A fluidized bed based trimethoxysilane continuous production system

Abstract

The utility model discloses a continuous production system of trimethoxysilane based on fluidized bed relates to trimethoxysilane production system technical field, including fluidized bed reactor, and the catalyst feed port of fluidized bed reactor is connected with continuous feeding unit, and continuous feeding unit is used for passing into the reaction catalytic material in fluidized bed reactor, and the reactant feed port of fluidized bed reactor is connected with reactant conveying unit, and reactant conveying unit is used for conveying reactant to fluidized bed reactor, and the discharge port of fluidized bed reactor is linked with the feed port of gas -solid separator, and the solid export of gas -solid separator is connected with catalyst regeneration unit, and catalyst is conveyed to continuous feeding unit after passing through catalyst regeneration unit and is used again, and the gas export of gas -solid separator is connected with product collection unit, and fluidized bed reactor and reactant conveying unit all are electrically connected with control unit. The utility model can realize the continuous production of trimethoxysilane and the regeneration utilization of catalyst.

Description

Technical Field

[0001] This utility model relates to the technical field of trimethoxysilane production systems, and in particular to a continuous trimethoxysilane production system based on a fluidized bed. Background Technology

[0002] Trimethoxysilane (HSi(OCH3)3) is a key intermediate in the synthesis of high-purity silanes and specialty silane coupling agents, playing an irreplaceable role in photovoltaic encapsulation materials, specialty coatings, and cable insulation materials. Currently, industrial production mainly relies on the following two technological routes:

[0003] (1) Liquid-phase esterification method: HSiCl3 and CH3OH are used as raw materials and reacted in batches in a reactor. This method requires precise control of the molar ratio (1:1-1.05:1), but the accuracy of manual adjustment is low, there are many by-products, the yield is only 50%, and the reaction produces a large amount of HCl that corrodes the equipment.

[0004] (2) Direct method: Using Si and CH3OH as raw materials and phenyl silicone oil as solvent, the reaction is carried out directly in a reactor under the action of Cu-based catalyst. Although corrosion problems are avoided, the reactor needs to be shut down and the raw materials replaced every 12 days (one reaction cycle).

[0005] In summary, the current industrial preparation of trimethoxysilane mainly adopts a batch reactor process, which has significant drawbacks: First, production is discontinuous: each batch requires stopping the reactor for feeding / unloading, resulting in low production efficiency; second, catalyst regeneration is difficult: deactivated catalysts must be removed from the reactor for regeneration, which is cumbersome, time-consuming, and costly. Utility Model Content

[0006] The purpose of this invention is to provide a fluidized bed-based continuous production system for trimethoxysilane to solve the problems existing in the prior art, thereby enabling continuous production of trimethoxysilane and regeneration of the blowing agent.

[0007] To achieve the above objectives, this utility model provides the following solution:

[0008] This utility model discloses a continuous production system for trimethoxysilane based on a fluidized bed reactor, comprising a fluidized bed reactor, wherein the catalyst inlet of the fluidized bed reactor is connected to a continuous feed unit for introducing reactive catalyst material into the fluidized bed reactor, the reactant inlet of the fluidized bed reactor is connected to a reactant conveying unit for conveying reactants into the fluidized bed reactor, the outlet of the fluidized bed reactor is connected to the inlet of a gas-solid separator, the solid outlet of the gas-solid separator is connected to a catalyst regeneration unit, the catalyst separated from the gas-solid separator is conveyed to the continuous feed unit for reuse after passing through the catalyst regeneration unit, the gas outlet of the gas-solid separator is connected to a product collection unit for collecting products, and both the fluidized bed reactor and the reactant conveying unit are electrically connected to a control unit.

[0009] Preferably, the fluidized bed reactor includes a fluidized bed body and a tubular furnace body, wherein the fluidized bed body is disposed inside the tubular furnace body, and the tubular furnace body is used to heat the fluidized bed body.

