Alkane dehydrogenation fluidized bed reaction regeneration device and system and alkane dehydrogenation method

Abstract

The invention discloses an alkane dehydrogenation fluidized bed reaction regeneration device and system and an alkane dehydrogenation method, and belongs to the field of low-carbon alkane deep processing. The alkane dehydrogenation fluidized bed reaction regeneration device comprises an outer cylinder and an inner cylinder, and the inner cylinder is arranged in an inner cavity of the outer cylinder and can be driven by a motor to rotate; the side wall of the inner cylinder is made of a porous material; an air outlet is formed in the inner cylinder, a filter is arranged in an inner cavity of the inner cylinder corresponding to the air outlet, and the filter is fixedly connected to the outer cylinder through the air outlet and does not rotate along with the inner cylinder; and an annular gas distributor is arranged around the side wall of the inner cylinder in the inner cavity of the outer cylinder. Under the action of centrifugal force which is several times to dozens of times of gravitational acceleration, the device disclosed by the invention can be used for effectively treating fine catalyst particles so as to eliminate the diffusion influence in particle pore channels, increase the operation gas speed, reduce the system pressure and improve the alkane conversion efficiency.

Description

Technical Field

[0001] The invention belongs to the field of low-carbon alkane deep processing, relates to low-carbon alkane dehydrogenation, and specifically relates to an alkane dehydrogenation fluidized bed reaction regeneration device, system and alkane dehydrogenation method. Background Art

[0002] The direct dehydrogenation of low-carbon alkanes (especially propane or isobutane) to produce olefins with corresponding carbon numbers and by-product hydrogen is a chemical reaction with high atomic utilization (C n H 2n+2 = C n H 2n + H2). Since this reaction is reversible and strongly endothermic ( Δ r H 298K =120~130 kJ / mol) and the number of molecules increases. Therefore, according to the principle of thermodynamics, high temperature and low pressure are favorable for this reaction. However, when operated at high temperature, side reactions such as thermal cracking and carbon generation are prone to occur, resulting in a decrease in olefin selectivity. At the same time, due to the accumulation of carbon on the catalyst surface and covering some active sites, the alkane conversion rate decreases accordingly.

[0003] In view of this, different types of reactors have been proposed, such as fixed bed reactors, moving bed reactors and fluidized bed reactors. In order to reduce the pressure drop of the bed, fixed bed reactors and moving bed reactors are usually loaded with catalyst particles of larger particle size (1~3mm), which leads to a long diffusion time of hydrocarbon compounds in the catalyst pores, and then over-reaction occurs to produce coke and other substances, so frequent reaction-regeneration switching operations are required, the number of reactor equipment is as high as 4~8, and the process control is complex; in comparison, the traditional gravity fluidized bed reactor can use fine-sized catalyst particles and reduce the number of equipment, but due to the presence of non-uniform structures such as bubbles in the catalyst bed, the gas-solid two-phase contact is uneven, especially the atmospheric velocity or negative pressure operation is prone to problems such as catalyst particle entrainment and loss, resulting in reduced olefin selectivity and yield, and low production efficiency.

[0004] Therefore, there is an urgent need for a new alkane dehydrogenation to olefin reaction and regeneration device and method that can handle fine catalyst particles with short molecular diffusion paths and prevent their serious loss. Summary of the invention

[0005] The present invention aims at the deficiencies of the above-mentioned prior art and provides an alkane dehydrogenation fluidized bed reaction regeneration device, system and alkane dehydrogenation method. The present invention discloses a supergravity fluidized bed device, which can g = 9.8 m / s 2) under the centrifugal force, it can process fine catalyst particles, reduce the impact of diffusion in the catalyst pores on the reaction, and delay carbon deposition and deactivation.

[0006] The specific technical solutions are as follows: One of the purposes of the present invention is to provide an alkane dehydrogenation fluidized bed reaction regeneration device, which comprises an outer cylinder and an inner cylinder, wherein the inner cylinder is arranged in the inner cavity of the outer cylinder and can rotate under the drive of a motor; The side wall of the inner cylinder is made of porous material; the inner cylinder is provided with an air outlet, and the inner cavity of the inner cylinder is provided with a filter corresponding to the air outlet, and the filter is fixedly connected to the outer cylinder through the air outlet and does not rotate with the inner cylinder; In the inner cavity of the outer cylinder, a gas annular distributor is arranged around the side wall of the inner cylinder.

