A fluidized bed reactor for naphtha production

Abstract

The invention discloses a fluidized bed reactor for naphtha production, which belongs to the field of naphtha reforming. The reactor comprises a reactor body and a reaction chamber provided inside the reactor body. The lower end of the reactor body is connected with an air intake assembly, and the air intake assembly comprises a bottom plate fixedly connected to the lower end of the reactor body and a gas outlet distribution plate located above the bottom plate and rotatably connected to the inner wall of the reactor body. An output port is provided inside the reactor body, and the output port is communicated with an input end of a cyclone separator. The invention can restore catalytic activity without stopping production, reduce downtime, and improve production continuity. At the same time, the catalyst particles in the fluidized bed reactor are in a fluidized state, and the contact between the gas and the catalyst is very uniform, which makes the reaction temperature distribution more uniform, reduces local overheating, can maintain a high reaction efficiency, and reduces the risk of coke accumulation.

Description

Technical Field

[0001] The present invention relates to the field of naphtha reforming, and more particularly to a fluidized bed reactor for naphtha production. Background Art

[0002] Naphtha is a light petroleum product, usually obtained from crude oil through distillation or cracking processes. It is an important raw material in the petrochemical industry and is widely used in the production of a variety of chemical products and fuels. Naphtha reforming is part of the naphtha production process and is usually one of the key steps in improving product quality and value in the oil refining process. The main purpose of the reforming process is to convert lower octane alkanes and cycloalkanes in naphtha into high octane aromatics and isoalkanes. This process can not only improve the performance of naphtha as a fuel, but also provide important raw materials for the downstream chemical industry, such as benzene, toluene and xylene (BTX).

[0003] At present, fixed bed reactors and fluidized bed reactors are mainly used for naphtha reforming. For example, the prior art (Chinese invention patent with announcement number CN107868674B) discloses a naphtha catalytic reforming method, which adopts a fixed bed reactor to catalytically reform naphtha. For example, the prior art (Chinese invention patent with announcement number CN111233609B) discloses a raw material conversion device containing naphtha, which adopts a fluidized bed reactor to achieve catalytic cracking of naphtha. The fluidized bed reactor can achieve dynamic circulation treatment, and the treatment efficiency is higher than that of the fixed bed reactor. Therefore, most of the fluidized bed reactors on the market are used to achieve catalytic treatment of naphtha;

[0004] Although catalytic treatment of naphtha can be achieved through a fluidized bed reactor, during the use of the fluidized bed reactor, the airflow discharged from the distribution plate inside the fluidized bed reactor may be concentrated in certain areas, resulting in local excessively high or low airflow rates. Especially in a fluidized bed with a large airflow and dense catalyst particles, this uneven airflow can easily cause aggregation, sedimentation or incomplete fluidization of the catalyst particles. Summary of the invention

[0005] In view of the problems existing in the prior art, the object of the present invention is to provide a fluidized bed reactor for naphtha production.

[0006] To solve the above problems, the present invention adopts the following technical solutions.

[0007] A fluidized bed reactor for naphtha production, comprising a reactor body and a reaction chamber disposed inside the reactor body, wherein the lower end of the reactor body is connected to an air intake assembly, and the air intake assembly comprises a bottom plate fixedly connected to the lower end of the reactor body and a gas outlet distribution plate located above the bottom plate and rotatably connected to the inner wall of the reactor body, wherein a rotary joint is fixedly connected to the lower end of the bottom plate, and an inner tube of the rotary joint penetrates the bottom plate and is plugged into an input end of the gas outlet distribution plate, and an outer surface of the inner tube is fixedly connected to the inner wall of the input end of the gas outlet distribution plate;

[0008] The lower end of the base plate is also connected to a flow-uniformizing and enhancing component, and the flow-uniformizing and enhancing component includes a motor 1 fixedly connected to the lower end of the base plate, a gear 1 rotatably connected to the upper end of the base plate, and a gear 2 meshing with the gear 1, and the gear 1 is fixedly sleeved on the outside of the inner tube of the rotary joint.

[0009] Furthermore, an output port is provided inside the reactor body, and the output port is connected to the input end of the cyclone separator, the upper end of the cyclone separator is connected to an exhaust portion, and the discharge end of the cyclone separator is connected to a feed portion, the other end of the feed portion is connected to the input end of the catalytic regenerator, and the discharge end of the catalytic regenerator is connected to the reaction chamber inside the reactor body, and an air inlet port is provided at the lower end of the catalytic regenerator.

