A method and system for recovering aluminum trichloride catalyst from chlorosilane disproportionation waste liquid

Abstract

The present invention provides a method and system for recovering aluminum trichloride catalyst from chlorosilane disproportionation waste liquid, belonging to the field of waste liquid treatment technology. The method comprises separating the chlorosilane disproportionation waste liquid by circulating filtration in combination with nitrogen purging, dissolving the high-boiling chlorosilane products coated on the surface of the aluminum trichloride catalyst in the obtained base slag with an organic solvent, and separating the obtained dissolved liquid by circulating filtration in combination with nitrogen purging to obtain the aluminum trichloride catalyst. The method and system of the present invention have a short operating process, flexible operation, low processing cost, no wastewater and noxious gas generation, significant environmental and economic benefits, and a catalyst recovery rate of over 93%, thus facilitating industrial promotion and implementation.

Description

Technical Field

[0001] The present invention relates to a chlorosilane disproportionation waste liquid treatment technology, and in particular to a method and system for recovering catalyst aluminum chloride from chlorosilane disproportionation waste liquid. Background Art

[0002] Aluminum trichloride, an excellent catalyst for the disproportionation of methyl and chlorine, is the only widely used methylchlorosilane disproportionation catalyst in industrial applications. Through the disproportionation reaction of chlorosilanes, it can convert low-value-added products such as monomethyltrichlorosilane, low-boiling products, high-boiling products, trimethylmonochlorosilane, and azeotropes produced during the methylchlorosilane production process into high-value-added, widely used dimethyldichlorosilane and trimethylmonochlorosilane. Because the high-boiling products produced during the disproportionation reaction encapsulate the aluminum trichloride catalyst, rendering it ineffective, the disproportionation reaction is a cyclical operation. After the disproportionation cycle is completed, the unit is shut down and the catalyst is discharged along with the generated waste high-boiling products. This process generates a large amount of wastewater, HCl, aluminum ions, and other wastewater, which can pollute the land. Furthermore, the waste of catalyst also places significant pressure on environmental protection.

[0003] Chinese invention patent application CN108726484A discloses a chemical method for recovering a low-boiling-point disproportionation catalyst from organosilicon. The method involves hydrolyzing the disproportionation wastewater to release aluminum ions. The aqueous phase is then reacted with a strong base to convert the aluminum ions into a solid precipitate. Finally, the catalyst is neutralized with hydrochloric acid to produce aluminum trichloride, enabling catalyst recovery. However, due to the high use of acid and base in the recovery process, a large amount of wastewater is generated, resulting in high treatment costs. Furthermore, the catalyst recovery rate after several reactions needs to be further improved. Summary of the Invention

[0004] In order to solve the above problems, the present invention provides a method and system for recovering aluminum trichloride catalyst from chlorosilane disproportionation waste liquid.

[0005] To achieve the above object, the technical solution adopted by the present invention is:

[0006] A method for recovering aluminum trichloride catalyst from chlorosilane disproportionation waste liquid, the method comprising the following steps:

[0007] S1. Separating the chlorosilane disproportionation waste liquid into base slag and liquid high-boiling products by circulating filtration combined with nitrogen purging;

[0008] S2, mixing the base slag with an organic solvent, and using the organic solvent to stir and dissolve the high-boiling chlorosilanes coated on the surface of the catalyst aluminum chloride in the base slag to obtain a solution;

[0009] The organic solvent is at least one of benzene, carbon disulfide, carbon tetrachloride, petroleum ether, ethyl ether, methyl ethyl ether, dimethyl carbonate and diethyl carbonate;

[0010] S3, the dissolved liquid is separated by circulating filtration with nitrogen purge to obtain the catalyst aluminum chloride and the recovered solvent;

[0011] The recovered solvent is directly returned to step S2 for use as an organic solvent;

[0012] After the recovered solvent is recycled multiple times, the solvent tower is used for secondary solvent recovery.

[0013] Furthermore, in step S2, the amount of the organic solvent is 2 to 6 times the weight of the catalyst aluminum chloride added during the disproportionation reaction of the chlorosilane disproportionation waste liquid;

[0014] The stirring and dissolving temperature is room temperature and the time is 1 to 3 hours.

[0015] Furthermore, the base slag is dry base slag or wet base slag; the liquid content of the dry base slag is less than 45wt%; the liquid content of the wet base slag is 45-65wt%.

[0016] Furthermore, the base slag is dry base slag.

