Organic silicon slurry residue treatment system and treatment method thereof

Abstract

The invention discloses an organic silicon slurry slag treatment system and a treatment method thereof, the organic silicon slurry slag treatment system is used for treating slurry slag generated in a methylchlorosilane synthesis process, the slurry slag comes from a reevaporator of a washing process, and the organic silicon slurry slag treatment system comprises a flash evaporation unit, a solid-liquid separation unit and an evaporation separation unit; the flash evaporation unit is connected with the re-evaporator through a pipeline, slurry residues are suitable for being discharged to the flash evaporation unit, and the flash evaporation unit is provided with a monomer feeding port; the solid-liquid separation unit is connected with the flash evaporation unit through a pipeline, and slurry residues in the flash evaporation unit are conveyed to the solid-liquid separation unit through a pump or pressure; the evaporation separation unit is connected with a liquid mixture outlet of the solid-liquid separation unit through a pipeline, the liquid mixture is separated by the evaporation separation unit to obtain methyl chlorosilane monomers, and the methyl chlorosilane monomers are suitable for returning to the flash evaporation unit. The treatment system provided by the invention is beneficial to improving the stability and safety of slurry residue treatment, reducing the labor cost during production and the post-treatment cost, and further improving the slurry residue treatment efficiency.

Description

Technical Field

[0001] The present application relates to the field of organosilicon, and in particular to an organosilicon slurry treatment system and a treatment method thereof. Background Art

[0002] At present, the synthesis process of organosilicon involves reacting solid silicon powder with gaseous chloromethyl in the presence of a catalyst to generate methylchlorosilane. During the reaction, the generated gaseous methylchlorosilane mixes with the unreacted chloromethyl and enters the cyclone separation system with the silicon powder. The cyclone separation system can remove most of the silicon powder, and the remaining silicon powder and methylchlorosilane enter the scrubber for further treatment. During the scrubbing process, the silicon powder and high-boiling methylchlorosilane discharged from the scrubber enter the re-evaporator, which needs to be discharged from time to time. This part of the product is called slurry residue.

[0003] At present, pulp residue is mainly transferred to the pulp residue treatment section by mobile tanks for direct hydrolysis treatment. However, in this process, the mobile tanks need to be disassembled and assembled, which increases the workload and safety risks of on-site workers. Since pulp residue contains a large amount of active metals, it is easy to spontaneously combust when it is exposed to air or moisture, or react with moisture in the air to generate hydrogen chloride gas, releasing corrosive hydrochloric acid mist, posing a serious threat to the environment and the safety of operators. Therefore, it is particularly important to optimize the pulp residue treatment process. Summary of the invention

[0004] One purpose of the present application is to provide a silicone slurry treatment system and a treatment method thereof, which are conducive to enhancing the stability and safety of slurry treatment and improving production efficiency.

[0005] Another object of the present application is to provide a silicone slurry treatment system and a treatment method thereof, which are conducive to reducing production costs and further reducing the generation of hazardous waste.

[0006] In order to achieve the above purpose, the technical solution adopted in the present application is to provide an organosilicon slurry treatment system for treating slurry produced by a methylchlorosilane synthesis process, wherein the slurry comes from a re-evaporator of a washing process, and the organosilicon slurry treatment system comprises a flash unit, a solid-liquid separation unit and an evaporation separation unit; the flash unit is connected to the re-evaporator via a pipeline, the slurry is suitable for being discharged to the flash unit, the flash unit has a monomer feeding port, and methylchlorosilane monomer is suitable for being added to the flash unit through the monomer feeding port to adjust the solid content of the slurry in the flash unit; the solid-liquid separation unit is connected to the flash unit via a pipeline The pulp in the flash unit is conveyed to the solid-liquid separation unit by a pump or pressure, and a solid mixture and a liquid mixture are obtained after solid-liquid separation. The solid-liquid separation unit includes a solid mixture outlet and a liquid mixture outlet; the evaporation separation unit is connected to the liquid mixture outlet of the solid-liquid separation unit via a pipeline, and the liquid mixture is separated by the evaporation separation unit to obtain methylchlorosilane monomer. The evaporation separation unit includes a methylchlorosilane monomer outlet, and the methylchlorosilane monomer outlet is connected to the flash unit, so that the methylchlorosilane monomer obtained by the evaporation separation unit is suitable for returning to the flash unit.

