A spiral distributor system for a circulating countercurrent bed reactor and its application method

Abstract

The present invention belongs to the technical field of devices for chemical method applications, and specifically relates to a spiral distributor system for a circulating countercurrent bed reactor and its application method. The spiral distributor system includes a settler, a reactor, a solid distributor, a feeder and an air duct; the solid distributor is a spiral three-dimensional disk, which includes an inner layer, an inner second layer, a middle layer, an outer layer and an outer second layer of spiral tubes from the inside to the outside, forming a three-dimensional disk from top to bottom, and is integrally formed; the outer second layer is installed on an annular support and fixed to the reactor wall through the annular support; the top of the solid distributor extends upward into the settler, and the air duct is evenly distributed at equal angles on the reactor and the circumference of the settler outside the solid distributor. The spiral solid distributor used in the present invention has circular holes evenly distributed on the bottom end surface of the spiral tube to achieve radial continuity, solve the problem of particles piling up and falling in the middle of the reactor, and achieve solid particles sliding evenly on the entire distributor disk.

Description

Technical Field

[0001] The present invention belongs to the technical field of devices for applying chemical methods, and specifically relates to a spiral distributor system of a circulating countercurrent bed reactor and an application method thereof, which can be applied to the fields of petrochemical industry, coal pyrolysis, waste plastic cracking, coking, etc. Background Art

[0002] At present, energy industries such as petrochemicals, coal chemicals, and waste plastic recycling chemicals mostly use circulating fluidized beds as the main catalytic reactors. Circulating fluidized beds are divided into co-current fluidized beds and counter-current fluidized beds. In the circulating counter-current fluidized bed, solid particles move downward from the top of the reactor, while the gas moves upward. The gas-solid phase is in a counter-current contact state, and the gas-solid contact efficiency is better than that of the co-current bed, which is conducive to reverse mass transfer and heat transfer between the gas-solid phase, and can significantly improve the reaction efficiency and the yield of the target product. Taking the catalytic cracking of waste plastics as an example, in the reactor, the hot gas of the waste plastics needs to achieve uniform contact with the solid catalyst particles to occur mass transfer and heat transfer. In the axial direction of the reactor, the reaction temperature and the active atmosphere of the catalyst are continuously increased and enhanced as the reaction proceeds, which can meet the energy demand of the negative correlation between the molecular weight of the same hydrocarbons and the cracking activation energy, and can achieve the purpose of adapting the optimal cracking conditions for hydrocarbons of different molecular weights in the process of waste plastic cracking, and improve the selectivity of the target product short-chain low-carbon olefins.

[0003] The circulating countercurrent bed in the energy industry is generally larger in inner diameter due to the sum of the solid particle processing volume and the reaction time, resulting in extremely uneven distribution of solid particles inside. If a solid distributor system is not installed, the solid particles generally present a "ring-core" flow distribution with the same diameter as the lower agent port, which limits the gas-solid contact area and significantly affects the gas-solid mass transfer and heat transfer efficiency. At present, the general circulating countercurrent bed solid distributor mostly adopts a horizontal plate distributor. Such distributors generally have openings arranged in sequence around the center of the circle, and there is a certain spacing between each row of openings, resulting in the true distribution form of catalyst particles inside the reactor being a multi-layer "ring-core" flow structure, resulting in alternating dilute phase and dense phase areas of solid particles inside the reactor, affecting gas-solid mass transfer. Moreover, the installation of a solid distributor will hinder the passage of rising gas, thereby causing particles to fall. Therefore, it is particularly necessary to design a reasonable solid distributor system to make the radial solid phase particles more evenly distributed and enable the particles to fall smoothly.

[0004] The purpose of installing a circulating countercurrent bed distributor is to ensure that solid particles exist in a uniform dilute and dense phase in the reactor and cannot accumulate on the distributor. Currently, most of these solid distributors do not consider the continuity of the openings in the radial direction, resulting in the particles being distributed in a "ring-core" form with alternating dilute and dense phase areas on the disk surface. Summary of the invention

[0005] The technical problem to be solved by the present invention is to provide a spiral distributor system for a circulating countercurrent bed reactor and an application method thereof, so as to solve the problem that the radial distribution of the solid distributor system is uneven and the gas velocity hinders the falling of solid particles.

