Polysilicon and organosilicon high-boiling pyrolysis reactor system promoting gas-solid-liquid three-phase mass transfer
By introducing catalyst stacking units and distributors into polycrystalline silicon and organosilicon high-boiling-point pyrolysis reactors, uniform contact between the gas, solid, and liquid phases is achieved, solving the problem of insufficient mass transfer, improving reaction efficiency and raw material utilization, and reducing production costs.
Patent Information
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- NINGXIA SHENGLAN CHEM ENVIRONMENTAL PROT TECH CO LTD
- Filing Date
- 2025-05-21
- Publication Date
- 2026-05-29
AI Technical Summary
Existing polycrystalline silicon and organosilicon high-boiling-point pyrolysis reactor systems suffer from insufficient contact in gas-solid-liquid three-phase mass transfer, resulting in slow and uneven reaction rates, low raw material utilization, high liquid-solid mass transfer resistance, and limited reaction depth and speed.
A high-boiling-point pyrolysis reactor system for polycrystalline silicon and organosilicon was designed to promote gas-solid-liquid three-phase mass transfer. By setting up a catalyst stacking unit, a liquid distributor and a gas distribution unit in the reactor body, and using a loading mesh and nozzles to achieve uniform mixing of gas and solid catalyst, the liquid feedstock is ensured to flow uniformly through the catalytic packing, thereby improving the reaction rate and mixing uniformity.
It improves the mixing effect and reaction rate of gas-solid-liquid three-phase reaction, reduces mass transfer resistance, increases raw material utilization and reaction efficiency, and reduces energy consumption and production costs.
Smart Images
Figure CN224293213U_ABST
Abstract
Description
Technical Field
[0001] This utility model relates to the field of chemical technology, specifically to a high-boiling-point pyrolysis reactor system for polycrystalline silicon and organosilicon that promotes gas-solid-liquid three-phase mass transfer. Background Technology
[0002] In today's chemical industry, the high-boiling-point pyrolysis and conversion of polysilicon and organosilicon plays a crucial role.
[0003] Traditional high-boiling-point pyrolysis processes for polycrystalline silicon and organosilicon face severe challenges in gas-solid-liquid three-phase mass transfer. Due to the special properties of polycrystalline silicon and organosilicon raw materials and the complexity of the reaction process, existing reactor systems often cannot achieve efficient contact and mass transfer between the gas, solid, and liquid phases. In gas-solid mass transfer, the gas and solid catalyst are difficult to contact fully, resulting in a slow and uneven reaction rate. A large amount of gas is discharged without effectively participating in the reaction, which seriously affects the utilization rate of raw materials and reaction efficiency. In liquid-solid mass transfer, the mass transfer resistance between the liquid and the solid catalyst is large, which limits the depth and speed of the reaction. These problems not only reduce production efficiency but also increase energy consumption and production costs, seriously restricting the further development of the polycrystalline silicon and organosilicon industry. Therefore, this application proposes a high-boiling-point pyrolysis reactor system for polycrystalline silicon and organosilicon that promotes gas-solid-liquid three-phase mass transfer. Utility Model Content
[0004] To address the shortcomings of existing technologies, this invention provides a high-boiling-point pyrolysis reactor system for polycrystalline silicon and organosilicon that promotes gas-solid-liquid three-phase mass transfer. This system solves the problem that existing reactor systems often fail to achieve efficient contact and mass transfer between the gas, solid, and liquid phases. In gas-solid mass transfer, the gas and solid catalyst have difficulty making sufficient contact, resulting in a slow and uneven reaction rate. A large amount of gas is discharged before it can effectively participate in the reaction, which seriously affects the utilization rate of raw materials and the reaction efficiency. In liquid-solid mass transfer, the mass transfer resistance between the liquid and the solid catalyst is relatively large, which limits the depth and speed of the reaction.
[0005] To achieve the above objectives, this utility model provides the following technical solution: a high-boiling-point pyrolysis reactor system for polycrystalline silicon and organosilicon that promotes gas-solid-liquid three-phase mass transfer, comprising a reactor body, a catalyst stacking unit disposed within the reactor body, a liquid distributor body disposed within the reactor body, the liquid distributor body being located directly below the catalyst stacking unit, a sealing seat installed above the reactor body, a gas distribution unit disposed within the sealing seat, the catalyst stacking unit comprising a placement rack installed within the reactor body, the placement rack having multiple partitions evenly distributed, and a feeding mesh cylinder inserted into each partition.
[0006] Preferably, a limiting seat is provided on the inner wall of the sealing seat, the limiting seat is in contact with the top end face of the partition, and the limiting seat is used to compress the partition to ensure the stability of the partition.
