Shell-and-tube heat exchange reaction device and reaction method

Abstract

The invention discloses a shell-and-tube heat exchange reaction device and a reaction method. The reaction device comprises an upper sealing head, a lower sealing head and a shell-and-tube heat exchanger, the shell is positioned at the lower part of the upper sealing head and is connected with the upper sealing head; the lower sealing head is positioned at the lower part of the shell and is connected with the shell; the air outlet pipe penetrates through the upper sealing head and is communicated with the shell; the air inlet pipe penetrates through the lower sealing head and is communicated with the shell; the feeding hole penetrates through the upper part of the shell; the discharge hole penetrates through the lower part of the shell; the fixed bed reactor is respectively communicated with the feed port and the discharge port; the feeding pipe is communicated with the shell; the discharging pipe is communicated with the shell and is positioned at the side part of the feeding pipe; reaction raw materials enter the fixed bed reactor through the reaction raw material feeding port, make contact with a catalyst in the fixed bed reactor and react under the heating effect of hot working medium particles entering the shell through the hot working medium particle feeding pipe.

Description

Technical Field

[0001] The invention relates to the technical field of chemical reaction engineering, and in particular to a shell and tube type heat exchange reaction device and a reaction method. Background Art

[0002] Under the background of energy transformation and "dual carbon", hydrogen energy has become an important strategic choice to accelerate energy transformation and upgrading and cultivate new economic growth points. A clean, low-carbon, low-cost diversified hydrogen production system is of great significance to building a clean, low-carbon, safe and efficient energy system and achieving the goals of carbon peak and carbon neutrality.

[0003] At present, the main methods of hydrogen production include water electrolysis and thermochemical reactions. The hydrogen production reaction process requires the absorption of a large amount of heat. Solar radiation energy is the most abundant renewable energy on Earth. In the concentrated solar thermal utilization system, the solar collector can convert solar radiation energy into thermal energy and store solar energy in the thermal medium. The high-temperature thermal medium after absorbing heat can further provide energy for various thermochemical hydrogen production reactions.

[0004] Compared with traditional thermal working fluids, such as heat transfer oil (upper limit of operating temperature ~400°C) and molten salt (upper limit of operating temperature ~600°C), particles can be used as a thermal working fluid with a higher operating temperature, and its upper limit of operating temperature can reach above 1000°C. In addition, particles are low in cost, and compared with molten salt thermal working fluids, particles can exhibit more stable physical and chemical properties during the heat charging and discharging process. Particles are different from liquid thermal working fluids. Particles must remain in a fluidized state during the heat transfer process to obtain excellent heat transfer performance. The heat transfer coefficient of particles under static conditions is extremely low. Therefore, it is necessary to develop a solar thermal utilization system that can use particles as a thermal working fluid and can use particles for heating stably and efficiently, so as to give full play to the value of clean energy solar energy. Summary of the invention

[0005] In view of this, the present application proposes a shell and tube heat exchange reaction device and a reaction method. The shell and tube heat exchange reactor with fluidized bed heat exchange proposed in the present invention can be connected to the hot working fluid particle heat storage system, and the sensible heat of the hot working fluid particles can be used to supply energy for the thermochemical reaction hydrogen production process and all other chemical reactions, phase changes and other endothermic processes carried out in the shell-and-tube reactor, so as to achieve clean and low-carbon production.

[0006] According to one aspect of the present application, the present invention provides a shell and tube heat exchange reaction device, characterized in that the shell and tube heat exchange reaction device comprises:

[0007] Upper head,

[0008] A shell, which is located at the lower part of the upper head and connected to the upper head;

[0009] A lower head, which is located at the lower part of the shell and connected to the shell;

[0010] A fluidizing gas outlet pipe, which passes through the upper head and is connected with the shell;

[0011] A fluidizing gas inlet pipe, which passes through the lower head and communicates with the shell;

[0012] A reaction raw material feed port, which passes through the upper portion of the shell;

[0013] A reaction raw material discharge port, which passes through the lower part of the shell;

[0014] A fixed bed reactor, which is respectively connected to the reaction raw material feed port and the reaction raw material discharge port;

[0015] A hot working medium particle feeding pipe, connected to the shell;

[0016] A hot working medium particle discharge pipe, which is in communication with the shell and is located on the side of the hot working medium particle feed pipe;

[0017] The reaction raw materials enter the fixed bed reactor through the reaction raw material feed port, contact the catalyst in the fixed bed reactor, and react under the heating effect of the hot working fluid particles entering the shell through the hot working fluid particle feed pipe.

