A new type of combined small diameter riser fluidized bed reactor

Abstract

The present invention discloses a novel combined small-diameter riser fluidized bed reaction device, comprising: a fluidized bed, a gas distributor, a compressor, an air supply device, a companion bed, and a buffer tank. The compressor is connected to the buffer tank, the gas distributor is disposed within the fluidized bed, the buffer tank is connected to the gas distributor, the fluidized bed is connected to the companion bed, the companion bed is connected to the fluidized bed, the companion bed is connected to a first cyclone separator, the first cyclone separator is connected to a second cyclone separator, and the second cyclone separator is connected to the companion bed. The air supply device is mounted on the fluidized bed, and the second exhaust port of the buffer tank is connected to the air supply device. The companion bed serves as an intermediate carrier for storing catalysts. The companion bed is disposed vertically higher than the small-diameter riser, thereby providing power for the catalyst to enter the small-diameter riser, thereby increasing the circulation intensity of the small-diameter riser, improving the gas-solid contact efficiency, enhancing the radial uniformity of the gas-solid flow axis within the small-diameter riser, and increasing production capacity.

Description

Technical Field

[0001] The invention belongs to the technical field of circulating fluidized beds, and in particular relates to a novel combined small-diameter section riser fluidized bed reaction device. Background Art

[0002] Fluidized beds have excellent mass and heat transfer properties, as well as efficient and rapid transport capabilities, and are widely used in various industries, including energy, chemicals, pharmaceuticals, food, and the environment. However, traditional circulating fluidized beds suffer from low particle concentrations, low gas-solid contact efficiency, and uneven axial and radial flow characteristics, leading to incomplete and uneven reactions and low product conversion rates. High-density or turbulent fluidized beds, while offering higher particle concentrations, can also experience severe backmixing within the fluidized bed reactor, leading to severe catalyst coking and failure, and adversely affecting continuous reactions. Summary of the Invention

[0003] In view of the shortcomings of the existing technology, the purpose of the present invention is to provide a new type of combined small-diameter section riser fluidized bed reaction device, which can fully solve the problems of uneven reaction of circulating fluidized bed and high back mixing of turbulent fluidized bed.

[0004] The purpose of the present invention is achieved through the following technical solutions.

[0005] A novel combined small-diameter riser fluidized bed reaction device comprises: a fluidized bed, a gas distributor, a compressor, a gas supply device, a companion bed and a buffer tank, wherein the compressor is connected to the gas inlet of the buffer tank through a first pipe, the gas distributor is arranged in the fluidized bed, the first exhaust port of the buffer tank is connected to the gas distributor in the fluidized bed through a second pipe, the top of the fluidized bed is connected to the first inlet of the companion bed through a tenth pipe, and is used to introduce catalyst and gas products into the companion bed through the tenth pipe, and the first outlet of the companion bed is connected to the fluidized bed through a ninth pipe. The fluidized bed is connected to the second outlet of the companion bed and is connected to the air inlet of a first cyclone separator through a third pipe, so as to perform gas-solid separation on the material in the third pipe. The dust discharge port of the first cyclone separator is connected to the air inlet of a second cyclone separator through a fourth pipe, so as to perform gas-solid separation on the material in the fourth pipe. The dust discharge port of the second cyclone separator is connected to the second inlet of the companion bed through a fifth pipe, so as to introduce the catalyst after gas-solid separation into the companion bed. The exhaust ports of the first cyclone separator and the second cyclone separator are both connected to the outside.

[0006] A catalyst inlet is provided on the companion bed, and a cover is installed on the catalyst inlet;

[0007] The air supply device is installed on the fluidized bed, and the second exhaust port of the buffer tank is connected to the air supply device through an eighth pipeline.

