Vertical fluidized bed reactor
By introducing breathable distributor and multi-stage cyclone separator components into the fluidized bed reactor, the problems of uneven gas distribution and large catalyst consumption are solved, the heat exchange efficiency and system stability are improved, higher production capacity is achieved and maintenance costs are reduced.
Patent Information
- Application Number
- CN202422291492.6
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-09-19
- Publication Date
- 2025-07-29
- Estimated Expiration
- 2034-09-19
AI Technical Summary
The existing fluidized bed reactors have problems such as uneven distribution of reaction gas, large catalyst consumption, low heat exchange efficiency and unstable system pressure.
The gas permeable distributor is used to achieve uniform distribution of hydrogen, the multi-stage cyclone separator assembly is used to improve the catalyst separation efficiency, and the forced cyclic heat exchanger is used to improve the heat exchange efficiency.
The uniform distribution of reaction gas is achieved, catalyst consumption is reduced, production capacity is improved, system pressure is maintained, and maintenance needs are reduced.
Smart Images
Figure CN223159220U_ABST
Abstract
Description
Technical Field
[0001] The utility model relates to the technical field of gas-solid two-phase reaction equipment, and particularly relates to a vertical fluidized bed reactor. Background Art
[0002] Fluidized bed reactors can achieve continuous input and output of solid materials. At the same time, they also have high heat transfer and mass transfer performance and are widely used in gas-solid multiphase reactions. For example, currently in industry, the gas-phase hydrogenation of nitrobenzene to prepare aniline and the hydrogenation of o-nitrotoluene to prepare o-toluidine are usually carried out in fluidized bed reactors. However, the fluidized bed reactors used for preparing aniline and o-toluidine in the prior art have the following defects:
[0003] 1. There is no gas distributor at the bottom end. After the reaction gas enters from the reactant inlet, the distribution in front of the distribution plate is uneven, manifested as large gas flow in the middle and small gas flow at the edge, which affects the stable operation of the fluidized bed;
[0004] 2. Filter tubes are used to separate catalysts, and their filter cloth is easily damaged, resulting in large catalyst consumption. Replacing the filter cloth will increase additional workload and cost. In addition, the filter tubes are also prone to coking, leading to an increase in system pressure;
[0005] 3. The heat exchanger adopts a natural circulation process, and the heat exchange effect is limited, resulting in limited production capacity.
[0006] Therefore, designing a fluidized bed reactor that can overcome the above defects has become a technical problem to be solved in this field. Summary of the Invention
[0007] The technical problem to be solved by the utility model is to provide a vertical fluidized bed reactor that can achieve uniform distribution of hydrogen, has good catalyst separation effect and low consumption, the production capacity is not restricted by the heat exchanger, and the system pressure is stable.
[0008] To solve the above technical problem, the vertical fluidized bed reactor provided by the utility model includes:
[0009] A reactor main body;
[0010] A multi-stage cyclone separator assembly, which is arranged in the dilute phase region inside the reactor main body;
[0011] Heat exchange tubes, which are arranged in the dense phase region inside the reactor main body;
[0012] A breathable distributor, which is arranged at the bottom end of the reactor main body, and the breathable distributor is formed into an inverted cone shape matching the shape of the bottom end;
[0013] A distribution plate, which is arranged between the heat exchange tubes and the breathable distributor.
[0014] Preferably, the multi-stage cyclone separator assembly includes a primary cyclone separator, a secondary cyclone separator, and a tertiary cyclone separator that are connected in sequence.
[0015] Preferably, a primary discharge channel is provided at the top of the primary cyclone separator, and a primary overflow pipe is provided in the primary discharge channel. The primary overflow pipe extends from the top sealing end of the reactor body to the outside of the reactor body.
[0016] The secondary cyclone separator is adjacent to the primary cyclone separator. It includes a secondary material inlet provided on its cylindrical side wall section. The secondary cyclone separator is connected to the primary discharge channel through the secondary material inlet. A secondary discharge channel is provided at the top of the secondary cyclone separator, and a secondary overflow pipe is provided at the top of the secondary discharge channel. The secondary overflow pipe extends from the top sealing end of the reactor body to the outside of the reactor body.