[0006] The technical solution adopted is as follows.

[0007] A spiral distributor system for a circulating countercurrent bed reactor, comprising a settler, a reactor and an air guide pipe, wherein the settler is connected to the reactor via an inclined gentle slope, and wherein the spiral distributor system further comprises a solid distributor and a feeder;

[0008] The feeder comprises a regeneration inclined tube, a buffer tube and a lower feed port, the end of the buffer tube is connected to the lower feed port vertically downward, the regeneration inclined tube, the buffer tube and the lower feed port are integrally formed and connected by smooth curved surfaces;

[0009] The solid distributor comprises a spiral tube, which forms a spiral three-dimensional disk and is integrally formed. The spiral tube comprises an inner layer, an inner second layer, a middle layer, an outer layer and an outer second layer from the inside to the outside, and spirally forms a three-dimensional disk from top to bottom, with the inner layer at the top and the outer second layer at the bottom; the outer second layer is installed on an annular support and fixed to the reactor wall through the annular support; circular holes are evenly distributed on the bottom end surface of the spiral tube;

[0010] The inner layer extends upward into the settler, with its top facing the bottom of the lower dose opening. A circular flat plate portion is arranged at the top of the inner layer, and the flat plate portion is opened, the size of the opening being adapted to the lower dose opening.

[0011] Preferably, the regeneration inclined tube extends from the side wall of the settler into the interior of the settler at an angle of 45°; the buffer tube includes a vertical buffer tube and an inclined buffer tube, the vertical buffer tube is parallel to the side wall of the settler, and the inclined buffer tube forms an angle of 45° with the vertical buffer tube.

[0012] Preferably, the top of the inner layer is connected to the bottom of the lower port or the distance between them is no more than 1 / 3 of the inner diameter of the reactor. The diameter of the spiral tube is equal to or slightly larger than the diameter of the lower port.

[0013] Preferably, the height from the top of the inner layer to the bottom of the outer layer is 1 to 2 times the inner diameter of the reactor; and the diameter of the settler is 2 to 5 times the diameter of the reactor.

[0014] Preferably, on the spiral three-dimensional disk of the solid distributor, the inner first layer, the inner second layer, the middle layer, the outer first layer and the outer second layer each occupy 20% of the disk diameter.

[0015] Preferably, the outer diameter of the annular support is the same as the inner diameter of the reactor, and is mounted on the reactor wall via a support rod or a fixing slot.

[0016] Preferably, the diameter of the circular hole accounts for 30-50% of the diameter of the spiral tube, and the total opening rate is 40-60%.

[0017] Preferably, the spiral tube is inclined and spirally distributed downward, and the inclination angle is greater than the repose angle of the catalyst solid particles used, and the inclination angle is 0.1 to 5 degrees higher than the repose angle.

[0018] Preferably, the number of the air guide pipes is 4 to 8, which are evenly distributed at equal angles around the reactor and settler outside the solid distributor; the top connection port of the air guide pipe is located on the settler wall above the lower agent port, and the bottom connection port is located on the reactor wall below the annular support.

[0019] An application method of a spiral distributor system of a circulating countercurrent bed reactor comprises the following steps:

[0020] (1) The outer side of the annular support of the solid distributor is in close contact with the wall of the reactor and is fixed to the reactor wall through a support rod or a fixing slot. The bottom end of the solid distributor is welded to the annular support;

[0021] (2) A connection hole adapted to the feeder regeneration inclined tube is arranged on the wall of the settler, and the regeneration inclined tube extends out of the settler through the connection hole to connect to the regenerator. The lower agent port is arranged on the central axis of the settler, and the catalyst solid particles are transported from the regenerator to the bottom of the lower agent port through the regeneration inclined tube conveying air and fall onto the solid distributor;

[0022] (3) After the catalyst solid particles fall onto the solid distributor, they slide down along the spiral tube through the inner layer, the second inner layer, the middle layer, the outer layer, and the second outer layer. The solid particles pass through the circular holes on the spiral tube to achieve uniform radial distribution.

