Distributor system of countercurrent reactor of circulating fluidized bed and use method of distributor system

Abstract

The invention provides a distributor system of a countercurrent reactor of a circulating fluidized bed and a use method of the distributor system, solves the problem that solid particles are concentrated on one side when entering the reactor, and realizes uniform distribution of the solid particles. Comprising a reactor, a conveying pipe, a first solid particle distributor, a second solid particle distributor, a rectifying gas distributor and a fluidizing gas distributor, the conveying pipe comprises an inclined conveying pipe and a transverse conveying pipe, the inclined conveying pipe is connected with the transverse conveying pipe, and the middle of the transverse conveying pipe is connected with a first solid particle distributor; the second solid particle distributor is located below the first solid particle distributor, and the first solid particle distributor is inserted into the second solid particle distributor; the second solid particle distributor comprises an overflow distributor and a bottom distributor, holes are formed in the periphery of the overflow distributor, the bottom of the overflow distributor is connected with the bottom distributor, and holes are formed in the bottom distributor; the rectifying gas distributor is arranged in the second solid particle distributor; and the fluidizing gas distributor is inserted into the first solid particle distributor.

Description

Technical Field

[0001] The present invention belongs to the field of chemical engineering, and particularly relates to a distributor system for a circulating fluidized bed countercurrent reactor and a method for using the same. Background Art

[0002] A circulating fluidized bed reactor is an efficient reaction device designed based on the principle of gas-solid two-phase flow, and is a core device in many application fields such as petroleum processing, energy conversion, nanoparticle synthesis, waste plastic recycling, etc. There are two operating modes for the gas-solid two-phase in the circulating fluidized bed reactor. One is the co-current flow mode in which the gas-solid two-phase flow in the same direction, and the other is the countercurrent flow mode in which the gas-solid two-phase flow in the opposite direction. In the countercurrent flow mode, the gas phase flow in the circulating fluidized bed reactor runs from bottom to top, and the solid particles fall from top to bottom. The two contact reversely in the reactor, with intense mass transfer, heat transfer and chemical reactions occurring. During the flow of the gas phase flow, due to the characteristic that the gas fills the entire space, it will spontaneously distribute evenly on the same cross-section. However, during the downward movement of the solid particles, they are mainly affected by the gravity, drag force and buoyancy of the gas of the solid particles, and the distribution around is very limited and cannot achieve the effect of uniform distribution. Therefore, whether the solid particles are evenly distributed determines the mass transfer and heat transfer efficiency in the reactor, and mass transfer and heat transfer are the basis for the reaction to proceed, so it also determines the reaction effect.

[0003] In the existing circulating fluidization form, for the process of solid particles entering the reactor through the conveying pipe, please refer to Figure 1 , Figure 1 discloses the structure and conveying process of a conveying pipe in the prior art, including: 1-1-solid particle conveying pipe, 2-1-connecting elbow, 3-1-reactor and 4-1-solid particles. The solid particles are conveyed to the reactor along the conveying pipeline, first entering the horizontal pipeline through the inclined pipe. When entering the vertical pipeline from the horizontal pipeline, due to inertia, the solid particles will concentrate on one side and fall into the reactor along one side of the vertical pipeline. The defect of this structure is that: when the solid particles enter the reactor from the conveying pipeline, they are already biased to one side, and they will still be biased to one side after being distributed by the distributor, and the uniform distribution of the solid particles in the reactor cannot be achieved.

[0004] Figure 2 discloses an improved structure and conveying process of a conveying pipe in the prior art, including 1-2-solid particle conveying pipe, 2-2-horizontal pipe blind plug, 3-2-reactor and 4-2-solid particles, Figure 2 The structure disclosed by Figure 1 Compared with Figure 2The middle part of the horizontal pipeline is connected to the vertical pipeline. The advantages of this structure are as follows: Solid particles are transported to the reactor along the transport pipeline. First, they enter the horizontal pipeline through the inclined pipe. When entering the vertical pipeline from the horizontal pipeline, some solid particles will enter the blind end of the horizontal pipe and then return to enter the vertical pipeline. This structure can, to a certain extent, weaken the situation where solid particles concentrate on one side due to inertia. After being distributed by the distributor, the solid particles in the reactor are still uneven.