[0007] In one embodiment, a stirring paddle is provided in the flash evaporation unit, and the stirring paddle is driven by a driving motor. The switch of the monomer feeding port is communicated with the driving motor, so that the solid content of the pulp residue in the flash evaporation unit is calculated according to the current change of the driving motor, and then the opening and closing of the monomer feeding port are controlled; when the solid content of the pulp residue in the flash evaporation unit is calculated to exceed 15%, the monomer feeding port is opened; when the solid content of the pulp residue in the flash evaporation unit is calculated to be less than 5%, the monomer feeding port is closed.

[0008] In one embodiment, the flash evaporation unit is further provided with a temperature control device for maintaining the flash evaporation unit at 10°C to 20°C.

[0009] In one embodiment, the solid-liquid separation unit includes a standing tank and a filter. The slurry from the flash unit is first stood in the standing tank for stratification, the upper layer of liquid is transported into the evaporation separation unit, and the lower layer of mixture is then transported into the filter. The filter further performs solid-liquid separation, and the separated liquid is transported into the evaporation separation unit.

[0010] In one embodiment, the solid-liquid separation unit further includes a buffer tank, and the buffer tank is arranged between the flash unit and the static tank.

[0011] In one embodiment, the evaporation separation unit further includes a high boiling point product outlet and an ultra-high boiling point product outlet, the ultra-high boiling point product having a boiling point exceeding 180°C is discharged from the ultra-high boiling point product outlet, the high boiling point product having a boiling point between the methylchlorosilane monomer and the ultra-high boiling point product is discharged from the high boiling point product outlet, the high boiling point product is suitable for being transported to a subsequent cracking device, the ultra-high boiling point product is suitable for being transported to a subsequent hydrolysis device, and the solid mixture obtained by the solid-liquid separation unit is also suitable for being transported to the hydrolysis device.

[0012] According to another aspect of the present application, a method for treating organosilicon slurry residue is also provided, comprising the following steps:

[0013] S1, discharging the pulp residue obtained by washing into a flash unit, and adding methylchlorosilane monomer into the flash unit so that the solid content of the pulp residue in the flash unit does not exceed 20%;

[0014] S2, pumping or pressure-transporting the slurry in the flash unit to a solid-liquid separation unit to separate a solid mixture and a liquid mixture;

[0015] S3, evaporating and separating the liquid mixture, recovering the methylchlorosilane monomer and replenishing it to the flash unit.

[0016] In one embodiment, in step S1, methylchlorosilane monomer is added to the flash unit so that the solid content of the pulp in the flash unit is maintained between 5% and 15%, and the temperature is maintained at 10°C to 20°C.

[0017] In one embodiment, in step S2, when pressure is used to transport the slurry in the flash unit, the pressure is maintained at 0.5MPa to 0.7MPa; the solid-liquid separation unit uses a static stratification method to perform primary solid-liquid separation, and then uses a filter to perform secondary solid-liquid separation on the lower layer mixture of the static stratification to obtain the solid mixture with a solid content of not less than 85%.

[0018] In one embodiment, in step S3, the liquid mixture is evaporated and separated to obtain methylchlorosilane monomer, ultra-high boiling point product with a boiling point exceeding 180°C and high boiling point product with a boiling point between the methylchlorosilane monomer and the ultra-high boiling point product, and the ultra-high boiling point product and the solid mixture in step S2 are transported to a subsequent hydrolysis device for hydrolysis, and the high boiling point product is transported to a subsequent cracking device for cracking.

[0019] Compared with the prior art, the beneficial effects of this application are:

[0020] (1) The present invention provides an organosilicon slurry treatment system and a treatment method thereof, which enhances the stability and safety of the organosilicon synthesis process by performing the organosilicon slurry treatment process in a closed environment, thereby further improving the safety of production.

[0021] (2) The present invention provides a silicone slurry residue treatment system and treatment method, which facilitates the transportation and treatment of slurry residues by recycling low-boiling point monomers, reduces the generation of hazardous waste, and further reduces the labor cost consumed during production and the cost of post-processing. BRIEF DESCRIPTION OF THE DRAWINGS

[0022] Figure 1 This is a schematic diagram of the structure of an organosilicon slurry treatment system in one embodiment of the present application.

