A slurry treatment system for a cold hydrogenation synthesis process

Abstract

The utility model relates to cold hydrogenation synthetic technique field, concretely is a kind of slurry treatment system of cold hydrogenation synthetic process, including feeding unit can preliminarily filter, and it is connected filtrate recovery tank and drum filter respectively and handles solid phase and liquid phase material;Drum filter secondary filtration, it is connected drying treatment unit and handles solid phase material, still connect and separate unit carries out gas-liquid separation, condensing unit liquefied gas phase material is connected to separate unit, and condensing unit is communicated with filtrate recovery tank and drying treatment unit;Filtrate recovery tank and drum filter between connection have composite unit and carry out liquid phase treatment to provide filter material, and filtrate recovery tank is connected with separate unit.Using this system can effectively separate solid-liquid in slurry to obtain solid waste residue and liquid chlorosilane, and finally obtained solid waste residue can be effectively treated, and obtained liquid chlorosilane can be reused in cold hydrogenation process.

Description

Technical Field

[0001] This utility model relates to the field of cold hydrogenation synthesis technology, specifically to a slurry treatment system for a cold hydrogenation synthesis process. Background Technology

[0002] During the production of polysilicon, the production of trichlorosilane generates a large amount of byproduct—slurry—which contains a significant amount of unreacted silicon tetrachloride and a small amount of trichlorosilane. Improper handling of this slurry can lead to environmental pollution and resource waste. To effectively address this issue and reduce production costs, most companies need to treat the slurry byproduct to recover the chlorosilanes, thereby conserving resources and meeting environmental protection requirements.

[0003] However, the cold hydrogenation slurry not only contains unreacted silicon powder, metal chlorides and other solid particles, but also contains substances such as chlorosilanes that have recycling value but are harmful to the environment. Existing technologies mostly use alkaline solution to neutralize and then discharge the slurry, which leads to waste of chlorosilanes and large consumption of alkaline solution. In addition, manual sludge removal poses environmental risks and operational safety hazards. Utility Model Content

[0004] To address the technical problems existing in the background art, this utility model provides a slurry treatment system for a cold hydrogenation synthesis process.

[0005] The technical solution of this utility model is as follows: A slurry treatment system for a cold hydrogenation synthesis process includes a feeding unit capable of preliminary filtration, which is connected to a filtrate recovery tank and a rotary drum filter to treat solid and liquid phases respectively. The rotary drum filter is used for secondary filtration. It is connected to a drying unit to process solids and a separation unit to separate gas and liquid. The separation unit is connected to a condensation unit to liquefy gas. The condensation unit is connected to the filtrate recovery tank and the drying unit. A composite unit is connected between the filtrate recovery tank and the drum filter to provide filter material and perform liquid phase treatment. The filtrate recovery tank is connected to the separation unit.

[0006] The feeding unit includes a slurry mixing tank and a slurry filter connected in sequence. The slurry filter is connected to a rotary drum filter and a filtrate recovery tank.

[0007] A slurry filter is added between the slurry mixing tank and the rotary drum filter to filter the slurry mixture from the mixing tank before it enters the rotary drum filter. Solids are separated by filtration; the filtered-out chlorosilane liquid enters the filtrate recovery tank, increasing the solids content of the slurry and reducing the chlorosilane content, thus improving the efficiency of subsequent slurry treatment. The filtered chlorosilane is a clear liquid without solids, reducing pressure on subsequent pipelines and preventing pipe blockage during venting.

[0008] The slurry that passes through the slurry filter enters the rotary drum filter for a second filtration, further separating the solids from the chlorosilanes—a secondary filtration process. The rotary drum filter itself has a filter cloth, which filters at 100-120 ppm / min, further filtering the solids from the slurry.

[0009] The separation unit includes a vacuum cooler, a vacuum filtration unit, and a gas-liquid separator connected in sequence. The vacuum cooler is connected to the drum filter, the gas-liquid separator is connected to the filtrate recovery tank, and the vacuum filtration unit is connected to the condensation unit.