[0005] Therefore, it is necessary to provide a technical solution to solve the above problems. Summary of the Invention

[0006] To solve the above problems, the present invention provides a distributor system to solve the problem that solid particles concentrate on one side when entering the reactor and achieve uniform distribution of solid particles.

[0007] To achieve the above object, the technical solution provided by the present invention is as follows:

[0008] A distributor system for a circulating fluidized bed countercurrent reactor, comprising: a reactor, a transport pipe, a first solid particle distributor, a second solid particle distributor, a rectifying gas distributor, and a fluidizing gas distributor; the transport pipe includes a transport inclined pipe and a transport horizontal pipe, the transport inclined pipe is connected to the transport horizontal pipe, and the middle part of the transport horizontal pipe is connected to the first solid particle distributor; the second solid particle distributor is located below the first solid particle distributor, and the first solid particle distributor is inserted into the second solid particle distributor; the second solid particle distributor includes an overflow distributor and a bottom distributor, the overflow distributor has holes around it, the bottom of the overflow distributor is connected to the bottom distributor, and the bottom distributor has holes; the rectifying gas distributor is arranged inside the second solid particle distributor; the fluidizing gas distributor is inserted into the first solid particle distributor.

[0009] In the technical solution provided by the present invention: the transport inclined pipe penetrates into the reactor through the reactor surface, and the end of the transport inclined pipe inside the reactor is connected to the transport horizontal pipe; one end of the transport horizontal pipe is connected to the transport inclined pipe, and the other end is a blind end; the middle part of the transport horizontal pipe is connected to the first solid particle distributor, and the transport horizontal pipe and the first solid particle distributor are of a T-shaped structure.

[0010] In the technical solution provided by the present invention, the first solid particle distributor has holes, and the hole opening rate is 5% - 70%, preferably 20% - 40%; preferably, the lower part of the first solid particle distributor has uniformly distributed holes.

[0011] In the technical solution provided by the present invention: the hole opening rate of the bottom distributor is 3% - 70%, preferably 40% - 65%; preferably, the hole opening of the bottom distributor is set such that the hole opening rate in the middle is low and the hole opening rate around is high; preferably, the bottom distributor is a circular plate.

[0012] In the technical solution provided by the present invention: the overflow distributor is frustum-shaped with the upper bottom surface facing downwards and the lower bottom surface facing upwards, and the aperture ratio of the overflow distributor is 4% - 75%, preferably 30% - 45%.

[0013] In the technical solution provided by the present invention: the included angle between the generatrix and the axis of the frustum-shaped overflow distributor is 15° - 80°, preferably 35° - 60°.

[0014] In the technical solution provided by the present invention: the ratio of the diameter of the second solid particle distributor system to the diameter of the reactor is 0.1 - 0.95, preferably 0.5 - 0.8.

[0015] In the technical solution provided by the present invention: the fluidizing gas distributor is one or more annular pipes; the aperture ratio of the fluidizing gas distributor is 5% - 40%, preferably 10% - 25%; the fluidizing gas of the fluidizing gas distributor includes but is not limited to one or more of air, nitrogen, dry gas, liquefied gas, and water vapor.

[0016] In the technical solution provided by the present invention: the rectifying gas distributor has openings on its surface, and the aperture ratio is 5% - 35%, preferably 10% - 20%; the rectifying gas of the rectifying gas distributor includes but is not limited to one or more of air, nitrogen, dry gas, liquefied gas, and water vapor.

[0017] A method for using a distributor system of a circulating fluidized bed countercurrent reactor, characterized by comprising the following steps:

[0018] (1) Install a conveying pipe, a first solid particle distributor, a second solid particle distributor, a rectifying gas distributor, and a fluidizing gas distributor on the reactor;

[0019] (2) The rectifying gas passes through the reactor wall and enters the rectifying gas distributor, and the fluidizing gas passes through the reactor wall and enters the fluidizing gas distributor;

[0020] (3) One end of the conveying inclined pipe outside the reactor is connected to the regenerator, and the solid particles enter the first solid particle distributor from the regenerator through the conveying inclined pipe and the conveying horizontal pipe, and enter the second solid particle distributor through the openings on the surface of the first solid particle distributor under the action of the rectifying gas of the rectifying gas distributor;

[0021] (4) The solid particles are in the second solid particle distributor and are uniformly fluidized into a fluidized bed layer under the fluidization of the fluidizing gas. The solid particles are divided into two parts and enter the reactor. The first part enters the reactor through the bottom distributor, and the second part enters the reactor through the overflow distributor;

[0022] (5) Adjust the equipment parameters and operation parameters of the distributor to make the solid particles evenly distributed;

[0023] (6) The raw material gas in the reactor flows upward from the lower part of the reactor, making countercurrent contact with the uniformly distributed solid particles to achieve mass transfer, heat transfer, and reaction.