[0023] In the figure: 100, fluidized bed; 200, cyclone separation unit; 300, re-evaporator; 400, washing tower; 500, flash unit; 510, monomer feeding port; 600, separation tower; 610, standing tank; 620, filter; 630, buffer tank; 700, cracking equipment; 800, hydrolysis equipment; 900, condensation equipment; 910, post-system equipment; 920, reflux tank; 930, tail gas treatment equipment. DETAILED DESCRIPTION

[0024] Below, the present application is further described in conjunction with specific implementation methods. It should be noted that, under the premise of no conflict, the various embodiments or technical features described below can be arbitrarily combined to form new embodiments.

[0025] In the description of the present application, it should be noted that directional words, such as the terms "center", "lateral", "longitudinal", "length", "width", "thickness", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inside", "outside", "clockwise", "counterclockwise", etc., indicating directions and positional relationships are based on the directions or positional relationships shown in the accompanying drawings, which are only for the convenience of narrating the present application and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and cannot be understood as limiting the specific scope of protection of the present application.

[0026] It should be noted that the terms "first", "second", etc. in the description and claims of the present application are used to distinguish similar objects, and are not necessarily used to describe a specific order or sequence.

[0027] The terms "including" and "having" and any variations thereof in the specification and claims of this application are intended to cover non-exclusive inclusions. For example, a process, method, system, product or apparatus comprising a series of steps or units is not necessarily limited to those steps or units explicitly listed, but may include other steps or units not explicitly listed or inherent to these processes, methods, products or apparatuses.

[0028] The present application aims to provide a system for treating organic silicon slurry residue, which is used to treat slurry residue produced by a methylchlorosilane synthesis process. Figure 1 As shown, the front-end process of the organosilicon slurry treatment system generally includes a fluidized bed 100, a cyclone separation unit 200, a washing tower 400 and a re-evaporator 300. The product of the methylchlorosilane synthesis reaction enters the cyclone separation unit 200 from the outlet of the fluidized bed 100. After most of the silicon powder is separated, the remaining product enters the washing tower 400. The washed methylchlorosilane monomer is output from the top of the tower and enters the subsequent process. The re-evaporator 300 is used to ensure that the liquid in the tower can continue to evaporate to form steam, so that the liquid can be continuously circulated and refluxed. The slurry generated during the operation of the re-evaporator 300 is transported to the organosilicon slurry treatment system of the present application through a pipeline. It is worth mentioning that the solid content of the slurry discharged from the re-evaporator 300 is generally 30% to 60%.

[0029] The organosilicon slurry treatment system includes a flash evaporation unit 500, a solid-liquid separation unit and an evaporation separation unit.

[0030] The flash unit 500 is connected to the re-evaporator 300 via a pipeline, and the pulp residue of the re-evaporator 300 is suitable for being discharged to the flash unit 500. The flash unit 500 has a monomer feeding port 510, and the methylchlorosilane monomer is suitable for being added into the flash unit 500 through the monomer feeding port 510 to dilute the pulp residue therein, improve the fluidity of the pulp residue in the flash unit 500, and facilitate the subsequent transportation of the pulp residue. Preferably, the solid content of the pulp residue in the flash unit 500 is controlled below 20%. It is worth mentioning that the methylchlorosilane monomer in the pulp residue may be evaporated in the flash unit 500, and the evaporated methylchlorosilane monomer is condensed and then returned to the flash unit 500, and the tail gas generated in the process enters the tail gas treatment equipment 930.

[0031] The solid-liquid separation unit is connected to the flash unit 500 via a pipeline. The slurry in the flash unit 500 is pumped or pressure-transported to the solid-liquid separation unit. After solid-liquid separation, a solid mixture and a liquid mixture are obtained, wherein the solid mixture mainly contains silicon powder and may also contain 5% to 15% of high-boiling substances; the liquid mixture includes methylchlorosilane monomer and high-boiling methylchlorosilane. The solid mixture subsequently enters the hydrolysis device 800 for hydrolysis, and the liquid mixture enters the evaporation separation unit to separate methylchlorosilane products with different boiling points. Furthermore, the solid-liquid separation unit includes a solid mixture outlet and a liquid mixture outlet.

[0032] The liquid mixture outlet of the evaporation separation unit is connected to the liquid mixture outlet of the solid-liquid separation unit through a pipeline, and the liquid mixture is separated by the evaporation separation unit to obtain methylchlorosilane monomer. The evaporation separation unit includes a methylchlorosilane monomer outlet, and the methylchlorosilane monomer outlet is connected to the flash unit 500, so that the methylchlorosilane monomer obtained by the evaporation separation unit is suitable for returning to the flash unit 500. It is worth mentioning that a condensation device 900 can also be set between the methylchlorosilane monomer outlet and the flash unit 500.