[0017] The tertiary cyclone separator is adjacent to the secondary cyclone separator. It includes a tertiary material inlet provided on its cylindrical side wall section. The tertiary cyclone separator is connected to the secondary discharge channel through the tertiary material inlet. A tertiary material outlet is provided at the top of the tertiary cyclone separator.
[0018] Preferably, a primary material inlet is provided on the cylindrical side wall of the primary cyclone separator, and the dipleg of the primary cyclone separator extends to a position close to the distribution plate.
[0019] The diplegs of the secondary cyclone separator and the tertiary cyclone separator extend to a position close to the dense phase region at the bottom of the dilute phase region.
[0020] Preferably, manholes are provided at the corresponding positions of the side wall of the reactor body where the dipleg discharge ports of the secondary cyclone separator and the dipleg discharge port of the tertiary cyclone separator are located.
[0021] Preferably, a porous plug is installed at the dipleg discharge port of the primary cyclone separator.
[0022] A flap valve is installed at the dipleg discharge port of the secondary cyclone separator.
[0023] A cone valve is installed at the discharge port of the tertiary cyclone separator.
[0024] Preferably, the heat exchange tubes adopt forced circulation heat exchangers.
[0025] Preferably, a reactant inlet is provided at the bottom sealing end of the reactor body.
[0026] Preferably, pressure measurement ports are provided at the top of the reactor body and on the side wall located in the dilute phase region.
[0027] The side walls of the reactor body in the dilute phase region and the dense phase region are both provided with temperature measurement ports;
[0028] The side wall of the reactor body in the dense phase region and near the bottom end is provided with a catalyst outlet.
[0029] Preferably, multiple layers of baffles are provided in the dense phase region of the reactor body.
[0030] The present utility model provides a vertical fluidized bed reactor, which realizes the uniform distribution of hydrogen through a gas-permeable distributor, making it uniformly distributed in front of the distribution plate, ensuring the stable operation of the fluidized bed; adopts a multi-stage cyclone separator assembly, with high catalyst separation efficiency, good separation effect, low consumption, not easy to coke, stable system pressure, and can achieve node-free maintenance; the heat exchange tubes preferably adopt forced circulation heat exchangers to improve the heat exchange efficiency, which is beneficial to improving production capacity, and at the same time utilizes heat energy to save steam. Description of the Drawings
[0031] In order to more clearly illustrate the technical solutions of the present utility model, the following briefly introduces the drawings required for the present utility model. Obviously, the drawings in the following description are only some embodiments of the present utility model. For those of ordinary skill in the art, without creative efforts, other drawings can also be obtained based on these drawings.
[0032] Figure 1 is a schematic diagram of an embodiment of the vertical fluidized bed reactor of the present utility model;
[0033] Figure 2 is a schematic diagram of the multi-stage cyclone separator assembly of an embodiment of the vertical fluidized bed reactor of the present utility model;
[0034] Figure 3 is a schematic diagram of the heat exchange tubes of an embodiment of the vertical fluidized bed reactor of the present utility model;
[0035] In the figure, 1 - reactor body; 11 - dilute phase region; 12 - dense phase region; 13 - reactant inlet; 14 - catalyst inlet; 15 - manhole; 16 - pressure measurement port; 17 - temperature measurement port; 18 - catalyst outlet; 19 - ear seat; 2 - multi-stage cyclone separator assembly; 21 - primary cyclone separator; 22 - secondary cyclone separator; 23 - tertiary cyclone separator; 211 - primary discharge channel; 212 - primary overflow pipe; 213 - primary material inlet; 221 - secondary material inlet; 222 - secondary discharge channel; 223 - secondary overflow pipe; 231 - tertiary material inlet; 232 - tertiary material outlet; 3 - heat exchange tubes; 4 - gas-permeable distributor; 5 - distribution plate; 6 - baffle. Detailed Embodiments
[0036] The technical solutions in the present utility model will be clearly and completely described below in conjunction with the accompanying drawings. Apparently, the described embodiments are some, but not all, of the embodiments of the present utility model. All other embodiments obtained by those of ordinary skill in the art based on the embodiments in the present utility model without creative efforts shall fall within the protection scope of the present utility model.