[0008] In the above technical solution, the air supply device includes: an upper air supply chamber and a lower air supply chamber, both of which are annular cavities and are sleeved outside the fluidized bed, and the fluidized bed is composed of a large-diameter section riser, a reducing section and a small-diameter section riser from top to bottom. The upper air supply chamber is sleeved on the lower part of the large-diameter section riser and the upper part of the reducing section is located in the upper air supply chamber, the lower air supply chamber is sleeved on the upper part of the small-diameter section riser and the lower part of the reducing section is located in the lower air supply chamber, a first air supply inlet is formed on the upper air supply chamber, and a second air supply inlet is formed on the lower air supply chamber; a plurality of first nozzles are arranged on the fluidized bed in the upper air supply chamber, and a plurality of second nozzles are arranged on the fluidized bed in the lower air supply chamber, and the first nozzle and the second nozzle are both located in the reducing section.

[0009] In the above technical solution, a first air supply chamber ash discharge port is formed on the upper air supply chamber, and a cover is installed on the first air supply chamber ash discharge port; a second air supply chamber ash discharge port is formed on the lower air supply chamber, and a cover is installed on the second air supply chamber ash discharge port.

[0010] In the above technical solution, a plurality of raised pyramids are formed on the inner wall of the diameter-changing section.

[0011] In the above technical solution, the pyramid is a triangular pyramid.

[0012] In the above technical solution, the number of the first nozzles is 4 to 12 and they are arranged on the fluidized bed along the circumferential direction, and the number of the second nozzles is 4 to 12 and they are arranged on the fluidized bed along the circumferential direction.

[0013] In the above technical solution, the angle θ between the inclined surface of the diameter-changing section and the horizontal plane is 40 to 89°.

[0014] In the above technical solution, the angle between the uppermost inclined surface of each pyramid and the inner wall of the diameter-changing section where the pyramid is located is 5-θ°.

[0015] In the above technical solution, the height of the upper air supply cabin is 0.25 to 1 m, and the height of the lower air supply cabin is 0.25 to 1 m.

[0016] In the above technical solution, the distance between the first nozzle and the central axis of the fluidized bed is r1, the distance between the second nozzle and the central axis of the fluidized bed is r2, and the radius of the large diameter section riser is R, then 0.75 <r1 / R<1,0.5<r2 / R<0.75。

[0017] In the above technical solution, the eighth pipeline consists of two branch pipelines, each branch pipeline is installed with a second gas flow meter and a second valve, and the first air supply inlet and the second air supply inlet are each connected to one of the branch pipelines.

[0018] In the above technical solution, the second outlet is located at the upper part of the companion bed, and the first outlet is located at the lower part of the companion bed.

[0019] In the above technical solution, a pressure sensor is provided on the fluidized bed, a temperature sensor is provided on the fluidized bed, a catalyst concentration sensor is provided on the fluidized bed, and a speed sensor is provided on the fluidized bed, and the speed sensor is used to detect the speed of the catalyst.

[0020] In the above technical solution, the exhaust ports of the first cyclone separator and the second cyclone separator are connected to an absorption device, and the absorption device is used to absorb the harmful gases and part of the catalyst discharged from the exhaust ports of the first cyclone separator and the second cyclone separator.

[0021] In the above technical solution, the gas distributor is arranged at the bottom of the small diameter section riser of the fluidized bed.

[0022] In the above technical solution, the ash discharge port of the second cyclone separator is connected to the companion bed through a fifth pipe.

[0023] In the above technical solution, the vent of the buffer tank is connected to the absorption device through a sixth pipeline, and a vent valve is provided on the sixth pipeline.

[0024] In the above technical solution, a first gas flow meter and a first valve are provided on the second pipeline.

[0025] In the above technical solution, the absorption device is connected to the outside through a seventh pipeline, which is used to discharge the gas after the harmful gas is removed and part of the catalyst.

[0026] The beneficial effects of the novel combined small-diameter riser fluidized bed reactor of the present invention are as follows:

[0027] 1. The companion bed is an intermediate carrier for catalyst storage. It is set higher than the small-diameter riser in the vertical direction, thus providing power for the catalyst to enter the small-diameter riser, thereby improving the circulation intensity of the small-diameter riser, improving the gas-solid contact efficiency, enhancing the radial uniformity of the gas-solid flow axis in the small-diameter riser, and increasing production capacity.