[0033] The present application dilutes the pulp residue by recycling low-boiling monomers, which is beneficial to the transportation and post-processing of the pulp residue in a closed environment. It is understandable that when the pulp residue is exposed to air or in contact with a moisture environment, it is prone to spontaneous combustion or release of corrosive hydrochloric acid mist, which poses a serious threat to the safety of the environment and operators. Therefore, the present application provides a processing system that is convenient for the transportation and post-processing of the pulp residue in a closed environment. Through the flash unit 500, the processing system is detected and regulated in real time, which improves the safety and stability of the operation in the synthesis process, further reduces the generation of hazardous waste, reduces the labor cost consumed during production and the cost of post-processing, and is conducive to improving production efficiency.

[0034] In one embodiment, a stirring paddle is provided in the flash unit 500, and the stirring paddle is driven by a driving motor. The switch of the monomer feeding port 510 is connected to the driving motor in communication, so that the solid content of the pulp residue in the flash unit 500 is measured according to the current change of the driving motor, and then the opening and closing of the monomer feeding port 510 is controlled. The monomer feeding port 510 can be connected to the methylchlorosilane monomer storage tank, and the switch is arranged between the monomer feeding port 510 and the methylchlorosilane monomer storage tank. The stirring paddle is provided to enhance the full mixing of the added monomer and the pulp residue, further enhance the fluidity of the pulp residue to be treated, and then facilitate the next step of transportation and post-processing. It can be understood that by measuring the solid content of the pulp residue in the flash unit 500 in real time, and then controlling the degree of monomer feeding, it is prevented that too much monomer is added to cause the solid content of the pulp residue to be too low, which reduces the processing efficiency and further increases the consumption cost in the processing process. Furthermore, by adding low-boiling-point methylchlorosilane to the pulp with higher viscosity, the fluidity of the pulp is increased, the clogging of the pulp in the equipment is reduced, and further processing is facilitated, thereby improving the processing efficiency of the pulp.

[0035] In one embodiment, when the solid content of the pulp residue in the flash unit 500 is measured to be more than 15%, the monomer feed port 510 is opened to add monomer to the flash unit 500; when the solid content of the pulp residue in the flash unit 500 is measured to be less than 5%, the monomer feed port 510 is closed. It can be understood that the solid content of the pulp residue input into the solid-liquid separation unit for treatment should not be too large, otherwise it is easy to cause pipeline blockage and equipment damage. The solid content of the undiluted pulp residue can reach 30% to 50%. In this case, it is basically impossible to transport the pulp residue by pumping or pressure transportation. Therefore, the prior art uses a mobile tank to transfer the pulp residue. In addition, the use of low-boiling point monomers to dilute the pulp residue can reduce the loss of high-boiling substances and reduce energy consumption in the production process. This not only improves economic benefits, but also further reduces environmental pollution. On the other hand, since the pulp residue has certain dangers during the treatment process, the dilution effect can effectively improve the safety and stability of the pulp residue treatment.

[0036] In one embodiment, the flash unit 500 is further provided with a temperature control device for maintaining the flash unit 500 at 10°C to 20°C. Specifically, the temperature of the flash unit 500 is maintained at 10°C, 11°C, 12°C, 13°C, 14°C, 15°C, 16°C, 17°C, 18°C, 19°C and 20°C. The appropriate flash temperature is conducive to ensuring that the pulp residue maintains good fluidity, stability and safety during the subsequent transportation process. It is understandable that when the flash temperature is too high, it is easy to cause safety problems. For example, at high temperatures, the pulp residue may spontaneously combust, resulting in fire accidents. Excessively high flash temperatures will also increase the volatility of the monomer and increase the overall energy consumption of the processing system. Therefore, it is not advisable to use a higher flash temperature during the processing of the pulp residue. On the other hand, when the flash temperature is too low, the viscosity of the pulp residue is relatively large, which is not conducive to transportation and may even be prone to blockage, increasing the danger in the production process.