[0017] Furthermore, in step S1, the nitrogen pressure introduced during the nitrogen purge is 0.2-0.5 MPa, the temperature is room temperature, and the time is 0.5-2 h;

[0018] In step S3, the nitrogen pressure introduced during the nitrogen purge is 0.3-0.5 MPa, the temperature is 40-60° C., the time is 2-2.5 h, and the cooling temperature of the recovered solvent is lower than 15° C.

[0019] Furthermore, the extraction temperature of the solvent tower bottom is 130-150°C, the top temperature is 35-104°C, the bottom temperature is 130-150°C, the top gauge pressure is 0-0.2002MPa, the number of theoretical plates is 35, the reflux ratio is 5-15:1, the bottom liquid level is 50-90%, and the number of tower plates is 40.

[0020] A system for recovering aluminum trichloride catalyst from chlorosilane disproportionation waste liquid, the system comprising: a circulating filter device, a first cooler, a high-boiling substance storage device, a dissolving device, a second circulating filter device, a second cooler, a solvent intermediate buffer device, a solvent tower, a third cooler, and a solvent condensing device;

[0021] The bottom end of the circulating filter device is connected to the chlorosilane disproportionation device through a pipeline, and a nitrogen purge channel is provided at the bottom end of the circulating filter device;

[0022] The top of the circulating filtration device is connected to the chlorosilane disproportionation device, the first cooler, and the high boiling point storage device through pipelines;

[0023] The bottom end of the circulating filtration device is connected to the dissolving device;

[0024] The dissolving device is connected to the second circulating filtering device through a pipeline, and a nitrogen purge channel is provided at the bottom end of the second circulating filtering device;

[0025] The bottom end of the second circulating filtration device is connected to the catalyst receiving device;

[0026] The top of the second circulating filtration device is connected to the dissolving device, the second cooler, and the solvent intermediate buffer device through pipelines respectively;

[0027] The solvent intermediate buffer device is connected with the dissolving device and the middle part of the solvent tower through a pipeline;

[0028] The top of the solvent tower is connected to the third cooler and the solvent condensing device through pipelines in sequence.

[0029] Furthermore, a control valve F1 is provided on the pipeline connecting the top of the circulating filtration device and the chlorosilane disproportionation device;

[0030] A control valve F2 is provided on the pipe connecting the top of the circulating filtration device and the high-boiling material storage device;

[0031] A control valve F3 is provided on the pipeline connecting the top end of the circulating filter device and the first cooler.

[0032] Furthermore, a control valve F4 is provided on the pipeline connecting the top of the second circulating filtration device and the dissolving device;

[0033] A control valve F5 is provided on the pipeline between the top of the second circulation filter device and the solvent intermediate buffer device;

[0034] A control valve F6 is provided on the pipeline connecting the top end of the second circulation filtering device and the second cooler.

[0035] Furthermore, a pre-purification pump is provided on the pipeline connecting the chlorosilane disproportionation device and the bottom end of the circulation filtration device;

[0036] A catalyst recovery pump is provided on the pipeline connecting the dissolving device and the second circulating filtering device;

[0037] A solvent recovery pump is provided on the pipeline between the solvent intermediate buffer device and the solvent tower.

[0038] The beneficial effects of the method and system for recovering the catalyst aluminum trichloride from chlorosilane disproportionation waste liquid of the present invention are:

[0039] The present invention performs solid-liquid separation on chlorosilane disproportionation waste liquid by adopting a circulating filtration combined with nitrogen purging method, then selects a specific solvent to dissolve chlorosilane high-boiling products coated on the surface of the catalyst aluminum trichloride in the base slag, and then separates the catalyst aluminum trichloride again by a circulating filtration combined with nitrogen purging method. The method and system of the present invention have a short operation process, flexible operation, low processing cost, no wastewater and harmful gas are generated, and significant environmental protection and economic benefits are achieved. The catalyst recovery rate can reach more than 93%, which is conducive to industrial promotion and implementation. BRIEF DESCRIPTION OF THE DRAWINGS

[0040] Figure 1 Schematic diagram of the system for recovering aluminum trichloride catalyst from chlorosilane disproportionation waste liquid in Example 1 of the present invention;