[0018] The shell and tube heat exchange reaction device as described above, wherein, further comprises a reaction raw material distributor, and the fixed bed reactor is connected with the reaction raw material feed port via the reaction raw material distributor.

[0019] The shell and tube heat exchange reaction device as described above, wherein, further comprises a reaction product collecting pipe, and the fixed bed reactor is connected with the reaction product discharge port via the reaction product collecting pipe.

[0020] In the shell and tube heat exchange reaction device as described above, the shell is in the shape of a cylinder with a diameter of D and a length of L, and its aspect ratio L / D ranges from 1 to 20.

[0021] The shell and tube heat exchange reaction device as described above, wherein the upper head is an elliptical head with a straight edge segment, with a diameter of D1, a total height of L1, and an aspect ratio L1 / D1 in the range of 1 to 10; and / or

[0022] The lower head is an elliptical head with a straight side segment, with a diameter of D2, a total height of L2, and an aspect ratio L2 / D2 in the range of 1-10.

[0023] The shell and tube heat exchange reaction device as described above, wherein the fixed bed reactor includes a plurality of shell and tube reactors arranged along the axial direction, the shell and tube reactor is in the shape of a cylinder, with a diameter of d and a length of l, and is filled with a catalyst, the filling amount of which accounts for 10% to 95% of the volume of the shell and tube reactor; the aspect ratio l / d ranges from 2 to 50, and the ratio l / D of the length l of the shell and tube reactor to the diameter of the shell ranges from 1 to 35.

[0024] As described above, in the shell and tube heat exchange reaction device, the connection points of the hot working fluid particle feed pipe and the hot working fluid particle discharge pipe with the shell are at the same height or at different heights, and the connection points of the hot working fluid particle feed pipe and the hot working fluid particle discharge pipe with the shell are located at 1 / 5 to 4 / 5 of the height of the fixed bed reactor.

[0025] The shell and tube heat exchange reaction device as described above, wherein the hot working medium particles entering the shell through the hot working medium particle feed pipe are Geldart-A or Geldart-B particles, and their density is 1500-5000 kg / m 3 , particle size is 50 to 300 μm, and the filling height is 1 / 5 to 4 / 5 of the height of the fixed bed reactor.

[0026] The shell and tube heat exchange reaction device as described above, wherein the tube-in-tube reactor is fixed in the shell by a fixing bracket.

[0027] According to another aspect of the present application, the present disclosure also provides a reaction method, wherein the reaction is carried out using the shell and tube heat exchange reaction device as described above.

[0028] The inventors have found that there have been reports on particle-type solar collectors and heat storage systems, but their applications are limited to the use of steam generation, etc. There have been no reports on chemical reactors using particles for energy supply.

[0029] The shell and tube heat exchange reactor proposed in the present invention, which is heated by a fluidized bed, can be connected to a particle heat storage system, and use the sensible heat of the hot working fluid particles to provide energy for the thermochemical reaction hydrogen production process, as well as all other endothermic processes such as chemical reactions and phase changes carried out in the shell-and-tube reactor, to achieve clean and low-carbon production.

[0030] Other features and advantages of the present application will be described in detail in the subsequent detailed description. BRIEF DESCRIPTION OF THE DRAWINGS

[0031] The accompanying drawings constituting a part of the present application are used to provide a further understanding of the present application, and the schematic implementation modes and descriptions of the present application are used to explain the present application. In the accompanying drawings:

[0032] Figure 1This is a schematic structural diagram of the shell and tube heat exchange reaction device provided in this application.

[0033] Description of reference numerals:

[0034] 1- Upper head;

[0035] 2- Shell;

[0036] 3-Lower head;

[0037] 4-hot working medium particle feeding pipe;

[0038] 5-hot working medium particle discharge pipe;

[0039] 6- Gas distributor;

[0040] 7- Fluidizing gas outlet pipe;

[0041] 8-reaction raw material feeding port;

[0042] 9-reaction raw material distributor;

[0043] 10-tube fixed bed reactor;

[0044] 11-reaction product collection tube;

[0045] 12-reaction product discharge port;

[0046] 13-Pipeline fixing bracket. DETAILED DESCRIPTION

[0047] It should be noted that, in the absence of conflict, the embodiments of the present application and the features in each embodiment may be combined with each other.

[0048] The present application will be described in detail below with reference to the accompanying drawings and in combination with implementation modes.