[0037] In one embodiment, the solid-liquid separation unit includes a standing tank 610 and a filter 620. The slurry residue of the flash unit 500 is firstly standing and layered in the standing tank 610, and the upper layer of liquid is transported to the evaporation separation unit, and the lower layer of the mixture is then transported to the filter 620. The filter 620 further performs solid-liquid separation, and the separated liquid is transported to the evaporation separation unit. By setting the standing tank 610 and the filter 620, the solid components in the slurry residue are effectively filtered out. Among them, the solid mixture separated by the filter 620 is transported to the hydrolysis equipment 800 for treatment, and the liquid mixture obtained by the standing tank 610 and the filter 620 is transported to the evaporation separation unit through the liquid mixture outlet for reuse, thereby increasing the utilization rate of by-products and economic benefits, and realizing the comprehensive utilization of resources and maximization of economic benefits.

[0038] In one embodiment, the solid-liquid separation unit further includes a buffer tank 630, which is disposed between the flash unit 500 and the standing tank 610. It is understandable that since the standing tank 610 needs a certain standing time for solid-liquid stratification treatment, and it is necessary to ensure that the standing tank 610 is not subjected to strong external effects, the buffer tank 630 is provided to control the flow rate of the slurry to be treated input into the standing tank 610, so that a suitable amount of slurry for stratification treatment can be input into the standing tank 610 within a certain period of time, thereby further improving the purity of solid-liquid separation and enhancing the efficiency of the post-treatment process.

[0039] In one embodiment, the evaporation separation unit further includes a high boiling point product outlet and an ultra-high boiling point product outlet. The ultra-high boiling point product with a boiling point exceeding 180°C is discharged from the ultra-high boiling point product outlet, and the high boiling point product with a boiling point between the methylchlorosilane monomer and the ultra-high boiling point product is discharged from the high boiling point product outlet. The high boiling point product is suitable for being transported to the subsequent cracking device 700, and the ultra-high boiling point product is suitable for being transported to the subsequent hydrolysis device 800. The solid mixture obtained by the solid-liquid separation unit is also suitable for being transported to the hydrolysis device 800.

[0040] Among them, since the recycling value of ultra-high boiling point products is not high, recycling them together with high boiling point products will also reduce the efficiency of high boiling point product cracking treatment, so they are directly input into the hydrolysis device 800 for treatment. Furthermore, by inputting the high boiling point products into the cracking device 700, not only the problem of by-product treatment is solved, but also a new source of raw materials is provided for the organosilicon industry, thereby efficiently converting by-products into valuable organosilicon products, realizing comprehensive utilization of resources and maximizing economic benefits.

[0041] It is understandable that the stability and safety of pulp and slag treatment can be increased by the treatment of the hydrolysis device 800, and the hydrolyzed product has the characteristic of being difficult to decompose, which is further beneficial to the stability and safety in storage and subsequent treatment. Furthermore, through the treatment of the hydrolysis device 800, metal elements such as copper are enriched in the solid hydrolyzate, which is beneficial to the subsequent recycling and utilization treatment, and improves the comprehensive utilization efficiency of resources in the entire treatment system, thereby enhancing economic benefits.

[0042] In one embodiment, the pressure of the slurry pressure of the flash unit 500 transported to the solid-liquid separation unit is controlled to be 0.5MPa to 0.7MPa. Specifically, the transportation pressure is 0.5MPa, 0.6MPa and 0.7MPa. It is understandable that when the transportation pressure is too high, it may increase the safety risk during the transportation of slurry, such as easily causing pipeline rupture or leakage, thereby causing pollution and harm to the production environment and operators. In other words, when the transportation pressure is too low, it is not conducive to the transportation of slurry with a certain viscosity, which in turn leads to slow transportation and reduces the efficiency of the slurry treatment system. Therefore, selecting an appropriate transportation pressure to participate in the transportation of slurry is conducive to increasing the transportation efficiency of the slurry and further increasing the efficiency of the slurry treatment system.

[0043] In one embodiment, the evaporation separation unit is a separation tower 600, and the methylchlorosilane monomer outlet at the top of the tower obtains the methylchlorosilane monomer, and the pressure at the top of the tower is 50kPa to 100kPa. The high boiling point product outlet is located in the middle of the separation tower 600, and the ultra-high boiling point product outlet is located at the bottom of the separation tower 600. It can be understood that, by providing the separation tower 600, the separation efficiency of methylchlorosilanes with different boiling points can be effectively improved, energy consumption can be further reduced, equipment corrosion and material loss can be reduced, and the purity of the separated product can be improved, which is conducive to increasing the efficiency of subsequent processing.