[0010] The condensation unit includes a primary recovery condenser and a secondary recovery condenser connected in sequence; The primary recovery condenser is connected to the drying and separation units, while the secondary recovery condenser is connected to the waste gas treatment unit.

[0011] The composite unit includes a de-weighting and recovery tower, which is connected to a rotary drum filter and a filtrate recovery tank.

[0012] The bottom of the deweight recovery tower is equipped with a deweight reactor heater, and the top is equipped with a deweight tower condenser and a deweight reflux tank connected to it. The de-weighting kettle heater is connected to the drum filter via a drum overflow tank, and the de-weighting return tank is connected to a storage tank.

[0013] The filtrate in the filtrate recovery tank is crude silicon tetrachloride, which is mixed with metal chlorides such as FeCl3 and AlCl3, as well as high-molecular-weight polychlorosilanes. It cannot be directly used in cold hydrogenation and requires further purification. The chlorosilanes enter the deweighting recovery tower from the filtrate recovery tank. The heavy metal chloride components, such as FeCl3 and AlCl3, are discharged from the bottom of the tower via a deweighting kettle heater and enter the rotary drum overflow tank. Subsequently, they are pumped into the rotary drum filter, repeating the previous process. Silicon tetrachloride is discharged from the top of the tower, condensed in the deweighting tower condenser, and then enters the deweighting reflux tank. At this point, the quality of the silicon tetrachloride in the deweighting reflux tank meets production requirements and can be directly discharged into the storage tank area for later use.

[0014] The composite unit includes a diatomaceous earth mixing tank and a diatomaceous earth adding tank connected in sequence; The diatomaceous earth mixing tank is connected to the gas-liquid separator and the rotary drum filter.

[0015] The diatomaceous earth mixture from the mixing tank can form a special filter coating on the filter cloth, resulting in a denser filter cake. The diatomaceous earth has a mesh size of 200-250 mesh, which is smaller and has a better filtration effect. It can filter out silicon powder, FeCl3, and AlCl3 solids. After the slurry is filtered through the diatomaceous earth coating, the solid content is further reduced.

[0016] The use of diatomaceous earth as a pre-coating material is for two reasons: firstly, it is an environmentally friendly material, being a green filter material; secondly, its smaller mesh size allows for further filtration of silica powder, FeCl3, and AlCl3 solids in the slurry.

[0017] The drying unit includes a rake dryer and a dry residue ton bag packaging machine connected in sequence; The rake dryer is connected to the drum filter and condenser unit.

[0018] The rake dryer is equipped with a drying filter and a drying exhaust fan connected in sequence inside, and the drying exhaust fan is connected to the condensation unit.

[0019] The dry residue ton bag packaging machine is equipped with a dry residue tank, a lime tank and a neutralization spiral inside, and the dry residue tank is connected to a rake dryer.

[0020] The dried slag from the rake dryer enters the dried slag tank, where it is mixed with lime from the lime tank to further adjust the acidity and alkalinity of the solid contents. Additionally, the lime reacts with any trace amounts of chlorosilanes that may be present in the slag to completely remove the chlorosilanes from the solid contents, ensuring safety and environmental protection.

[0021] The beneficial effects of this application are as follows: 1. The chlorosilanes in the slurry were effectively recovered, with a recovery rate of up to 99%, saving resources and avoiding waste; 2. The trace amounts of chlorosilanes that may be present in the dry residue are reacted with lime to adjust the acidity or alkalinity of the solid contents of the dry residue, and the chlorosilanes in the solid contents are completely removed. The treatment process is safe and environmentally friendly. 3. This system performs two filtration processes. The filtered chlorosilane liquid enters the filtrate recovery tank, increasing the solids content in the slurry and reducing the chlorosilane content, thereby improving the efficiency of subsequent slurry treatment. Furthermore, the filtered chlorosilane is a clear liquid without solids, reducing pressure on subsequent pipelines and making it less likely to clog pipelines during the venting process. Attached Figure Description

[0022] In the attached diagram: Figure 1 A schematic diagram of the slurry treatment system for the cold hydrogenation synthesis process; Figure 2 A detailed schematic diagram of the slurry treatment system for the cold hydrogenation synthesis process; Figure 3 This is a schematic diagram of the heavy weight recovery tower structure; Figure 4 This is a schematic diagram of a rake dryer. Figure 5 This is a schematic diagram of a dry residue ton bag packaging machine.