[0007] Preferably, the gas distribution unit includes:
[0008] A connecting groove is formed in the sealing seat;
[0009] An air intake pipe is fixedly connected to the top end of the sealing seat, and the air intake pipe is connected to the inside of the communicating groove;
[0010] Multiple exhaust pipes are fixedly connected to the bottom end face of the connecting groove, and the exhaust pipes are connected to the interior of the connecting groove.
[0011] Preferably, the exhaust pipe is placed corresponding to the material filling mesh cylinder, and a nozzle is threadedly connected to the bottom end of the exhaust pipe, with the nozzle located at the top end face of the material filling mesh cylinder.
[0012] Preferably, the liquid distributor body is installed at the bottom of the reactor body, the liquid distributor body is closely connected to the catalyst stacking unit, and the outer wall of the reactor body is provided with a liquid inlet, which is connected to the liquid distributor body.
[0013] Preferably, the liquid distributor body is provided with multiple liquid dispensing ports, which are arranged corresponding to the loading mesh cylinder, to further improve the liquid-solid mass transfer efficiency.
[0014] Preferably, a base is installed at the bottom of the reactor body.
[0015] Preferably, the outer wall of the reactor body is connected to a separator and a circulation pump.
[0016] This utility model discloses a high-boiling-point pyrolysis reactor system for polycrystalline silicon and organosilicon that promotes gas-solid-liquid three-phase mass transfer, and its beneficial effects are as follows:
[0017] This polycrystalline silicon and organosilicon high-boiling-point pyrolysis reactor system, which promotes gas-solid-liquid three-phase mass transfer, connects the inlet pipe to the gas catalyst storage tank. When the gas catalyst is delivered to the inlet pipe by a gas pump, it enters the exhaust pipe through a connecting groove. Then, the gas catalyst is evenly sprayed into the catalytic packing of the loading screen cylinder through a nozzle. The liquid feedstock is ensured to flow evenly through the catalytic packing of the loading screen cylinder through the liquid separator, so that the gas and solid catalyst are mixed in the loading screen cylinder, which improves the reaction rate and ensures the uniformity of mixing. This enhances the mixing effect between the liquid feedstock and the gas, accelerates the reaction and the generation of products, and avoids the problem of the large mass transfer resistance between the liquid and the solid catalyst limiting the depth and speed of the reaction. Attached Figure Description
[0018] To more clearly illustrate the technical solutions in the embodiments of this utility model or the prior art, the drawings used in the description of the embodiments or the prior art 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.
[0019] Figure 1 This is a schematic diagram of the overall structure of this embodiment;
[0020] Figure 2 This is a schematic diagram of the main structure of the reactor in this embodiment;
[0021] Figure 3 This is a schematic diagram of the gas distribution unit structure in this embodiment;
[0022] Figure 4 This is a schematic diagram of the catalyst stacking unit structure in this embodiment.
[0023] In the diagram: 1. Reactor body; 2. Sealing seat; 21. Gas distribution unit; 211. Connecting channel; 212. Inlet pipe; 213. Exhaust pipe; 214. Nozzle; 22. Limiting seat; 3. Base; 4. Catalyst stacking unit; 41. Placement rack; 42. Partition; 43. Feeding mesh cylinder; 5. Liquid distributor body; 51. Liquid inlet; 52. Liquid distribution port. Detailed Implementation
[0024] To make the objectives, technical solutions, and advantages of the embodiments of this utility model clearer, the technical solutions in the embodiments of this utility model are described clearly and completely. Obviously, the described embodiments are only some embodiments of this utility model, not all embodiments. Based on the embodiments of this utility model, all other embodiments obtained by those skilled in the art without creative effort are within the protection scope of this utility model.
[0025] This application provides a high-boiling-point pyrolysis reactor system for polycrystalline silicon and organosilicon that promotes gas-solid-liquid three-phase mass transfer. It solves the problem that existing reactor systems often fail to achieve efficient contact and mass transfer between the gas, solid, and liquid phases. In gas-solid mass transfer, the gas and solid catalyst are difficult to contact fully, resulting in slow and uneven reaction rates. A large amount of gas is discharged before effectively participating in the reaction, severely affecting raw material utilization and reaction efficiency. In liquid-solid mass transfer, the large mass transfer resistance between the liquid and solid catalyst limits the depth and speed of the reaction. The system connects the inlet pipe 212 to the gas catalyst storage tank, allowing gas to pass through... The pump delivers the gaseous catalyst to the inlet pipe 212, and the gaseous catalyst enters the exhaust pipe 213 through the connecting groove 211. Then, the gaseous catalyst is evenly sprayed into the catalytic packing of the loading screen cylinder 43 through the nozzle 214. The liquid distribution port 52 ensures that the liquid raw material flows evenly through the catalytic packing of the loading screen cylinder 43, so that the gas and solid catalyst are mixed in the loading screen cylinder 43, which improves the reaction rate and ensures the uniformity of mixing. This improves the mixing effect between the liquid raw material and the gas, accelerates the reaction and the generation of products, and avoids the problem that the mass transfer resistance between the liquid and the solid catalyst is large, which limits the depth and speed of the reaction.