[0049] The present application provides a shell and tube heat exchange reaction device, wherein the shell and tube heat exchange reaction device comprises:

[0050] Upper head 1;

[0051] Shell 2, which is located at the lower part of the upper head and connected to the upper head;

[0052] A lower head 3, which is located at the lower part of the shell and connected to the shell;

[0053] A fluidizing gas outlet pipe 7, which passes through the upper head 1 and communicates with the shell 2;

[0054] A fluidizing gas inlet pipe (i.e., an opening of the gas distributor 6), which passes through the lower head 3 and communicates with the shell 2;

[0055] A reaction raw material feed port 8, which passes through the upper portion of the housing 2;

[0056] a reaction product discharge port 12 passing through the lower portion of the housing 2;

[0057] A fixed bed reactor (including a tube-in-tube fixed bed reactor 10), which is respectively connected to the feed port and the discharge port;

[0058] A hot working medium particle feeding pipe 4 is connected to the shell 2;

[0059] A hot working medium particle discharge pipe 5, which is connected to the shell 2 and is located at the side of the feed pipe;

[0060] The reaction raw materials enter the fixed bed reactor through the reaction raw material feed port, contact the catalyst in the fixed bed reactor, and react under the heating effect of the hot working fluid particles entering the shell through the hot working fluid particle feed pipe.

[0061] Specifically, the present invention proposes a shell and tube heat exchange reaction device using a fluidized bed for heating, such as Figure 1 As shown, it is composed of an upper end cap 1, a shell 2, a lower end cap 3, a hot working medium particle feed pipe 4, a hot working medium particle discharge pipe 5, a gas distributor 6, a fluidizing gas outlet pipe 7, a reaction raw material feed port 8, a reaction raw material distributor 9, a tube-in-tube fixed bed reactor 10, a reaction product collection pipe 11, a reaction product discharge port 12, and a tube pass fixed bracket 13. Its external body is composed of an upper end cap 1, a shell 2, and a lower end cap 3; the space between the upper end cap 1, the shell 2, the lower end cap 3, the gas distributor 6, and the tube-in-tube fixed bed reactor 10 constitutes a shell pass; the reaction raw material feed port 8, the reaction raw material distributor 9, the tube-in-tube fixed bed reactor 10, the reaction product collection pipe 11, and the reaction product discharge port 12 constitute a tube pass.

[0062] When the device is in operation, the reactor is placed vertically, and the high-temperature hot working fluid particles continuously enter the shell side through the hot working fluid particle feed pipe 4; the fluidizing gas is usually air, but it can also be nitrogen or water vapor, which enters the shell side from the bottom area of ​​the heat exchange reactor and is evenly distributed under the action of the gas distributor 6. The hot working fluid particles in the shell side become a bubbling fluidized bed under the action of the fluidizing gas, and its heat transfer performance is greatly improved, and continuous feeding and discharging can be achieved under the action of gravity. The fluidized bed has excellent mixing and heat transfer performance. After entering the shell side, the high-temperature hot working fluid particles quickly release heat, and the temperature is consistent with the fluidized bed as a whole. After releasing the heat, the hot working fluid particles flow out of the shell side from the hot working fluid particle discharge pipe 5, and the fluidizing gas flows out from the fluidizing gas outlet pipe 7 at the top. After the shell side operation state is stable, the flow rate of hot working fluid particles entering the shell side is equal to the flow rate of hot working fluid particles flowing out of the shell side.

[0063] In a specific embodiment, the device is placed vertically during operation, high-temperature hot working medium particles enter the shell side through the hot working medium particle feed pipe 4 and flow out of the shell side from the hot working medium particle discharge pipe 5, and the fluidizing gas enters the shell side through the gas distributor 6 and flows out of the shell side from the fluidizing gas outlet pipe 7; the hot working medium particles in the shell side become a bubbling fluidized bed under the action of the fluidizing gas, the heat transfer performance is improved, and continuous feeding and discharging under the action of gravity provide continuous and stable heat supply; the hot working medium of the device is high-temperature particles, which are Geldart-A or B particles, and their absolute density is 1500-5000kg / m 3 , particle size 50-300 μm, filling height 1 / 5-4 / 5 of the overall height of the reactor; the velocity of the fluidizing gas is 2-15 times the minimum fluidizing gas velocity of the hot working medium particles; the minimum fluidizing gas velocity of the hot working medium particles is 0.1-5 cm / s.

