A green synthesis system for preparing organoalkylsilanes
By combining continuous catalytic reaction and separation and purification units, the problems of high cost, high energy consumption and environmental risks in the production of organoalkylsilanes have been solved, realizing efficient, energy-saving and environmentally friendly organoalkylsilane synthesis, and improving product purity and reactant utilization.
Patent Information
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- SHANGHAI XUENTIAN TECHNOLOGY CO LTD
- Filing Date
- 2025-06-30
- Publication Date
- 2026-05-26
AI Technical Summary
Existing methods for producing organoalkyl silanes suffer from high costs, high energy consumption, high requirements for equipment corrosion resistance, limited selectivity, significant environmental pressure, and high safety risks. In particular, the production of long-chain alkyl silanes is characterized by low yields and the potential for corrosion and pollution due to improper handling of byproducts.
A continuous catalytic reaction device and a separation and purification unit are used to continuously catalyze the reaction of silane and olefin in the presence of a catalyst to generate organoalkylsilane. The separation and purification unit separates the silane from excess olefin to obtain a high-purity product. The excess olefin is recycled, thereby improving the utilization rate of reactants.
The system enables the efficient, energy-saving, and environmentally friendly synthesis of organoalkylsilanes under normal pressure. Its compact structure improves production efficiency, reduces energy consumption and environmental risks, and enhances product purity and reactant utilization.
Smart Images
Figure CN224271117U_ABST
Abstract
Description
Technical Field
[0001] This invention relates to the field of synthetic technology, and in particular to a green synthetic system for preparing organoalkylsilanes. Background Technology
[0002] Organoalkylsilanes are an important class of organosilicon compounds. At room temperature, they are mostly colorless, volatile liquids, readily soluble in organic solvents such as benzene and methyl ether. However, they undergo vigorous hydrolysis in water to form silanols and release hydrogen chloride; some products are flammable. Their boiling point increases with increasing alkyl chain length. These compounds occupy a central position in the organosilicon industry, primarily used in the preparation of silicone rubbers, silicone resins (such as high-temperature resistant aerospace materials), hydrophobic coatings (such as glass surface treatment agents), and semiconductor packaging materials. They also act as coupling agents to enhance the interfacial bonding between organic and inorganic materials.
[0003] The main industrial production method is direct synthesis, which produces complex products: a mixture requiring separation and purification, increasing energy consumption. The reaction conditions are harsh: high temperature (250-350℃) and high pressure are required, necessitating highly corrosion-resistant equipment. Selectivity is limited: it is mainly suitable for short-chain alkyl groups (such as methyl), with low yields for long-chain alkyl chlorosilanes. Environmental pressure is significant: the byproduct HCl requires treatment, and improper recovery can easily cause corrosion and pollution.
[0004] The Grignard reagent method is costly: Grignard reagents (such as RMgBr) are complex to prepare, requiring strictly anhydrous and oxygen-free conditions, and the raw materials and solvents (such as diethyl ether) are expensive. Operation is complex: the reaction conditions are sensitive (requiring low temperature and inert gas protection), making scale-up production difficult. Safety risks: Grignard reagents are flammable and explosive, and improper handling can easily lead to accidents.
[0005] Therefore, it is essential to develop novel, low-cost methods for synthesizing organoalkylsilanes and corresponding reaction apparatus. Utility Model Content
[0006] To address the problems existing in the prior art, the purpose of this invention is to provide a green synthesis system for preparing organoalkylsilanes. This system uses a continuous catalytic reaction apparatus as its core equipment, realizing the synthesis of organoalkylsilanes from silanes and olefins in the presence of a catalyst. The subsequent separation and purification unit uses separation and purification to obtain high-purity organoalkylsilanes, and excess olefins can be returned to the reaction unit for recycling, improving reactant utilization.
[0007] The technical solution of this utility model is as follows:
[0008] A green synthetic system for preparing organoalkylsilanes, comprising, in sequence:
[0009] The reaction unit is used to mix silanes and olefins with a catalyst and then heat them to produce organoalkylsilanes.
[0010] The separation and purification unit is used to separate the organoalkylsilanes from the excess olefins in the crude product generated by the reaction unit, obtaining organoalkylsilanes and returning the olefins to the reaction unit for recycling.