[0010] Furthermore, a conical inner expansion section is provided in the middle of the reactor body, and an air inlet portion is fixedly connected to the inner part of the conical inner expansion section at an angle.

[0011] Furthermore, a return pipe is horizontally fixedly inserted inside the conical inner expansion section, and one end of the return pipe is connected to the discharge end. The return pipe is used to send the regenerated catalyst and gas from the discharge end into the reactor body in a tangential shape.

[0012] Furthermore, an internal circulation unit is connected to the reactor body, and the internal circulation unit includes a lower circulation part fixedly connected to the reactor body and an upper circulation part connected to the upper end of the reactor body. The lower circulation part includes a hollow sleeve fixedly connected to the reactor body, a conical drainage groove opened in the center of the hollow sleeve, and a plurality of trapezoidal circulation grooves opened in the hollow sleeve. The upper circulation part includes a seat body movably connected to the reactor body and fitted with the inner wall of the reaction chamber, a conical drainage part opened in the center of the lower end of the seat body, and an arc-shaped drainage part opened at the edge of the lower end of the seat body and connected to the conical drainage part. The upper end of the reactor body is also connected to a discharge adjustment component for driving the seat body to move to adjust the discharge amount of the output port.

[0013] Furthermore, a plurality of flanges 1 are integrally formed on the inner wall of the conical drainage groove, and a plurality of flanges 2 are integrally formed on the outer wall of the arc-shaped drainage portion.

[0014] Furthermore, a plurality of spoilers are integrally formed on the outer wall of the conical drainage portion, a top plate is fixedly connected to the upper end of the seat body, and a second motor is fixedly connected to the upper end of the top plate, an output shaft of the second motor passes through the top plate and is fixedly connected to the upper end of the seat body, and a dynamic sealing portion is fixedly connected to the inner wall of the reaction chamber of the reactor body.

[0015] Furthermore, the discharge adjustment assembly includes two extension parts that are integrally formed on the outside of the reactor body and are symmetrical to each other, a hydraulic cylinder fixed to the outside of the reactor body, and a guide rod fixed to the lower end of the top plate and movably inserted into one of the extension parts. The telescopic end of the hydraulic cylinder passes through the other extension part and is fixed to the lower end of the top plate.

[0016] Furthermore, the lower end of the air outlet distribution plate is also connected to a sedimentation and suspension component, and the sedimentation and suspension component includes a ring body 1 fixedly connected to the lower end of the air outlet distribution plate, a movable groove opened inside the ring body 1, a guide column movably inserted in the movable groove, a spring located inside the movable groove and sleeved on the outside of the guide column, a ring body 2 fixedly connected to the lower end of the guide column, an inclined groove opened inside the ring body 2, and an inclined top block located in the inclined groove, and the inclined top block is fixedly connected to the upper end of the bottom plate, and the two ends of the spring are respectively connected to the inner wall of the movable groove and one side of the guide column.

[0017] Furthermore, an annular groove is provided on the inner wall of the reaction chamber, and an annular fixing ring is fixedly connected in the annular groove. An exhaust nozzle is fixedly connected to the inner wall of the annular fixing ring, and the gas outlet end of the exhaust nozzle faces the gas outlet distribution plate. The input end of the exhaust nozzle passes through the annular fixing ring and the reactor body and extends outward.

[0018] Compared with the prior art, the present invention has the following beneficial effects:

[0019] (1) This scheme adopts a fluidized bed reactor to catalytically reform naphtha. The atomized naphtha and hydrogen enter the reactor body through the air inlet assembly and react with the suspended catalyst inside the reactor body to achieve catalytic reforming. The gas and catalyst are separated by a cyclone separator. The separated catalyst enters the catalytic regenerator for regeneration and then re-enters the fluidized bed reactor. The fluidized bed reactor allows the catalyst to circulate dynamically online, the contact between the catalyst and the airflow is more frequent, and the online regeneration is more efficient. The catalytic activity can be restored without stopping production, reducing downtime and improving production continuity. At the same time, the catalyst particles in the fluidized bed reactor are in a fluidized state, and the contact between the gas and the catalyst is very uniform, which makes the reaction temperature distribution more uniform, reduces local overheating, can maintain a high reaction efficiency, and reduces the risk of coke accumulation. (2) This scheme is provided with a uniform flow enhancement component, which drives gears 1 and 2 to rotate through motor 1, and the rotation of gear 2 drives the gas outlet distribution plate to rotate. When the gas outlet distribution plate rotates, the position and angle of the gas entering the reaction chamber will constantly change, allowing the gas to be more evenly distributed across the bottom of the reactor, breaking the original gas flow deviation and dead zones of incomplete reaction, improving the distribution of gas in the reactor, and reducing local areas where the gas flow rate is too high or too low, thereby improving the reaction efficiency. At the same time, the rotating gas outlet distribution plate may help break up the area where particles accumulate and promote more uniform fluidization of the catalyst particles, which helps to avoid particle retention and accumulation, ensure better distribution of catalyst particles, and thus improve the reaction rate and catalytic efficiency.