[0024] The beneficial effects that can be obtained by the present invention are as follows:

[0025] When the distributor provided by the present invention is in use, the solid particles do not directly enter the reactor through the conveying inclined pipe and the conveying horizontal pipe. Instead, they first enter the first solid particle distributor. By controlling the opening ratio of the first solid particle distributor, a certain height of the material level is formed therein. The solid particles that are offset to one side of the conveying pipe do not directly enter the distributor, but aggregate into a cylindrical material in the first solid particle distributor and enter the second solid particle distributor in the form of dense-phase transportation, which can solve the problem that the solid particles concentrate on one side when entering the reactor.

[0026] The rectifying gas distributor arranged in the first solid particle distributor has two functions. One is to make the solid particles entering the first solid particle distributor in a deflected flow state in a uniform fluidization state through the fluidization effect, and at the same time prevent the solid particles from accumulating in the first solid particle distributor. The other is the distribution function. The air flow size and direction of the rectifying distributor control the solid particle flow rate of the solid particles entering the second solid particle distributor in all directions.

[0027] The solid particles entering the second solid particle distributor are divided into three paths after being fluidized by the fluidizing gas distributor. The first path falls into the reactor through the openings of the bottom distributor. The second path enters the reactor through the surface openings of the overflow distributor. The third path flows upward through the overflow distributor and falls from the outside of the overflow distributor when the material is higher than the overflow distributor. By controlling the opening ratio of each part of the distributor, the gas flow rate of the fluidizing gas distributor, and the size of the distributor, the solid particles are evenly distributed in the reactor. Description of the Drawings

[0028] Appendix Figure 1 It is a schematic diagram of the situation where the solid particles are offset to one side in the background art.

[0029] Appendix Figure 2 It is a schematic diagram of the situation where the solid particles are offset to one side in the background art.

[0030] Appendix Figure 3 It is a front view of the distributor of the present invention.

[0031] Appendix Figure 4 It is a top view of the bottom distributor of the present invention.

[0032] Appendix Figure 5 It is a side expanded view of the overflow distributor of the present invention.

[0033] Appendix Figure 6 It is a top view of the fluidizing gas distributor of the present invention.

[0034] Attached Figure 7 is a side unfolded view of the first solid particle distributor of the present invention.

[0035] Attached Figure 8 is a side unfolded view of the rectifying gas distributor of the present invention.

[0036] Attached Figure 9 is a front view of the conveying structure used in Experimental Group 1 of the present invention.

[0037] The descriptions of each number in the attached drawings are as follows: 1-1 - solid particle conveying pipe, 2-1 - connecting elbow, 3-1 - reactor, 4-1 - solid particles, 1-2 - solid particle conveying pipe, 2-2 - horizontal pipe blind plug, 3-2 - reactor, 4-2 - solid particles, 5 - conveying inclined pipe, 6 - conveying horizontal pipe, 7 - first solid particle distributor, 8 - overflow distributor, 9 - fluidizing gas distributor gas, 10 - bottom distributor, 11 - fluidizing gas, 12 - rectifying gas, 13 - blind plug, 14 - rectifying gas distributor, 15 - reactor, 16 - bottom distributor opening, 17 - first solid particle distributor opening, 18 - rectifying gas distributor opening, 19 - overflow distributor opening, 20 - fluidizing gas distributor opening, 5 and 6 form the conveying pipe, 9 and 10 form the second solid particle distributor. Detailed implementation manners

[0038] The attached drawings are only for illustrative purposes, and prior art or common knowledge is omitted. The following will be further described in combination with the attached drawings of the present invention.