[0037] Referring to Figure 1 , the vertical fluidized bed reactor provided by the present utility model includes:
[0038] A reactor main body 1;
[0039] A multi-stage cyclone separator assembly 2, which is arranged in the dilute-phase zone 11 inside the reactor main body 1;
[0040] Heat exchange tubes 3, which are arranged in the dense-phase zone 12 inside the reactor main body 1;
[0041] A gas-permeable distributor 4, which is arranged at the bottom end of the reactor main body 1, and the gas channels of the gas-permeable distributor 4 are divergently distributed from the conical tip part towards the conical bottom surface, facilitating the uniform distribution of the reactant mixed gas after passing through the gas-permeable distributor 4. Thus, the reactant mixed gas passes through the distribution plate 5 in a uniformly distributed state, thereby ensuring the stable operation of the fluidized bed; it should be noted that the gas-permeable distributor 4 and the distribution plate 5 can be installed at the bottom end by means such as fastening with fasteners. It should be noted that the vertical fluidized bed reactor of the present utility model can be installed and fixed, for example, through an ear seat 19, and the distribution plates 5 in the prior art can all be applicable to the present utility model.
[0042] A distribution plate 5, which is arranged between the heat exchange tubes 3 and the gas-permeable distributor 4.
[0043] For the vertical fluidized bed reactor provided by the present utility model, a gas-permeable distributor 4 is arranged at the bottom end of the reactor main body 1, and the gas channels of the gas-permeable distributor 4 are divergently distributed from the conical tip part towards the conical bottom surface, facilitating the uniform distribution of the reactant mixed gas after passing through the gas-permeable distributor 4. Thus, the reactant mixed gas passes through the distribution plate 5 in a uniformly distributed state, thereby ensuring the stable operation of the fluidized bed; it should be noted that the gas-permeable distributor 4 and the distribution plate 5 can be installed at the bottom end by means such as fastening with fasteners. It should be noted that the vertical fluidized bed reactor of the present utility model can be installed and fixed, for example, through an ear seat 19, and the distribution plates 5 in the prior art can all be applicable to the present utility model.
[0044] For the vertical fluidized bed reactor provided by the present utility model, the catalyst (solid state) separation adopts a multi-stage cyclone separator assembly 2. After multiple separations, the separation effect is good, the catalyst consumption is reduced, and no special maintenance is required, reducing the maintenance time and cost. Moreover, the multi-stage cyclone separator assembly 2 is not prone to coking, the system pressure is stable, and node-free maintenance can also be achieved; it should be noted that the multi-stage cyclone separator assembly 2 can be installed on the side wall of the reactor main body 1 by means such as fastening with fasteners.
[0045] The vertical fluidized bed reactor provided by the present utility model, referring to Figure 3, the heat exchange tube 3 preferably adopts a forced circulation heat exchanger. By using the forced circulation heat exchange process, the heat exchange efficiency is increased, which is convenient for improving the production capacity. At the same time, heat energy is utilized to save steam. It should be noted that the forced circulation pump of the forced circulation heat exchanger can be, for example, externally placed outside the vertical fluidized bed reactor. The heat exchange tube 3 is placed inside the dense phase zone 12 of the vertical fluidized bed reactor. After the refrigerant is pressurized by the forced circulation pump, it enters the heat exchange tube 3. The heat exchange tube 3 can be, for example, composed of multiple groups of U-shaped heat exchange tubes. The inlets and outlets of multiple groups of U-shaped heat exchange tubes converge at the inlets and outlets of the main pipe and are connected to the forced circulation pump. This can be achieved through existing technologies and will not be elaborated here.
[0046] In a specific embodiment, referring to Figure 2 , the multi-stage cyclone separator assembly 2 includes a primary cyclone separator 21, a secondary cyclone separator 22, and a tertiary cyclone separator 23 that are connected in sequence.
[0047] More specifically, a primary discharge channel 211 is provided at the top of the primary cyclone separator 21. A primary overflow pipe 212 is provided in the primary discharge channel 211. The primary overflow pipe 212 extends from the top end cap of the reactor main body 1 to the outside of the reactor main body 1;
[0048] The secondary cyclone separator 22 is adjacent to the primary cyclone separator 21. It includes a secondary material inlet 221 provided on its cylindrical side wall section. The secondary cyclone separator 22 is communicated with the primary discharge channel 211 through the secondary material inlet 221. A secondary discharge channel 222 is provided at the top of the secondary cyclone separator 22. A secondary overflow pipe 223 is provided at the top of the secondary discharge channel 222. The secondary overflow pipe 223 extends from the top end cap of the reactor main body 1 to the outside of the reactor main body 1;
[0049] The tertiary cyclone separator 23 is adjacent to the secondary cyclone separator 22. It includes a tertiary material inlet 231 provided on its cylindrical side wall section. The tertiary cyclone separator 23 is communicated with the secondary discharge channel 222 through the tertiary material inlet 231. A tertiary material outlet 232 is provided at the top of the tertiary cyclone separator 23.