[0007] When using the above device, the dehydrogenation catalyst particles are loaded into the inner cylinder, and the inner cylinder is rotated by the motor, and the centrifugal acceleration generated reaches 5 to 50 times the acceleration of gravity; the alkane gas enters the annular gap between the outer cylinder and the inner cylinder through the gas annular distributor, flows through the side wall of the inner cylinder and enters the inner cylinder through the pores, and the catalyst bed in the inner cylinder expands and fluidizes under the action of the gas and catalyzes the dehydrogenation reaction of the alkane, and then the dehydrogenated gas flows out through the filter and is collected through the gas outlet. After separation, the olefin product can be obtained. The above device can be operated at negative pressure, preferably in the pressure range of 10 to 100 kPa, and is preferably suitable for catalyst particles with a particle size range of 10 to 100 μm. During the reaction, the outer cylinder of the device is heated by a heating furnace to provide the temperature required for the reaction. Specifically, the outer cylinder can be placed in the heating furnace. After the dehydrogenation reaction is completed, nitrogen can be introduced through the gas ring distributor to purge the residual hydrocarbon gas; after the purge is completed, air is introduced to perform the catalyst charring regeneration operation; after regeneration, dry gas is introduced through the gas ring distributor to perform the catalyst reduction operation; after the catalyst reduction is completed, the alkane dehydrogenation reaction can be carried out again.

[0008] Under the centrifugal force of supergravity acceleration, the catalyst particles of the above device adhere to the side wall of the inner tube, and under the action of the alkane gas entering the inner tube, the bed expands and fluidizes. When the gas drag force tending to move away from the inner tube wall and the centrifugal force tending to approach the inner tube wall of the catalyst particles reach a force balance, a stable fluidized state can be obtained. It can be foreseen that since the centrifugal acceleration is several to dozens of times the traditional gravitational acceleration, the catalyst particles can withstand greater gas drag force compared to the traditional fluidized bed, thereby inhibiting the large-scale precipitation of particles. At the same time, in a supergravity environment, the ability of gas to gather into bubbles is limited, and the two phases are in more uniform contact when the gas passes through the catalyst bed, which is beneficial to the reaction.

[0009] Furthermore, the inner cylinder is preferably a hollow truncated cone structure with a thick top and a thin bottom, which rotates around its central axis under the drive of a motor; the angle between the side of the inner cylinder and the vertical plane is preferably no more than 25°. Such a setting is conducive to the uniform distribution of catalyst particles on the side wall under the action of centrifugal force, so as to achieve uniform contact with the gas.

[0010] Furthermore, the outer cylinder is preferably a hollow cylindrical structure, and is preferably concentric with the inner cylinder.

[0011] Furthermore, a shaft seal is provided at the connection between the inner cylinder and the outer cylinder, and the shaft seal is used for sealing. Specifically, the inner cylinder is connected to a drive shaft driven by a motor, and the drive shaft and the outer cylinder are sealed by a shaft seal. Similarly, the air outlet is also sealed by a shaft seal; specifically, corresponding to the air outlet of the inner cylinder, an air outlet pipe is provided on the top of the outer cylinder, and the air outlet channel includes a cylindrical part concentric with the inner cylinder, which extends into the air outlet and is connected to a filter, and the air outlet pipe and the inner cylinder are sealed by a shaft seal; such a setting does not affect the rotation of the inner cylinder, and the filter is in a stationary state. Among them, the shaft seal can be a mechanical seal or a magnetic fluid seal.

[0012] Furthermore, the gas annular distributor is preferably provided with 4 to 64 gas nozzles, and each nozzle is preferably evenly distributed along the circumference.

[0013] Furthermore, the outlet of the gas nozzle on the gas annular distributor is preferably oriented toward the bottom of the inner cavity of the outer cylinder, rather than directly toward the side wall of the inner cylinder. This arrangement is conducive to eliminating the gas velocity, inhibiting the gas flow from directly hitting the side wall of the inner cylinder, causing adverse effects on the fluidization state of the catalyst particles in the inner cylinder, and at the same time ensuring that the alkane gas has been fully preheated in the inner cavity of the outer cylinder before entering the inner cylinder.