[0064] In a specific embodiment, the reaction carried out in the tube side is an endothermic gas-gas, gas-liquid, or liquid-liquid chemical reaction; the reaction material enters the tube side from the reaction raw material feed port 8, is dispersed into each tubular fixed bed reactor 10 through the reaction raw material distributor 9, exchanges heat with the shell side partition wall and reacts, and the reaction product flows out of the tube side from the reaction product discharge port 12 through the reaction product collecting pipe 11; the tube side is fixed in the shell 2 by a fixed bracket 13.

[0065] In a specific embodiment, the shell 2 is in the shape of a cylinder with a diameter of D and a length of L, and its aspect ratio L / D ranges from 1 to 20; a hot working fluid particle feed pipe 4 and a hot working fluid particle discharge pipe 5 are respectively opened on its two sides; and 2 to 5 fixed brackets 13 are welded on its inner wall.

[0066] In a specific embodiment, the upper head 1 is an elliptical head with a straight edge segment, with a diameter of D1, a total height of L1, and an aspect ratio of L1 / D1 in the range of 1 to 10. A fluidizing gas outlet pipe 7 is provided on the top, and the bottom is connected to the shell 2; the lower head 3 is an elliptical head with a straight edge segment, with a diameter of D2, a total height of L2, and an aspect ratio of L2 / D2 in the range of 1 to 10. The top is connected to the shell 2, and a gas distributor 6 is provided on the side. The distance from the tube center of the gas distributor 6 to the bottom of the lower head 3 is L3, and L3 / D is in the range of 0.1 to 5.

[0067] In a specific embodiment, the shell-and-tube fixed bed reactor 2 is in the shape of a cylinder with a diameter of d and a length of l; the interior is filled with catalyst, and the filling amount accounts for 10% to 95% of the tube volume; its aspect ratio l / d ranges from 2 to 50, and its length to shell 2 diameter l / D ranges from 1 to 35.

[0068] In a specific embodiment, the connection points between the hot working fluid particle feed pipe 4 and the hot working fluid particle discharge pipe 5 and the shell can be at the same height or at different heights; the connection points between the hot working fluid particle feed pipe 4 and the hot working fluid particle discharge pipe 5 and the shell are located at 1 / 5 to 4 / 5 of the overall height of the reactor.

[0069] In a specific embodiment, the reaction raw material feed port 8 can be located at the upper head 1 or at the shell 2 ; the reaction product discharge port 12 can be located at the shell 2 or at the lower head 3 .

[0070] After the shell side is stable, the liquid or gaseous reactants are introduced into the tube side from the reaction raw material feed port 8, and dispersed into each tubular fixed bed reactor 10 through the reaction raw material distributor 9 for reaction, and the reaction products flow out of the tube side from the reaction product discharge port 12 through the reaction product collecting pipe 11. Each part of the tube side is fixed by flange or welding, and then fixed in the shell 2 by the fixing bracket 13.

[0071] During operation, the materials in the shell side and the tube side are not in direct contact, and heat is transferred from the high-temperature material to the low-temperature material through the heat exchange between the partition walls. If the parameters of the hot working medium and the reaction system input into the heat exchange reactor remain unchanged, that is, the hot working medium high-temperature particle feed amount, feed temperature, fluidizing gas feed amount, fluidizing gas feed temperature, reactant feed amount, and reactant feed temperature remain unchanged, the equipment will be stable after running for a period of time, that is, all operating parameters of the heat exchange reaction device will remain basically stable.

[0072] A reaction method uses the shell and tube heat exchange reaction device as described above to carry out the reaction, and the shell and tube heat exchange reaction device will not be described in detail here.

[0073] For example, in a specific embodiment, the device is placed vertically during operation, high-temperature hot working medium particles enter the shell side through the hot working medium particle feed pipe 4 and flow out of the shell side from the hot working medium particle discharge pipe 5, and the fluidizing gas enters the shell side through the gas distributor 6 and flows out of the shell side from the fluidizing gas outlet pipe 7; the hot working medium particles in the shell side become a bubbling fluidized bed under the action of the fluidizing gas, the heat transfer performance is improved, and continuous feeding and discharging under the action of gravity provide continuous and stable heat supply; the hot working medium of the device is high-temperature particles, which are Geldart-A or B particles, and have an absolute density of 1500-5000 kg / m 3 , particle size is 50 to 300 μm, and the filling height is 1 / 5 to 4 / 5 of the overall height of the reactor; the gas velocity of the fluidizing gas is 2 to 15 times the minimum fluidizing gas velocity of the hot working medium particles.

[0074] In the present invention, the minimum fluidizing gas velocity of the hot working medium particles is 0.1-5 cm / s.

