Continuous production method of alkyl methoxy acetoxime silane and reaction device

Abstract

The invention relates to the technical field of chemical synthesis, and discloses a continuous production method of alkyl methoxy acetoxime silane and a reaction device, the method adopts a membrane catalytic reaction unit to carry out catalytic reaction on alkyl triacetoxime silane and alkyl trimethoxy silane, the device can continuously produce alkyl methoxy acetoxime silane, and the production efficiency is high. The reaction speed is high, the reaction period is short, the conversion rate of the alkyl methoxy acetoxime silane product is high, the multiple membrane catalytic reaction units are arranged in the shell of the reaction device, the mixing back effect of a mixture can be reduced by arranging the multiple membrane catalytic reaction units, it is guaranteed that the reaction product can continue to react in the upper layer of membrane catalytic reaction unit, and the reaction efficiency is improved. The catalyst does not return to the bottom to reduce the reaction rate of the reaction product, thereby enhancing the conversion rate of the reaction product and enabling the reaction materials to react thoroughly.

Description

Technical Field

[0001] The invention relates to the technical field of chemical synthesis, and in particular to a continuous production method and a reaction device for alkylmethoxyacetoneoxime silane. Background Art

[0002] Room temperature curing silicone rubber, also known as room temperature vulcanized silicone rubber, is based on hydroxyl-terminated polysiloxane as the base polymer, with fillers, crosslinking agents, coupling agents, plasticizers, catalysts, pigments, etc. added to mix into a rubber compound under dry conditions. When used, the rubber compound can undergo a crosslinking reaction to form an elastomer when it comes into contact with moisture at room temperature. Room temperature curing silicone rubber mainly includes acetic acid type, ketone oxime type, and alcohol type according to the different by-products released during vulcanization. Among them, ketone oxime type room temperature curing silicone rubber has good comprehensive performance and good storage. The commonly used crosslinking agents for ketone oxime type silicone rubber are alkyl tributylacetoximine silanes such as methyl tributylacetoximine silane and vinyl tributylacetoximine silane. The above crosslinking agents will produce butanone oxime after curing, and butanone oxime is a carcinogen, so it has been banned at present.

[0003] In order to solve the problem that alkyl trisbutyl ketoxime silane produces carcinogen butanone oxime, the existing technology has developed pentanone oxime silane and acetone oxime silane. Compared with pentanone oxime silane, acetone oxime silane has low production cost and high activity, so acetone oxime silane has high application value. However, the freezing point of acetone oxime silane is 15°C, and it is difficult to use in an environment below 15°C. In addition, since the melting point of acetone oxime is 60°C, the acetone oxime produced when using acetone oxime silane crosslinker to prepare RTV silicone rubber will be released in the form of crystals and dispersed on the surface of the silicone rubber. After the silicone rubber is cured, a large number of spots will appear on the surface, seriously affecting the quality of the silicone rubber.

[0004] In view of the problems existing in the application of the above-mentioned acetone oxime, the German company Nitrochem has developed vinyl methoxyacetone oxime silicon, which introduces methoxy groups into vinyl methoxyacetone oxime silicon, so that the vinyl methoxyacetone oxime silicon is hydrolyzed to produce methanol and acetone oxime when curing silicone rubber, and the acetone oxime is dissolved and dispersed in the rubber by methanol. However, the present application found that the above-mentioned vinyl methoxyacetone oxime silicon was prepared by an intermittent production process, which has a long reaction time, a high product chromaticity, and the catalyst needs to be filtered out after the reaction, and the production efficiency is low and the product conversion rate is low. Summary of the invention

[0005] In order to overcome the problems of long reaction time, high product chromaticity, low production efficiency and low product conversion rate in the intermittent production process of alkyl methoxyacetone oxime silicon in the prior art, the present invention provides a continuous production method and reaction device for alkyl methoxyacetone oxime silane, wherein the method adopts a membrane catalytic reaction unit to catalyze the reaction of alkyl triacetone oxime silane and alkyl trimethoxy silane, and the method can continuously produce alkyl methoxyacetone oxime silane, has a fast reaction rate, a short reaction cycle and a high product conversion rate of alkyl methoxyacetone oxime silane.