[0014] Furthermore, the filter is preferably a ceramic filter; the maximum pore size of the filter is smaller than the catalyst particle size, preferably 2-10 μm, to prevent the catalyst from being carried by the product gas and causing loss.

[0015] Furthermore, the pore size of the inner cylinder side wall should be smaller than the catalyst particle size to ensure that the gas can enter smoothly but the catalyst particles will not leak out from the side wall pores; the material of the inner cylinder side wall is preferably a sintered porous plate, the opening rate is preferably 5% to 30%, and the maximum pore size is preferably 8 to 10 μm. The upper and lower surfaces of the inner cylinder are preferably non-porous and airtight materials.

[0016] A second object of the present invention is to provide an alkane dehydrogenation fluidized bed reaction regeneration system, which comprises two of the above-mentioned alkane dehydrogenation fluidized bed reaction regeneration devices.

[0017] When using the above system, the first alkane dehydrogenation fluidized bed reaction regeneration device performs alkane dehydrogenation reaction. After the reaction is completed, the alkane gas feed is switched to the second alkane dehydrogenation fluidized bed reaction regeneration device to continue the alkane dehydrogenation reaction; the first alkane dehydrogenation fluidized bed reaction regeneration device performs purging, regeneration, and reduction operations; after reduction, the alkane gas is switched back to the first alkane dehydrogenation fluidized bed reaction regeneration device to perform alkane dehydrogenation reaction again, and the second alkane dehydrogenation fluidized bed reaction regeneration device performs purging, regeneration, and reduction operations, and so on, to perform a "reaction-purging-regeneration-reduction" cycle. While one of the devices is performing a dehydrogenation reaction, the other device is performing purging, regeneration, and reduction operations. All operations can be achieved using two supergravity fluidized bed devices. Among them, the purging, regeneration, and reduction operations are the same as the reaction operation method, and the total duration of the purging, regeneration, and reduction operations is equal to the duration of the reaction operation.

[0018] The third object of the present invention is to provide an alkane dehydrogenation method using the aforementioned alkane dehydrogenation fluidized bed reaction regeneration device, specifically an alkane dehydrogenation and catalyst regeneration method, which comprises the following steps: The dehydrogenation catalyst particles are loaded into the inner cylinder, which is driven by a motor to rotate to generate centrifugal force. The alkane gas is introduced into the outer cylinder through a gas annular distributor, and the alkane gas enters the inner cylinder through the pores on the side wall of the inner cylinder. Under the action of the gas, the catalyst bed in the inner cylinder expands and fluidizes, and a dehydrogenation reaction occurs. The gas then passes through a filter and is collected through the gas outlet.

[0019] The alkane is preferably a low-carbon alkane having 2 to 5 carbon atoms, more preferably propane or isobutane.

[0020] The dehydrogenation catalyst preferably has a particle size range of 10 to 100 μm. Specifically, the dehydrogenation catalyst may be a dehydrogenation catalyst disclosed in the invention patent "A high-strength low-carbon alkane dehydrogenation catalyst and its preparation method" with application number CN201410265574.1 developed by the applicant team of the present invention.

[0021] The centrifugal acceleration generated when the inner cylinder rotates is preferably 5 to 50 times the gravitational acceleration.

[0022] The dehydrogenation reaction temperature is preferably 540-600°C.

[0023] Among them, the dehydrogenation reaction pressure operating range is preferably 10~100 kPa.

[0024] The dehydrogenation reaction gas hourly space velocity is preferably 1200-3000 h -1 .

[0025] Furthermore, after the dehydrogenation reaction is completed, purging, regeneration and reduction operations are performed.

[0026] The purging includes: introducing nitrogen through a gas annular distributor to purge the residual hydrocarbon gas.

[0027] The regeneration includes: after the purging is completed, air is introduced through a gas annular distributor to perform a catalyst charring regeneration operation.

[0028] The reduction includes: after regeneration, dry gas (methane and hydrogen) is introduced through a gas annular distributor to perform catalyst reduction operation.