[0050] More specifically, a primary material inlet 213 is provided on the cylindrical side wall section of the primary cyclone separator 21. The dipleg of the primary cyclone separator 21 extends to a position close to the distributor plate 5;
[0051] The diplegs of the secondary cyclone separator 22 and the tertiary cyclone separator 23 extend to a position close to the dense phase zone 12 at the bottom of the dilute phase zone 11.
[0052] In this specific embodiment, the materials in the dilute phase region 11 enter the primary cyclone separator 21 from the primary material inlet 213; the catalyst separated by the primary cyclone separator 21 is sent into the dense phase region 12 through the dipleg to continue participating in the reaction, improving the utilization efficiency of the catalyst; for the gas-phase materials separated by the primary cyclone separator 21, most of them enter the secondary cyclone separator 22 through the primary discharge channel 211 and the secondary material inlet 221 for further cyclone separation, and a small part overflows to the outside of the reactor body 1 through the primary overflow pipe 212, and the materials are collected; for the gas-phase materials separated by the secondary cyclone separator 22, most of them enter the tertiary cyclone separator 23 through the secondary discharge channel 222 and the tertiary material inlet 231 for further cyclone separation, and a small part overflows to the outside of the reactor body 1 through the secondary overflow pipe 223, and the materials are collected; the gas-phase materials separated by the tertiary cyclone separator 23 are transported to the outside of the reactor body 1 through the tertiary material outlet 232 and collected therein.
[0053] In a specific embodiment, a porous plug is installed at the dipleg outlet of the primary cyclone separator 21, and a flap valve is installed at the dipleg outlet of the secondary cyclone separator 22; a cone valve is installed at the outlet of the tertiary cyclone separator 23. In this specific embodiment, the catalyst separated by the primary cyclone separator 21 enters the dense phase region 12 again through the porous plug to participate in the reaction, and at the same time, the porous plug also plays a good role in preventing the reactants from flowing upwards; less catalyst is separated by the secondary cyclone separator 22, and preferably a flap valve is used, which can not only prevent the reverse flow of materials, but also facilitate the automatic opening of the flap valve by the gravity principle when a certain amount of catalyst accumulates, and then enter the dense phase region 12 again to participate in the reaction; extremely little catalyst is separated by the tertiary cyclone separator 23, and preferably a cone valve is used, which can not only improve the cyclone dust removal efficiency, but also effectively prevent the upward flow of gas. After using the cone valve, this node can be maintained without maintenance. Preferably, manholes 15 are provided at the positions of the dipleg outlets of the secondary cyclone separator 22 and the dipleg outlet of the tertiary cyclone separator 23 on the side wall of the reactor body 1 to facilitate the inspection and maintenance of the equipment.
[0054] In a specific embodiment, a reactant inlet 13 is provided at the bottom end of the reactor body 1. In this specific embodiment, the reaction mixture (such as nitrobenzene and hydrogen mixture, o-nitrotoluene and hydrogen mixture, etc.) enters the reactor body 1 from the reactant inlet 13. After entering, it will first pass through the breathable distributor 4 and be evenly distributed, and then contact the catalyst fed from the catalyst inlet 14 to carry out the reaction.
[0055] In a specific embodiment, pressure measuring ports 16 are provided at the top of the reactor main body 1 and on the side wall located in the dilute phase zone 11; temperature measuring ports 17 are provided on the side walls of the reactor main body 1 in the dilute phase zone 11 and the dense phase zone 12; a catalyst outlet 18 is provided on the side wall of the reactor main body 1 in the dense phase zone 12 and near the bottom end. It can be understood that the arrangement of the pressure measuring ports 16 facilitates the measurement and monitoring of the pressure at corresponding positions inside the reactor main body 1; the arrangement of the temperature measuring ports 17 facilitates the measurement and monitoring of the temperature at corresponding positions inside the reactor main body 1; the arrangement of the catalyst outlet 18 on the side wall of the dense phase zone 12 and near the bottom end is to facilitate the discharge and collection of the catalyst after the sulfidation is completed.