[0039] As Figure 3 shown, a distributor of a circulating fluidized bed countercurrent reactor includes: a reactor (15), a conveying pipe (5 and 6), a first solid particle distributor (7), a second solid particle distributor (8 and 10), a rectifying gas distributor (14), and a fluidizing gas distributor (9); the conveying pipe (5 and 6) includes a conveying inclined pipe (5) and a conveying horizontal pipe (6), the conveying inclined pipe (5) is connected to the conveying horizontal pipe (6), and the middle of the conveying horizontal pipe (6) is connected to the first solid particle distributor (7); the second solid particle distributor (8 and 10) is located below the first solid particle distributor (7), and the first solid particle distributor (7) is inserted into the second solid particle distributor (8 and 10); the second solid particle distributor (8 and 10) includes an overflow distributor (8) and a bottom distributor (10), the overflow distributor (8) is perforated around, the bottom of the overflow distributor (8) is connected to the bottom distributor (10), and the bottom distributor (10) is perforated; the rectifying gas distributor (14) is arranged in the second solid particle distributor (8 and 10); the fluidizing gas distributor (9) is inserted into the first solid particle distributor (7).

[0040] The conveying inclined pipe (5) penetrates into the reactor (15) through the surface of the reactor (15), and one end of the conveying inclined pipe (5) inside the reactor (15) is connected to the conveying horizontal pipe (6); one end of the conveying horizontal pipe (6) is connected to the conveying inclined pipe (5), and the other end is blind-plugged; the middle of the conveying horizontal pipe (6) is connected to the first solid particle distributor (7), and the conveying horizontal pipe (6) and the first solid particle distributor (7) are of a T-shaped structure; the lower part of the first solid particle distributor (7) is uniformly provided with holes, and the hole opening rate is 30%.

[0041] The bottom distributor (10) is a circular plate, with a hole opening rate of 10% in the middle and 15% and a hole opening rate of 25% in the remaining part.

[0042] The overflow distributor (8) is a frustum of a cone with the upper bottom surface facing down and the lower bottom surface facing up, and the hole opening rate of the overflow distributor (8) is 35%; the included angle between the generatrix and the axis of the overflow distributor (8) is 45°.

[0043] The ratio of the diameter of the second solid particle distributor (8 and 10) system to the diameter of the reactor (15) is 0.75.

[0044] The fluidizing gas distributor (9) is a single annular pipe; the hole opening rate of the fluidizing gas distributor (9) is 15%; the fluidizing gas of the fluidizing gas distributor (9) is nitrogen.

[0045] The rectifying gas distributor (14) has holes on its surface, and the hole opening rate is 15%; the rectifying gas of the rectifying gas distributor (14) is nitrogen.

[0046] A method for using a distributor system of a circulating fluidized bed counter-current reactor, which is characterized by including the following steps:

[0047] (1) Install the conveying pipes (5 and 6), the first solid particle distributor (7), the second solid particle distributor (8 and 10), the rectifying gas distributor (14), and the fluidizing gas distributor (9) on the reactor (15);

[0048] (2) The rectifying gas passes through the reactor (15) wall and enters the rectifying gas distributor (14), and the fluidizing gas passes through the reactor (15) wall and enters the fluidizing gas distributor (9);

[0049] (3) One end of the conveying inclined pipe (5) outside the reactor (15) is connected to the regenerator, and the solid particles enter the first solid particle distributor (7) from the regenerator through the conveying inclined pipe (5) and the conveying horizontal pipe (6), and enter the second solid particle distributor (8 and ①) through the holes on the surface of the first solid particle distributor (7) under the action of the rectifying gas of the rectifying gas distributor (14);

[0050] (4) The solid particles are fluidized by the fluidizing gas in the second solid particle distributor (8 and 10) to form a uniform fluidized bed. The solid particles enter the reactor (15) in two parts. The first part enters the reactor (15) through the bottom distributor (10), and the second part enters the reactor (15) through the overflow distributor (8);

[0051] (5) The solid particles are evenly distributed by adjusting the equipment parameters and operating parameters of the distributor;

[0052] (6) The raw gas in the reactor (15) flows upward from the bottom of the reactor (15), contacts the evenly distributed solid particles in reverse direction, and realizes mass transfer, heat transfer and reaction.

[0053] Example 1.