[0023] (4) The pressure difference between the settler and the reactor caused by the transportation of solid particles is balanced through the air duct, so that there is no particle accumulation above the solid distributor and the particles fall smoothly and stably, thereby achieving steady-state long-term operation of the reaction.

[0024] Compared with the prior art, the present invention has the following beneficial effects.

[0025] (1) The spiral solid distributor used in the present invention has the same inclination angles for the inner layer, the second inner layer, the middle layer, the outer layer, and the second outer layer on the spiral channel, which can solve the problem of particles accumulating and falling in the middle of the reactor and achieve uniform sliding of solid particles on the entire distributor disc.

[0026] (2) The spiral solid distributor used in the present invention, the spiral channel and the different opening sizes and opening densities on each layer of the channel can achieve the continuity of the openings in the radial direction, avoiding the "ring-core" distribution of particles on the disk surface in the form of alternating dilute phase and dense phase areas, and presenting a continuous uniform distribution.

[0027] (3) The upper and lower connected air ducts used in the present invention can solve the problem that particles are difficult to fall due to the installation of a solid distributor, ensure the stability of the particle circulation rate, and realize the steady-state long-term operation of the entire circulating countercurrent bed. BRIEF DESCRIPTION OF THE DRAWINGS

[0028] Figure 1 It is a front view of the spiral solid distributor system of the present invention.

[0029] Figure 2 1 is a structural diagram of the spiral solid distributor of the present invention, wherein (I) is a top view and (II) is a front view.

[0030] Figure 3 This is an axial position diagram of the measurement site of the reactor in an embodiment of the present invention.

[0031] Figure 4 This is a radial position azimuth diagram of the reactor measurement site in an embodiment of the present invention.

[0032] Figure 5 This is a comparison curve of the dimensionless radial position and solid volume fraction in the SN direction with and without a solid distributor in Example 1 of the present invention.

[0033] Figure 6 This is a comparison curve of the dimensionless radial position and solid volume fraction in the EW direction when a solid distributor is added and when no solid distributor is added in Example 1 of the present invention.

[0034] Figure 7 This is a dimensionless radial position and solid volume fraction curve when the spiral distributor is installed in Example 2 of the present invention when the axial height Z is 210 mm.

[0035] Figure 8 This is a dimensionless radial position and solid volume fraction curve when a spiral distributor is installed in Example 2 of the present invention when the axial height Z is 40 mm.

[0036] In the figure, 1-regeneration inclined tube, 2-vertical buffer tube, 3-inclined buffer tube, 4-lower agent port, 5-settler, 6-solid distributor, 7-air guide tube, 8-annular support, 9-support rod, 10-inner layer, 11-inner second layer, 12-middle layer, 13-outer layer, 14-outer second layer, 15-reactor, 16-circular hole. DETAILED DESCRIPTION

[0037] The accompanying drawings are only used for illustrative purposes, and the prior art or common knowledge is omitted. The present application is further described in detail below in conjunction with the accompanying drawings. It is necessary to point out that the following specific implementation methods are only used to further illustrate the present application and cannot be understood as limiting the scope of protection of the present application. Those skilled in the art can make some non-essential improvements and adjustments to the present application based on the above application content.

[0038] The present invention has been applied to the cold state device and the hot state device of the waste plastic circulating countercurrent bed. The cold state device is made of acrylic organic glass, and the hot state device is made of 304 stainless steel material due to the need for high temperature of waste plastic cracking; and the cold state device and the hot state device have the same size, and the inner diameter of the reactor 15 is 10 cm.

[0039] like Figure 1 As shown, a spiral distributor system of a circulating countercurrent bed reactor includes a settler 5 and a reactor 15. The settler 5 is connected to the reactor 15 by an inclined gentle slope. The spiral distributor system also includes a solid distributor 6, a feeder and an air guide pipe 7.