[0044] In one embodiment, the separation tower 600 further includes a high-removal tower and a low-removal tower. It is understandable that by combining the high-removal tower and the low-removal tower, ultra-high boiling point products and high boiling point products can be effectively separated. The high-removal tower mainly separates components with higher boiling points, while the low-removal tower separates components with lower boiling points. The separation equipment formed by the combination further realizes the efficient separation of methylchlorosilanes with different boiling points. Furthermore, compared with using a single distillation tower, the double-tower system can reduce the equipment investment cost while enhancing the purity of the separated product.

[0045] In one embodiment, the front-end process of the organosilicon slurry treatment system further includes a condensation device 900 and a reflux tank 920. The condensation device 900 is connected to the top of the washing tower 400. The reflux tank 920 is connected to the condensation device 900 and the washing tower 400 to condense the washing liquid and reflux it into the washing tower 400. The methylchlorosilane obtained by washing enters the post-system device 910.

[0046] According to another aspect of the present application, a method for treating organosilicon slurry residue is also provided, comprising the following steps:

[0047] S1, discharging the pulp residue obtained by washing into the flash unit 500, and adding methylchlorosilane monomer into the flash unit 500, so that the solid content of the pulp residue in the flash unit 500 does not exceed 20%;

[0048] S2, pumping or pressure-transporting the slurry in the flash unit 500 to a solid-liquid separation unit to separate a solid mixture and a liquid mixture;

[0049] S3, evaporating and separating the liquid mixture, recovering the methylchlorosilane monomer and replenishing it to the flash evaporation unit 500.

[0050] The method for treating silicone slurry provided in the present application can improve the safety and stability of operations in the synthesis process, further reduce the generation of hazardous waste, and reduce the labor cost consumed during production and the cost of post-processing, thereby helping to improve production efficiency and further improve economic benefits.

[0051] In one embodiment, in step S1, methylchlorosilane monomer is added to the flash unit 500 so that the solid content of the pulp in the flash unit 500 is maintained between 5% and 15%, and the temperature is maintained at 10°C to 20°C.

[0052] In one embodiment, in step S2, when pressure is used to transport the slurry in the flash unit 500, the pressure is maintained at 0.5MPa to 0.7MPa; the solid-liquid separation unit uses a static stratification method to perform primary solid-liquid separation, and then uses a filter 620 to perform secondary solid-liquid separation on the lower layer mixture of the static stratification to obtain a solid mixture with a solid content of not less than 85%.

[0053] In one embodiment, in step S3, the liquid mixture is evaporated and separated to obtain methylchlorosilane monomer, ultra-high boiling point products with a boiling point exceeding 180°C, and high boiling point products with a boiling point between the methylchlorosilane monomer and the ultra-high boiling point products. The ultra-high boiling point products and the solid mixture in step S2 are transported to a subsequent hydrolysis device 800 for hydrolysis, and the high boiling point products are transported to a subsequent cracking device 700 for cracking.

[0054] By adjusting the process parameters in the treatment method of silicone slurry, it is beneficial to improve the fluidity and transportation safety of the slurry material, achieve stable and safe treatment of the slurry material in a confined space, and produce various chemical by-products, further improve economic benefits, and improve the treatment efficiency of the entire silicone slurry treatment system.

[0055] The above describes the basic principles, main features and advantages of the present application. Those skilled in the art should understand that the present application is not limited by the above embodiments, and the above embodiments and the specification only describe the principles of the present application. The present application may have various changes and improvements without departing from the spirit and scope of the present application, and these changes and improvements fall within the scope of the present application for which protection is sought. The scope of protection claimed by the present application is defined by the attached claims and their equivalents.

Claims

1. An organosilicon slurry treatment system, used for treating slurry produced by a methylchlorosilane synthesis process, wherein the slurry comes from a re-evaporator of a washing process, characterized in that: The organosilicon slurry treatment system comprises a flash evaporation unit, a solid-liquid separation unit and an evaporation separation unit; The flash unit is connected to the re-evaporator via a pipeline, the pulp residue is suitable for being discharged to the flash unit, the flash unit has a monomer feeding port, and the methylchlorosilane monomer is suitable for being added into the flash unit through the monomer feeding port to dilute the pulp residue therein; The solid-liquid separation unit is connected to the flash unit via a pipeline, the slurry in the flash unit is transported to the solid-liquid separation unit by a pump or pressure, and a solid mixture and a liquid mixture are obtained after solid-liquid separation, and the solid-liquid separation unit includes a solid mixture outlet and a liquid mixture outlet; The evaporation separation unit is connected to the liquid mixture outlet via a pipeline, and the liquid mixture is separated by the evaporation separation unit to obtain methylchlorosilane monomer. The evaporation separation unit includes a methylchlorosilane monomer outlet, and the methylchlorosilane monomer outlet is connected to the flash unit, so that the methylchlorosilane monomer obtained by the evaporation separation unit is suitable for returning to the flash unit.