[0010] Preferably, the reactant inlet of the fluidized bed reactor is located at the bottom of the fluidized bed body, and the interior of the fluidized bed body is provided with a perforated plate, which is located above the reactant inlet of the fluidized bed reactor.

[0011] Preferably, the outlet of the fluidized bed reactor is located at the top of the fluidized bed body, and at least one air outlet baffle is fixed inside the fluidized bed body, and the air outlet baffle is inclined.

[0012] Preferably, the porous plate is a porous ceramic plate, and the inner wall of the fluidized bed body is provided with a ceramic layer.

[0013] Preferably, the continuous feeding unit includes a catalyst storage tank, a silicon powder storage tank, and a mixing silo. The outlets of the catalyst storage tank and the silicon powder storage tank are both connected to the inlet of the mixing silo, and the outlet of the mixing silo is connected to the catalyst inlet of the fluidized bed reactor.

[0014] Preferably, the reactant delivery unit includes a reactant storage tank, which is connected to the reactant inlet of the fluidized bed reactor via a reactant feed pipe, and a metering pump is provided on the reactant feed pipe.

[0015] Preferably, the gas-solid separator is a cyclone separator.

[0016] Preferably, the catalyst regeneration unit includes a microwave processor, which is connected to a nitrogen tank via a nitrogen delivery pipe, and the nitrogen tank is capable of filling the microwave processor with nitrogen.

[0017] Preferably, the product collection unit includes a distillation column, the feed inlet of which is connected to the gas outlet of the gas-solid separator via a product collection pipeline, and a condenser is provided on the product collection pipeline.

[0018] The present invention achieves the following technical advantages over the prior art:

[0019] This invention features a continuous feeding unit and a reactant conveying unit, enabling the continuous delivery of reaction materials to the fluidized bed reactor. This ensures the continuous production of trimethoxysilane, increases production capacity, eliminates batch-to-batch downtime, and improves equipment utilization. Furthermore, this invention includes a catalyst regeneration unit, which regenerates the catalyst exiting the fluidized bed reactor, thus enabling catalyst reuse. Attached Figure Description

[0020] To more clearly illustrate the technical solutions in the embodiments of this utility model or the prior art, the drawings used in the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of this utility model. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0021] Figure 1 This is a schematic diagram of the structure of a fluidized bed-based continuous production system for trimethoxysilane according to an embodiment of this utility model;

[0022] In the diagram: 1-Fluidized bed reactor; 101-Fluidized bed body; 102-Tube furnace body; 103-Perforated plate; 104-Outlet baffle; 2-Continuous feed unit; 201-Catalyst storage tank; 202-Silicon powder storage tank; 203-Mixing bin; 3-Gas-solid separator; 4-Catalyst regeneration unit; 401-Microwave processor; 402-Nitrogen tank; 5-Product collection unit; 501-Distillation column; 502-Condenser; 6-Reactant conveying unit; 601-Reactant storage tank; 602-Metering pump; 7-Control unit. Detailed Implementation

[0023] The technical solutions of the present utility model will be clearly and completely described below with reference to the accompanying drawings of the embodiments. Obviously, the described embodiments are only some embodiments of the present utility model, and not all embodiments. Based on the embodiments of the present utility model, all other embodiments obtained by those of ordinary skill in the art without creative effort are within the protection scope of the present utility model.

[0024] The purpose of this invention is to provide a fluidized bed-based continuous production system for trimethoxysilane to solve the problems existing in the prior art, thereby enabling continuous production of trimethoxysilane and regeneration of the blowing agent.

[0025] To make the above-mentioned objectives, features and advantages of this utility model more apparent and understandable, the utility model will be further described in detail below with reference to the accompanying drawings and specific embodiments.