[0020] (3) This scheme is provided with a sedimentation and suspension component. When the gas outlet distribution plate rotates, the ring body 1 and the ring body 2 are driven to rotate. When the ring body 2 rotates, the inclined groove can contact the inclined top block. The inclined top block pushes the ring body 2 to move toward the bottom plate through the inclined groove. When the inclined surface of the inclined groove is separated from the inclined surface of the inclined top block, the spring can drive the guide column and the ring body 2 to move toward the direction of the ring body 1. The contact between the ring body 1 and the ring body 2 generates vibration, and the vibration is transmitted to the catalyst particles on the gas outlet distribution plate. When the catalyst particles tend to agglomerate or begin to settle, the vibration of the gas outlet distribution plate can break the adhesion between the catalyst particles or re-suspend the settled particles, thereby overcoming this agglomeration force, keeping the particles in a good fluidized state, and promoting uniform fluidization. BRIEF DESCRIPTION OF THE DRAWINGS

[0021] Figure 1 It is a schematic diagram of the overall structure of the present invention;

[0022] Figure 2 It is a schematic diagram of the structure of the return pipe, the second motor and the extension part of the present invention;

[0023] Figure 3 is a cross-sectional view of the present invention;

[0024] Figure 4 It is a schematic diagram of the structure of the air intake assembly and the uniform flow enhancement assembly of the present invention;

[0025] Figure 5 It is a schematic diagram of the structure of the upper circulation part of the present invention;

[0026] Figure 6 It is a schematic diagram of the structure of the lower circulation part of the present invention;

[0027] Figure 7 It is a schematic diagram of the structure of the sedimentation suspension assembly and the gas outlet distribution plate of the present invention;

[0028] Figure 8 It is a schematic diagram of the structure of the ring body 1, the ring body 2, the inclined groove and the inclined top block of the present invention;

[0029] Fig. 9 It is a schematic diagram of the guide column and spring structure of the present invention;

[0030] Fig.10 It is a schematic diagram of the movable slot structure of the present invention.

[0031] Description of the numbers in the figure:

[0032] 1. Reactor body; 2. Cyclone separator; 3. Exhaust section; 4. Feeding section; 5. Catalytic regenerator; 6. Inlet end; 7. Discharge end; 8. Inlet assembly; 81. Discharge distribution plate; 82. Bottom plate; 83. Rotary joint; 9. Flow enhancement assembly; 91. Motor 1; 92. Gear 1; 93. Gear 2; 10. Annular groove; 101. Annular fixing ring; 102. Exhaust nozzle; 11. Feeding pipe; 12. Inlet section; 13. Discharge port; 14. In-vessel circulation unit; 141. Lower circulation section; 1411. Hollow casing; 1412. Conical drainage groove; 1 413. flange one; 1414. trapezoidal circulation groove; 142. upper circulation part; 1421. seat body; 1422. conical drainage part; 1423. arc-shaped drainage part; 1424. flange two; 1425. spoiler; 1426. dynamic sealing part; 143. top plate; 144. motor two; 15. extension part; 16. discharge adjustment assembly; 161. hydraulic cylinder; 162. guide rod; 17. sedimentation and suspension assembly; 171. ring body one; 172. ring body two; 173. inclined groove; 174. inclined top block; 175. guide column; 176. spring; 177. movable groove. DETAILED DESCRIPTION

[0033] The technical solutions in the embodiments of the present invention will be clearly and completely described below in conjunction with the drawings in the embodiments of the present invention; it is obvious that the described embodiments are only part of the embodiments of the present invention, rather than all the embodiments, and all other embodiments obtained by ordinary technicians in this field based on the embodiments of the present invention without making creative work are within the scope of protection of the present invention.