[0041] Among them, 1. Chlorosilane disproportionation device; 2. Pre-purification pump; 3. Circulation filtration device; 4. First cooler; 5. High-boiling-point storage device; 6. Dissolution device; 7. Catalyst recovery pump; 8. Second circulation filtration device; 9. Catalyst receiving device; 10. Second cooler; 11. Solvent intermediate buffer device; 12. Solvent recovery pump; 13. Solvent tower; 14. Third cooler; 15. Solvent condensation device; F1, control valve F1; F2, control valve F2; F3, control valve F3; F4, control valve F4; F5, control valve F5; F6, control valve F6. DETAILED DESCRIPTION

[0042] The technical solutions in the embodiments of the present invention are described clearly and completely below. Many specific details are set forth in the following description to facilitate a full understanding of the present invention. However, the present invention may also be implemented in other ways different from those described herein, and those skilled in the art may make similar generalizations without violating the scope of the present invention. Therefore, the present invention is not limited to the specific embodiments disclosed below.

[0043] Example 1 A method and system for recovering aluminum trichloride catalyst from chlorosilane disproportionation waste liquid

[0044] 1. A system for recovering aluminum trichloride catalyst from chlorosilane disproportionation wastewater

[0045] This embodiment is a system for recovering aluminum trichloride catalyst from chlorosilane disproportionation waste liquid. Figure 1 The system includes a circulating filtration device 3, a first cooler 4, a high boiling point storage device 5, a dissolving device 6, a second circulating filtration device 8, a second cooler 10, a solvent intermediate buffer device 11, a solvent tower 13, a third cooler 14 and a solvent condensing device 15;

[0046] The bottom end of the circulation filter device 3 is connected to the chlorosilane disproportionation device 1 through a pipeline, and is used to receive the chlorosilane disproportionation waste liquid generated after the reaction of the chlorosilane disproportionation device 1 is completed; a pre-purification pump 2 is provided on the pipeline connecting the chlorosilane disproportionation device 1 and the bottom end of the circulation filter device 3; and a nitrogen purge channel is provided at the bottom end of the circulation filter device 3;

[0047] The top of the circulation filter device 3 is connected to the chlorosilane disproportionation device 1, the first cooler 4, and the high-boiling-point storage device 5 through pipelines. A control valve F1 is provided on the pipeline connecting the top of the circulation filter device 3 to the chlorosilane disproportionation device 1; a control valve F2 is provided on the pipeline connecting the top of the circulation filter device 3 to the high-boiling-point storage device 5; and a control valve F3 is provided on the pipeline connecting the top of the circulation filter device 3 to the first cooler 4.

[0048] The bottom end of the circulating filter device 3 is connected to the dissolving device 6, which is generally a dissolving kettle. In this embodiment, the circulating filter device 3 is arranged at a higher position, and the dissolving device 6 is arranged at a lower position. The base slag obtained in the circulating filter device 3 is transported to the dissolving device 6 by gravity through a pipeline.

[0049] The dissolving device 6 is connected to the second circulating filter device 8 through a pipeline, and a nitrogen purge channel is provided at the bottom of the second circulating filter device 8; a catalyst recovery pump 7 is provided on the pipeline connecting the dissolving device 6 and the second circulating filter device 8;

[0050] The bottom end of the second circulating filter device 8 is connected to the catalyst receiving device 9 (generally a catalyst receiving tank can be used);

[0051] The top of the second circulation filter device 8 is connected to the dissolution device 6, the second cooler 10, and the solvent intermediate buffer device 11 through pipelines respectively; a control valve F4 is provided on the pipeline connecting the top of the second circulation filter device 8 and the dissolution device 6; a control valve F5 is provided on the pipeline connecting the top of the second circulation filter device 8 and the solvent intermediate buffer device 11; and a control valve F6 is provided on the pipeline connecting the top of the second circulation filter device 8 and the second cooler 10;

[0052] The solvent intermediate buffer device 11 is connected to the dissolving device 6 and the solvent tower 13 through a pipeline; a solvent recovery pump 12 is provided on the pipeline between the solvent intermediate buffer device 11 and the solvent tower 13; during the organic solvent recycling process, the recovered solvent recovered in the solvent intermediate buffer device 11 is returned to the dissolving device 6 for use as an organic solvent; after 3 to 7 cycles, the recovered solvent recovered in the solvent intermediate buffer device 11 is pumped into the solvent tower 13 by the solvent recovery pump 12 for solvent distillation recovery;

[0053] The top of the solvent tower 13 is connected to the third cooler 14 and the solvent condensing device 15 through pipelines in sequence.