[0054] This embodiment includes 2 experimental groups and 1 control group. Control group 1 illustrates the distribution of solid particles in a biased flow state, experimental group 1 illustrates the function of the first solid particle distributor, and experimental group 2 illustrates the overall function of the distributor provided by this patent. Both the experimental group and the control group were tested in a cold countercurrent reactor. The test conditions are as follows: the cold countercurrent reactor used in this embodiment is made of acrylic material, so the situation inside the reactor can be directly observed; the control group 1 uses Figure 2 The transport structure shown in the figure, experimental group 1 uses Figure 9 The conveying structure shown (in Figure 3 The overflow distributor and fluidizing gas distributor are removed based on the transport structure shown in the figure. The bottom of the first solid particle distributor is sealed with a circular plate with a 10% opening rate. Figure 3 The transport structure shown in the figure; the solid particles used are spherical catalyst particles with an average particle size of 80 microns; the gas phase medium is nitrogen; the reactor inner diameter is 45 cm, the height is 235 cm, the gas velocity in the reactor is 0.3 m / s, and the catalyst circulation speed is 50 kg / (m 2 ·s); the delivery pipe has an inner diameter of 70 mm and an outer diameter of 100 mm; the first solid particle distributor has an inner diameter of 80 mm and an outer diameter of 100 mm; the uppermost diameter of the overflow distributor is 340 mm, and the lowermost diameter of the overflow distributor is 160 mm; 16 evenly distributed measuring holes with a diameter of 8 mm are opened on the same cross-section in the middle of the reactor, the measuring hole located below the delivery inclined pipe is marked as the 0° measuring hole, and the measuring holes are marked as 45°, 90°, 135°, 180°, 225°, 270°, and 315° in the clockwise direction when viewed from top to bottom; the distribution of the catalyst in the reactor is detected using an insert-type solid particle concentration meter, and each measuring hole measures 11 points outward from the center of the reactor, and the measuring points are 0 cm, 2 cm, 4 cm, 6 cm, 8 cm, 10 cm, 12 cm, 14 cm, 16 cm, 18 cm, and 20 cm from the center of the reactor from the inside to the outside.

[0055] The circulation routes of the catalysts in the test process of the three groups in this embodiment are as follows: the catalyst of the experimental group enters the distributor from the regenerator through the delivery pipe, enters the reactor after being distributed by the distributor, and moves downward after entering the reactor to form a dense phase zone at the bottom of the reactor. The catalyst in the dense phase zone enters the regenerator through the catalyst delivery pipeline, and the gaseous medium is divided into two paths, one entering the bottom of the reactor and the other entering the lower part of the reactor (above the catalyst dense phase zone). Both gaseous media move upward and exit the device through the filter at the top of the reactor; the catalyst circulation route of the control group does not pass through the distributor, and the rest is the same as the experimental group.

[0056] According to the above test conditions, the catalyst flow rate at each measuring point is detected.

[0057] The results of control group 1 are shown in Table 1.

[0058] Table 1 Catalyst flow rate data at different distances between each measuring port and the reactor center in control group 1

[0059]

[0060] The results of experimental group 1 are shown in Table 2.

[0061] Table 2 Catalyst flow rate data at different distances from each measuring port to the reactor center in experimental group 1

[0062]

[0063] The results of experimental group 2 are shown in Table 2.

[0064] Table 3 Catalyst flow rate data at different distances from each measuring port to the reactor center in experimental group 2

[0065]

[0066] The results of the control group in Table 1 show that the catalyst flow rate at the 0° measuring hole is the lowest, and the catalyst flow rate at the 180° measuring hole is the highest, that is, the catalyst flow rate is low on the side close to the transport inclined tube, and high on the side away from the transport inclined tube. The catalyst is more distributed on one side of the transport inclined tube due to inertia. The results of experimental group 1 in Table 2 show that the catalyst in the reactor is more in the center and less around, and the overall distribution is symmetrical, which corrects the problem of catalyst deviation due to inertia. The results of experimental group 2 in Table 3 show that the catalyst flow rate at various locations in the reactor is basically uniform, with a flow rate of 56 to 64 kg / (m 2 ·s).

Claims

1. A distributor system for a circulating fluidized bed countercurrent reactor, characterized in that: include: Reactor, conveying pipe, first solid particle distributor, second solid particle distributor, rectifying gas distributor, fluidizing gas distributor; The delivery pipe includes a delivery inclined pipe and a delivery transverse pipe, the delivery inclined pipe is connected to the delivery transverse pipe, and the middle of the delivery transverse pipe is connected to the first solid particle distributor; The second solid particle distributor is located below the first solid particle distributor, and the first solid particle distributor is inserted into the second solid particle distributor; The second solid particle distributor includes an overflow distributor and a bottom distributor, the overflow distributor has holes around it, the bottom of the overflow distributor is connected to the bottom distributor, and the bottom distributor has holes; The rectifying gas distributor is arranged in the second solid particle distributor; The fluidizing gas distributor is inserted into the first solid particle distributor.