[0029] The third object of the present invention is to provide an alkane dehydrogenation method using the aforementioned alkane dehydrogenation fluidized bed reaction regeneration device, which comprises the following steps: The first alkane dehydrogenation fluidized bed reaction regeneration unit carries out alkane dehydrogenation reaction. After the reaction is finished, the alkane gas feed is switched to the second alkane dehydrogenation fluidized bed reaction regeneration unit to continue the alkane dehydrogenation reaction. Meanwhile, the first alkane dehydrogenation fluidized bed reaction regeneration unit carries out purging, regeneration and reduction operations. After reduction, the alkane gas is switched back to the first alkane dehydrogenation fluidized bed reaction regeneration unit to carry out alkane dehydrogenation reaction again. Meanwhile, the second alkane dehydrogenation fluidized bed reaction regeneration unit carries out purging, regeneration and reduction operations. And so on, a "reaction-purging-regeneration-reduction" cycle is carried out.

[0030] The operation methods of alkane dehydrogenation reaction, purging, regeneration and reduction are as described above.

[0031] Specifically, the single dehydrogenation reaction time of a single alkane dehydrogenation fluidized bed reaction regeneration device is preferably 30 to 180 minutes. Due to the decrease in coke yield, the reaction time in a single device is much higher than the fixed bed reactor dehydrogenation process (about 10 to 15 minutes).

[0032] Specifically, the dehydrogenation reaction operation time is equal to the total operation time of the subsequent three steps of purging, regeneration and reduction. The purging time is preferably 10 to 30 minutes, the regeneration time is preferably 10 to 120 minutes, and the reduction time is preferably 10 to 60 minutes.

[0033] The beneficial effects of the present invention are as follows: The present invention overcomes the problems of a large number of fixed bed and moving bed reactors, high equipment cost due to large catalyst particle size, difficulty in eliminating internal diffusion effects, as well as uneven gas-solid contact in traditional fluidized bed reactors, and catalyst particle loss easily caused by atmospheric velocity and negative pressure operation. A new type of supergravity fluidized bed reaction regeneration device and method for alkane dehydrogenation to olefins is provided. Under the action of centrifugal force several to dozens of times the acceleration of gravity, fine catalyst particles can be effectively processed to eliminate the influence of diffusion in particle pores, the operating gas velocity is increased and the system pressure is reduced to promote the depth of alkane conversion, the processing capacity of the device is increased, and the number of equipment is reduced. BRIEF DESCRIPTION OF THE DRAWINGS

[0034] Figure 1 It is a schematic diagram of an alkane dehydrogenation fluidized bed reaction regeneration device in a specific embodiment of the present invention; Figure 2 The present invention is a flow chart of a method for using an alkane dehydrogenation fluidized bed reaction regeneration system for alkane dehydrogenation and catalyst regeneration in a specific embodiment of the present invention.

[0035] In the figure: 1. outer cylinder; 11. gas outlet pipe; 2. inner cylinder; 21. drive shaft; 3. shaft seal; 4. gas annular distributor; 5. ceramic filter. DETAILED DESCRIPTION

[0036] The principles and features of the present invention are described below in conjunction with examples. The examples are only used to explain the present invention and are not used to limit the scope of the present invention.

[0037] In a specific embodiment, the dehydrogenation catalyst uses the dehydrogenation catalyst disclosed in Example 2 of the invention patent “A high-strength low-carbon alkane dehydrogenation catalyst and its preparation method” with application number CN201410265574.1. Example 1