[0023] The components represented by the various reference numerals in the diagram are: 1. Feeding unit; 11. Slurry mixing tank; 12. Slurry filter; 2. Rotary drum filter; 3. Filtrate recovery tank; 4. Separation unit; 41. Vacuum cooler; 42. Vacuum filtration unit; 43. Gas-liquid separator; 5. Condensation unit; 51. Primary recovery condenser; 52. Secondary recovery condenser; 6. Composite unit; 61. Deweight recovery tower; 611. Deweight kettle heater; 612. Deweight tower condenser; 613. Deweight reflux tank; 62. Diatomaceous earth mixing tank; 63. Diatomaceous earth addition tank; 64. Rotary drum overflow tank; 7. Drying unit; 71. Rake dryer; 711. Drying filter; 712. Drying exhaust fan; 72. Dry residue ton bag packaging machine; 721. Dry residue tank; 722. Lime tank; 723. Neutralization spiral. Detailed Implementation

[0024] Example: This embodiment provides a slurry treatment system for a cold hydrogenation synthesis process, combined with... Figure 1 The feeding unit 1 is capable of preliminary filtration, and it is connected to the filtrate recovery tank 3 and the rotary drum filter 2 to process solid and liquid phases respectively. The rotary drum filter 2 performs secondary filtration. It is connected to the drying unit 7 to process solids and is also connected to the separation unit 4 for gas-liquid separation. The separation unit 4 is connected to the condensation unit 5 to liquefy gas. The condensation unit 5 is connected to the filtrate recovery tank 3 and the drying unit 7. A composite unit 6 is connected between the filtrate recovery tank 3 and the rotary drum filter 2 to provide filter material and perform liquid phase treatment. The filtrate recovery tank 3 is connected to the separation unit 4.

[0025] The structure of each part will be described in detail below with reference to the accompanying drawings.

[0026] In this embodiment, the feeding unit 1 includes a slurry mixing tank 11 and a slurry filter 12 connected in sequence. The slurry filter 12 is connected to the rotary drum filter 2 and the filtrate recovery tank 3, as follows: Figure 2 As shown.

[0027] In use, the slurry produced by the cold hydrogenation process is collected in the slurry mixing tank 11, and the solid and liquid phases are separated by the slurry filter 12. The chlorosilane liquid is separated and recycled and stored in the filtrate recovery tank 3. The remaining slurry after the chlorosilane liquid is separated is discharged into the rotary drum filter 2 through the drain port of the slurry filter 12.

[0028] Preferably, the slurry filter 12 first filters and separates the supernatant into the filtrate recovery tank 3. When the solid content in the slurry filter 12 is controlled to between 5-10%, filtration is stopped and slag discharge begins.

[0029] Furthermore, the temperature of the slurry mixing tank 11 is controlled between 40-120℃, the pressure between 0.01-0.12MPaG, the liquid level between 20-80%, and the weight between 3000-15000kg; furthermore, the temperature of the slurry filter 12 is controlled between 40-80℃, the pressure between 0.20-0.50MPaG, and the filtration accuracy is controlled below 1μm; furthermore, the temperature of the filtrate recovery tank 3 is controlled between 25-60℃, the pressure between 0.01-0.20MPaG, and the liquid level inside the tank is controlled between 30-70%.

[0030] In this embodiment, the separation unit 4 includes a vacuum cooler 41, a vacuum filtration unit 42, and a gas-liquid separation tank 43 connected in sequence; the vacuum cooler 41 is connected to the drum filter 2, the gas-liquid separation tank 43 is connected to the filtrate recovery tank 3, and the vacuum filtration unit 42 is connected to the condensation unit 5.