2. The distributor system of a circulating fluidized bed countercurrent reactor according to claim 1, characterized in that: The delivery inclined tube penetrates into the reactor through the surface of the reactor, and one end of the delivery inclined tube in the reactor is connected to the delivery horizontal tube; One end of the conveying horizontal pipe is connected to the conveying inclined pipe, and the other end is blindly blocked; The middle portion of the conveying transverse pipe is connected to the first solid particle distributor, and the conveying transverse pipe and the first solid particle distributor are T-shaped structures.

3. The distributor system of a circulating fluidized bed countercurrent reactor according to claim 1, characterized in that: The first solid particle distributor has openings, and the opening rate is 5% to 70%; Preferably, the first solid particle distributor has uniform openings at the bottom; Preferably, the opening rate of the first solid particle distributor is 20% to 40%.

4. The distributor system of a circulating fluidized bed countercurrent reactor according to claim 1, characterized in that: The bottom distributor has an opening rate of 3% to 70%; Preferably, the opening rate of the bottom distributor is 40% to 65%; Preferably, the bottom distributor opening is set as follows: the opening rate in the middle is low and the opening rate around is high; Preferably, the bottom distributor is a circular plate.

5. The distributor system of a circulating fluidized bed countercurrent reactor according to claim 1, characterized in that: The overflow distributor is in the shape of a truncated cone with the upper bottom facing downward and the lower bottom facing upward, and the opening rate of the overflow distributor is 4% to 75%; Preferably, the opening rate of the overflow distributor is 30% to 45%.

6. The overflow distributor according to claim 5, characterized in that: The included angle between the generatrix and the axis of the truncated cone overflow distributor is 15° to 80°, preferably 35° to 60°.

7. The distributor system of a circulating fluidized bed countercurrent reactor according to claim 1, characterized in that: The ratio of the diameter of the second solid particle distributor system to the diameter of the reactor is 0.1 to 0.95; Preferably, the ratio of the solid particle distributor system diameter to the reactor diameter is 0.5 to 0.

8.

8. The distributor system of a circulating fluidized bed countercurrent reactor according to claim 1, characterized in that: The fluidizing gas distributor is one annular tube or multiple annular tubes, the opening rate of the fluidizing gas distributor is 5% to 40%, and the fluidizing gas of the fluidizing gas distributor includes but is not limited to one or more of air, nitrogen, dry gas, liquefied gas and water vapor; Preferably, the opening rate of the rectifying gas distributor is 10% to 25%.

9. The distributor system of a circulating fluidized bed countercurrent reactor according to claim 1, characterized in that: The surface of the rectifying gas distributor is perforated, and the porosity is 5% to 35%. The rectifying gas of the rectifying gas distributor is but not limited to one or more of air, nitrogen, dry gas, liquefied gas and water vapor; Preferably, the opening rate of the rectifying gas distributor is 10% to 20%.

10. The method for using the distributor system of a circulating fluidized bed countercurrent reactor according to any one of claims 1 to 9, characterized in that: The steps include: (1) Installing a conveying pipe, a first solid particle distributor, a second solid particle distributor, a rectifying gas distributor, and a fluidizing gas distributor on the reactor; (2) The rectifying gas passes through the reactor wall into the rectifying gas distributor, and the fluidizing gas passes through the reactor wall into the fluidizing gas distributor; (3) One end of the transport inclined tube reactor is connected to a regenerator, and solid particles enter the first solid particle distributor from the regenerator through the transport inclined tube and the transport horizontal tube, and enter the second solid particle distributor through the openings on the surface of the first solid particle distributor under the action of the rectifying gas of the rectifying gas distributor; (4) The solid particles are fluidized by the fluidizing gas in the second solid particle distributor to form a uniform fluidized bed. The solid particles enter the reactor in two parts. The first part enters the reactor through the bottom distributor, and the second part enters the reactor through the overflow distributor. (5) The solid particles are evenly distributed by adjusting the equipment parameters and operating parameters of the distributor; (6) The raw gas in the reactor flows upward from the bottom of the reactor, contacts the evenly distributed solid particles in reverse direction, and realizes mass transfer, heat transfer and reaction.

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