[0038] A fluidized bed reaction regeneration device for dehydrogenating alkanes, such as Figure 1 As shown, it comprises an outer cylinder 1 and an inner cylinder 2, wherein the inner cylinder 2 is arranged in the inner cavity of the outer cylinder 1 and can rotate under the drive of a motor; The inner cylinder 2 is a hollow truncated cone structure with a thickness on the top and a thickness on the bottom, and has a volume of 0.6 L. It rotates around its central axis driven by a motor; the angle α between the side surface of the inner cylinder 2 and the vertical plane is 5°; the material of the side wall of the inner cylinder 2 is a sintered porous plate, and its opening rate is 10% and the maximum pore size is 10 μm; the upper surface and the lower surface of the inner cylinder 2 are both non-porous and airtight materials; The outer cylinder 1 is a hollow cylindrical structure concentric with the inner cylinder 2; The inner cylinder 2 is provided with an air outlet leading to the outside of the outer cylinder 1, and the inner cavity of the inner cylinder 2 is provided with a ceramic filter 5 corresponding to the air outlet, and the maximum pore size of the ceramic filter 5 is 10 μm; corresponding to the air outlet of the inner cylinder 2, the outer cylinder 1 is fixed with an air outlet pipe 11 leading to the outside of the device, and the air outlet pipe 11 is a cylindrical shape concentric with the inner cylinder 2, extending into the air outlet to connect with the ceramic filter 5; the air outlet pipe 11 and the inner cylinder 2 are sealed by a shaft seal 3; the bottom of the inner cylinder 2 is connected to a driving shaft 21 driven by a motor, and the driving shaft 21 and the outer cylinder 1 are sealed by a shaft seal 3; the shaft seal 3 adopts a mechanical seal; In the inner cavity of the outer tube 1, a gas annular distributor 4 is provided around the side wall of the inner tube 2; 16 gas nozzles are evenly arranged along the circumference of the gas annular distributor 4; the outlets of the gas nozzles on the gas annular distributor 4 face the bottom of the inner cavity of the outer tube 1.

[0039] An alkane dehydrogenation fluidized bed reaction regeneration system comprises two of the above-mentioned alkane dehydrogenation fluidized bed reaction regeneration devices.

[0040] The above-mentioned alkane dehydrogenation fluidized bed reaction regeneration system is used to carry out propane dehydrogenation reaction, referring to Figure 2 , the method steps are as follows: The dehydrogenation catalyst particles are loaded into the inner cylinder 2 of the above-mentioned alkane dehydrogenation fluidized bed reaction regeneration device; the inner cylinder 2 of the first device is driven by a motor to rotate, and the outer cylinder is stationary; the alkane gas is introduced into the outer cylinder 1 through the gas annular distributor 4, and the alkane gas enters the inner cylinder 2 through the pores on the side wall of the inner cylinder 2. Under the action of the gas, the catalyst bed of the inner cylinder 2 expands and fluidizes and undergoes a dehydrogenation reaction, and then the gas is filtered out through the ceramic filter 5 to remove a small amount of particle dust carried and discharged through the gas outlet pipe 11. The collected gas is separated to obtain olefin products. During the reaction, the outer cylinder of the device is heated by a heating furnace to provide the temperature required for the reaction. After the dehydrogenation reaction of the first device is completed, the alkane gas feed valve is switched to the second device to continue the dehydrogenation reaction, while the first device performs purging, regeneration, and reduction operations: Specifically, the first device introduces nitrogen through the gas annular distributor 4 to purge the residual hydrocarbon gas. After the purging is completed, air is introduced through the gas annular distributor 4 to perform catalyst charring regeneration operation; after regeneration, dry gas (methane and hydrogen) is introduced through the gas annular distributor 4 to perform catalyst reduction operation. After reduction, the alkane gas is switched back to the first device to perform alkane dehydrogenation reaction again, while the second alkane dehydrogenation fluidized bed reaction regeneration device performs purging, regeneration, and reduction operations. By analogy, a "reaction-purging-regeneration-reduction" cycle is performed.

[0041] In the above method steps: the centrifugal acceleration generated by the rotation of the inner cylinder 2 is 40 times the gravitational acceleration, the propane raw material (purity> 95% wt) intake flow rate is 5 L / min, the reaction pressure is 20 kPa, and the reaction temperature is 580 ° C; the average particle size of the catalyst is 30 μm, and the loading amount of each device is 0.15 L; the reaction time is 60 min, the purge time is 10 min, the regeneration time is 30 min, and the reduction time is 20 min.