[0031] The composite unit 6 includes a diatomaceous earth mixing tank 62 and a diatomaceous earth adding tank 63 connected in sequence; the diatomaceous earth mixing tank 62 is connected to the gas-liquid separator 43 and the rotary drum filter 2.

[0032] Before feeding slurry into the rotary drum filter 2, the rotary drum filter 2 should first undergo a diatomaceous earth pre-coating process. The diatomaceous earth pre-coating process is as follows: First, open the diatomaceous earth addition tank 63 and add the specified amount of diatomaceous earth to the tank for later use.

[0033] Add the specified amount of silicon tetrachloride to the diatomaceous earth mixing tank 62 and stir. All the diatomaceous earth in the diatomaceous earth adding tank 63 is then transferred into the diatomaceous earth mixing tank 62. During this process, nitrogen gas can be used to purge the diatomaceous earth in the adding tank 63 to prevent diatomaceous earth residue. After completion, close the diatomaceous earth adding valve.

[0034] After the diatomaceous earth mixing tank 62 has been mixed for a specified time and is fully mixed, it is fed into the rotary drum filter 2. When the liquid level in the rotary drum filter 2 reaches a certain level, the circulating water valve on the vacuum filtration unit 42 and the vacuum cooler 41 is opened to perform circulating filtration. The filtrate enters the gas-liquid separator 43.

[0035] When the liquid level in the gas-liquid separator 43 reaches the specified level, the filtrate in the drum filter 2 is replenished, and the excess filtrate is collected and temporarily stored in the filtrate recovery tank 3.

[0036] Furthermore, the temperature inside the rotary drum filter 2 is controlled between 20-50℃, the external pressure is controlled between 5-40kPaG, the vacuum inside the drum is controlled between -40kPaG and -100kPaG, and the coating thickness of the diatomaceous earth is controlled between 50-160mm.

[0037] Furthermore, the temperature of the diatomaceous earth addition tank 63 is controlled between 20-40℃, the pressure is controlled between 0.01-0.50MPaG, and the addition amount of diatomaceous earth is 500-1500kg / time; the temperature of the diatomaceous earth mixing tank 62 is controlled between 20-40℃, the pressure is controlled between 0.01-0.50MPaG, the feed amount of diatomaceous earth is controlled between 500-1500kg / time; the feed amount of silicon tetrachloride is controlled between 2000-12000kg / time, and the concentration of the pre-coating liquid is controlled between 5-20%.

[0038] The condensation unit 5 includes a primary recovery condenser 51 and a secondary recovery condenser 52 connected in sequence; The primary recovery condenser 51 is connected to the drying unit 7 and the separation unit 4, and the secondary recovery condenser 52 is connected to the waste gas treatment unit.

[0039] The drying unit 7 includes a rake dryer 71 connected in sequence to the rotary drum filter 2 and the condenser unit 5. Inside the rake dryer 71 are a drying filter 711 and a drying exhaust fan 712 connected in sequence. The drying exhaust fan 712 is connected to the condenser unit 5. Figure 4 As shown.

[0040] During use, the slurry is filtered in the rotary drum filter 2. During the rotation, the filtered solids and filter cake are scraped out by the internal scraper and fall into the rake dryer 71. At this time, the stirring shaft in the rake dryer is running normally and the discharge port is closed.

[0041] The filtered clear liquid and the extracted N2 are discharged together into the gas-liquid separator 43 for gas-liquid phase separation. The gas phase is discharged from the upper gas phase outlet of the gas-liquid separator 43 and pumped into the air inlet of the vacuum unit 42. Most of the gas discharged from the vacuum unit 42 is cooled by the vacuum cooler 41 and then returned to the circulating gas (N2) return port of the drum filter 2 for recycling. A small portion of the gas is discharged to the primary recovery condenser 51 and the secondary recovery condenser 52 when the gas pressure on the drum shell of the drum filter 2 exceeds the process specified pressure, and is finally discharged into other waste gas treatment.