[0034] See also Figures 1 to 10 A fluidized bed reactor for naphtha production comprises a reactor body 1 and a reaction chamber provided inside the reactor body 1, wherein an air inlet assembly 8 is connected to the lower end of the reactor body 1, and the air inlet assembly 8 comprises a bottom plate 82 fixedly connected to the lower end of the reactor body 1 and a gas outlet distribution plate 81 located above the bottom plate 82 and rotatably connected to the inner wall of the reactor body 1, an output port 13 is provided inside the reactor body 1, and the output port 13 is communicated with the input end of a cyclone separator 2, an exhaust portion 3 is connected to the upper end of the cyclone separator 2, and a feed portion 4 is connected to the discharge end of the cyclone separator 2, the other end of the feed portion 4 is connected to the input end of a catalytic regenerator 5, and a discharge end 7 of the catalytic regenerator 5 is communicated with the reaction chamber inside the reactor body 1, and an air inlet end 6 is provided at the lower end of the catalytic regenerator 5.

[0035] A rotary joint 83 is fixedly connected to the lower end of the bottom plate 82 , and an inner tube of the rotary joint 83 passes through the bottom plate 82 and is inserted into the input end of the gas outlet distribution plate 81 . The outer surface of the inner tube is fixedly connected to the inner wall of the input end of the gas outlet distribution plate 81 .

[0036] By adopting the above technical solution, the atomized naphtha (the atomized naphtha is the liquid naphtha converted into a state of fine droplets by spraying technology, which helps to increase the surface area of ​​the naphtha, thereby enhancing its contact effect with the catalyst and hydrogen) and hydrogen (as a hydrogen source for the hydrogenation reaction, participating in the rearrangement of the molecular structure, and preventing the catalyst from being poisoned by reducing the accumulation of unsaturated hydrocarbons in the raw material) are mixed and then enter the gas outlet distribution plate 81 through the rotary joint 83, and are discharged from the gas outlet distribution plate 81 into the reactor body 1. The naphtha and hydrogen entering the reactor body 1 are mixed with the catalyst inside the reactor body 1 (in the fluidized bed In the bed reactor, the catalyst needs to have good fluidity and high reaction activity, and at the same time be able to withstand the reaction temperature and the requirements of cyclic regeneration. In this application, precious metal catalysts are used. For example, precious metals such as platinum, palladium, and rhodium have excellent dehydrogenation, aromatization, and isomerization reaction performance, which are suitable for the reforming process of naphtha. These catalysts are usually dispersed on carriers with smaller particle sizes, such as bauxite, silica gel, or aluminosilicate carriers, which can provide a larger specific surface area and improve the catalytic efficiency) to carry out catalytic reaction to realize the reforming of naphtha (the catalyst particles are blown up by the air flow in the reactor body 1 to form a state similar to the flow of liquid, that is, the "fluidized" state.When the gas flow passes through the catalyst particles, the particles are suspended in the gas flow, and the catalyst particles are fully in contact with the gas and liquid raw materials. In the catalytic reforming process, the catalyst mainly promotes the following reactions: the alkanes in the naphtha are converted into olefins through dehydrogenation reaction (for example, n-hexane is converted into hexene); the alkane molecules are rearranged to form branched alkanes, thereby increasing the octane number; some alkanes are converted into aromatic hydrocarbons (such as benzene, toluene and xylene, etc.) through the action of the catalyst; large molecular alkanes can be cracked into smaller olefins and hydrogen; the gas flow and particle catalyst inside the reactor body 1 will enter from the outlet 13 The catalyst particles are separated from the cyclone separator 2 (which is a mature prior art and will not be described in detail here). The naphtha after the reforming reaction is discharged from the exhaust part 3 along with the gas. The naphtha in the gas is separated by condensation collection and other means in the prior art, and is discharged from the lower end of the cyclone separator 2 and enters the feeding part 4. The feeding part 4 uses a mechanical conveying method to convey the catalyst particles from the cyclone separator 2. The catalyst particles are conveyed by a transmission device (such as a screw conveyor, a belt conveyor, a bucket elevator, etc., which are commonly used conveying means and will not be described in detail here). The cyclone separator 2 is transported into the catalytic regenerator 5, which is a fluidized bed. A reducing atmosphere (hydrogen) is introduced into the catalytic regenerator 5 through the air inlet 6. At an appropriate temperature (usually 300-500°C), the reducing gas reacts with the metal oxide on the surface of the catalyst to reduce the metal to its active state and restore the catalytic activity. The regenerated and reduced particle catalyst reenters the reactor body 1 together with the hydrogen from the discharge end 7 (the discharge end 7 is a pipeline, and a heat exchange cooling structure is provided in the pipeline to cool the discharge end 7 and the hydrogen and particle catalyst inside the discharge end 7 to avoid excessive temperature of the regenerated particle catalyst) to continue the catalytic reaction. In summary, the present application allows the catalyst to be dynamically circulated online, the catalyst is in contact with the airflow more frequently, and the online regeneration is more efficient. The catalytic activity can be restored without stopping production, reducing downtime and improving production continuity. At the same time, since the catalyst particles are in a fluidized state, the contact between the gas and the catalyst is very uniform, which makes the reaction temperature distribution more uniform, reduces local overheating, maintains a high reaction efficiency, and reduces the risk of coke accumulation.