[0040] The feeder is integrally formed, including a regeneration inclined pipe 1, a buffer pipe and a lower agent port 4. The buffer pipe includes a vertical buffer pipe 2 and an inclined buffer pipe 3. The connection is a smooth curved surface connection. The regeneration inclined pipe 1 penetrates into the settler 5 from the side wall of the settler 5 at an angle of 45°. The vertical buffer pipe 2 is parallel to the side wall of the settler 5, and the inclined buffer pipe 3 is at an angle of 45° with the vertical buffer pipe. This ensures smooth transportation of catalyst particles.

[0041] like Figure 2 As shown, the solid distributor 6 is a spiral three-dimensional disk, which includes five layers of spiral tubes from the inside to the outside, namely, the inner layer 10, the inner second layer 11, the middle layer 12, the outer layer 13 and the outer second layer 14, forming a three-dimensional disk from top to bottom, which is integrally formed, with the inner layer 10 at the top and the outer second layer 14 at the bottom. Among them, the outer second layer 14 is installed on the annular support 8 and fixed to the wall of the reactor 15 through the annular support 8. The outer side of the outer second layer 14 is connected to the annular support 8, the outer diameter of the annular support 8 is the same as the inner diameter of the reactor 15, and is fixed to the wall of the reactor 15 through the support rod 9, thereby fixing the solid distributor 6. Circular holes 16 are evenly distributed on the bottom end surface of the spiral tube.

[0042] The top of the solid distributor 6 extends upward into the settler 5 , and a circular flat plate portion is provided at the top of the inner layer 10 . The flat plate portion is open and connected to the bottom end of the lower port 4 . The diameter of the spiral tube is equal to that of the lower port 4 .

[0043] The number of the air guide pipes 7 is 4 and they are evenly distributed at equal angles around the reactor 15 and the settler 5 outside the solid distributor 6 .

[0044] As a further preferred embodiment, the height from the top of the inner layer 10 to the bottom of the outer second layer 14 is 1.5 times the inner diameter of the reactor 15. The diameter of the settler 5 is twice the diameter of the reactor 15.

[0045] On the spiral three-dimensional disk of the solid distributor 6, the inner layer 10, the inner second layer 11, the middle layer 12, the outer layer 13 and the outer second layer 14 each account for 20% of the disk diameter, and the spiral tube forms a spiral channel for the catalyst solid particles; circular holes 16 are evenly distributed on each layer of the spiral tube. The diameter of the circular hole 16 accounts for 50% of the diameter of the spiral tube, and the total opening rate is 50%. In general, the diameter of the circular hole 16 is set to match the diameter of the catalyst solid particles used.

[0046] The spiral tube is inclined and spirally distributed downward, and the inclination angle is greater than the repose angle of the catalyst solid particles used, and the inclination angle is 0.5 degrees higher than the repose angle.

[0047] The top connection port of the air guide pipe 7 is located on the wall of the settler 5 above the lower agent port 4 , and the bottom connection port is located on the wall of the reactor 15 below the annular support 8 .

[0048] An application method of a spiral distributor system of a circulating countercurrent bed reactor comprises the following steps:

[0049] (1) The outer side of the annular support 8 of the solid distributor 6 is in close contact with the wall of the reactor 15 and is fixed to the wall of the reactor 15 by the support rod 9. The bottom end of the solid distributor 6 is welded to the annular support 8.

[0050] (2) The wall of the settler 5 is provided with a connection hole adapted to the regeneration inclined tube 1 of the feeder. The regeneration inclined tube 1 extends out of the settler 5 through the connection hole to connect with the regenerator. The lower agent port 4 is provided on the central axis of the settler 5. The catalyst solid particles are transported from the regenerator to the bottom of the lower agent port 4 through the conveying air of the regeneration inclined tube 1 and fall onto the solid distributor 6.