[0026] Example 1

[0027] like Figure 1 As shown, this embodiment provides a fluidized bed-based continuous production system for trimethoxysilane, including a fluidized bed reactor 1. The catalyst inlet of the fluidized bed reactor 1 is connected to a continuous feed unit 2 via a pipeline, which introduces the reaction catalyst into the fluidized bed reactor 1. The reactant inlet of the fluidized bed reactor 1 is connected to a reactant conveying unit 6 via a pipeline, which conveys the reactants into the fluidized bed reactor 1. The outlet of the fluidized bed reactor 1 is connected to the inlet of a gas-solid separator 3 via a pipeline. The solid outlet of the gas-solid separator 3 is connected to a catalyst regeneration unit 4. The catalyst separated from the gas-solid separator 3 is manually conveyed to the continuous feed unit 2 for reuse after passing through the catalyst regeneration unit 4. The gas outlet of the gas-solid separator 3 is connected to a product collection unit 5 via a pipeline, which collects the product. Both the fluidized bed reactor 1 and the reactant conveying unit 6 are electrically connected to a control unit 7, which controls the operation of the relevant components.

[0028] In practical use, reactants are fed into the fluidized bed reactor 1 via the continuous feed unit 2. Simultaneously, the continuous feed unit 2 also feeds the catalyst materials required for the reaction process into the fluidized bed reactor 1, thus achieving continuous reaction. The gaseous product exiting the fluidized bed reactor 1 contains some catalyst particles, so it first enters the gas-solid separator 3. The separated solids (i.e., catalyst) enter the catalyst regeneration unit 4 to regenerate the catalyst. Then, workers use trolleys or other conveying devices to transport it back to the continuous feed unit 2 for reuse. The gas separated from the gas-solid separator 3 is collected by the product collection unit 5, packaged in corresponding containers, and then transported away.

[0029] In this embodiment, the fluidized bed reaction gas is an existing fluidized bed tubular furnace. Specifically, the fluidized bed reactor 1 includes a fluidized bed body 101 and a tubular furnace body 102. The fluidized bed body 101 is disposed inside the tubular furnace body 102, and the tubular furnace body 102 is used to heat the fluidized bed body 101, thereby providing the heat required for the reaction.

[0030] The fluidized bed body 101 is a common cylindrical tank structure with a height-to-inner diameter ratio of 5:1. This relatively large height-to-diameter ratio makes it closer to a "tall and narrow" fluidized bed. This is beneficial for establishing a more stable axial concentration and temperature gradient, and is more conducive to series reactions. Of course, those skilled in the art can adjust the specific dimensions and materials of the fluidized bed body 101 according to actual needs, and no further restrictions are imposed. The tubular furnace body 102 is electrically connected to the control unit 7, which can control the switching and temperature of the tubular furnace body 102. In addition, in order to monitor the internal temperature of the fluidized bed body 101 in real time, a temperature sensor can be installed inside the fluidized bed body 101, and the temperature sensor is electrically connected to the control unit 7. The control unit 7 adjusts the temperature of the tubular furnace body 102 based on the temperature parameters detected by the temperature sensor.

[0031] In this embodiment, the reactant inlet of the fluidized bed reactor 1 is located at the bottom of the fluidized bed body 101. A porous plate 103 is provided inside the fluidized bed body 101, with porous vent holes of 100 μm in diameter. The porous plate 103 is positioned above the reactant inlet of the fluidized bed reactor 1. The porous plate 103 serves two purposes: first, it allows reactants to pass through from bottom to top, ensuring uniform distribution of the gaseous reactants as they pass through, thus facilitating full contact between the reactants and the catalyst material and improving reaction efficiency; second, the vent diameter of the porous plate 103 is smaller than the diameter of the catalyst material, thus providing support for the catalyst material above it.

[0032] In this embodiment, the outlet of the fluidized bed reactor 1 is located at the top of the fluidized bed body 101, and at least one gas outlet baffle 104 is fixed inside the fluidized bed body 101. The gas outlet baffle 104 has an annular structure and is inclined. Specifically, the angle between the gas outlet baffle 104 and the horizontal direction is 40°, which is between vertical (90°) and horizontal (0°). This effectively breaks up rising bubbles and guides solid particles to move downward or outward along the inclined plane, forming an internal circulation and significantly extending the contact time / path between particles and the gas phase. When the gas inside the fluidized bed body 101 flows from bottom to top, it is blocked when it encounters the gas outlet baffle 104, thereby increasing the residence time of the reactant gas in the fluidized bed body 101, allowing it to react fully inside the fluidized bed body 101 and improving the reaction efficiency.