[0028] 2. Under the action of the air supply device, a negative pressure zone is formed in the upper part of the small-diameter section of the riser, which increases the pulling effect of the gas-solid fluid in the lower part of the small-diameter section of the riser, thereby suppressing the occurrence of choking in the lower part of the small-diameter section of the riser, so that the gas-solid flow characteristics in the lower part of the small-diameter section of the riser achieve a higher particle concentration and axial and radial flow uniformity;

[0029] 3. Under the action of the air supply device, the upper part of the large-diameter section riser provides a lifting effect for the gas-solid fluid in the upper part of the large-diameter section riser, accelerates the transportation of the gas-solid fluid, and reduces the gas-solid back mixing in the upper side wall area of the large-diameter section riser.

[0030] 4. Under the action of the air supply device, the solid-fluid flow pattern in the fluidized bed can be divided into zones. The small-diameter section of the riser is a dense phase zone with a relatively large solid-gas ratio, presenting a turbulent fluidization flow pattern or a high-density fluidization flow pattern. The large-diameter section of the riser is a dilute phase zone with a relatively small solid-gas ratio, presenting a rapid fluidization or pneumatic conveying flow pattern.

[0031] 5. The setting of the gas supply device can flexibly control the large diameter section riser and the small diameter section riser respectively, thereby reducing the probability of side reactions and overreactions in the large diameter section riser and the small diameter section riser, thereby improving the yield of the target product of the overall reaction.

[0032] 6. The tapered edges are evenly distributed on the oblique side of the variable diameter section, which can hinder the gas-solid mixture flowing downward along the surface of the variable diameter section and guide it into the high-speed upward gas-solid main flow in the center of the large diameter section riser. While accelerating the mixing of oil and agent, it also effectively suppresses the back mixing of the catalyst. BRIEF DESCRIPTION OF THE DRAWINGS

[0033] Figure 1 This is a schematic structural diagram of a novel combined small-diameter riser fluidized bed reactor according to the present invention;

[0034] Figure 2 It is a structural diagram of the air supply device;

[0035] Figure 3 It is a structural diagram of the air supply device (with pyramid).

[0036] Among them, 1: compressor, 2: buffer tank, 3: vent valve, 4: first gas flowmeter, 5: gas distributor, 6: small diameter section riser, 7: pressure sensor, 8: computer, 9: air supply device, 9-1: ash discharge port of the second air supply chamber, 9-2: second air supply inlet, 9-3: first air supply inlet, 9-4: ash discharge port of the first air supply chamber, 10: fluidized bed, 10-1: first nozzle, 10-2: second nozzle, 11: companion bed, 12: first cyclone separator, 13: second cyclone separator, 14: absorption device, 15: first pipeline, 16: second pipeline, 17: fifth pipeline, 18: fourth pipeline, 19: third pipeline, 20: tenth pipeline, 21: sixth pipeline, 22: first valve, 23: eighth pipeline, 24: ninth pipeline, 25: seventh pipeline. DETAILED DESCRIPTION

[0037] The technical solution of the novel combined small-diameter riser fluidized bed reactor of the present invention will be further described below with reference to specific embodiments.

[0038] The gas distributor 5 can adopt the gas-solid distributor in CN201210405627.6.