[0051] (3) The catalyst solid particles fall onto the solid distributor 6, enter the spiral tube through the top opening of the inner layer, and slide downward through the spiral channels of the inner layer 10, the second inner layer 11, the middle layer 12, the outer layer 13, and the second outer layer 14, and complete uniform radial distribution through the circular holes 16 on the spiral tube. Due to the setting of the appropriate inclination angle, the amount of falling particles in the conical area is guaranteed, and the accumulation of particles inside is avoided.

[0052] (4) The settler 5 and the reactor 15 balance the pressure difference caused by the transportation of solid particles through the air duct 7, so that there is no particle accumulation above the solid distributor 6 and the particles fall smoothly and stably, thereby achieving steady-state long-term operation of the reaction.

[0053] The cold state embodiment measures the particle concentration at seven radial positions at each axial height in the reactor 15 by means of an optical fiber concentration tester, mainly illustrating the influence of the spiral distributor system on the radial distribution uniformity of solid particles in the reactor 15 .

[0054] The hot state example catalytically cracks waste plastics at high temperature in a hot state device to explore the distribution of waste plastic catalytic cracking products before and after the installation of the solid distributor 6, and further illustrate the effect of the installation of the solid distributor 6 on mass transfer, heat transfer and reaction efficiency in the circulating countercurrent bed reactor.

[0055] Example 1.

[0056] This embodiment includes two groups of cases, an experimental group and a control group, both of which are carried out in a cold circulating countercurrent bed device, wherein the experimental group is installed with the solid distributor 6, feeder and air guide pipe 7 of the spiral distributor system, while the control group is not installed.

[0057] In both experiments, the countercurrent gas velocity in the reactor 15 was controlled to be 0.6 m / s, and the particle circulation rate was 43.23 kg / (m 2 •s), the solid concentration at each radial position is measured by an optical fiber concentration tester, and the solid concentration at different radial positions in the SN direction and EW direction of the reactor countercurrent section is measured respectively (expressed as solid volume fraction, which will not be repeated below). The radial position is expressed by dimensionless radial r / R, where r / R=0 at the center and r / R=1 at the side wall. Figure 4 The experimental results of the solid concentration in the SN and EW directions measured by the radial position azimuth diagram are shown in Figure 5 , Figure 6 shown.

[0058] like Figure 5 As shown in the figure, the data of the control group are analyzed to show that when the solid distributor 6, feeder and air duct 7 are not installed, the solid particles as a whole show the characteristics of low center concentration and high wall concentration, which is a typical feature of "ring-core" flow distribution. The maximum deviation on both sides of the SN direction is -115%~+105% compared with the deviation at the center. Figure 6 As shown, the solid particles in the control group also show the characteristics of low center concentration and high wall concentration. The maximum deviation on both sides of the EW direction is -105%~+107% compared with the deviation in the center. Figure 5 , Figure 6 The data of the experimental group show that when the solid distributor 6, feeder and air guide 7 of the rotating distributor system are placed, the "ring-core" flow distribution of particles is significantly improved, and the solid particle concentration at each position fluctuates up and down, with a fluctuation range of ±5%. Through the above case analysis, the spiral channel in the spiral distributor system can avoid the "ring-core" distribution of particles on the disk surface in the form of alternating dilute phase and dense phase areas, and achieve radial continuous uniform distribution.

[0059] Example 2.

[0060] This embodiment is carried out in a cold circulating countercurrent bed device, with a solid distributor 6 installed, an air guide pipe 7 provided, and a feeder installed, including a regeneration inclined pipe 1, a vertical buffer pipe 2, an inclined buffer pipe 3 and a lower feed port 4.

[0061] In the experiment, the countercurrent gas velocity in the reactor 15 was controlled to be 0.4 m / s, and the particle circulation rate was 29.64 kg / (m 2 •s), the solid concentration at each radial position is measured by an optical fiber concentration tester, and the solid concentration at different radial positions in the SN direction and EW direction of the reactor countercurrent section is measured respectively (expressed as solid volume fraction, which will not be repeated below). The radial position is expressed by dimensionless radial r / R, where r / R=0 at the center and r / R=1 at the side wall. Figure 3 The axial position azimuth diagram was used to measure the solid phase concentration at two axial positions of the reactor countercurrent section at axial height Z=210mm and Z=40mm. The test results are as follows: Figure 7 , Figure 8 shown.