[0033] The specific number of exhaust baffles 104 can be one, two, or more. When two or more exhaust baffles 104 are provided, they are arranged parallel to each other. The multi-layer design can form multiple "disturbance-mixing-extended path" regions in the height direction of the fluidized bed body 101, optimizing the flow field of the entire bed.

[0034] In this embodiment, the porous plate 103 is a porous ceramic plate, and the inner wall of the fluidized bed body 101 is provided with a ceramic layer as an inner lining. The reason for providing a ceramic layer is that the reaction catalyst material in this embodiment includes silicon powder. Silicon powder has high hardness, and when the gaseous reactants blow away the silicon powder, the silicon powder may cause wear on the inner wall of the fluidized bed body 101. Therefore, a ceramic layer is provided as an inner lining to improve the wear resistance of the fluidized bed body 101.

[0035] In this embodiment, the continuous feeding unit 2 includes a catalyst storage tank 201, a silicon powder storage tank 202, and a mixing bin 203. The catalyst storage tank 201 contains a catalyst, and the catalyst used in different reactions varies, so the type of catalyst is not limited here. The silicon powder storage tank 202 contains silicon powder, which has been pre-treated by ball milling to a particle size of 100-150 μm. The outlets of both the catalyst storage tank 201 and the silicon powder storage tank 202 are connected to the inlet of the mixing bin 203 via pipelines. The catalyst in the catalyst storage tank 201 and the silicon powder in the silicon powder storage tank 202 are both transported to the mixing bin 203 via pipelines. The outlet of the mixing bin 203 is connected to the catalyst inlet of the fluidized bed reactor 1 via a pipeline. That is, the reaction catalyst material supplied by the continuous feeding unit 2 to the fluidized bed reactor 1 is a mixture of catalyst and silicon powder.

[0036] In this embodiment, the reactant delivery unit 6 includes a reactant storage tank 601, which contains liquid methanol. The reactant storage tank 601 is connected to the reactant inlet of the fluidized bed reactor 1 via a reactant feed pipe. That is, the reactant storage tank 601 can deliver methanol to the fluidized bed reactor 1 through the reactant feed pipe. It should be noted that because the fluidized bed reactor 1 itself has a high temperature, when the liquid methanol is delivered to the vicinity of the fluidized bed body 101 (before it enters the fluidized bed), the liquid methanol will vaporize. Therefore, the reactant delivered to the fluidized bed body 101 is gaseous methanol. A metering pump 602 is installed on the reactant feed pipe, and the metering pump 602 is electrically connected to the control module to achieve quantitative delivery of methanol.

[0037] It should be noted that simply introducing methanol gas into the fluidized bed body 101 can also fluidize the material inside the fluidized bed body 101. However, relying solely on methanol gas to fluidize the packing material inside the fluidized bed body 101 requires a large amount of methanol gas, resulting in high costs. To reduce costs, nitrogen gas can also be introduced into the fluidized bed body 101. Specifically, the fluidized bed body 101 is connected to a carrier gas cylinder filled with nitrogen gas via a carrier gas delivery pipe. When the carrier gas from the carrier gas cylinder is introduced into the fluidized bed body 101, it can agitate the material inside the fluidized bed body 101, causing it to fluidize.

[0038] In this embodiment, the gas-solid separator 3 is a conventional cyclone separator. The products flowing out of the fluidized bed reactor 1 include trimethoxysilane, tetramethoxysilane, and some catalyst solid particles. In order to purify the final product, it is necessary to remove the catalyst from the mixture. Therefore, a cyclone separator is provided to remove the catalyst from the trimethoxysilane mixture.