[0042] Under this operating condition, the propane conversion rate is 60.19%, the propylene selectivity is 92.88%, and the propylene yield is 55.90%. Moreover, due to the decrease in coke yield, the reaction time in a single device is much higher than the fixed bed reactor dehydrogenation process (about 10~15min). Example 2

[0043] The isobutane dehydrogenation reaction was carried out with reference to Example 1, which differed from Example 1 in that: The angle between the side of the inner tube 2 of the alkane dehydrogenation fluidized bed reaction regeneration and the vertical plane is 15°, and the opening rate of the sintered porous plate on the side of the inner tube 2 is 15%; The raw material was replaced with isobutane; the centrifugal acceleration generated by the rotation of the inner cylinder 2 was 20 times the acceleration of gravity, the inlet flow rate of the isobutane raw material (purity > 99% wt) was 4 L / min, the reaction pressure was 20 kPa, and the reaction temperature was 550°C; the average particle size of the catalyst was 25 μm, and the loading amount of each device was 0.15 L; the reaction time was 60 min, the purge time was 10 min, the regeneration time was 30 min, and the reduction time was 20 min.

[0044] Other technical features are the same as those of Example 1.

[0045] Under this operating condition, the isobutane conversion rate was 68.29%, the isobutene selectivity was 95.69%, and the isobutene yield was 65.34%. Example 3

[0046] The isobutane dehydrogenation reaction was carried out with reference to Example 1, which differed from Example 1 in that: The angle between the side of the inner cylinder 2 of the alkane dehydrogenation fluidized bed reaction regeneration and the vertical plane is 25°, and the opening rate of the sintered porous plate on the side of the inner cylinder 2 is 20%; 32 nozzles are arranged on the gas annular distributor 4, and the maximum pore size of the ceramic filter 5 is 5 μm; The raw material was replaced with isobutane; the centrifugal acceleration generated by the rotation of the inner cylinder 2 was 10 times the acceleration of gravity, the inlet flow rate of the isobutane raw material (purity> 99% wt) was 4 L / min, the reaction pressure was 50 kPa, and the reaction temperature was 550 ℃; the average particle size of the catalyst was 20 μm, and the loading amount of each device was 0.15 L. The reaction time was 90 min, the purge time was 10 min, the regeneration time was 50 min, and the reduction time was 30 min.

[0047] Other technical features are the same as those of Example 1.

[0048] Under this operating condition, the isobutane conversion rate was 61.06%, the isobutene selectivity was 94.26%, and the isobutene yield was 57.55%. Comparative Example 1

[0049] The propane dehydrogenation reaction was carried out using a conventional fixed fluidized bed experimental device, and the fixed fluidized bed device used was referenced to the following document: Yupeng Du, Lin Zhang, Abdallah S. Berrouk. Exergy analysis of propanedehydrogenation in a fluidized bed reactor: Experiment and MP-PIC simulation. Energy Conversion and Management 202 (2019) 112213. This document is a paper published by the applicant team.

[0050] The specific reaction conditions are as follows: propane feedstock (purity> 95% wt), inlet flow rate 2.0 L / min, reaction pressure 100 kPa, reaction temperature 580°C, catalyst average particle size 70 μm, loading amount 0.15 L. Reaction time 20 min, purge time 5 min, regeneration time 10 min, reduction time 5 min.

[0051] The reaction results are shown in Table 1. Comparative Example 2

[0052] The isobutane dehydrogenation reaction was carried out using a conventional fixed fluidized bed test apparatus, and the fixed fluidized bed apparatus used was the same as that in Comparative Example 1.

[0053] The specific reaction conditions are as follows: isobutane raw material (purity> 99% wt), inlet flow rate 1.5 L / min, reaction pressure 100 kPa, reaction temperature 550°C, catalyst average particle size 70 μm, loading amount 0.15 L. Reaction time 25 min, purge time 5 min, regeneration time 15 min, reduction time 5 min.

[0054] The reaction results are shown in Table 1.