[0006] The specific technical scheme of the present invention is: A method for continuously producing alkyl methoxyacetone oxime silane comprises the following steps: preheating alkyl triacetone oxime silane and alkyl trimethoxy silane and injecting them into a membrane catalytic reaction unit for reaction to obtain alkyl methoxyacetone oxime silane, wherein the membrane catalytic reaction unit comprises a filter membrane cavity and a catalyst arranged in the filter membrane cavity, and the catalyst is a strong base microsphere catalyst.

[0007] The invention provides a method for continuously producing alkyl methoxyacetone oxime silane. The method adopts a membrane catalytic reaction unit to catalyze the reaction of alkyl triacetone oxime silane and alkyl trimethoxy silane. The method can continuously produce alkyl methoxyacetone oxime silane, has a fast reaction rate, a short reaction cycle and a high conversion rate of the alkyl methoxyacetone oxime silane product. The membrane catalytic reaction unit in the method is composed of a filter membrane cavity and a catalyst arranged in the filter membrane cavity. A mixed liquid of alkyl triacetone oxime silane and alkyl trimethoxy silane enters the interior of the filter membrane cavity through the filter holes of the filter membrane cavity as needed. After the liquid passes through the filter holes of the filter membrane cavity, it can contact with the catalyst and undergo a catalytic reaction, thereby accelerating the reaction speed of alkyl triacetone oxime silane and alkyl trimethoxy silane to generate alkyl methoxy acetone oxime silane. In addition, due to the effect of the filter membrane micropores, the liquid passing through the microporous membrane occurs in the form of molecular flow. After the molecular flow contacts the catalyst, the reaction rate is fast and the conversion rate of the target product alkyl methoxy acetone oxime silane is high. The reaction of alkyl triacetone oxime silane and alkyl trimethoxy silane is more thorough, the reaction product does not need to be filtered, and the chromaticity of the reaction product is good.

[0008] Preferably, the filtration accuracy of the filter membrane cavity is 0.1 to 5 μm, and the particle size of the catalyst is 10 to 100 μm.

[0009] Preferably, the alkyl triacetone oxime silane is one of methyl triacetone oxime silane and vinyl triacetone oxime silane.

[0010] Preferably, the alkyltrimethoxysilane is one of methyltrimethoxysilane and vinyltrimethoxysilane.

[0011] Preferably, the reaction temperature is 50-60° C., the reaction pressure is 0.1-0.4 MPa, and the material residence time of the reaction is 1-2 h.

[0012] A reaction device comprises a reaction shell and a plurality of membrane reaction modules arranged in the shell.

[0013] The present application also provides a reaction device, in which a plurality of membrane catalytic reaction units are arranged in the shell of the reaction device. The plurality of membrane catalytic reaction units can reduce the mixing effect of the mixture, ensure that the reaction products can continue to react in the upper membrane catalytic reaction unit, and will not return to the bottom to reduce the reaction rate of the reaction products, thereby improving the conversion rate of the reaction products and allowing the reaction materials to react thoroughly.

[0014] Preferably, the reaction shell is provided with a hot water jacket.

[0015] Preferably, the reaction shell further comprises a liquid inlet and a liquid outlet, the liquid inlet is connected to a mixer, the mixer is connected to an alkyl triacetone oxime silane preheating device and an alkyl trimethoxy silane preheating device, and the liquid outlet is connected to an intermediate tank.

[0016] Preferably, a plurality of partitions are provided in the reaction shell, and the membrane reaction module is located in a space formed by adjacent partitions.

[0017] Preferably, the partition is a stainless steel mesh plate.

[0018] Compared with the prior art, this application has the following technical effects: (1) The present invention provides a method for continuously producing alkyl methoxyacetone oxime silane, which uses a membrane catalytic reaction unit to catalyze the reaction of alkyl triacetone oxime silane and alkyl trimethoxy silane. The method can continuously produce alkyl methoxyacetone oxime silane, has a fast reaction rate, a short reaction cycle, and a high conversion rate of the alkyl methoxyacetone oxime silane product.

[0019] (2) The present application also provides a reaction device, in which a plurality of membrane catalytic reaction units are arranged in the shell of the reaction device. The arrangement of the plurality of membrane catalytic reaction units can reduce the mixing effect of the mixture, ensure that the reaction product can continue to react in the upper membrane catalytic reaction unit, and will not return to the bottom to reduce the reaction rate of the reaction product, thereby improving the conversion rate of the reaction product and allowing the reaction materials to react thoroughly. BRIEF DESCRIPTION OF THE DRAWINGS

[0020] Figure 1 It is a cross-sectional view of the reaction device of the present invention.