[0026] To better understand the above technical solutions, the following will provide a detailed explanation of the technical solutions in conjunction with the accompanying drawings and specific implementation methods.
[0027] This utility model discloses a high-boiling-point pyrolysis reactor system for polycrystalline silicon and organosilicon that promotes gas-solid-liquid three-phase mass transfer.
[0028] Example 1:
[0029] According to the appendix Figure 1-4 As shown, the reactor includes a reactor body 1, a catalyst stacking unit 4 is provided in the reactor body 1, the catalyst stacking unit 4 is used for uniform distribution of catalytic packing, and a liquid distributor body 5 is provided in the reactor body 1, the liquid distributor body 5 is located directly below the catalyst stacking unit 4, the liquid distributor body 5 is used to ensure that the liquid raw material flows uniformly through the catalytic packing.
[0030] A sealing seat 2 is installed above the reactor body 1. A gas distribution unit 21 is provided in the sealing seat 2. The gas distribution unit 21 is used to uniformly spray the gas entering the reactor body 1. The gas distribution unit 21 uniformly sprays the gas into the charging mesh cylinder 43, which will make the reactants fully contact the catalytic packing in the charging mesh cylinder 43. The liquid distributor body 5 ensures that the liquid raw materials flow uniformly through the catalytic packing in the charging mesh cylinder 43.
[0031] The catalyst stacking unit 4 includes a placement rack 41, which is installed in the reactor body 1. The placement rack 41 has multiple partitions 42, which are evenly distributed. A feeding mesh cylinder 43 is inserted into the partitions 42. The partitions 42 and the feeding mesh cylinder 43 are made of high-strength, corrosion-resistant materials, such as stainless steel alloy or special ceramic materials, which can withstand the high temperature, high pressure and chemical corrosion during the reaction process.
[0032] The loading screen 43 is used for filling the catalytic packing. The multiple loading screens 43 ensure that the catalytic packing is evenly distributed and prevents accumulation.
[0033] A limiting seat 22 is provided on the inner wall of the sealing seat 2. The limiting seat 22 is in contact with the top end face of the partition 42. The limiting seat 22 is used to squeeze the partition 42 to ensure the stability of the partition 42.
[0034] Gas distribution unit 21 includes:
[0035] A connecting groove 211 is formed in the sealing seat 2;
[0036] The intake pipe 212 is fixedly connected to the top end of the sealing seat 2, and the intake pipe 212 is connected to the inside of the connecting groove 211.
[0037] Multiple exhaust pipes 213 are fixedly connected to the bottom end face of the connecting groove 211, and the exhaust pipes 213 are connected to the interior of the connecting groove 211.
[0038] The exhaust pipe 213 is placed corresponding to the material filling cylinder 43. The bottom end of the exhaust pipe 213 is threadedly connected to the nozzle 214, which is located on the top end face of the material filling cylinder 43.
[0039] The intake pipe 212 is connected to the gas catalyst storage tank. When the gas catalyst is delivered to the intake pipe 212 by the gas pump, the gas catalyst enters the exhaust pipe 213 through the connecting groove 211, and then the gas catalyst is evenly sprayed into the catalytic packing of the loading mesh cylinder 43 through the nozzle 214.
[0040] Example 2:
[0041] According to the appendix Figure 1-4 As shown, the reactor includes a reactor body 1, a catalyst stacking unit 4 is provided in the reactor body 1, the catalyst stacking unit 4 is used for uniform distribution of catalytic packing, a liquid distributor body 5 is provided in the reactor body 1, the liquid distributor body 5 is located directly below the catalyst stacking unit 4, the liquid distributor body 5 is used to ensure that the liquid raw material flows uniformly through the catalytic packing, a sealing seat 2 is installed above the reactor body 1, a gas distribution unit 21 is provided in the sealing seat 2, the gas distribution unit 21 is used to uniformly spray the gas entering the reactor body 1;
[0042] The catalyst stacking unit 4 includes a placement rack 41, which is installed in the reactor body 1. The placement rack 41 has multiple partitions 42, which are evenly distributed. A feeding mesh cylinder 43 is inserted into the partition 42.
[0043] The liquid distributor body 5 is installed at the bottom of the reactor body 1. The liquid distributor body 5 is closely connected to the catalyst stacking unit 4. The outer wall of the reactor body 1 is provided with a liquid inlet 51, which is connected to the liquid distributor body 5 and the liquid inlet 51 is connected to the liquid catalyst storage tank.
[0044] The liquid distributor body 5 is provided with multiple liquid distribution ports 52, which are set to correspond to the feeding screen cylinder 43, thereby further improving the liquid-solid mass transfer efficiency.