[0056] In a specific embodiment, multiple layers of baffles 6 are provided in the dense phase zone 12 of the reactor main body 1 to disperse the materials. In this specific embodiment, the baffle 6 is preferably a corrugated baffle, which can well play the roles of blocking the catalyst, reducing the pressure of the cyclone separation, and dispersing the reaction system; the number of layers of the baffle 6 can be set as required, such as 5 layers, 8 layers, 10 layers, 12 layers, 20 layers, etc.
[0057] The above are only the preferred embodiments of the present invention and are not intended to limit the protection scope of the present invention. Any modifications, equivalent replacements, improvements, etc. made within the spirit and principle of the present invention shall be included within the protection scope of the present invention.
Claims
1. A vertical fluidized bed reactor, characterized in that, It includes: The reactor main body; A multi-stage cyclone separator assembly, which is arranged in the dilute phase zone inside the reactor main body; Heat exchange tubes, which are arranged in the dense phase zone inside the reactor main body; A gas-permeable distributor, which is arranged at the bottom end of the reactor main body, and the gas-permeable distributor is formed into an inverted cone shape matching the shape of the bottom end; A distribution plate, which is arranged between the heat exchange tubes and the gas-permeable distributor.
2. The vertical fluidized bed reactor according to claim 1, characterized in that, The multi-stage cyclone separator assembly includes a primary cyclone separator, a secondary cyclone separator and a tertiary cyclone separator that are connected in sequence.
3. The vertical fluidized bed reactor according to claim 2, characterized in that, A primary discharge channel is arranged at the top of the primary cyclone separator, a primary overflow pipe is arranged in the primary discharge channel, and the primary overflow pipe extends from the top end of the reactor main body to the outside of the reactor main body; The secondary cyclone separator is adjacent to the primary cyclone separator. It includes a secondary material inlet arranged on its cylindrical side wall section. The secondary cyclone separator is connected to the primary discharge channel through the secondary material inlet. A secondary discharge channel is arranged at the top of the secondary cyclone separator, and a secondary overflow pipe is arranged at the top of the secondary discharge channel. The secondary overflow pipe extends from the top end of the reactor main body to the outside of the reactor main body; The tertiary cyclone separator is adjacent to the secondary cyclone separator. It includes a tertiary material inlet arranged on its cylindrical side wall section. The tertiary cyclone separator is connected to the secondary discharge channel through the tertiary material inlet, and a tertiary material outlet is arranged at the top of the tertiary cyclone separator.
4. The vertical fluidized bed reactor according to claim 3, characterized in that, A primary material inlet is arranged on the cylindrical side wall of the primary cyclone separator, and the dipleg of the primary cyclone separator extends to a position close to the distribution plate; The diplegs of the secondary cyclone separator and the tertiary cyclone separator extend to a position close to the dense phase zone at the bottom of the dilute phase zone.
5. The vertical fluidized bed reactor according to claim 3, characterized in that, Manholes are opened at the corresponding positions of the side wall of the reactor main body where the dipleg discharge ports of the secondary cyclone separator and the dipleg discharge port of the tertiary cyclone separator are located.
6. The vertical fluidized bed reactor according to claim 4, characterized in that A porous plug is installed at the dipleg discharge port of the primary cyclone separator; A flap valve is installed at the dipleg discharge port of the secondary cyclone separator; A cone valve is installed at the dipleg discharge port of the tertiary cyclone separator.
7. The vertical fluidized bed reactor according to claim 1, characterized in that, The heat exchange tubes adopt forced circulation heat exchangers.
8. The vertical fluidized bed reactor according to claim 1, characterized in that, A reactant inlet is arranged at the bottom end of the reactor main body.
9. The vertical fluidized bed reactor according to claim 1, characterized in that, Pressure measurement ports are arranged at the top of the reactor main body and on the side wall in the dilute phase zone; Temperature measurement ports are arranged on the side walls of the reactor main body in the dilute phase zone and the dense phase zone; A catalyst outlet is arranged on the side wall of the reactor main body in the dense phase zone and close to the bottom end.
10. The vertical fluidized bed reactor according to claim 1, characterized in that, Multiple layers of baffles are arranged in the dense phase zone of the reactor main body.