[0021] In the figure, there are a shell 1, a membrane catalytic reaction unit 2, a hot water jacket 3, a liquid inlet 4, a liquid outlet 5, a static mixer 6, a partition 7, a filter membrane 8, a filter membrane cavity 9, a catalyst 10, an alkyl triacetone oxime silane preheater 11 and an alkyl trimethoxy silane preheater 12. DETAILED DESCRIPTION

[0022] The present invention will be further described below in conjunction with the embodiments.

[0023] Embodiment 1: like Figure 1 As shown, a reaction device comprises a shell 1 and a membrane catalytic reaction unit 2 arranged in the shell, a hot water jacket 3 is provided on the shell, a water inlet and a water outlet are provided on the hot water jacket, the water inlet and the water outlet are connected to a water heater, a liquid inlet 4 is provided at the bottom of the shell, the liquid inlet is connected to a static mixer 6, the static mixer is connected to an alkyl triacetone oxime silane preheater 11 and an alkyl trimethoxy silane preheater 12, a liquid outlet 5 is provided at the top of the shell, the liquid outlet is connected to an intermediate tank, and 12 layers of partitions 7 are provided in the shell, and the partition area is 1m 2 The spacing between adjacent partitions is 50 mm. A filter membrane 8 is fixed on the partition, and the filter membrane is a PVDF membrane (the pore size of the filter membrane is 0.1 μm). The filter membranes between adjacent partitions form a filter membrane cavity 9. A catalyst 10 is arranged in the filter membrane cavity. The particle size of the catalyst is 50 μm, and the catalyst is a strong base microsphere catalyst.

[0024] A method for continuously producing alkyl methoxyacetone oxime silane using the above-mentioned reaction device comprises the following steps: preheating methyl triacetone oxime silane to 60°C in an alkyl triacetone oxime silane preheater, preheating methyl trimethoxy silane to 60°C in an alkyl trimethoxy silane preheater, pumping the preheated methyl triacetone oxime silane and methyl trimethoxy silane into a static mixer at a molar ratio of 2:1 to mix evenly to form a mixed material, pumping the mixed material into the bottom of the shell of the reaction device through a liquid inlet, the mixed material enters the membrane catalytic reaction unit at the bottom to contact with the catalyst and react, the membrane catalytic reaction unit at the bottom is filled and enters the upper membrane catalytic reaction unit adjacent to it, and after entering the membrane catalytic reaction units step by step, it is ensured that the mixed liquid stays in the membrane catalytic reactor for 1 to 2 hours, and the reaction product reaches the top of the shell and enters the intermediate tank through the liquid outlet for standby.

[0025] Embodiment 2: like Figure 1As shown, a reaction device comprises a shell 1 and a membrane catalytic reaction unit 2 arranged in the shell, a hot water jacket 3 is provided on the shell, a water inlet and a water outlet are provided on the hot water heat jacket, the water inlet and the water outlet are connected to a water heater, a liquid inlet 4 is provided at the bottom of the shell, the liquid inlet is connected to a static mixer 6, the static mixer is connected to an alkyl triacetone oxime silane preheater and an alkyl trimethoxy silane preheater, a liquid outlet 5 is provided at the top of the shell, the liquid outlet is connected to an intermediate tank, and 50 layers of partitions 7 are provided in the shell, and the partition area is 1m 2 The spacing between adjacent partitions is 10 mm. A filter membrane 8 is fixed on the partition, and the filter membrane is a PVDF membrane (the pore size of the filter membrane is 2 μm). The filter membranes between adjacent partitions form a filter membrane cavity 9. A catalyst 10 is arranged in the filter membrane cavity. The particle size of the catalyst is 10 μm, and the catalyst is a strong base microsphere catalyst.

[0026] A method for continuously producing alkyl methoxyacetone oxime silane using the above-mentioned reaction device comprises the following steps: preheating methyl triacetone oxime silane to 60°C in an alkyl triacetone oxime silane preheater, preheating methyl trimethoxy silane to 60°C in an alkyl trimethoxy silane preheater, pumping the preheated methyl triacetone oxime silane and methyl trimethoxy silane into a static mixer at a molar ratio of 2:1 to mix evenly to form a mixed material, pumping the mixed material into the bottom of the shell of the reaction device through a liquid inlet, the mixed material enters the membrane catalytic reaction unit at the bottom to contact with the catalyst and react, the membrane catalytic reaction unit at the bottom is filled and enters the upper membrane catalytic reaction unit adjacent to it, and after entering the membrane catalytic reaction units step by step, it is ensured that the mixed liquid stays in the membrane catalytic reactor for 1 to 2 hours, and the reaction product reaches the top of the shell and enters the intermediate tank through the liquid outlet for standby.