[0039] Example 1

[0040] like Figure 1 As shown, it includes: a fluidized bed 10, a gas distributor 5, a compressor 1, an air supply device 9, a companion bed 11 and a buffer tank 2. The compressor 1 is connected to the air inlet of the buffer tank 2 through a first pipe 15. The gas distributor 5 is arranged in the fluidized bed 10. The buffer tank 2 is provided with two exhaust ports: a first exhaust port and a second exhaust port. The first exhaust port of the buffer tank 2 is connected to the gas distributor 5 in the fluidized bed 10 through a second pipe 16. The top of the fluidized bed 10 is connected to the first inlet of the companion bed 11 through a tenth pipe 20, which is used to introduce catalyst and gaseous products into the companion bed 11 through the tenth pipe 20. The first outlet of the companion bed 11 is connected to the fluidized bed 10 through a ninth pipe 24, which is used to introduce catalyst into the fluidized bed 10. The second outlet of the companion bed 11 is connected to the air inlet of a first cyclone separator 12 through a third pipe 19, which is used to perform gas-solid separation on the substances in the third pipe 19. The second outlet is located at the upper part of the companion bed 11 and the first outlet is located at the lower part of the companion bed 11.

[0041] The ash discharge port of the first cyclone separator 12 is connected to the air inlet of the second cyclone separator 13 through the fourth pipe 18, and is used to perform gas-solid separation on the substances in the fourth pipe 18. The ash discharge port of the second cyclone separator 13 is connected to the second inlet of the companion bed 11 through the fifth pipe 17, and is used to introduce the catalyst after gas-solid separation into the companion bed 11. The exhaust ports of the first cyclone separator 12 and the second cyclone separator 13 are both connected to the outside world.

[0042] A catalyst inlet is provided on the companion bed 11, and a cover is installed on the catalyst inlet;

[0043] The air supply device 9 is installed on the fluidized bed 10 , and the second exhaust port of the buffer tank 2 is connected to the air supply device 9 through the eighth pipeline 23 .

[0044] The compressor delivers the feed gas to the buffer tank, and then it enters the gas distributor in the fluidized bed or the gas supply device. After the catalyst in the solid particle state and the feed gas react in the fluidized bed, they enter the companion bed. Most of the catalyst in the companion bed is recycled back to the fluidized bed through the ninth pipeline 24, and a small amount of catalyst and the feed gas are separated into gas and solids through the first cyclone separator and the second cyclone separator. During operation, the gas supply device can realize the zoning control of the fluidized bed state, forming a dense phase zone with a relatively large solid-to-gas ratio (solid content between 0.25-0.3) in the small-diameter section of the riser 6, and forming a dilute phase zone with a relatively small solid-to-gas ratio (solid content between 0.03-0.08) in the large-diameter section of the riser.

[0045] Example 2

[0046] like Figure 2 and 3 As shown, on the basis of Example 1, the air supply device 9 includes: an upper air supply chamber and a lower air supply chamber, both of which are annular cavities and are sleeved outside the fluidized bed 10. The fluidized bed 10 is composed of a large-diameter section riser, a reducing section and a small-diameter section riser 6 from top to bottom. The upper air supply chamber is sleeved on the lower part of the large-diameter section riser and the upper part of the reducing section is located in the upper air supply chamber, the lower air supply chamber is sleeved on the upper part of the small-diameter section riser 6 and the lower part of the reducing section is located in the lower air supply chamber, a first air supply inlet 9-3 is formed on the upper air supply chamber, and a second air supply inlet 9-2 is formed on the lower air supply chamber; a plurality of first nozzles 10-1 are provided on the fluidized bed 10 in the upper air supply chamber, and a plurality of second nozzles 10-2 are provided on the fluidized bed 10 in the lower air supply chamber, and the first nozzles 10-1 and the second nozzles 10-2 are both located in the reducing section. The first nozzle and the second nozzle arranged in the air supply device divide the fluidized bed into upper and lower flow patterns. The small-diameter section of the riser 6 is a dense phase zone with a relatively large solid-gas ratio, presenting a turbulent fluidization flow pattern or a high-density fluidization flow pattern. The large-diameter section of the riser is a dilute phase zone with a relatively small solid-gas ratio, presenting a rapid fluidization or pneumatic conveying flow pattern.

[0047] The gas first enters the upper air supply chamber and the lower air supply chamber through the eighth pipeline 23, and then enters the fluidized bed through the first nozzle and the second nozzle.