[0011] The reaction unit mainly includes a mixing device and a continuous reaction device connected in sequence. The mixing device is used to mix silane with a portion of olefins to form reactant A. The continuous reaction device is located downstream of the mixing device and connected by a pipeline. It receives reactant A from the mixing device and simultaneously supplies another portion of reactant B, a mixture of olefins and catalyst, to the continuous reaction device. Reactant A and reactant B are mixed and heated in the continuous reaction device to produce a mixture of silane, olefins, and catalyst as the product.
[0012] The separation and purification unit, located downstream of the continuous reaction device and connected via pipeline, mainly includes a separation device and a heat exchange device. It receives the products generated after the reaction in the reaction unit, and after separation, it separates the excess olefins, organoalkylsilanes, and catalyst to obtain qualified organoalkylsilane products. The excess olefins obtained are returned to the mixing device of the reaction unit via pipeline for recycling.
[0013] Preferably, the mixing device is a group of mixers connected in parallel, in series, or in a combination of series and parallel. The mixers include, but are not limited to, one or more of the following: static mixers, jet mixers, dynamic mixers, centrifugal mixers, and continuous stirred tank reactors.
[0014] Preferably, the mixing device is equipped with a heating device for heating the mixture of silane and a portion of olefins.
[0015] Preferably, the continuous reaction device is one of a microchannel continuous reactor, a dynamic tubular reactor, a loop reactor, or a continuous stirred tank reactor.
[0016] Preferably, the separation device is a distillation column, a scraped film evaporator, or a molecular distillation apparatus.
[0017] Preferably, the distillation column is a Westerly column, a triangular spiral column, or a Raschig column, with 5-30 theoretical plates.
[0018] Preferably, the evaporation area of the scraped film evaporator is 1-8 m². 2 The heating temperature is 80-150℃, the condensation temperature is 0-30℃, and the film scraping speed is 100-300 rpm.
[0019] Preferably, the evaporation area of the molecular distillation apparatus is 1-6 m². 2The heating temperature is 80-150℃, the condensation temperature is 0-30℃, and the film scraping speed is 100-300 rpm.
[0020] Beneficial effects
[0021] This invention discloses a green synthesis system for preparing organoalkylsilanes. Under normal pressure, organoalkylsilanes are synthesized from silanes and olefins through continuous catalytic reaction and continuous separation in the presence of a catalyst. The system has a compact structure and a reasonable matching of material and energy flows, making it an energy-saving, environmentally friendly, economical, and efficient green process device. Attached Figure Description
[0022] In drawings that are not necessarily drawn to scale, the same reference numerals may describe similar parts in different views. The same reference numerals with or without letter suffixes may indicate different instances of similar parts. The drawings generally illustrate various embodiments by way of example rather than limitation and, together with the description and claims, serve to explain embodiments of the utility model. Where appropriate, the same reference numerals are used in all drawings to refer to the same or similar parts. Such embodiments are illustrative and not intended to be exhaustive or exclusive embodiments of the apparatus or method.
[0023] Figure 1 This is a schematic diagram of a green synthesis system for preparing organoalkylsilanes according to one embodiment of the present invention;
[0024] Figure reference numerals: 1-reaction unit, 2-separation and purification unit, 11-mixing device, 12-continuous reaction device, 21-separation device, 22-heat exchange device. Detailed Implementation
[0025] The specific embodiments of the present invention will now be described in detail with reference to the accompanying drawings, but these are not intended to limit the scope of the present invention.
[0026] It should be understood that various modifications can be made to the embodiments disclosed herein. Therefore, the following description should not be considered as limiting, but merely as an example of embodiments. Other modifications within the scope and spirit of this disclosure will be apparent to those skilled in the art.
[0027] The accompanying drawings, which are included in and form part of this specification, illustrate embodiments of the present disclosure and, together with the general description of the disclosure given above and the detailed description of the embodiments given below, serve to explain the principles of the disclosure.
[0028] These and other features of the present invention will become apparent from the following description of preferred forms of embodiments given as non-limiting examples, with reference to the accompanying drawings.
[0029] It should also be understood that although the present invention has been described with reference to some specific examples, those skilled in the art can certainly implement many other equivalent forms of the present invention, which have the features described in the claims and are therefore all within the scope of protection defined herein.
[0030] The above and other aspects, features and advantages of this disclosure will become more apparent when taken in conjunction with the accompanying drawings and in view of the following detailed description.