[0027] Embodiment 3: like Figure 1 As shown, a reaction device comprises a shell 1 and a membrane catalytic reaction unit 2 arranged in the shell, a hot water jacket 3 is provided on the shell, a water inlet and a water outlet are provided on the hot water heat jacket, the water inlet and the water outlet are connected to a water heater, a liquid inlet 4 is provided at the bottom of the shell, the liquid inlet is connected to a static mixer 6, the static mixer is connected to an alkyl triacetone oxime silane preheater and an alkyl trimethoxy silane preheater, a liquid outlet 5 is provided at the top of the shell, the liquid outlet is connected to an intermediate tank, and 6 layers of partitions 7 are provided in the shell, and the partition area is 1m 2 The spacing between adjacent partitions is 100 mm. A filter membrane 8 is fixed on the partition, and the filter membrane is a PVDF membrane (the pore size of the filter membrane is 5 μm). The filter membranes between adjacent partitions form a filter membrane cavity 9. A catalyst 10 is arranged in the filter membrane cavity. The particle size of the catalyst is 100 μm, and the catalyst is a strong base microsphere catalyst.

[0028] A method for continuously producing alkyl methoxyacetone oxime silane using the above-mentioned reaction device comprises the following steps: preheating methyl triacetone oxime silane to 60°C in an alkyl triacetone oxime silane preheater, preheating methyl trimethoxy silane to 60°C in an alkyl trimethoxy silane preheater, pumping the preheated methyl triacetone oxime silane and methyl trimethoxy silane into a static mixer at a molar ratio of 2:1 to mix evenly to form a mixed material, pumping the mixed material into the bottom of the shell of the reaction device through a liquid inlet, the mixed material enters the membrane catalytic reaction unit at the bottom to contact with the catalyst and react, the membrane catalytic reaction unit at the bottom is filled and enters the upper membrane catalytic reaction unit adjacent to it, and after entering the membrane catalytic reaction units step by step, it is ensured that the mixed liquid stays in the membrane catalytic reactor for 1 to 2 hours, and the reaction product reaches the top of the shell and enters the intermediate tank through the liquid outlet for standby.

[0029] Embodiment 4: like Figure 1 As shown, a reaction device comprises a shell 1 and a membrane catalytic reaction unit 2 arranged in the shell, a hot water jacket 3 is provided on the shell, a water inlet and a water outlet are provided on the hot water jacket, the water inlet and the water outlet are connected to a water heater, a liquid inlet 4 is provided at the bottom of the shell, the liquid inlet is connected to a static mixer 6, the static mixer is connected to an alkyl triacetone oxime silane preheater and an alkyl trimethoxy silane preheater, a liquid outlet 5 is provided at the top of the shell, the liquid outlet is connected to an intermediate tank, and 12 layers of partitions 7 are provided in the shell, and the partition area is 1m 2 The spacing between adjacent partitions is 50 mm. A filter membrane 8 is fixed on the partition, and the filter membrane is a PVDF membrane (the pore size of the filter membrane is 2 μm). The filter membranes between adjacent partitions form a filter membrane cavity 9. A catalyst 10 is arranged in the filter membrane cavity. The particle size of the catalyst is 50 μm, and the catalyst is a strong base microsphere catalyst.

[0030] A method for continuously producing alkyl methoxyacetone oxime silane using the above-mentioned reaction device comprises the following steps: preheating vinyl triacetone oxime silane to 60°C in an alkyl triacetone oxime silane preheater, preheating vinyl trimethoxy silane to 60°C in an alkyl trimethoxy silane preheater, pumping the preheated vinyl triacetone oxime silane and vinyl trimethoxy silane into a static mixer at a molar ratio of 2:1 to mix them evenly to form a mixed material, pumping the mixed material into the bottom of the shell of the reaction device through a liquid inlet, the mixed material enters the membrane catalytic reaction unit at the bottom to contact with the catalyst and react, the membrane catalytic reaction unit at the bottom is filled and enters the upper membrane catalytic reaction unit adjacent to it, and after entering the membrane catalytic reaction units step by step in sequence, it is ensured that the mixed liquid stays in the membrane catalytic reactor for 1 to 2 hours, and the reaction product reaches the top of the shell and enters the intermediate tank through the liquid outlet for standby.