[0037] like Figure 2-Figure 4 As shown, the lower end of the base plate 82 is also connected to a flow-uniformizing component 9, and the flow-uniformizing component 9 includes a motor 91 fixedly connected to the lower end of the base plate 82, a gear 92 rotatably connected to the upper end of the base plate 82, and a gear 93 meshing with the gear 92, and the gear 92 is fixedly sleeved on the outside of the inner tube of the rotary joint 83.

[0038] A conical inner expansion section is arranged in the middle of the reactor body 1, and an air inlet 12 is fixedly connected to the inner part of the conical inner expansion section at an angle.

[0039] A return pipe 11 is also horizontally fixedly inserted into the interior of the conical inner expansion section, and one end of the return pipe 11 is connected to the discharge end 7. The return pipe 11 is used to send the regenerated catalyst and gas from the discharge end 7 into the reactor body 1 in a tangential shape.

[0040] By adopting the above technical solution, when the motor 1 91 is working, it can drive the gear 1 92 and the gear 2 93 to rotate, and the rotation of the gear 2 93 drives the gas outlet distribution plate 81 to rotate. When the gas outlet distribution plate 81 rotates, the position and angle of the gas entering the reaction chamber will continue to change, so that the gas can be more evenly distributed at the bottom of the entire reactor body 1, breaking the original airflow deviation and the dead zone of incomplete reaction, improving the distribution of gas in the reactor body 1, and reducing the local area where the gas flow rate is too high or too low, thereby improving the reaction efficiency. At the same time, the rotating gas outlet distribution plate 81 may help to break the area where particles are accumulated and promote more uniform fluidization of catalyst particles, which helps to avoid particle retention and accumulation, ensure better distribution of catalyst particles, thereby improving the reaction rate and catalytic efficiency. Atomized naphtha and hydrogen can be introduced into the reactor body 1. The introduced naphtha and hydrogen can react with the catalyst circulating in the reactor body 1 on the one hand, and can react with the particulate catalyst discharged from the return pipe 11 on the other hand. The regenerated catalyst particles are reintroduced into the reactor body 1 through a tangent angle, so that the catalyst particles can obtain a certain rotational kinetic energy or radial velocity. This inflow method is conducive to the uniform distribution of the catalyst in the reactor and avoids the concentration of the catalyst in a certain position. The rotation coordination with the gas outlet distribution plate 81 can disturb the airflow pattern in the fluidized bed, increase the turbulent intensity of the fluid, and enhance the interaction between the gas and the catalyst particles. This turbulent effect helps to keep the catalyst suspended and evenly distributed, thereby improving the efficiency of the reaction.

[0041] like Figure 3 , Figure 5 and Figure 6As shown, the reactor body 1 is connected to an internal circulation unit 14, and the internal circulation unit 14 includes a lower circulation part 141 fixedly connected to the reactor body 1 and an upper circulation part 142 connected to the upper end of the reactor body 1, and the lower circulation part 141 includes a hollow casing 1411 fixedly connected to the reactor body 1, a conical drainage groove 1412 opened in the center of the hollow casing 1411, and a plurality of trapezoidal circulation grooves 1412 opened in the hollow casing 1411. 14, the upper circulation part 142 includes a seat body 1421 movably connected to the inside of the reactor body 1 and fitted with the inner wall of the reaction chamber, a conical drainage part 1422 opened at the center of the lower end of the seat body 1421, and an arc-shaped drainage part 1423 opened at the edge of the lower end of the seat body 1421 and connected to the conical drainage part 1422. The upper end of the reactor body 1 is also connected to a discharge adjustment component 16 for driving the seat body 1421 to move to adjust the discharge amount of the output port 13.