[0031] Specific embodiments of the present disclosure are described thereafter with reference to the accompanying drawings; however, it should be understood that the disclosed embodiments are merely examples of the present disclosure and can be implemented in various ways. Well-known and / or repeated functions and structures are not described in detail to avoid unnecessary or redundant details that could obscure the present disclosure. Therefore, the specific structural and functional details disclosed herein are not intended to be limiting, but merely to serve as the basis and representative basis for the claims to teach those skilled in the art to use the present disclosure in a variety of substantially any suitable detailed structures.
[0032] This specification may use the phrases “in one embodiment,” “in another embodiment,” “in yet another embodiment,” or “in still another embodiment,” all of which may refer to one or more of the same or different embodiments according to this disclosure.
[0033] The following is in conjunction with the appendix Figure 1 The structure of the green synthesis system for preparing organoalkylsilanes of this invention will be described in further detail below.
[0034] According to one embodiment of the present invention, a green synthesis system for preparing organoalkylsilanes is provided, comprising:
[0035] Reaction unit 1 is used to react silane and olefin with a catalyst and then heat to produce organoalkylsilane;
[0036] Separation and purification unit 2 is used to separate the organoalkylsilane from the excess olefin in the crude product generated by the reaction unit, obtaining organoalkylsilane, while the olefin is returned to the reaction unit for recycling.
[0037] The reaction unit 1 mainly includes a mixing device 11 and a continuous reaction device 12 connected in sequence. The mixing device 11 is used to mix silane with a portion of olefins to form reactant A. The continuous reaction device 12 is located downstream of the mixing device 11 and is connected by a pipeline to receive reactant A from the mixing device 11. At the same time, it supplies another portion of reactant B, a mixture of olefins and catalyst, to the continuous reaction device 12. The reactant A and reactant B are mixed and heated in the continuous reaction device 12 to produce a mixture of silane, olefins, and catalyst.
[0038] The separation and purification unit 2, located downstream of the continuous reaction device 12 and connected by pipeline, mainly includes a separation device 21 and a heat exchange device 22. It receives the mixture from the reaction unit 1 after reaction, and after separation, it separates the excess olefins, organoalkylsilanes and catalysts to obtain qualified organoalkylsilane products. The excess olefins obtained are returned to the mixing device 12 of the reaction unit 1 for recycling.
[0039] Preferably, the mixing device 11 can be a single mixer or a combination of multiple mixers. The connection can be in parallel, series, or a combination of series and parallel. Specific mixer equipment forms include, but are not limited to, one or more of the following: static mixer, jet mixer, dynamic mixer, centrifugal mixer, and continuous stirred tank reactor.
[0040] Preferably, the mixing device 11 is equipped with a heating device for heating the mixture of silane and a portion of olefins.
[0041] Preferably, the continuous reaction device 12 is one of a microchannel continuous reactor, a dynamic tubular reactor, a loop reactor, or a continuous stirred tank reactor.
[0042] Preferably, the separation device is a distillation column, a scraped film evaporator, or a molecular distillation apparatus.
[0043] Preferably, the distillation column is a Westerly column, a triangular spiral column, or a Raschig column, with 5-30 theoretical plates.
[0044] Preferably, the evaporation area of the scraped film evaporator is 1-8 m². 2 The heating temperature is 80-150℃, the condensation temperature is 0-30℃, and the film scraping speed is 100-300 rpm.
[0045] Preferably, the evaporation area of the molecular distillation apparatus is 1-6 m². 2 The heating temperature is 80-150℃, the condensation temperature is 0-30℃, and the film scraping speed is 100-300 rpm.
[0046] Preferably, the silane is selected from methyldichlorosilane, ethyldichlorosilane, propyldichlorosilane, butyldichlorosilane, isopropyldichlorosilane, dichlorodihydrosilane, dimethylsilane, diethylsilane, dipropylsilane, dibutylsilane, and diisopropylsilane.
[0047] More preferably, the silane is selected from methyldichlorosilane, dichlorosilane and dimethylsilane.
[0048] Preferably, the olefin is selected from 1,3-butadiene, 1,4-pentadiene, isoprene, 1,5-hexadiene, 1,6-heptadiene, 1,7-octadiene, 1,8-nonadiene, and 1,9-decadiene.
[0049] More preferably, the olefin is selected from 1,5-hexadiene, 1,6-heptadiene, 1,7-octadiene and 1,8-nonadiene.