[0031] Comparative Example 1: Compared with Example 1, Comparative Example 1 adopted an intermittent production process.

[0032] Comparative Example 2: Compared with Example 1, the spacing of the membrane catalytic reaction units in Comparative Example 2 is too large, the spacing between adjacent partitions is 200 mm, the number of partitions is 4 layers, and other conditions are the same as in Example 1.

[0033] Comparative Example 3: Compared with Example 1, the particle size of the catalyst in Comparative Example 3 is too large. The particle size of the catalyst is 200 μm, and the other conditions are the same as those in Example 1.

[0034] Comparative Example 4: Compared with Example 1, the particle size of the catalyst in Comparative Example 4 is too small, the catalyst particle size is 2 μm, and the other conditions are the same as those in Example 1.

[0035] Comparative Example 5: Compared with Example 1, the filtration accuracy of the filter membrane in Comparative Example 5 is too large. The filtration accuracy of the filter membrane is 10 μm, and the other conditions are the same as those in Example 1.

[0036] Comparative Example 6: Compared with Example 1, the filtration accuracy of the filter membrane in Comparative Example 6 is too small, the filtration accuracy of the filter membrane is 0.05 μm, and the other conditions are the same as those in Example 1.

[0037] Test example: The alkylmethoxyacetoneoxime silane products obtained in Examples 1 to 4 and Comparative Examples 1 to 6 were tested, and the test items included conversion rate, chromaticity and production efficiency; The test results are shown in Table 1, in which A is the product conversion rate (%), B is the product chromaticity (APHA), C is the product appearance, D is the alkyltrimethoxysilane content in the product (w%), E is the alkyltriacetoneoximesilane content in the product (w%), and F is the alkylmethoxyacetoneoximesilane content in the product (w%); G is the production efficiency (Kg / day); Table 1 Test results condition A B C D E F G Example 1 Continuous production 97.7 20 Colorless and transparent 0.61 1.82 96.57 11520 Example 2 Continuous production 99.1 20 Colorless and transparent 0.20 0.74 97.06 11520 Example 3 Continuous production 94.5 20 Colorless and transparent 2.52 8.93 87.55 11520 Example 4 Continuous production 97.7 20 Colorless and transparent 0.98 3.47 94.55 11520 Comparative Example 1 Batch production process 35 45 Light yellow, slightly turbid 8.09 51.48 39.43 \ Comparative Example 2 The spacing between partitions is too large 82.3 20 Colorless and transparent 3.89 13.79 81.32 11520 Comparative Example 3 Catalyst particle size is too large 86.3 20 Colorless and transparent 3.01 10.67 85.32 11520 Comparative Example 4 Catalyst particle size is too small \ 20 Colorless and transparent 0.18 0.53 98.29 2400 Comparative Example 5 The filter membrane filtration accuracy is too large 96.5 20 Slightly turbid 0.78 2.73 95.47 11520 Comparative Example 6 The filter membrane filtration accuracy is too small \ \ \ \ \ \ \ As shown in Table 1, Examples 1 to 4 are technical solutions for continuously producing alkyl triacetone oxime silane and alkyl trimethoxy silane using the continuous production method of alkyl methoxy acetone oxime silane provided by the present invention. The results show that the product conversion rate of the alkyl methoxy acetone oxime silane produced can reach a maximum of 99.1%, the product chromaticity is 20, the color is colorless and transparent, the alkyl trimethoxy silane content in the product can reach a minimum of 0.2w%, and the alkyl triacetone oxime silane content in the product can reach a minimum of 0. .74w%, the content of alkyl methoxyacetone oxime silane in the product can reach up to 97.06w%, and the production efficiency of the product can reach 11520Kg / day. The above results show that the method provided by the present invention has a fast reaction rate, a short reaction cycle, a high conversion rate of alkyl methoxyacetone oxime silane product, continuous production, and high production efficiency. The obtained product has a high content of alkyl methoxyacetone oxime silane, extremely low contents of alkyl triacetone oxime silane and alkyl trimethoxy silane, high chromaticity, colorless and transparent, and excellent product quality.