[0042] A plurality of flanges 1413 are integrally formed on the inner wall of the conical drainage groove 1412 , and a plurality of flanges 1424 are integrally formed on the outer wall of the arc-shaped drainage portion 1423 .

[0043] A plurality of spoilers 1425 are integrally formed on the outer wall of the conical drainage portion 1422, a top plate 143 is fixedly connected to the upper end of the seat body 1421, and a second motor 144 is fixedly connected to the upper end of the top plate 143, an output shaft of the second motor 144 passes through the top plate 143 and is fixedly connected to the upper end of the seat body 1421, and a dynamic sealing portion 1426 is fixedly connected to the inner wall of the reaction chamber of the reactor body 1 (dynamic sealing is a common technology in the prior art, such as packing seals, mechanical seals, floating oil seals, etc., which will not be described in detail here).

[0044] The discharge adjustment assembly 16 includes two extension parts 15 integrally formed on the outside of the reactor body 1 and symmetrical to each other, a hydraulic cylinder 161 fixed to the outside of the reactor body 1, and a guide rod 162 fixed to the lower end of the top plate 143 and movably inserted into one of the extension parts 15. The telescopic end of the hydraulic cylinder 161 passes through the other extension part 15 and is fixed to the lower end of the top plate 143.

[0045] By adopting the above technical solution, the hydraulic cylinder 161 can drive the top plate 143 and the seat body 1421 to move up and down. When the seat body 1421 moves upward, the shielding area of ​​the output port 13 becomes smaller, and the airflow and catalyst discharged from the output port 13 become more. When the seat body 1421 moves downward, the shielding area of ​​the output port 13 becomes larger, and the airflow and catalyst discharged from the output port 13 become less. The reduced discharge amount can enable the airflow and catalyst inside the reactor body 1 to fully react. The atomized naphtha and hydrogen discharged from the gas outlet distribution plate 81 drive the granular catalyst to flow upward. The flow rate of the mixed airflow is accelerated when it passes through the conical drainage groove 1412, and the mixed airflow is discharged from the top of the conical drainage groove 1412. Between the seat body 1421 and the hollow sleeve body 1411, the mixed air flow is guided into a plurality of trapezoidal circulation grooves 1414 via the conical guide portion 1422 and the arc-shaped guide portion 1423, and is discharged from the bottom of the trapezoidal circulation grooves 1414 and merges with the air flow discharged from the gas outlet distribution plate 81, the atomized naphtha and hydrogen discharged from the air inlet 12, and the particulate catalyst discharged from the return pipe 11, thereby realizing the upward and downward circulation of the air flow inside the reactor body 1. The arrangement of flange 1 1413 and flange 2 1424 can increase the disturbance of the air flow, and the motor 2 144 can drive the seat body 1421 and the spoiler 1425 to rotate, thereby increasing the disturbance of the mixed air flow discharged from the top of the conical guide groove 1412.

[0046] like Figure 7-Figure 10 As shown, the lower end of the gas outlet distribution plate 81 is also connected to a sedimentation suspension assembly 17, and the sedimentation suspension assembly 17 includes a ring body 171 fixedly connected to the lower end of the gas outlet distribution plate 81, a movable groove 177 opened inside the ring body 171, a guide column 175 movably inserted in the movable groove 177, a spring 176 located inside the movable groove 177 and sleeved on the outside of the guide column 175, a ring body 172 fixedly connected to the lower end of the guide column 175, an inclined groove 173 opened inside the ring body 172, and an inclined top located in the inclined groove 173. Block 174, and the inclined top block 174 is fixedly connected to the upper end of the bottom plate 82, the two ends of the spring 176 are respectively connected to the inner wall of the movable groove 177 and one side of the guide column 175, the inner wall of the reaction chamber is provided with an annular groove 10, and an annular fixing ring 101 is fixedly connected in the annular groove 10, an exhaust nozzle 102 is fixedly connected to the inner wall of the annular fixing ring 101, and the gas outlet end of the exhaust nozzle 102 faces the gas outlet distribution plate 81, and the input end of the exhaust nozzle 102 passes through the annular fixing ring 101 and the reactor body 1 and extends outward.