[0050] Preferably, the catalyst is a metal nanoparticle, and the metal is one or more of Pd, Pt, Ru, Rh, and Ir.
[0051] Preferably, the molar ratio of silane to olefin in the reactant A is 1:2-1:10, more preferably 1:2-1:8.
[0052] Preferably, the mass ratio of catalyst to olefin in the reactant B is 1:10000-1:100, more preferably 1:10000-1:500.
[0053] Preferably, the molar ratio of silane to olefin in the mixing device 11 is 1:1-1:8, and more preferably 1:1-1:4.
[0054] Preferably, the temperature in the mixing device 12 is controlled at 40-150℃ and the pressure is 0.1-2.0 MPa, more preferably the temperature is 50-120℃ and the pressure is 0.1-1.0 MPa.
[0055] Preferably, the reaction time in the reaction device 12 is 5s-20min, more preferably 10s-10min, and even more preferably 30s-5min.
[0056] Preferably, the operating temperature of the bottom of the separation device 21 is 70-160℃, the operating temperature at the top of the column is 50-150℃, the operating pressure at the bottom of the column is 5-10 kPa, and the operating pressure at the top of the column is 1-5 kPa.
[0057] The following is for reference. Figure 1 The specific operation mode of the green synthesis system according to this utility model includes the following steps:
[0058] 1) The raw material silane and a portion of the olefin are pumped into the mixing device 11 respectively, and the mixture forms reactant A, which then enters the continuous reaction device 12; at the same time, another portion of the olefin and the catalyst mixture reactant B is pumped into the continuous reaction device 12 for heating reaction, and the resulting reaction product mixture enters the separation and purification unit 2.
[0059] 2) The reaction products are separated in the separation and purification unit 2 by the separation device 21 (e.g., a distillation column). The olefin gas introduced from the top of the column passes through the heat exchanger 22 and then re-enters the mixing device 11. The bottom of the column yields an organoalkylsilane product.
[0060] The following embodiments are merely examples of implementation schemes of this utility model and do not constitute any limitation on this utility model. Those skilled in the art will understand that modifications that do not depart from the essence and concept of this utility model fall within the protection scope of this utility model. Unless otherwise specified, the reagents and instruments used in the following embodiments are all commercially available products.
[0061] Example 1
[0062] 1) Methyldichlorosilane and hexadiene are mixed separately by a plunger pump through the static mixer and then pumped into the continuous reactor 12. The continuous reactor 12 is a microchannel continuous reactor with a liquid holding volume of 54 ml and a molar ratio of methyldichlorosilane to hexadiene of 1:2. At the same time, a mixture of hexadiene and catalyst Pt nanoparticles (the mass ratio of Pt nanoparticles to methyldichlorosilane is 1:2000) is pumped into the microchannel continuous reactor by a plunger pump. The total molar ratio of methyldichlorosilane to olefins is 1:6. The reaction is carried out at 65°C with a reaction residence time of 5 min, and then enters the separation and purification unit 2.
[0063] 2) The product passes through the distillation column in the separation and purification unit 2. The column bottom temperature is 80-88℃, the column bottom pressure is 6 kPa, the column top temperature is 63-67℃, the column top pressure is 3 kPa, and the distillation column has 10 trays. 5-Hexenylmethyldichlorosilane with a purity of 97% is obtained at the bottom of the column, with a molar yield of 96%.
[0064] Example 2
[0065] 1) Methyldichlorosilane and hexadiene are mixed separately by a plunger pump through the static mixer and then pumped into the continuous reactor 12. The continuous reactor 12 is a dynamic tubular reactor with a liquid holding volume of 1200 ml. The molar ratio of methyldichlorosilane to hexadiene is 1:2. At the same time, a mixture of hexadiene and catalyst Pd nanoparticles (the mass ratio of Pd nanoparticles to methyldichlorosilane is 1:2000) is pumped into the continuous reactor 12 by a plunger pump. The total molar ratio of methyldichlorosilane to olefins is 1:5.5. The reaction is carried out at 130°C with a reaction residence time of 3 min, and then enters the separation and purification unit 2.
[0066] 2) The product passes through the distillation column in the separation and purification unit 2. The column bottom temperature is 80-88℃, the column bottom pressure is 6 kPa, the column top temperature is 63-67℃, the column top pressure is 3 kPa, and the distillation column has 10 trays. 5-Hexenylmethyldichlorosilane with a purity of 98% is obtained at the bottom of the column, with a molar yield of 94%.
