl effect in the fluidized bed 1, further strengthening the fluidization effect of the particles; on the other hand, it can blow on the wall surface, and will not react on the reactor wall surface during vapor deposition, ensuring the long-term stable operation of the fluidized bed 1;

[0042] 2. The gas-solid mixture discharged from the fluidized bed outlet 12 is separated into gas and solid by the cyclone separator 2, and the airflow of the cyclone brings the particles back into the fluidized bed 1, thereby improving the utilization rate of the particles;

[0043] 3. The fluidized bed reactor 1 can be used for fluidization of large quantities of particles. The swirl helps to break up the agglomeration of sticky particles, causing the particles to rise in a vortex shape, enhancing the contact between gas and solid, and shortening the fluidization reaction time, thereby improving the reaction efficiency.

[0044] The above is only a specific implementation of the present invention, but the protection scope of the present invention is not limited thereto. Any changes or substitutions that can be easily thought of by any technician familiar with the art within the technical scope disclosed in the present invention should be included in the protection scope of the present invention. Therefore, the protection scope of the present invention should be based on the protection scope of the claims.

Claims

1. A high-efficiency cyclonic circulating fluidized bed reactor, comprising a fluidized bed (1) and a cyclone separator (2), wherein the fluidized bed (1) is connected to the cyclone separator (2) via a feed pipe (22) and a return pipe (23), respectively, and the fluidized bed (1) is provided with a fluidized bed feed port (11) for introducing a heat exchange medium and a fluidized bed discharge port (15) for discharging the heat exchange medium, characterized in that: The fluidized bed (1) comprises an air inlet cavity (16) arranged inside the fluidized bed (1) and an air inlet pipe (17) connected to the air inlet cavity (16); a swirl air distribution plate (3) is arranged inside the air inlet cavity (16); a plurality of swirl jet pipes (13) are arranged on the outer wall of the fluidized bed (1); the swirl jet pipes (13) are evenly arranged along the circumferential direction of the outer side of the fluidized bed (1); the included angle between the axis of the swirl jet pipe (13) and the axis of the outer wall of the fluidized bed (1) is in the range of 30° to 85°; and the included angle between the axis of the swirl jet pipe (13) and the tangent of the outer wall of the fluidized bed (1) is in the range of 0° to 40°.

2. A high-efficiency cyclone circulating fluidized bed reactor according to claim 1, characterized in that: The swirl jet pipes (13) are arranged in the vertical direction outside the fluidized bed (1).

3. A high-efficiency cyclone circulating fluidized bed reactor according to claim 1, characterized in that: A plurality of guide blades (31) are provided on the swirl air distribution plate (3).

4. A high-efficiency cyclone circulating fluidized bed reactor according to claim 3, characterized in that: The guide blades (31) are evenly distributed along the circumferential direction of the swirl air distribution plate (3).

5. A high-efficiency cyclone circulating fluidized bed reactor according to claim 3, characterized in that: The guide blade (31) has an arc-shaped cross section.

6. A high-efficiency cyclone circulating fluidized bed reactor according to claim 3, characterized in that: The cross section of the guide blade (31) is an airfoil.

7. A high-efficiency cyclone circulating fluidized bed reactor according to any one of claims 1 to 6, characterized in that: The number of the swirl jet pipes (13) arranged in the circumferential direction outside the fluidized bed (1) is 4 to 30.

8. A high-efficiency cyclone circulating fluidized bed reactor according to claim 7, characterized in that: The number of layers of the swirl jet pipes (13) arranged in the axial direction of the fluidized bed (1) is 1 to 10.

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