[0039] In this embodiment, the catalyst regeneration unit 4 includes a microwave processor 401, which is a common existing device in industry or laboratories. The microwave processor 401 effectively removes carbon deposits on the catalyst surface through 2.45 GHz microwave irradiation, thereby achieving catalyst regeneration. Furthermore, a nitrogen delivery pipe is connected to the microwave processor 401, and a nitrogen tank 402 is connected to the microwave processor 401 via the nitrogen delivery pipe. The nitrogen tank 402 can fill the microwave processor 401 with nitrogen. The end of the nitrogen delivery pipe located inside the microwave processor can have a porous structure, or multiple nozzles can be installed to allow for multi-point nitrogen filling. The purpose of introducing nitrogen into the microwave processor 401 is to purge the desorption byproducts (i.e., carbon deposits on the catalyst surface), ensuring the effective regeneration of the catalyst.

[0040] In this embodiment, the product collection unit 5 includes a distillation column 501. The feed inlet of the distillation column 501 is connected to the gas outlet of the gas-solid separator 3 via a product collection pipeline. A condenser 502 is provided on the product collection pipeline. The condenser 502 is used to condense the gaseous product fed to the distillation column 501. The condenser 502 can be an existing tubular heat exchanger, or it can be a condenser tube that is serpentinely wound around the product collection pipeline. The gas in the product collection pipeline can be condensed by passing cold water through the condenser tube.

[0041] The gas products from the gas outlet of gas-solid separator 3 include trimethoxysilane and impurity gases such as tetramethoxysilane. When the mixed gas enters distillation column 501, the fractionated products will vary depending on the height and temperature of the column. High-boiling-point substances (i.e., siloxane polymers) in the mixed gas will flow from the bottom of distillation column 501 and can then be introduced into a neutralization tank for treatment. Since the high-boiling-point substances vary in different reactions, the specific type of neutralization solution in the neutralization tank is not limited here. Low-boiling-point substances (silanes, dimethoxyhydrosilanes, etc.) fractionated in the 80-84℃ range, along with the carrier gas (i.e., nitrogen transported from the carrier gas bottle to the fluidized bed body 101), will flow from the top of distillation column 501 and can then be transported to the catalyst inlet of fluidized bed reactor 1 for reaction. Trimethoxysilane will be distilled out in the 84-87℃ range, with a purity of up to 99%. It is then fed into the finished product tank, awaiting later packaging and transportation.

[0042] In this embodiment, the control unit 7 is an existing PID controller, and the control module can control the operation of electrical control components such as the tubular furnace body 102 and the metering pump 602.

[0043] Example 2

[0044] This embodiment provides a production process for a fluidized bed-based continuous production system of trimethoxysilane, based on the fluidized bed-based continuous production system of trimethoxysilane disclosed in Embodiment 1, including the following steps:

[0045] (1) Continuous feeding: Silicon powder (100-150μm) is mixed with catalyst (Cu2O / CuCl, 3wt%) and fed into the fluidized bed body 101; methanol is vaporized (200℃) and fed into the fluidized bed body 101 at a rate of 6L / h.

[0046] (2) Continuous reaction: The nitrogen flow rate is 30 mL / min (a flow valve is set on the carrier gas delivery pipeline to control the flow rate) to keep the bed in the fluidized bed body 101 in a fluidized state, the reaction temperature is 200℃±5℃; the gas baffle is tilted at 40° to enhance turbulence, and the reaction time is 30 minutes.

[0047] (3) Product processing: The gaseous product is condensed by condenser 502 and then enters distillation column 501. The fraction at 84-87℃ is collected as the product; the low-boiling part is returned to fluidized bed reactor 1 for re-reaction.