[0067] Example 3
[0068] 1) Methyldichlorosilane and octadiene are mixed separately by a plunger pump through the jet mixer and then pumped into the continuous reactor 12. The continuous reactor 12 is a dynamic tubular reactor with a liquid holding volume of 1200 ml. The molar ratio of methyldichlorosilane to hexadiene is 1:2. At the same time, a mixture of hexadiene and catalyst Pt nanoparticles (the mass ratio of Pt nanoparticles to methyldichlorosilane is 1:3000) is pumped into the continuous reactor 12 by a plunger pump. The total molar ratio of methyldichlorosilane to olefins is 1:6. The reaction is carried out at 130°C with a reaction residence time of 5 min, and then enters the separation and purification unit 2.
[0069] 2) The product passes through the distillation column in the separation and purification unit 2. The column bottom temperature is 130-135℃, the column bottom pressure is 6 kPa, the column top temperature is 116-122℃, the column top pressure is 3 kPa, and the distillation column has 10 trays. 7-Octenylmethyldichlorosilane with a purity of 98% is obtained at the bottom of the column, with a molar yield of 97%.
[0070] Example 4
[0071] 1) Dichlorosilane and octadiene are separately introduced into a stirrer and mixed, and then pumped into the continuous reactor 12. The continuous reactor 12 is a microchannel continuous reactor with a liquid holding volume of 54 ml. The molar ratio of dichlorosilane to octadiene is 1:2. At the same time, a mixture of octadiene and catalyst Pt nanoparticles (the mass ratio of Pt nanoparticles to dichlorosilane is 1:3000) is pumped into the continuous reactor 12 through a plunger pump. The total molar ratio of dichlorosilane to olefins is 1:6. The reaction is carried out at 130°C with a reaction residence time of 5 min, and then enters the separation and purification unit 2.
[0072] 2) The product passes through the scraped film evaporator in the separation and purification unit 2. The scraped film evaporator has an evaporation area of 2 m2, a heating temperature of 140-145℃, a condensation temperature of 10-15℃, and a vacuum degree of 10 kPa, to obtain bis(7-octenyl)dichlorosilane with a purity of 98% and a molar yield of 96%.
[0073] Example 5
[0074] 1) Dimethylsilane and octadiene are separately introduced into a stirrer and mixed, and then pumped into the continuous reactor 12. The continuous reactor 12 is a microchannel continuous reactor with a liquid holding volume of 54 ml. The molar ratio of dichlorosilane to octadiene is 1:2. At the same time, a mixture of octadiene and catalyst Pt nanoparticles (the mass ratio of Pt nanoparticles to dimethylsilane is 1:3000) is pumped into the continuous reactor 12 through a plunger pump. The total molar ratio of dimethylsilane to olefins is 1:4. The reaction is carried out at 130°C with a reaction residence time of 5 min, and then enters the separation and purification unit 2.
[0075] 2) The product passes through the scraped film evaporator in the separation and purification unit 2. The scraped film evaporator has an evaporation area of 2 m2, a heating temperature of 140-145℃, a condensation temperature of 10-15℃, and a vacuum degree of 10 kPa, to obtain bis(7-octenyl)dimethylsilane with a purity of 98% and a molar yield of 95%.
[0076] Example 6
[0077] 1) Dimethylsilane and hexadiene are separately introduced into a stirrer and mixed, and then pumped into the continuous reactor 12. The continuous reactor 12 is a dynamic tubular reactor with a liquid holding volume of 1200 ml. The molar ratio of dimethylsilane to hexadiene is 1:2. At the same time, a mixture of hexadiene and catalyst Pt nanoparticles (the mass ratio of Pt nanoparticles to dimethylsilane is 1:3000) is pumped into the continuous reactor 12 through a plunger pump. The total molar ratio of dimethylsilane to olefins is 1:4. The reaction is carried out at 80°C with a reaction residence time of 5 min, and then enters the separation and purification unit 2.
[0078] 2) The product passes through the scraped film evaporator in the separation and purification unit 2. The scraped film evaporator has an evaporation area of 2 m2, a heating temperature of 75-80℃, a condensation temperature of 0-10℃, and a vacuum degree of 20 kPa to obtain bis(5-hexenyl)dimethylsilane with a purity of 98% and a molar yield of 96%.