[0054] 2. A method for recovering aluminum trichloride catalyst from chlorosilane disproportionation waste liquid

[0055] This embodiment is a method for recovering aluminum trichloride catalyst from chlorosilane disproportionation waste liquid using a system, which specifically includes the following steps:

[0056] S1, pre-purification section

[0057] After the disproportionation reaction of low-boiling-point organic silicon or the disproportionation reaction of organic silicon-trimethylammonium in the chlorosilane disproportionation device 1 is completed, the generated chlorosilane disproportionation waste liquid is pumped into the circulation filtration device 3 through the pre-purification pump 2. At this time, the control valve F1 is opened, and the control valve F2 and the control valve F3 are closed to carry out circulation filtration. After the filter cake is formed in the circulation filtration device 3 and the liquid is observed to be clear through the front mirror of the control valve F1, the control valve F2 is gradually opened and the control valve F1 is closed. The obtained high-boiling point is stored in the high-boiling point storage device 5. After the filtration of the chlorosilane disproportionation waste liquid in the chlorosilane disproportionation device 1 is completed, the purification pump and the control valve F2 are closed, and the control valve F3 is opened. 3, and nitrogen with a pressure of 0.2-0.5 MPa and a temperature of room temperature is introduced into the nitrogen purge channel provided at the bottom of the circulating filter device 3, and the liquid inside the obtained filter cake is pressed upward through the bottom of the circulating filter device 3, and the nitrogen is continuously purged for 0.5-2 hours, so that the nitrogen separates the high boiling points entrained in the filter cake from the filter cake along with the nitrogen, and then the nitrogen entrained with the high boiling points enters the first condenser for condensation, and the entrained high boiling points are recovered and sent to the high boiling point storage device 5. The condensed and purified nitrogen is discharged at a high point, and the high boiling points in the high boiling point storage device 5 are recovered and utilized, and the base slag is obtained in the circulating filter device 3.

[0058] The obtained base residue is dry base residue, and the liquid content in the dry base residue is less than 45wt%; the obtained base residue is preferably dry base residue to increase the number of subsequent solvent recycling and facilitate the subsequent separation and purification of the catalyst aluminum chloride;

[0059] The obtained base slag can also be a wet base slag, wherein the liquid content in the wet base slag is 45 to 65 wt%;

[0060] The nitrogen used for purging is condensed in the first condenser with low-temperature water below 15°C and then discharged.

[0061] S2, base slag dissolution section

[0062] The base slag is transported from the circulation filter device 3 to the dissolution device 6 by gravity, and stirred and mixed with the organic solvent at room temperature for 1 to 3 hours. The organic solvent dissolves the high-boiling chlorosilanes wrapped on the surface of the catalyst aluminum chloride in the base slag, and the dissolution effect of the high-boiling chlorosilanes is improved by the stirring time;

[0063] The amount of the organic solvent is 2 to 6 times the weight of the catalyst aluminum chloride added in the process of obtaining the disproportionation reaction of the chlorosilane disproportionation waste liquid;

[0064] The organic solvent is at least one of benzene, carbon disulfide, carbon tetrachloride, petroleum ether, ethyl ether, methyl ethyl ether, dimethyl carbonate and diethyl carbonate. In this embodiment, benzene is used as the organic solvent.

[0065] S3, Recovery Section

[0066] S31, catalyst recovery section

[0067] After the base slag is stirred and dissolved in the dissolving device 6, it enters the catalyst recovery stage. The catalyst recovery pump 7 is used to send the dissolved liquid in the dissolving device 6 to the second circulation filtering device 8 for circulation filtration and nitrogen purging. At this time, the control valve F4 needs to be opened, and the control valve F5 and the control valve F6 need to be closed. The dissolved liquid passes through the catalyst recovery pump 7, the second circulation filtering device 8, and the control valve F4 and then returns to the dissolving device 6; after the catalyst filter cake is formed in the second circulation filtering device 8 and the solvent is observed to be clear through the front sight glass of the control valve F4, the control valve F5 is gradually opened and the control valve F4 is closed to store the recovered solvent in the solvent intermediate buffer device 11;