2. The organosilicon slurry treatment system according to claim 1, characterized in that: A stirring paddle is arranged in the flash evaporation unit, and the stirring paddle is driven by a driving motor. The switch of the monomer feeding port is connected to the driving motor for communication, so that the solid content of the pulp residue in the flash evaporation unit is calculated according to the current change of the driving motor, and then the opening and closing of the monomer feeding port are controlled; when the solid content of the pulp residue in the flash evaporation unit is calculated to exceed 15%, the monomer feeding port is opened; when the solid content of the pulp residue in the flash evaporation unit is calculated to be less than 5%, the monomer feeding port is closed.

3. The organosilicon slurry treatment system according to claim 1, characterized in that: The flash evaporation unit is also provided with a temperature control device for maintaining the flash evaporation unit at 10°C to 20°C.

4. The organosilicon slurry treatment system according to claim 1, characterized in that: The solid-liquid separation unit includes a standing tank and a filter. The slurry residue of the flash unit is firstly standing and layered in the standing tank, and the upper layer of liquid is transported to the evaporation separation unit, and the lower layer of mixture is then transported to the filter. The filter further performs solid-liquid separation, and the separated liquid is transported to the evaporation separation unit.

5. The organosilicon slurry treatment system according to claim 4, characterized in that: The solid-liquid separation unit further includes a buffer tank, which is arranged between the flash unit and the static tank.

6. The organosilicon slurry treatment system according to any one of claims 1 to 5, characterized in that: The evaporation separation unit also includes a high boiling point product outlet and an ultra-high boiling point product outlet. The ultra-high boiling point product with a boiling point exceeding 180°C is discharged from the ultra-high boiling point product outlet, and the high boiling point product with a boiling point between the methylchlorosilane monomer and the ultra-high boiling point product is discharged from the high boiling point product outlet. The high boiling point product is suitable for being transported to a subsequent cracking device, and the ultra-high boiling point product is suitable for being transported to a subsequent hydrolysis device. The solid mixture obtained by the solid-liquid separation unit is also suitable for being transported to the hydrolysis device.

7. A method for treating organosilicon slurry residue, characterized in that: The following steps are involved: S1, discharging the pulp residue obtained by washing into a flash unit, and adding methylchlorosilane monomer into the flash unit so that the solid content of the pulp residue in the flash unit does not exceed 20%; S2, pumping or pressure-transporting the slurry in the flash unit to a solid-liquid separation unit to separate a solid mixture and a liquid mixture; S3, evaporating and separating the liquid mixture, recovering the methylchlorosilane monomer and replenishing it to the flash unit.

8. The method for treating organosilicon slurry according to claim 7, characterized in that: In the step S1, methylchlorosilane monomer is added to the flash unit so that the solid content of the pulp in the flash unit is maintained between 5% and 15%, and the temperature is maintained at 10° C. to 20° C.

9. The method for treating organosilicon slurry according to claim 7, characterized in that: In the step S2, when the slurry in the flash unit is transported under pressure, the pressure is maintained at 0.5 MPa to 0.7 MPa; The solid-liquid separation unit uses a static stratification method to perform primary solid-liquid separation, and then uses a filter to perform secondary solid-liquid separation on the lower layer mixture of the static stratification to obtain the solid mixture with a solid content of not less than 85%.

10. The method for treating organosilicon slurry according to claim 7, characterized in that: In the step S3, the liquid mixture is evaporated and separated to obtain methylchlorosilane monomer, ultra-high boiling point product with a boiling point exceeding 180°C and high boiling point product with a boiling point between the methylchlorosilane monomer and the ultra-high boiling point product; the ultra-high boiling point product and the solid mixture in the step S2 are transported to a subsequent hydrolysis device for hydrolysis, and the high boiling point product is transported to a subsequent cracking device for cracking.

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