[0048] The number of the first nozzles 10 - 1 is 4 to 12 and they are arranged on the fluidized bed 10 along the circumferential direction. The number of the second nozzles 10 - 2 is 4 to 12 and they are arranged on the fluidized bed 10 along the circumferential direction.

[0049] The distance between the first nozzle 10-1 and the central axis of the fluidized bed 10 is r1, the distance between the second nozzle 10-2 and the central axis of the fluidized bed 10 is r2, and the radius of the large diameter section of the riser is R, then 0.75 <r1 / R<1,0.5<r2 / R<0.75。

[0050] A first air supply chamber dust discharge port 9-4 is formed on the upper air supply chamber, and a cover is installed on the first air supply chamber dust discharge port 9-4. A second air supply chamber dust discharge port 9-1 is formed on the lower air supply chamber, and a cover is installed on the second air supply chamber dust discharge port 9-1. The purpose of providing the first air supply chamber dust discharge port 9-4 and the second air supply chamber dust discharge port 9-1 is to discharge solid particles in the upper and lower air supply chambers in the event of an emergency. During the air supply process, the covers on the first air supply chamber dust discharge port 9-4 and the second air supply chamber dust discharge port 9-1 are closed. When an abnormal situation occurs, the air supply is stopped, and the covers on the first air supply chamber dust discharge port 9-4 and the second air supply chamber dust discharge port 9-1 are opened for dust cleaning.

[0051] A plurality of raised pyramids are formed on the inner wall of the diameter-changing section. Preferably, the pyramids are triangular pyramids. The angle between the uppermost inclined surface of each pyramid and the inner wall of the diameter-changing section where the pyramid is located is 5 to θ degrees.

[0052] The included angle θ between the inclined surface of the diameter-changing section and the horizontal plane is 40 to 89 degrees.

[0053] The height of the upper air supply chamber is 0.25 to 1m, and the height of the lower air supply chamber is 0.25 to 1m.

[0054] The height of the first outlet of the companion bed 11 is higher than that of the small-diameter section riser 6, so that the catalyst discharged from the first outlet can re-enter the fluidized bed under the action of gravity.

[0055] Example 3

[0056] Based on Example 2, the eighth pipeline 23 is composed of two branch pipelines, each of which is equipped with a second gas flowmeter and a second valve. A branch pipeline is connected to each of the first and second supplemental gas inlets 9-3 and 9-2. The two branch pipelines can independently control the flow rate.

[0057] Fluidized bed 10 is equipped with a pressure sensor 7, a temperature sensor, a catalyst concentration sensor, and a velocity sensor for detecting the velocity of the catalyst. Pressure sensor 7, temperature sensor, catalyst concentration sensor, and velocity sensor are all electrically connected to computer 8.

[0058] The exhaust ports of the first cyclone separator 12 and the second cyclone separator 13 are connected to an absorption device 14, which is used to absorb harmful gases and a portion of the catalyst discharged from the exhaust ports of the first cyclone separator 12 and the second cyclone separator 13. The absorption device 14 is connected to the outside world via a seventh pipeline 25 and is used to discharge the gases after the harmful gases are removed and a portion of the catalyst. The absorption device 14 is filled with a modified fiber material to absorb the harmful gases and a portion of the catalyst, thereby improving the environment. For example, the modified fiber material can be the renewable fiber balls described in Application No. 2018113390028.

[0059] The gas distributor 5 is arranged at the bottom of the small diameter section riser 6 of the fluidized bed 10 .

[0060] The ash discharge port of the second cyclone separator 13 is connected to the small-diameter section riser 6 of the fluidized bed 10 through a fifth pipe 17 .

[0061] A first gas flow meter 4 and a first valve 22 are provided on the second pipeline 16 .