[0079] Example 7
[0080] 1) Dimethylsilane and octadiene are separately introduced into a stirrer and mixed, and then pumped into the continuous reactor 12. The continuous reactor 12 is a microchannel continuous reactor with a liquid holding volume of 54 ml. The molar ratio of dichlorosilane to octadiene is 1:2. At the same time, a mixture of octadiene and catalyst Pt nanoparticles (the mass ratio of Pt nanoparticles to dimethylsilane is 1:3000) is pumped into the continuous reactor 12 through a plunger pump. The total molar ratio of dimethylsilane to olefins is 1:4. The reaction is carried out at 130°C with a reaction residence time of 5 min, and then enters the separation and purification unit 2.
[0081] 2) The product passes through the scraped film evaporator in the separation and purification unit 2. The scraped film evaporator has an evaporation area of 2 m2, a heating temperature of 140-145℃, a condensation temperature of 10-15℃, and a vacuum degree of 10 kPa, to obtain bis(7-octenyl)dimethylsilane with a purity of 98% and a molar yield of 98%.
[0082] The above description is merely a specific embodiment of this utility model, but the protection scope of this utility model is not limited thereto. Any variations or substitutions that can be easily conceived by those skilled in the art within the technical scope disclosed in this utility model should be included within the protection scope of this utility model. Therefore, the protection scope of this utility model should be determined by the scope of the claims.
Claims
1. A green synthetic system for preparing organoalkylsilanes, characterized in that, In order, they include: The reaction unit is used to mix silanes and olefins with a catalyst and then heat them to produce organoalkylsilanes. The separation and purification unit is used to separate the organoalkylsilanes from the excess olefins in the crude product generated by the reaction unit, obtaining organoalkylsilanes and returning the olefins to the reaction unit for recycling. The reaction unit mainly includes a mixing device and a continuous reaction device connected in sequence. The mixing device is used to mix silane with a portion of olefins to form reactant A. The continuous reaction device is located downstream of the mixing device and connected by a pipeline. It receives reactant A from the mixing device and simultaneously supplies another portion of reactant B, a mixture of olefins and catalyst, to the continuous reaction device. Reactant A and reactant B are mixed and heated in the continuous reaction device to produce a mixture of silane, olefins, and catalyst as the product. The separation and purification unit, located downstream of the continuous reaction device and connected via pipeline, mainly includes a separation device and a heat exchange device. It receives the products generated after the reaction in the reaction unit, and after separation, separates the excess olefins, organoalkylsilanes, and catalyst to obtain qualified organoalkylsilane products. The excess olefins obtained are returned to the mixing device of the reaction unit for recycling via pipeline.
2. The green synthesis system for preparing organoalkylsilanes according to claim 1, characterized in that, The mixing device is a group of mixers connected in parallel, in series, or in a combination of series and parallel. The mixer includes one or more of the following: static mixer, jet mixer, dynamic mixer, centrifugal mixer, and continuous stirred tank reactor.
3. The green synthesis system for preparing organoalkylsilanes according to claim 1, characterized in that, The mixing device is equipped with a heating device for heating the mixture of silane and some olefins.
4. The green synthesis system for preparing organoalkylsilanes according to claim 1, characterized in that, The continuous reaction device is one of the following: microchannel continuous reactor, dynamic tubular reactor, loop reactor, or continuous stirred tank reactor.
5. The green synthesis system for preparing organoalkylsilanes according to claim 1, characterized in that, The separation device includes a distillation column, a scraped film evaporator, and a molecular distillation apparatus.
6. The green synthesis system for preparing organoalkylsilanes according to claim 5, characterized in that, The distillation column is of the West Tower type, triangular spiral type, or Raschig type, with a theoretical number of 5-30 plates.
7. The green synthesis system for preparing organoalkylsilanes according to claim 5, characterized in that, The evaporation area of the scraped film evaporator is 1-8 m². 2 The heating temperature is 80-150℃, the condensation temperature is 0-30℃, and the film scraping speed is 100-300 rpm.
8. The green synthesis system for preparing organoalkylsilanes according to claim 5, characterized in that, The evaporation area of the molecular distillation apparatus is 1-6 m². 2 The heating temperature is 80-150℃, the condensation temperature is 0-30℃, and the film scraping speed is 100-300 rpm.