[0047] By adopting the above technical solution, when the outlet gas distribution plate 81 rotates, it drives the ring body 171 and the ring body 172 to rotate. When the ring body 172 rotates, the inclined groove 173 can contact the inclined top block 174, and the inclined surface of the inclined top block 174 contacts the inclined surface of the inclined groove 173, so that the inclined top block 174 pushes the ring body 172 to move toward the bottom plate 82. When the inclined surface of the inclined groove 173 separates from the inclined surface of the inclined top block 174, the spring 176 can drive the guide column 175 and the ring body 172 to move toward the direction of the ring body 171, and the ring body 171 and The second ring body 172 generates vibration upon contact, and the vibration is transmitted to the catalyst particles on the gas outlet distribution plate 81. When the catalyst particles tend to agglomerate or begin to settle, the vibration of the gas outlet distribution plate 81 can break the adhesion between the catalyst particles or re-suspend the settled particles. By periodically applying external force to the gas outlet distribution plate 81 to make it vibrate, the agglomeration force is overcome, the particles are kept in a good fluidized state, uniform fluidization is promoted, and at the same time, in conjunction with the airflow ejected from the exhaust nozzle 102, the situation of catalyst settling on the gas outlet distribution plate 81 can be avoided.

[0048] Method of use: The atomized naphtha and hydrogen are mixed and enter the gas outlet distribution plate 81 through the rotary joint 83 and are discharged from the gas outlet distribution plate 81 into the reactor body 1. The naphtha and hydrogen entering the reactor body 1 react with the catalyst inside the reactor body 1 to reform the naphtha. The airflow and particulate catalyst inside the reactor body 1 enter the cyclone separator 2 from the output port 13. The particulate catalyst is separated by the cyclone separator 2. The naphtha after the reforming reaction is discharged from the exhaust part 3 along with the gas. The naphtha in the gas is separated by condensation collection and other means in the prior art. The granular catalyst is transported from the cyclone separator 2 to the catalytic regenerator 5 through a transmission device. The catalytic regenerator 5 is a fluidized bed. A reducing atmosphere is introduced into the catalytic regenerator 5 through an air inlet 6. At an appropriate temperature, the reducing gas reacts with the metal oxide on the surface of the catalyst to reduce the metal to its active state and restore the catalytic activity. The regenerated and reduced granular catalyst re-enters the reactor body 1 together with the hydrogen from the discharge end 7 to continue the catalytic reaction.

[0049] The above is only a preferred specific implementation of the present invention; however, the protection scope of the present invention is not limited thereto. Any technician familiar with the technical field can make equivalent replacements or changes according to the technical solution and its improved conception within the technical scope disclosed by the present invention, which should be covered by the protection scope of the present invention.

Claims

1. A fluidized bed reactor for naphtha production, comprising a reactor body (1) and a reaction chamber disposed inside the reactor body (1), characterized in that: The lower end of the reactor body (1) is connected to an air intake assembly (8), and the air intake assembly (8) comprises a bottom plate (82) fixedly connected to the lower end of the reactor body (1) and a gas outlet distribution plate (81) located above the bottom plate (82) and rotatably connected to the inner wall of the reactor body (1), a rotary joint (83) is fixedly connected to the lower end of the bottom plate (82), and an inner tube of the rotary joint (83) passes through the bottom plate (82) and is plugged into the input end of the gas outlet distribution plate (81), and an outer surface of the inner tube is fixedly connected to the inner wall of the input end of the gas outlet distribution plate (81); The lower end of the bottom plate (82) is also connected to a flow-uniformizing and enhancing component (9), and the flow-uniformizing and enhancing component (9) comprises a motor 1 (91) fixedly connected to the lower end of the bottom plate (82), a gear 1 (92) rotatably connected to the upper end of the bottom plate (82), and a gear 2 (93) meshing with the gear 1 (92), wherein the gear 1 (92) is fixedly sleeved on the outside of the inner tube of the rotary joint (83); A conical inner expansion section is provided in the middle of the reactor body (1), and an air inlet portion (12) is fixedly connected to the inner portion of the conical inner expansion section at an angle; A return pipe (11) is also horizontally fixedly inserted into the interior of the conical inner expansion section, and one end of the return pipe (11) is connected to the discharge end (7). The return pipe (11) is used to send the regenerated catalyst and gas from the discharge end (7) into the reactor body (1) in a tangential manner; The reactor body (1) is connected to an in-vessel circulation unit (14), and the in-vessel circulation unit (14) comprises a lower circulation part (141) fixedly connected to the inside of the reactor body (1) and an upper circulation part (142) connected to the upper end of the inside of the reactor body (1), the lower circulation part (141) comprising a hollow casing (1411) fixedly connected to the inside of the reactor body (1), a conical drainage groove (1412) provided at the center of the hollow casing (1411), and a plurality of trapezoidal circulation grooves (1412) provided in the hollow casing (1411). 4), the upper circulation part (142) comprises a seat body (1421) movably connected to the inside of the reactor body (1) and in contact with the inner wall of the reaction chamber, a conical drainage part (1422) provided at the center of the lower end of the seat body (1421), and an arc-shaped drainage part (1423) provided at the edge of the lower end of the seat body (1421) and connected to the conical drainage part (1422), and the upper end of the reactor body (1) is also connected to a discharge adjustment component (16) for driving the seat body (1421) to move and adjust the discharge amount of the output port (13).