[0045] The liquid feedstock is ensured to flow uniformly through the catalytic packing of the feeding mesh cylinder 43 via the liquid separator 52, so that the gas and solid catalyst are mixed in the feeding mesh cylinder 43, thereby increasing the reaction rate and ensuring the uniformity of mixing. This improves the mixing effect between the liquid feedstock and the gas, accelerates the reaction and the formation of products, and avoids the problem of the reaction depth and speed being limited by the large mass transfer resistance between the liquid and the solid catalyst.
[0046] A base 3 is installed at the bottom of the reactor body 1.
[0047] The outer wall of reactor body 1 is connected to a separator and a circulating pump.
[0048] The separator uses efficient cyclone separation or filtration separation technology to quickly separate unreacted gases from the reaction mixture.
[0049] The separated gas is collected in a special collection tank and then pumped back to a specific location in the reactor body 1, effectively avoiding the waste of catalyst.
[0050] The foregoing has shown and described the basic principles, main features, and advantages of this utility model. Those skilled in the art should understand that this utility model is not limited to the above embodiments. The embodiments and descriptions in the specification are merely illustrative of the principles of this utility model. Various changes and modifications can be made to this utility model without departing from its spirit and scope, and all such changes and modifications fall within the scope of the claims. The scope of protection of this utility model is defined by the appended claims and their equivalents.
Claims
1. A high-boiling-point pyrolysis reactor system for polycrystalline silicon and organosilicon that promotes gas-solid-liquid three-phase mass transfer, characterized in that, The reactor includes a reactor body (1), a catalyst stacking unit (4) is provided in the reactor body (1), a liquid distributor body (5) is provided in the reactor body (1), the liquid distributor body (5) is located directly below the catalyst stacking unit (4), a sealing seat (2) is installed above the reactor body (1), a gas distribution unit (21) is provided in the sealing seat (2), the catalyst stacking unit (4) includes a placement rack (41), which is installed in the reactor body (1), the placement rack (41) has multiple partitions (42) which are evenly distributed, and a feeding mesh cylinder (43) is inserted into the partition (42).
2. The polycrystalline silicon and organosilicon high-boiling-point pyrolysis reactor system for promoting gas-solid-liquid three-phase mass transfer according to claim 1, characterized in that, A limiting seat (22) is provided on the inner wall of the sealing seat (2). The limiting seat (22) is in contact with the top end face of the partition (42). The limiting seat (22) is used to squeeze the partition (42) to ensure the stability of the partition (42).
3. The polycrystalline silicon and organosilicon high-boiling-point pyrolysis reactor system for promoting gas-solid-liquid three-phase mass transfer according to claim 1, characterized in that, The gas distribution unit (21) includes: A connecting groove (211) is formed in the sealing seat (2); An air intake pipe (212) is fixedly connected to the top end of the sealing seat (2), and the air intake pipe (212) is connected to the inside of the communicating groove (211); Multiple exhaust pipes (213) are fixedly connected to the bottom end face of the connecting groove (211), and the exhaust pipes (213) are connected to the interior of the connecting groove (211).
4. The polycrystalline silicon and organosilicon high-boiling-point pyrolysis reactor system for promoting gas-solid-liquid three-phase mass transfer according to claim 3, characterized in that, The exhaust pipe (213) is placed corresponding to the loading mesh cylinder (43), and the bottom end of the exhaust pipe (213) is threadedly connected to a nozzle (214), which is located on the top end face of the loading mesh cylinder (43).
5. The polycrystalline silicon and organosilicon high-boiling-point pyrolysis reactor system for promoting gas-solid-liquid three-phase mass transfer according to claim 1, characterized in that, The liquid distributor body (5) is installed at the bottom of the reactor body (1). The liquid distributor body (5) is closely connected to the catalyst stacking unit (4). The outer wall of the reactor body (1) is provided with a liquid inlet (51), which is connected to the liquid distributor body (5).
6. The polycrystalline silicon and organosilicon high-boiling-point pyrolysis reactor system for promoting gas-solid-liquid three-phase mass transfer according to claim 5, characterized in that, The liquid distributor body (5) is provided with multiple liquid distribution ports (52), which are provided in relation to the loading mesh cylinder (43) to further improve the liquid-solid mass transfer efficiency.
7. The polycrystalline silicon and organosilicon high-boiling-point pyrolysis reactor system for promoting gas-solid-liquid three-phase mass transfer according to claim 1, characterized in that, The reactor body (1) is fitted with a base (3) at its bottom.
8. The polycrystalline silicon and organosilicon high-boiling-point pyrolysis reactor system for promoting gas-solid-liquid three-phase mass transfer according to claim 7, characterized in that, The outer wall of the reactor body (1) is connected to a separator and a circulation pump.