[0042] The clear liquid separated by the gas-liquid separator 43 is partially returned to replenish the drum filter 2, while the excess is temporarily stored in the filtrate recovery tank 3.

[0043] Furthermore, the temperature inside the gas-liquid separator 43 is controlled between 20-50℃, the vacuum degree is controlled between -40kPaG and -120kPaG, and the liquid level inside the tank is controlled between 30-70%.

[0044] Preferably, the steam temperature of the rake dryer 71 is controlled between 70-120℃, the steam pressure is controlled between 0.01-0.50MPaG, the steam consumption is 200-600kg / batch, the drying temperature is controlled between 70-120℃, the drying pressure is controlled between 50kPaG and -60kPaG, and the drying capacity is 1000-5000kg / batch.

[0045] Furthermore, the temperature of the vacuum unit 42 is controlled between 20-50℃, the vacuum degree is controlled between -40kPaG and -120kPaG, and the pumping volume is controlled between 500-2000Nm. 3 The exhaust pressure is controlled between 10-50 kPaG, the internal liquid level is controlled between 30-70%, and the cooling water flow rate is controlled between 15-35 L / min. The medium inlet temperature of vacuum cooler 41 is controlled between 20-50℃, the medium inlet pressure is controlled between 10-80 kPaG, the circulating water inlet temperature is 32℃, the outlet temperature is 38℃, and the pumping speed is controlled between 500-2000 Nm³. 3 The exhaust pressure is controlled between 10-50 kPaG, the internal liquid level is controlled between 30-70%, and the cooling water flow rate is controlled between 15-35 L / min.

[0046] Preferably, in the condensing unit 5, the inlet temperature of the primary recovery condenser 51 is controlled between 50-120℃, the outlet temperature is controlled between 45-50℃, and the inlet and outlet pressures are controlled between 0.01-0.50 MPaG. The inlet temperature of the circulating water is 32℃, the outlet temperature is 38℃, and the inlet and outlet pressures are controlled between 0.10-0.50 MPaG. The inlet temperature of the secondary recovery condenser 52 is controlled between 20-60℃, the outlet temperature is controlled between -30℃ and -45℃, and the inlet and outlet pressures are controlled between 0.01-0.50 MPaG. It uses a refrigerant, with the refrigeration evaporation temperature controlled at -45℃ and the refrigeration evaporation pressure controlled between 0.001-0.10 MPaG.

[0047] When the slurry discharge from the slurry mixing tank 11 reaches the specified lower limit liquid level, the feeding into the drum filter 2 is stopped, the liquid level in the drum filter 2 is kept basically unchanged, and the clear liquid is not collected into the filtrate recovery tank 3, maintaining the current state. The drum filter 2 also stops feeding into the rake dryer 71.

[0048] Specifically, when the liquid level in the slurry mixing tank 11 is below 20%, the discharge is stopped. The rotary drum filter 2 and the gas-liquid separator 43 continue to filter and circulate, keeping the liquid level in the rotary drum filter 2 stable, and the gas-liquid separator 43 stops discharging to the filtrate recovery tank 3.

[0049] Turn on the rake dryer 71, the dryer filter 711 and the dryer exhaust fan 712, and keep the slight negative pressure value inside the rake dryer 71 within the specified process value to dry the wet residue inside the rake dryer 71.

[0050] After the rake dryer 71 has been running for about 10-90 minutes, the silicon tetrachloride content in the dried residue is tested. If it is less than the process specification value (0.5w%), the dried residue can be discharged.

[0051] Furthermore, the filter gas temperature of the dryer filter 711 is controlled between 70-120℃, and the filter gas pressure is controlled between 0.01-0.10MPaG; the inlet temperature of the dryer exhaust fan 712 is controlled between 50-120℃, the outlet temperature of the precooler is controlled between 30-60℃, the exhaust pressure is controlled between 30-100kPaG, and the exhaust temperature is controlled between 50-120℃.