[0075] The present invention provides a shell and tube heat exchange reaction device which uses a fluidized bed to provide heat for an endothermic reaction. In the shell side, high-temperature particles of a hot working medium are fluidized to provide heat for the reaction, and flow under the action of gravity to achieve continuous feeding and discharging. The tube side is a fixed bed reactor, and the reactants obtain the heat required for the reaction from the shell side through wall heat exchange.

[0076] Compared with the traditional shell and tube heat exchange reactor, the hot working medium used in the shell side of the present invention is fluidized hot particles, rather than traditional liquid or gas phase fluids. Through this device, it can be connected with a particle-type solar thermal collection-storage system to achieve efficient use of the sensible heat of hot particles. This device can be used for all heat-absorbing gas-gas, gas-liquid, and liquid-liquid chemical reactions, such as methanol-steam catalytic reforming hydrogen production, ethanol-steam catalytic reforming hydrogen production, methane dry reforming hydrogen production, etc.

[0077] III. Examples

[0078] The present invention is described in detail below through specific examples. The experimental methods described below, unless otherwise specified, are all routine laboratory methods. The experimental materials described below, unless otherwise specified, can all be obtained from commercial channels.

[0079] Example 1: Methanol-water hydrogen production using a shell-and-tube heat exchange reaction device with fluidized bed heating

[0080] Methanol and aqueous solution are used as reactants, which exchange heat with high-temperature hot working fluid particles in the shell side in a fixed bed reactor, and are fully contacted and mixed with the catalyst in the fixed bed reactor to produce methanol-water reforming hydrogen to produce hydrogen and by-product carbon dioxide. When the reaction device is running, the 400°C hot working medium particles preferably continuously enter the shell side through the feed pipe 4 at a flow rate of 20-50kg / h, the hot air of the fluidizing gas 200°C enters the shell side from the bottom area of ​​the heat exchange reactor through the gas distributor 6 at a flow rate of 100L / min (gas velocity 8cm / s), and is evenly distributed, the reactant 20°C methanol-water solution is passed into the tube side from the feed port 8 at a flow rate of 10g / min, and is dispersed to each tubular fixed bed reactor 10 through the reaction raw material distributor 9, mixed, contacted, and gasified with the catalyst in the tubular fixed bed reactor, and a methanol-water vapor catalytic reforming reaction is carried out. After running for a certain period of time, preferably 1-3 hours, the device stably generates at a yield of 70-95%, and the hot working medium particles flow out stably from the discharge pipe 5, the particle flow rate is stable at 25kg / h, and the shell side temperature, reactant conversion rate, hydrogen yield, reaction product outflow temperature, and fluidizing gas outflow temperature no longer change, and remain stable until the equipment stops running.

[0081] Example 2: Using a shell-and-tube heat exchange reaction device with fluidized bed heating to produce hydrogen from ethanol-water

[0082] Ethanol and aqueous solution are used as reactants, which exchange heat with high-temperature hot working fluid particles in the shell side in a fixed bed reactor, and are fully contacted and mixed with the catalyst in the fixed bed reactor to cause an ethanol-water reforming hydrogen production reaction to produce hydrogen and by-product carbon dioxide. When the reaction device is running, the 600°C hot working medium particles preferably continuously enter the shell side through the feed pipe 4 at a flow rate of 100kg / h, the hot air of the fluidizing gas 400°C enters the shell side from the bottom area of ​​the heat exchange reactor through the gas distributor 6 at a flow rate of 200L / min (gas velocity 16cm / s), and is evenly distributed. The reactant 20°C ethanol-water solution is passed into the tube side from the feed port 8 at a flow rate of 20g / min, and is dispersed to each tubular fixed bed reactor 10 through the reaction raw material distributor 9, mixed, contacted, and gasified with the catalyst in the tubular fixed bed reactor, and an ethanol-water vapor catalytic reforming reaction is carried out. After running for a certain period of time, preferably 1-3 hours, the device stably generates at a yield of 70-90%, and the hot working medium particles flow out stably from the discharge pipe 5, the particle flow rate is stable at 25kg / h, and the shell side temperature, reactant conversion rate, hydrogen yield, reaction product outflow temperature, and fluidizing gas outflow temperature no longer change, and remain stable until the equipment stops running.