[0048] After continuous operation of this embodiment, the comparison data with the traditional reactor are as follows:

[0049] parameter Traditional reactor This utility model Single run cycle 8 hours (including downtime) 720 hours Catalyst replacement frequency Each batch (approximately 12 days) 30 days / time Catalyst cost per ton of product ￥2800 ￥1120

[0050] In addition, a regeneration process is initiated every 48 hours of operation: the reaction powder enters the gas-solid separator 3, the catalyst fine powder is separated and sent to the microwave processor 401; it is irradiated with 2.45 GHz microwave for 5 minutes, while nitrogen is purged (flow rate 10 L / min); the regenerated catalyst is returned to the fluidized bed reactor 1, with an activity recovery rate of >95%.

[0051] The fluidized bed-based continuous production system for trimethoxysilane disclosed in Example 1 and the production process of the fluidized bed-based continuous production system for trimethoxysilane disclosed in Example 2 have the following advantages compared to traditional reactors:

[0052] (1) Continuous production: Fluidized bed reactor 1 enables continuous feeding of raw materials and continuous output of products, thereby increasing production capacity; it also eliminates downtime between batches and improves equipment utilization.

[0053] (2) Reduced energy consumption: The reaction temperature is reduced to 180-200℃, resulting in reduced energy consumption.

[0054] (3) Advantages of catalyst regeneration: Microwave regeneration cycle ≤ 0.5 hours, while traditional bed dismantling and regeneration requires 24 hours; the single-use cycle of the catalyst is extended.

[0055] (4) Improved product purity: The online purification of the 501 distillation column increases the yield to 82% and the purity to ≥99%, while the traditional method yields 95% and the purity is ≤65%.

[0056] In the description of this utility model, it should be understood that the terms "longitudinal," "lateral," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," and "outer," etc., indicating orientation or positional relationships, are based on the orientation or positional relationships shown in the accompanying drawings and are only for the convenience of describing this utility model. They do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation, and therefore should not be construed as a limitation on this utility model. Furthermore, the terms "first," "second," and "third," etc., are used for descriptive purposes only and should not be construed as indicating or implying relative importance. Thus, features defined with "first," "second," etc., may explicitly or implicitly include one or more of that feature. In the description of this utility model, unless otherwise stated, "a plurality of" means two or more.

[0057] In the description of this utility model, unless otherwise explicitly specified and limited, the terms "installation," "connection," and "joining" should be interpreted broadly. For example, they can refer to fixed connections, detachable connections, or integral connections; they can refer to mechanical connections or electrical connections; they can refer to direct connections or indirect connections through an intermediate medium; and they can refer to the internal communication between two components. Those skilled in the art can understand the specific meaning of the above terms in this application based on the specific circumstances.

[0058] If this utility model discloses or relates to mutually fixedly connected parts or structural components, then, unless otherwise stated, a fixed connection can be understood as: a detachable fixed connection (e.g., using bolts or screws), or a non-detachable fixed connection (e.g., riveting, welding). Of course, mutually fixed connections can also be replaced by an integral structure (e.g., manufactured using a casting process) (except where it is obviously impossible to use an integral forming process).

[0059] In addition, unless otherwise stated, the terms used in any of the technical solutions disclosed in this utility model to indicate positional relationships or shapes include states or shapes that are similar to, close to, or approximate with those states or shapes.

[0060] Any component provided by this utility model can be assembled from multiple individual components, or it can be a single component manufactured by a one-piece molding process.

[0061] It should be noted that the structures, proportions, sizes, etc., depicted in the accompanying drawings of this specification are only for the purpose of assisting those skilled in the art in understanding and reading the content disclosed in the specification, and are not intended to limit the conditions under which this utility model can be implemented. Therefore, they have no substantial technical significance. Any modifications to the structure, changes in the proportions, or adjustments to the size, without affecting the effects and objectives that this utility model can produce, should still fall within the scope of the technical content disclosed in this utility model.

[0062] It should also be noted that in the embodiments of this application, the same reference numerals are used to denote the same component or the same part.

[0063] Any adaptive changes made according to actual needs are within the protection scope of this utility model.