2. A fluidized bed reactor for naphtha production according to claim 1, characterized in that: The reactor body (1) is provided with an output port (13) inside, and the output port (13) is connected to the input end of the cyclone separator (2), the upper end of the cyclone separator (2) is connected to an exhaust portion (3), and the discharge end of the cyclone separator (2) is connected to a feed portion (4), the other end of the feed portion (4) is connected to the input end of the catalytic regenerator (5), and the discharge end (7) of the catalytic regenerator (5) is connected to the reaction chamber inside the reactor body (1), and the lower end of the catalytic regenerator (5) is provided with an air inlet port (6).

3. A fluidized bed reactor for naphtha production according to claim 2, characterized in that: A plurality of flanges 1 (1413) are integrally formed on the inner wall of the conical drainage groove (1412), and a plurality of flanges 2 (1424) are integrally formed on the outer wall of the arc-shaped drainage portion (1423).

4. A fluidized bed reactor for naphtha production according to claim 3, characterized in that: A plurality of spoilers (1425) are integrally formed on the outer wall of the conical drainage portion (1422); a top plate (143) is fixedly connected to the upper end of the seat body (1421); a second motor (144) is fixedly connected to the upper end of the top plate (143); an output shaft of the second motor (144) passes through the top plate (143) and is fixedly connected to the upper end of the seat body (1421); and a dynamic sealing portion (1426) is fixedly connected to the inner wall of the reaction chamber of the reactor body (1).

5. A fluidized bed reactor for naphtha production according to claim 4, characterized in that: The discharge adjustment assembly (16) comprises two extensions (15) integrally formed on the outside of the reactor body (1) and symmetrical to each other, a hydraulic cylinder (161) fixedly connected to the outside of the reactor body (1), and a guide rod (162) fixedly connected to the lower end of the top plate (143) and movably inserted into one of the extensions (15); the telescopic end of the hydraulic cylinder (161) passes through the other extension (15) and is fixedly connected to the lower end of the top plate (143).

6. A fluidized bed reactor for naphtha production according to claim 5, characterized in that: The lower end of the gas outlet distribution plate (81) is also connected to a sedimentation suspension assembly (17), and the sedimentation suspension assembly (17) comprises a ring body (171) fixedly connected to the lower end of the gas outlet distribution plate (81), a movable groove (177) provided inside the ring body (171), a guide column (175) movably inserted in the movable groove (177), a spring (176) located inside the movable groove (177) and sleeved on the outside of the guide column (175), a ring body (172) fixedly connected to the lower end of the guide column (175), an inclined groove (173) provided inside the ring body (172), and an inclined top block (174) located in the inclined groove (173), wherein the inclined top block (174) is fixedly connected to the upper end of the bottom plate (82), and the two ends of the spring (176) are respectively connected to the inner wall of the movable groove (177) and one side of the guide column (175).

7. A fluidized bed reactor for naphtha production according to claim 6, characterized in that: An annular groove (10) is formed on the inner wall of the reaction chamber, and an annular fixing ring (101) is fixedly connected in the annular groove (10); an exhaust nozzle (102) is fixedly connected to the inner wall of the annular fixing ring (101), and the gas outlet end of the exhaust nozzle (102) faces the gas outlet distribution plate (81); the input end of the exhaust nozzle (102) passes through the annular fixing ring (101) and the reactor body (1) and extends outward.

Images