[0062] The vent port of the buffer tank 2 is connected to the absorption device 14 through the sixth pipeline 21, and a vent valve 3 is provided on the sixth pipeline 21. Before the new combined small-diameter section riser fluidized bed reactor of the present invention is started up, the vent valve 3 should be opened to avoid excessive pressure in the buffer tank; when the new combined small-diameter section riser fluidized bed reactor is in operation, the vent valve 3 is regulated (when the first valve 22 and the second valve are adjusting a large gas flow rate, the vent valve 3 is closed; when the first valve 22 and the second valve are adjusting a small gas flow rate, the vent valve 3 is opened to avoid excessive pressure in the buffer tank), and by cooperating with the first valve 22 on the second pipeline 16, the gas-solid flow in the fluidized bed reaches a specific flow pattern; before the new combined small-diameter section riser fluidized bed reactor is shut down, the vent valve 3 is opened again.

[0063] The above is an exemplary description of the present invention. It should be noted that, without departing from the core of the present invention, any simple deformation, modification or other equivalent replacement that can be made by other skilled in the art without expending creative labor falls within the scope of protection of the present invention.

Claims

1. A novel combined small diameter riser fluidized bed reactor, characterized in that: include: A fluidized bed (10), a gas distributor (5), a compressor (1), an air supply device (9), a companion bed (11) and a buffer tank (2), wherein the compressor (1) is connected to the air inlet of the buffer tank (2) through a first pipe (15), the gas distributor (5) is arranged in the fluidized bed (10), the first exhaust port of the buffer tank (2) is connected to the gas distributor (5) in the fluidized bed (10) through a second pipe (16), the top of the fluidized bed (10) is connected to the first inlet of the companion bed (11) through a tenth pipe (20), and is used to introduce catalyst and gas products into the companion bed (11) through the tenth pipe (20), and the first outlet of the companion bed (11) is connected to the fluidized bed (10) through a ninth pipe (24). a passage for introducing the catalyst into the fluidized bed (10); the second outlet of the companion bed (11) is connected to the air inlet of a first cyclone separator (12) through a third pipe (19), and is used for performing gas-solid separation on the material in the third pipe (19); the ash discharge port of the first cyclone separator (12) is connected to the air inlet of a second cyclone separator (13) through a fourth pipe (18), and is used for performing gas-solid separation on the material in the fourth pipe (18); the ash discharge port of the second cyclone separator (13) is connected to the second inlet of the companion bed (11) through a fifth pipe (17), and is used for introducing the catalyst after gas-solid separation into the companion bed (11); the exhaust ports of the first cyclone separator (12) and the second cyclone separator (13) are both connected to the outside; A catalyst inlet is provided on the companion bed (11), and a cover is installed on the catalyst inlet; The air supply device (9) is installed on the fluidized bed (10), and the second exhaust port of the buffer tank (2) is connected to the air supply device (9) through an eighth pipeline (23); The air supply device (9) comprises: an upper air supply chamber and a lower air supply chamber, both of which are annular cavities and are sleeved outside the fluidized bed (10), and the fluidized bed (10) is composed of a large diameter section riser, a variable diameter section, and a small diameter section riser (6) from top to bottom, the upper air supply chamber is sleeved on the lower part of the large diameter section riser, and the upper part of the variable diameter section is located inside the upper air supply chamber, the lower air supply chamber is sleeved on the upper part of the small diameter section riser (6), and the variable diameter section is located inside the upper air supply chamber, and the lower air supply chamber is sleeved on the upper part of the small diameter section riser (6). The lower part of the air supply chamber is located in the lower air supply chamber, a first air supply inlet (9-3) is formed on the upper air supply chamber, and a second air supply inlet (9-2) is formed on the lower air supply chamber; a plurality of first nozzles (10-1) are provided on the fluidized bed (10) in the upper air supply chamber, and a plurality of second nozzles (10-2) are provided on the fluidized bed (10) in the lower air supply chamber, and the first nozzles (10-1) and the second nozzles (10-2) are both located in the diameter-reducing section; The angle θ between the inclined surface of the diameter-changing section and the horizontal plane is 40 to 89°; A plurality of raised pyramids are formed on the inner wall of the diameter-changing section, and the pyramids are triangular pyramids; the angle between the uppermost inclined surface of each pyramid and the inner wall of the diameter-changing section where the pyramid is located is 5° to θ°; Under the action of the air supply device, a negative pressure zone is formed on the upper part of the small diameter section riser, which increases the pulling effect of the gas-solid fluid in the lower part of the small diameter section riser, thereby suppressing the occurrence of choking in the lower part of the small diameter section riser; The upper part of the large diameter section riser, under the action of the air supply device, provides a lifting effect for the gas-solid fluid in the upper part of the large diameter section riser, accelerates the transportation of gas-solid fluid, and reduces the gas-solid back-mixing in the upper side wall area of the large diameter section riser; The tapered edges create an obstruction for the gas-solid mixture flowing downward along the surface of the variable diameter section, and can guide it into the high-speed upward gas-solid main flow in the center of the large diameter section riser.