[0068] After the dissolved liquid in the dissolving kettle is completely filtered, the catalyst recovery pump 7 and the control valve F5 are closed, and the control valve F6 is opened. Hot nitrogen is used to pass through the nitrogen purge channel provided at the bottom of the second circulating filter 8 into nitrogen with a pressure of 0.3 to 0.5 MPa and a temperature of 40 to 60 ° C. The liquid inside the catalyst filter cake is pressed upward through the bottom of the circulating filter 3, and the second circulating filter is continuously purged with hot nitrogen for 1 to 3 hours, so that the nitrogen separates the recovered solvent entrained in the catalyst filter cake from the catalyst filter cake along with the nitrogen. The nitrogen entrained with the recovered solvent enters the second condenser for condensation, and the entrained recovered solvent is recovered to the intermediate buffer device. The condensed and purified nitrogen is vented at a high point, and the recovered solvent in the intermediate buffer device is returned to step S2 for use as an organic solvent. The recovered catalyst aluminum chloride is obtained in the second circulating filter 8, and the recovered catalyst aluminum chloride is discharged into the catalyst receiving device 9 for the next disproportionation reaction.

[0069] The hot nitrogen used for organic solvent purging is cooled by low-temperature water below 15°C and then discharged.

[0070] S32, solvent secondary utilization section

[0071] After 3 to 7 cycles of recycling, the organic solvent is sent to the solvent secondary utilization section for recovery. At this time, the recovered solvent is sent from the solvent intermediate buffer device 11 to the middle of the solvent tower 13 via the solvent recovery pump 12. After distillation separation in the solvent tower 13, the chlorosilane high-boiling products are obtained at the bottom of the tower kettle of the solvent tower 13 and are combined with the high-boiling products in the high-boiling product storage device 5 for recovery.

[0072] The solvent obtained from the top of the solvent tower 13 is condensed in the third cooler 14 and then transported to the solvent condensation tank device. The obtained solvent is returned to the dissolving device 6 in step S2 for use as an organic solvent.

[0073] Among them, the extraction temperature of the solvent tower is 130-150°C, the top temperature is 35-104°C, the bottom temperature is 130-150, the top gauge pressure is 0-0.2002MPa, the number of theoretical plates is 35, the reflux ratio is 5-15:1, the bottom liquid level is 50-90%, and the number of plates is 40.

[0074] The third cooler 14 is cooled by low-temperature water below 15°C.

[0075] The method of this embodiment uses the chlorosilane disproportionation waste liquid produced by the disproportionation reaction of low-boiling-point organic silicon as raw material. The process conditions and recovery results of 3 to 7 cycles are shown in Table 1:

[0076] Table 1 List of process parameters and recovery results in Example 1

[0077]

[0078]

[0079] The method of this embodiment uses the chlorosilane disproportionation waste liquid produced by the organosilicon-trimethyl disproportionation reaction as raw material, carbon disulfide as organic solvent, and the process conditions and recovery results of 3 to 7 cycles are shown in Table 2:

[0080] Table 2 List of process parameters and recovery results in Example 1

[0081]

[0082]

[0083] Example 2-5 Method for recovering aluminum trichloride catalyst from chlorosilane disproportionation waste liquid

[0084] Examples 2-5 are methods for recovering aluminum trichloride catalyst from chlorosilane disproportionation waste liquid. The steps are basically the same as the method for recovering aluminum trichloride catalyst from chlorosilane disproportionation waste liquid in Example 1. The only difference is the amount of raw materials used and the process parameters. See Table 3 for details:

[0085] Table 3 List of process parameters in Examples 2 to 5

[0086]

[0087] The rest of the contents of Examples 2 to 5 are the same as those of Example 1 and will not be repeated here.

[0088] Obviously, the embodiments described are only some of the embodiments of the present invention, not all of them. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without making creative efforts are within the scope of protection of the present invention.

Claims

1. A method for recovering aluminum trichloride catalyst from chlorosilane disproportionation waste liquid, characterized in that: The method comprises the following steps: S1. Separating the chlorosilane disproportionation waste liquid into base slag and liquid high-boiling products by circulating filtration combined with nitrogen purging; S2, mixing the base slag with an organic solvent, and using the organic solvent to dissolve the high-boiling chlorosilanes coated on the surface of the aluminum chloride catalyst in the base slag to obtain a dissolving solution; The organic solvent is at least one of benzene, carbon disulfide, carbon tetrachloride, petroleum ether, ethyl ether, methyl ethyl ether, dimethyl carbonate and diethyl carbonate; S3, the dissolved liquid is separated by circulating filtration with nitrogen purge to obtain the catalyst aluminum chloride and the recovered solvent; The recovered solvent is directly returned to step S2 for use as an organic solvent; After the recovered solvent is recycled multiple times, the solvent tower is used for secondary solvent recovery.