[0062] Combination Figure 7 , Figure 8 As shown, by analyzing the data of the experimental group, it can be seen that after placing the solid distributor 6, feeder and air duct 7 of the rotating distributor at different axial heights, the disturbance during the operation of the reactor 15 is changed by changing the countercurrent gas velocity and particle circulation rate. It is found that the disturbance cannot change the stability of the solid particle distribution inside the reactor 15, and the solid particle concentration at each position still fluctuates up and down, with a fluctuation range of ±6%. Through the above case analysis, the radial continuous uniform distribution achieved in the spiral distributor system is less affected by external disturbances and can operate stably and continuously.

[0063] Example 3.

[0064] This embodiment includes two groups of cases, namely the experimental group and the control group. Both experiments were conducted in a waste plastic cracking circulating countercurrent bed hot state device. The circulating countercurrent bed hot state device and the cold state device have the same size, and both are provided with an air guide pipe 7 and a feeder of the present invention.

[0065] In this implementation case, the experimental group was equipped with a solid distributor 6, and the control group was not equipped with a solid distributor 6. The hot state experimental feed was domestic waste plastics, the feed rate was 2.2 kg / h, the agent-to-material ratio was 50.77, the reaction temperature was 560 °C, the reaction pressure was 60 kPa, and the circulating countercurrent bed operation time was 2 h. The experimental results are shown in Table 1.

[0066] Table 1 Comparison of product distribution between hot state experiment without solid distributor and with solid distributor in Example 3

[0067] Whether to install a solid distributor Gas phase product yield, % Liquid product yield, % Coke yield, % Not installed 45.6 39.2 15.9 Retrofit 76.5 21.3 2.0

[0068] It can be seen from the data in Table 1 that the yield of gas phase products in the waste plastic cracking products with the solid distributor 6 installed is higher than that without the solid distributor 6, the yield of liquid phase products is reduced, and the yield of coke is significantly reduced. The gas phase products in the products are mostly small molecular hydrocarbons, and the liquid phase products are mostly large molecular hydrocarbons. The energy required to crack the waste plastics into small molecular hydrocarbons is higher. By installing the solid distributor 6, the yield of gas phase products is increased and the yield of liquid phase products is reduced, indicating that the external energy obtained by the waste plastics in the reactor 15 is higher, which means that the solid particles are used as heat sources and catalysts at the same time. Under the action of the solid distributor 6, the distribution is more uniform, and the mass transfer and heat transfer in contact with the gas phase are more sufficient.

[0069] Through the above case analysis, the spiral distributor system of the present invention can improve the gas-solid flow and heat transfer effect in the circulating countercurrent bed reactor by improving the distribution of radial particle concentration. The uniform particle concentration distribution improves the heat transfer efficiency. The good heat transfer effect can increase the gas phase product yield and reduce the coke yield.

[0070] Of course, the above description is not a limitation of the present invention, and the present invention is not limited to the above examples. Changes, modifications, additions or substitutions made by technicians in this technical field within the essential scope of the present invention should also fall within the protection scope of the present invention.