[0038] Comparative Example 1 adopts the intermittent reaction in the prior art. The results of Comparative Example 1 show that the conversion rate of alkyl methoxyacetone oxime silane in the product obtained by the intermittent production process after two hours of reaction is only 35%, and the product conversion rate is significantly lower than that of Examples 1 to 4. The chromaticity of the product is 45, and the color is light yellow and slightly turbid. Compared with the products obtained in Examples 1 to 4, the product chromaticity of Comparative Example 1 is high, there are turbidities, and the product quality is poor. In addition, due to the poor quality of the product after two hours of reaction in the intermittent process, it is usually necessary to extend the reaction time to 8 hours before the conversion rate in the product can reach 95%. Although the conversion rate of the product is increased to a qualified level, the chromaticity of the product will exceed 100. The quality of the product is extremely poor and needs to be filtered and decolorized before it can be made into a product with better quality. Therefore, the production efficiency of the intermittent production process is only 2400Kg / day, and the production efficiency of the intermittent production process is significantly lower than the production efficiency of Examples 1 to 4.

[0039] Comparative Examples 2 and 3 are technical solutions in which the partition spacing is too large and the catalyst particle size is too large, respectively. The results of Comparative Examples 2 and 3 show that the product conversion rates are both lower than 90%, and the low product conversion rate cannot obtain high-quality products.

[0040] Comparative Example 4 is a technical solution in which the catalyst particle size is too small. In actual operation of Comparative Example 4, it was found that the equipment pressure exceeded 0.4Mpa after 2 hours of reaction, causing equipment blockage and making it impossible to continue production.

[0041] Comparative Example 5 is a technical solution in which the filter membrane precision is too large. The results of Comparative Example 5 show that the liquid in the product is slightly turbid, resulting in reduced product quality.

[0042] Comparative Example 6 is a technical solution in which the filter membrane precision is too small. In the actual operation of Comparative Example 6, the equipment builds up pressure quickly, and when the pressure exceeds 0.4Mpa, the equipment is clogged and cannot produce continuously.

[0043] The above description is only a preferred embodiment of the present invention and does not limit the present invention in any way. Any simple modification, change and equivalent transformation made to the above embodiment based on the technical essence of the present invention still falls within the protection scope of the technical solution of the present invention.

Claims

1. A method for continuously producing alkylmethoxyacetoneoxime silane, characterized in that: The following steps are involved: Alkyl triacetone oxime silane and alkyl trimethoxy silane are preheated and then injected into a membrane catalytic reaction unit for reaction to obtain alkyl methoxy acetone oxime silane. The membrane catalytic reaction unit comprises a filter membrane cavity and a catalyst arranged in the filter membrane cavity. The catalyst is a strong base microsphere catalyst.

2. The method for continuous production of alkylmethoxyacetoneoximesilane according to claim 1, characterized in that: The filtration accuracy of the filter membrane cavity is 0.1-5 μm, and the particle size of the catalyst is 10-100 μm.

3. The method for continuous production of alkylmethoxyacetoneoximesilane according to claim 1 or 2, characterized in that: The alkyl triacetone oxime silane is one of methyl triacetone oxime silane and vinyl triacetone oxime silane.

4. The method for continuously producing alkylmethoxyacetoneoximesilane according to claim 1 or 2, characterized in that: The alkyltrimethoxysilane is one of methyltrimethoxysilane and vinyltrimethoxysilane.

5. The method for continuous production of alkylmethoxyacetoneoximesilane according to claim 1, characterized in that: The reaction temperature is 50-60°C, the reaction pressure is 0.1-0.4 MPa, and the material residence time of the reaction is 1-2 h.

6. A reaction device, characterized in that: It comprises a reaction shell (1) and a plurality of membrane reaction modules (2) arranged in the shell, wherein the membrane reaction modules are the membrane reaction modules described in claim 1.

7. The reaction device according to claim 6, characterized in that: The reaction shell is provided with a hot water jacket (3).

8. The reaction device according to claim 6, characterized in that: The reaction shell further comprises a liquid inlet (4) and a liquid outlet (5), the liquid inlet being connected to a mixer (6), and the mixer being connected to an alkyl triacetone oxime silane preheating device and an alkyl trimethoxy silane preheating device.

9. The reaction device according to claim 6, characterized in that: A plurality of partitions (7) are arranged in the reaction shell, and the membrane reaction module is located in the space formed by adjacent partitions.

10. The reaction device according to claim 9, characterized in that: The partition is a stainless steel mesh plate.

Images