[0055] Table 1 Comparison of dehydrogenation reaction results between the fluidized bed of the present invention and the conventional fixed fluidized bed Serial number Reaction temperature / ℃ Propane or isobutane conversion rate / % Propylene or isobutylene selectivity / % Propylene or isobutylene yield / % Example 1 580 60.19 92.88 55.90 Example 2 550 68.29 95.69 65.34 Example 3 550 61.06 94.26 57.55 Comparative Example 1 580 40.35 84.45 34.07 Comparative Example 2 550 48.76 90.12 43.94 It can be seen from the data in Table 1 that, compared with the traditional fixed fluidized bed reaction device, the use of the supergravity fluidized bed reaction device of the present invention has a higher conversion rate of propane or isobutane and an increased yield of propylene or isobutylene due to the use of small-size catalyst particles and negative pressure operation, and more complete gas-solid contact. That is, the supergravity fluidized bed proposed in the present invention can significantly improve the dehydrogenation reaction effect of light alkanes.

[0056] The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. Any modifications, equivalent substitutions, improvements, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.

Claims

1. An alkane dehydrogenation fluidized bed reaction regeneration device, characterized in that: It comprises an outer cylinder (1) and an inner cylinder (2), wherein the inner cylinder (2) is arranged in the inner cavity of the outer cylinder (1) and can rotate under the drive of a motor; The side wall of the inner cylinder (2) is made of porous material; the inner cylinder (2) is provided with an air outlet leading to the outside of the outer cylinder (1); the inner cavity of the inner cylinder (2) is provided with a filter corresponding to the air outlet; the filter is fixedly connected to the outer cylinder (1) via the air outlet; In the inner cavity of the outer cylinder (1), a gas annular distributor (4) is provided around the side wall of the inner cylinder (2).

2. The alkane dehydrogenation fluidized bed reaction regeneration device according to claim 1, characterized in that: The inner cylinder (2) is a hollow truncated cone structure that is thick at the top and thin at the bottom, and rotates around its central axis when driven by a motor.

3. The alkane dehydrogenation fluidized bed reaction regeneration device according to claim 2, characterized in that: The angle between the side surface of the inner cylinder (2) and the vertical plane does not exceed 25°.

4. The alkane dehydrogenation fluidized bed reaction regeneration device according to claim 1, characterized in that: A shaft seal (3) is provided at the connection between the inner cylinder (2) and the outer cylinder (1).

5. The alkane dehydrogenation fluidized bed reaction regeneration device according to claim 1, characterized in that: The gas annular distributor (4) is provided with 4 to 64 gas nozzles.

6. The alkane dehydrogenation fluidized bed reaction regeneration device according to claim 1, characterized in that: The outlet of the gas nozzle on the gas annular distributor (4) faces the bottom of the inner cavity of the outer tube (1).

7. The alkane dehydrogenation fluidized bed reaction regeneration device according to claim 1, characterized in that: The filter is a ceramic filter (5).

8. An alkane dehydrogenation fluidized bed reaction regeneration system, characterized in that: It comprises two alkane dehydrogenation fluidized bed reaction regeneration devices as described in any one of claims 1 to 7.

9. An alkane dehydrogenation method, using the alkane dehydrogenation fluidized bed reaction regeneration device according to any one of claims 1 to 7, characterized in that: The steps include: Dehydrogenation catalyst particles are loaded into an inner cylinder (2), and the inner cylinder (2) is driven to rotate by a motor; alkane gas is introduced into the outer cylinder (1) through a gas annular distributor (4); the alkane gas enters the inner cylinder (2) through the pores on the side wall of the inner cylinder (2) after being evenly distributed; the catalyst bed layer of the inner cylinder (2) expands and fluidizes under the action of the gas and catalyzes the dehydrogenation reaction; and then the gas passes through a filter and is collected through a gas outlet.

10. An alkane dehydrogenation method, using the alkane dehydrogenation fluidized bed reaction regeneration system as claimed in claim 8, characterized in that: The steps include: The first alkane dehydrogenation fluidized bed reaction regeneration unit carries out alkane dehydrogenation reaction. After the reaction is completed, the alkane gas feed is switched to the second alkane dehydrogenation fluidized bed reaction regeneration unit to continue the alkane dehydrogenation reaction, while the first alkane dehydrogenation fluidized bed reaction regeneration unit carries out purging, regeneration and reduction operations; after reduction, the alkane gas is switched back to the first alkane dehydrogenation fluidized bed reaction regeneration unit to carry out alkane dehydrogenation reaction again, while the second alkane dehydrogenation fluidized bed reaction regeneration unit carries out purging, regeneration and reduction operations.

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