Claims

1. A spiral distributor system for a circulating countercurrent bed reactor, comprising a settler, a reactor and an air guide pipe, wherein the settler is connected to the reactor with an inclined gentle slope, characterized in that: The spiral distributor system also includes a solid distributor and a feeder; The feeder comprises a regeneration inclined tube, a buffer tube and a lower dosage port, the end of the buffer tube is connected to the lower dosage port vertically downward, the regeneration inclined tube, the buffer tube and the lower dosage port are integrally formed, and the regeneration inclined tube, the buffer tube and the lower dosage port are connected by a smooth curved surface; The regeneration inclined pipe extends from the side wall of the settler into the interior of the settler at an angle of 45°; the buffer pipe includes a vertical buffer pipe and an inclined buffer pipe, the vertical buffer pipe is parallel to the side wall of the settler, and the inclined buffer pipe forms an angle of 45° with the vertical buffer pipe; The solid distributor comprises a spiral tube, the spiral tube forms a spiral three-dimensional disk, the spiral tube is integrally formed, and the spiral tube comprises an inner layer, an inner second layer, a middle layer, an outer layer and an outer second layer from the inside to the outside, and the spiral tube forms a three-dimensional disk from top to bottom, the inner layer is at the top, and the outer second layer is at the bottom; the outer second layer is installed on an annular support and fixed to the reactor wall through the annular support; circular holes are evenly distributed on the bottom end surface of the spiral tube; The inner layer extends upward into the settler, the top of the inner layer faces the bottom of the lower dose opening, and a circular flat plate portion is provided at the top of the inner layer, the flat plate portion is opened, and the size of the opening is adapted to the lower dose opening; The air guide pipes are arranged in 4 to 8 pieces, which are evenly distributed at equal angles around the reactor and the settler outside the solid distributor; the top connection port of the air guide pipe is located on the settler wall above the lower agent port, and the bottom connection port is located on the reactor wall below the annular support.

2. The spiral distributor system of a circulating countercurrent bed reactor according to claim 1, characterized in that: The top end of the inner layer is connected to the bottom end of the lower agent port or the distance therebetween does not exceed 1 / 3 of the inner diameter of the reactor.

3. The spiral distributor system of a circulating countercurrent bed reactor according to claim 2, characterized in that: The height from the top of the inner layer to the bottom of the outer layer is 1 to 2 times the inner diameter of the reactor; the diameter of the settler is 2 to 5 times the diameter of the reactor.

4. The spiral distributor system of a circulating countercurrent bed reactor according to claim 2, characterized in that: On the spiral three-dimensional disk of the solid distributor, the inner first layer, the inner second layer, the middle layer, the outer first layer and the outer second layer each occupy 20% of the disk diameter.

5. The spiral distributor system of a circulating countercurrent bed reactor according to claim 1, characterized in that: The outer diameter of the annular support is the same as the inner diameter of the reactor, and is installed on the reactor wall through a support rod or a fixed slot.

6. The spiral distributor system of a circulating countercurrent bed reactor according to claim 5, characterized in that: The diameter of the circular hole accounts for 30~50% of the diameter of the spiral tube, and the total opening rate is 40~60%.

7. The spiral distributor system of a circulating countercurrent bed reactor according to claim 1, characterized in that: The spiral tube is inclined and spirally distributed downward, and the inclination angle is greater than the repose angle of the catalyst solid particles used. The inclination angle is 0.1 to 5 degrees higher than the repose angle.

8. The method for applying the spiral distributor system of a circulating countercurrent bed reactor according to any one of claims 1 to 7, characterized in that: The steps include: (1) The outer side of the annular support of the solid distributor is in close contact with the wall of the reactor and is fixed to the reactor wall through a support rod or a fixing slot. The bottom end of the solid distributor is welded to the annular support; (2) A connection hole is provided on the wall of the settler to match the regeneration inclined tube of the feeder. The regeneration inclined tube extends out of the settler through the connection hole to connect with the regenerator. The lower agent port is provided on the central axis of the settler. The catalyst solid particles are transported from the regenerator to the bottom of the lower agent port through the regeneration inclined tube conveying air and fall onto the solid distributor. (3) After the catalyst solid particles fall onto the solid distributor, they slide down along the spiral tube through the inner layer, the second inner layer, the middle layer, the outer layer, and the second outer layer. The solid particles are evenly distributed radially through the circular holes on the spiral tube. (4) The pressure difference between the settler and the reactor caused by the transportation of solid particles is balanced through the air duct, so that there is no particle accumulation above the solid distributor and the particles fall smoothly and stably, thereby achieving steady-state long-term operation of the reaction.

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