[0064] This utility model uses specific examples to illustrate its principles and implementation methods. The above description of the embodiments is only for the purpose of helping to understand the method and core idea of ​​this utility model. At the same time, for those skilled in the art, there will be changes in the specific implementation methods and application scope based on the idea of ​​this utility model. In summary, the content of this specification should not be construed as a limitation of this utility model.

Claims

1. A fluidized bed-based continuous production system for trimethoxysilane, characterized in that: The system includes a fluidized bed reactor (1), the catalyst inlet of which is connected to a continuous feed unit (2), which is used to feed the reaction catalyst into the fluidized bed reactor (1). The reactant inlet of the fluidized bed reactor (1) is connected to a reactant conveying unit (6), which is used to convey reactants into the fluidized bed reactor (1). The outlet of the fluidized bed reactor (1) is connected to the inlet of a gas-solid separator (3). The solid outlet of the gas-solid separator (3) is connected to a catalyst regeneration unit (4). The catalyst separated from the gas-solid separator (3) is conveyed to the continuous feed unit (2) for reuse after passing through the catalyst regeneration unit (4). The gas outlet of the gas-solid separator (3) is connected to a product collection unit (5), which is used to collect products. Both the fluidized bed reactor (1) and the reactant conveying unit (6) are electrically connected to a control unit (7).

2. The fluidized bed-based continuous production system for trimethoxysilane according to claim 1, characterized in that: The fluidized bed reactor (1) includes a fluidized bed body (101) and a tubular furnace body (102). The fluidized bed body (101) is disposed inside the tubular furnace body (102), and the tubular furnace body (102) is used to heat the fluidized bed body (101).

3. The fluidized bed-based continuous production system for trimethoxysilane according to claim 2, characterized in that: The reactant inlet of the fluidized bed reactor (1) is located at the bottom of the fluidized bed body (101). The fluidized bed body (101) is provided with a perforated plate (103) inside, and the perforated plate (103) is located above the reactant inlet of the fluidized bed reactor (1).

4. The fluidized bed-based continuous production system for trimethoxysilane according to claim 2, characterized in that: The outlet of the fluidized bed reactor (1) is located at the top of the fluidized bed body (101). At least one air outlet baffle (104) is fixed inside the fluidized bed body (101), and the air outlet baffle (104) is inclined.

5. The fluidized bed-based continuous production system for trimethoxysilane according to claim 3, characterized in that: The porous plate (103) is a porous ceramic plate, and the inner wall of the fluidized bed body (101) is provided with a ceramic layer.

6. The fluidized bed-based continuous production system for trimethoxysilane according to claim 1, characterized in that: The continuous feeding unit (2) includes a catalyst storage tank (201), a silicon powder storage tank (202), and a mixing silo (203). The outlet of the catalyst storage tank (201) and the outlet of the silicon powder storage tank (202) are both connected to the inlet of the mixing silo (203). The outlet of the mixing silo (203) is connected to the catalyst inlet of the fluidized bed reactor (1).

7. The fluidized bed-based continuous production system for trimethoxysilane according to claim 1, characterized in that: The reactant delivery unit (6) includes a reactant storage tank (601), which is connected to the reactant inlet of the fluidized bed reactor (1) through a reactant feed pipe. A metering pump (602) is provided on the reactant feed pipe.

8. The fluidized bed-based continuous production system for trimethoxysilane according to claim 1, characterized in that: The gas-solid separator (3) is a cyclone separator.

9. The fluidized bed-based continuous production system for trimethoxysilane according to claim 1, characterized in that: The catalyst regeneration unit (4) includes a microwave processor (401), which is connected to a nitrogen tank (402) via a nitrogen delivery pipe. The nitrogen tank (402) can fill the microwave processor (401) with nitrogen.

10. The fluidized bed-based continuous production system for trimethoxysilane according to claim 1, characterized in that: The product collection unit (5) includes a distillation column (501), the inlet of which is connected to the gas outlet of the gas-solid separator (3) via a product collection pipeline, and a condenser (502) is provided on the product collection pipeline.

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