2. The novel combined small-diameter riser fluidized bed reactor according to claim 1 is characterized in that: A first air supply chamber ash discharge port (9-4) is formed on the upper air supply chamber, and a cover is installed on the first air supply chamber ash discharge port (9-4); a second air supply chamber ash discharge port (9-1) is formed on the lower air supply chamber, and a cover is installed on the second air supply chamber ash discharge port (9-1).

3. The novel combined small-diameter riser fluidized bed reactor according to claim 1, characterized in that: The number of the first nozzles (10-1) is 4 to 12 and they are arranged on the fluidized bed (10) along a circumferential direction; the number of the second nozzles (10-2) is 4 to 12 and they are arranged on the fluidized bed (10) along a circumferential direction; The distance between the first nozzle (10-1) and the central axis of the fluidized bed (10) is r1, the distance between the second nozzle (10-2) and the central axis of the fluidized bed (10) is r2, and the radius of the large diameter section riser is R, then 0.75 <r1 / R<1,0 .5<r2 / R<0.75; The height of the upper air supply chamber is 0.25-1m, and the height of the lower air supply chamber is 0.25-1m.

4. The novel combined small-diameter riser fluidized bed reactor according to claim 1, characterized in that: The eighth pipeline (23) is composed of two branch pipelines, each branch pipeline is installed with a second gas flow meter and a second valve, and the first gas supplement inlet (9-3) and the second gas supplement inlet (9-2) are each connected to one of the branch pipelines; The second outlet is located at the upper part of the companion bed (11), and the first outlet is located at the lower part of the companion bed (11).

5. The novel combined small-diameter riser fluidized bed reactor according to claim 1, characterized in that: A pressure sensor (7) is provided on the fluidized bed (10), a temperature sensor is provided on the fluidized bed (10), a catalyst concentration sensor is provided on the fluidized bed (10), and a speed sensor is provided on the fluidized bed (10). The speed sensor is used to detect the speed of the catalyst.

6. The novel combined small-diameter riser fluidized bed reactor according to claim 1, characterized in that: The exhaust ports of the first cyclone separator (12) and the second cyclone separator (13) are in communication with an absorption device (14), and the absorption device (14) is used to absorb the harmful gas and part of the catalyst discharged from the exhaust ports of the first cyclone separator (12) and the second cyclone separator (13); The gas distributor (5) is arranged at the bottom of the small diameter section riser (6) of the fluidized bed (10); The ash discharge port of the second cyclone separator (13) is connected to the companion bed (11) through a fifth pipe (17); The vent of the buffer tank (2) is connected to the absorption device (14) through a sixth pipeline (21), and a vent valve (3) is provided on the sixth pipeline (21).

7. The novel combined small-diameter riser fluidized bed reactor according to claim 1, characterized in that: A first gas flow meter (4) and a first valve (22) are provided on the second pipeline (16).

8. The novel combined small-diameter riser fluidized bed reactor according to claim 6, characterized in that: The absorption device (14) is connected to the outside through a seventh pipe (25) and is used to discharge the gas after the harmful gas is removed and part of the catalyst.

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