2. The method for recovering catalyst aluminum chloride from chlorosilane disproportionation waste liquid according to claim 1, characterized in that: In step S2, the amount of the organic solvent is 2 to 6 times the weight of the catalyst aluminum chloride added during the disproportionation reaction of the chlorosilane disproportionation waste liquid; The dissolution temperature is room temperature and the dissolution time is 1~3h.

3. The method for recovering catalyst aluminum chloride from chlorosilane disproportionation waste liquid according to claim 1 or 2, characterized in that, The base slag is dry base slag or wet base slag; the liquid content of the dry base slag is less than 45wt%; the liquid content of the wet base slag is 45~65wt%.

4. The method for recovering catalyst aluminum chloride from chlorosilane disproportionation waste liquid according to claim 3, characterized in that: The base slag is dry base slag.

5. The method for recovering catalyst aluminum chloride from chlorosilane disproportionation waste liquid according to claim 1, 2 or 4, characterized in that: In step S1, the nitrogen pressure introduced during the nitrogen purge is 0.2-0.5 MPa, the temperature is room temperature, and the time is 0.5-2 h; In step S3, the nitrogen pressure introduced during the nitrogen purge is 0.3-0.5 MPa, the temperature is 40-60° C., the time is 2-2.5 h, and the cooling temperature of the recovered solvent is lower than 15° C.

6. The method for recovering catalyst aluminum chloride from chlorosilane disproportionation waste liquid according to claim 1, 2 or 4, characterized in that: The extraction temperature of the solvent tower bottom is 130~150℃, the tower top temperature is 35~104℃, the tower bottom temperature is 130~150℃, the tower top gauge pressure is 0~0.2002MPa, the theoretical plate number is 35, the reflux ratio is 5~15:1, the tower bottom liquid level is 50~90%, and the tower plate number is 40.

7. A system for recovering aluminum trichloride catalyst from chlorosilane disproportionation waste liquid, characterized in that: The system comprises: a circulation filtering device, a first cooler, a high boiling point storage device, a dissolving device, a second circulation filtering device, a second cooler, a solvent intermediate buffer device, a solvent tower, a third cooler and a solvent condensing device; The bottom end of the circulating filter device is connected to the chlorosilane disproportionation device through a pipeline, and a nitrogen purge channel is provided at the bottom end of the circulating filter device; The top of the circulating filtration device is connected to the chlorosilane disproportionation device, the first cooler, and the high boiling point storage device through pipelines; The bottom end of the circulating filtration device is connected to the dissolving device; The dissolving device is connected to the second circulating filtering device through a pipeline, and a nitrogen purge channel is provided at the bottom end of the second circulating filtering device; The top of the second circulating filtration device is connected to the dissolving device, the second cooler, and the solvent intermediate buffer device through pipelines respectively; The solvent intermediate buffer device is connected with the dissolving device and the solvent tower through a pipeline; The top of the solvent tower is connected to the third cooler and the solvent condensing device through pipelines in sequence.

8. The system for recovering aluminum trichloride catalyst from chlorosilane disproportionation waste liquid according to claim 7, characterized in that: A control valve F1 is provided on the pipe connecting the top of the circulating filtration device and the chlorosilane disproportionation device; A control valve F2 is provided on the pipe connecting the top of the circulating filtration device and the high-boiling material storage device; A control valve F3 is provided on the pipeline connecting the top end of the circulating filter device and the first cooler.

9. The system for recovering aluminum trichloride catalyst from chlorosilane disproportionation waste liquid according to claim 7 or 8, characterized in that: A control valve F4 is provided on the pipe connecting the top of the second circulating filtration device and the dissolving device; A control valve F5 is provided on the pipeline between the top of the second circulation filter device and the solvent intermediate buffer device; A control valve F6 is provided on the pipeline connecting the top end of the second circulation filtering device and the second cooler.

10. The system for recovering aluminum trichloride catalyst from chlorosilane disproportionation waste liquid according to claim 7 or 8, characterized in that: A pre-purification pump is provided on the pipeline connecting the chlorosilane disproportionation device and the bottom end of the circulation filtration device; A catalyst recovery pump is provided on the pipeline connecting the dissolving device and the second circulating filtering device; A solvent recovery pump is provided on the pipeline between the solvent intermediate buffer device and the solvent tower.

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