[0083] Laboratory research and industrial implementation cases show that the shell-and-tube heat exchange reactor with fluidized bed heating proposed in the present invention can be used as an efficient and stable chemical reaction device to achieve high-value utilization of hot particle sensible heat, and further broaden the high-value application path of particle-type solar thermal collection and storage systems. The device proposed in the present invention can be used for all endothermic gas-gas and gas-solid chemical reactions occurring in a tubular reactor, and is particularly suitable for thermochemical hydrogen production reactions such as methanol-steam catalytic reforming hydrogen production, ethanol-steam catalytic reforming hydrogen production, and methane dry reforming hydrogen production. For example, the device is used for endothermic gas-gas chemical reactions, that is, chemical reactions in which the reactants are one or more gases or volatile liquids and the catalyst is a fixed bed or fluidized bed. The device can also be used in the vaporization process of volatile liquids to provide energy for vaporization processes such as steam production.

[0084] The above description is only a preferred implementation mode of the present application and is not intended to limit the present application. Any modifications, equivalent substitutions, improvements, etc. made within the spirit and principles of the present application should be included in the protection scope of the present application.

Claims

1. A shell and tube heat exchange reaction device, characterized in that: The shell and tube heat exchange reaction device comprises: Upper head, A shell, which is located at the lower part of the upper head and connected to the upper head; A lower head, which is located at the lower part of the shell and connected to the shell; A fluidizing gas outlet pipe, which passes through the upper head and is connected with the shell; A fluidizing gas inlet pipe, which passes through the lower head and communicates with the shell; A reaction raw material feed port, which passes through the upper portion of the shell; a reaction product discharge port passing through the lower portion of the shell; A fixed bed reactor, which is respectively connected to the reaction raw material feed port and the reaction product discharge port; A hot working medium particle feeding pipe, connected to the shell; A hot working medium particle discharge pipe, which is connected to the shell and is located on the side of the hot working medium particle feed pipe; The reaction raw materials enter the fixed bed reactor through the reaction raw material feed port, contact the catalyst in the fixed bed reactor, and react under the heating effect of the hot working fluid particles entering the shell through the hot working fluid particle feed pipe.

2. The shell and tube heat exchange reaction device according to claim 1, characterized in that: It also includes a reaction raw material distributor, and the fixed bed reactor is connected with the reaction raw material feed port through the reaction raw material distributor.

3. The shell and tube heat exchange reaction device according to claim 2, characterized in that: It also includes a reaction product collecting pipe, and the fixed bed reactor is connected with the reaction product discharge port through the reaction product collecting pipe.

4. The shell and tube heat exchange reaction device according to claim 1, characterized in that: The shell is in the shape of a cylinder, with a diameter of D and a length of L, and an aspect ratio L / D ranging from 1 to 20.

5. The shell and tube heat exchange reaction device according to claim 1, characterized in that: The upper head is an elliptical head with a straight side segment, with a diameter of D1, a total height of L1, and an aspect ratio L1 / D1 in the range of 1 to 10; and / or The lower head is an elliptical head with a straight side segment, with a diameter of D2, a total height of L2, and an aspect ratio L2 / D2 in the range of 1-10.

6. The shell and tube heat exchange reaction device according to claim 1, characterized in that: The fixed bed reactor comprises a plurality of tubular reactors arranged along the axial direction, wherein the tubular reactor is in the shape of a cylinder with a diameter of d and a length of l, and is filled with a catalyst, the filling amount of which accounts for 10% to 95% of the volume of the tubular reactor; the aspect ratio l / d ranges from 2 to 50, and the ratio l / D of the length l of the tubular reactor to the diameter of the shell ranges from 1 to 35.

7. The shell and tube heat exchange reaction device according to claim 1, characterized in that: The connection points of the hot working fluid particle feed pipe and the hot working fluid particle discharge pipe with the shell are at the same height or at different heights. The connection points of the hot working fluid particle feed pipe and the hot working fluid particle discharge pipe with the shell are located at 1 / 5 to 4 / 5 of the height of the fixed bed reactor.

8. The shell and tube heat exchange reaction device according to claim 1, characterized in that: The hot working medium particles entering the shell through the hot working medium particle feeding pipe are Geldart-A or Geldart-B particles, and their density is 1500-5000 kg / m 3 , particle size is 50 to 300 μm, and the filling height is 1 / 5 to 4 / 5 of the height of the fixed bed reactor.

9. The shell and tube heat exchange reaction device according to any one of claims 1 to 8, characterized in that: The shell-and-tube reactor is fixed in the shell by a fixing bracket.

10. A reaction method, characterized in that: The reaction is carried out using the shell and tube heat exchange reaction device according to any one of claims 1 to 9.

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