[0052] Drying unit 7 includes a dry residue ton bag packaging machine 72 connected to rake dryer 71; see also Figure 5 The dry residue ton bag packaging machine 72 is equipped with a dry residue tank 721, a lime tank 722 and a neutralization spiral 723. The dry residue tank 721 is connected to the rake dryer 71.

[0053] During operation, after installing the ton bag in the dry slag ton bag packaging machine 72, the neutralization screw 723 is turned on, and the lime tank 722 discharges material. Based on the dry slag analysis results, the prescribed amount of lime is added. After neutralization with lime, the pH of the dry slag is controlled between 6 and 9. The dry slag tank 721 discharges material. When the ton bag reaches the prescribed value, the dry slag ton bag packaging machine 72 automatically shuts off the dry slag tank 721, the lime tank 722, and the neutralization screw 723, stopping the discharge. An alarm is triggered to notify the personnel to replace the ton bag and prepare for the next dry slag packaging.

[0054] Specifically, the temperature inside the dry slag ton bag packaging machine 72 is controlled between 20-40℃, the pressure is controlled at atmospheric pressure (101kPaG), and the ton bag weighing capacity is controlled between 500-2000kg / bag; the temperature inside the neutralizing spiral 723 is controlled between 50-90℃, the pressure is controlled at 101kPaG, and the conveying capacity is controlled between 1000-3000kg / h; the temperature inside the lime hopper 722 is controlled between 20-40℃, the pressure is controlled between 0.01-0.20MPaG, the weighing capacity inside the hopper is controlled between 1000-3000kg, and the material level inside the hopper is controlled below 80%; the temperature inside the dry slag hopper 721 is controlled between 70-120℃, the pressure is controlled between 0.01-0.20MPaG, the weighing capacity inside the hopper is controlled between 1000-3000kg, and the material level inside the hopper is controlled below 80%.

[0055] The composite unit 6 includes a de-weighting and recovery tower 61, which is connected to the rotary drum filter 2 and the filtrate recovery tank 3.

[0056] The bottom of the de-weight recovery tower 61 is equipped with a de-weight kettle heater 611, and the top is equipped with a de-weight tower condenser 612 and a de-weight reflux tank 613 connected to it. The de-weight kettle heater 611 is connected to the drum filter 2 through a drum overflow tank 64, and the de-weight reflux tank 613 is connected to a storage tank, as detailed below. Figure 3 As shown.

[0057] Since the filtrate also contains some high-boiling-point impurities such as FeCl3 and AlCl3, if it is directly reused in the cold hydrogenation unit, it will cause the accumulation of heavy components such as FeCl3 and AlCl3 in the cold hydrogenation unit. This will affect the stable operation of the system and the quality of subsequent products. Therefore, the filtrate needs to be de-heavy and impurity removed again before it can be reused.

[0058] Once the filtrate in the filtrate recovery tank 3 reaches the specified level, it is fed into the deweighting and recovery tower 61. Simultaneously, the stirring of the deweighting kettle heater 611 is activated. When the liquid level in the deweighting kettle heater 611 reaches the specified level, heating and evaporation of the material inside the kettle begins. The chlorosilanes in the deweighting kettle heater 611 are heated and evaporated, then circulate within the deweighting and recovery tower 61. High-boiling-point impurities such as FeCl3 and AlCl3 are discharged from the bottom of the kettle into the rotary drum overflow tank 64, and then return from the rotary drum overflow tank 64 to the rotary drum filter 2 for cyclic filtration.

[0059] The pressure of the de-weight recovery tower 61 is controlled between 0.10-0.50 MPaG. The de-weight tower condenser 612 is turned on, and the condensate enters the de-weight reflux tank 613. When the liquid level in the de-weight reflux tank 613 reaches the process specification value, the reflux operation into the tower begins.

[0060] The top vent valve of the de-heavy recovery tower 61 automatically vents air to control the pressure at the top of the tower. After stable operation, the components in the de-heavy reflux tank 613 are sampled and analyzed. Once the components meet the process requirements, the material is fed into the tetrachloro storage tank area for storage and use in the cooling hydrogenation unit.

[0061] Silicon tetrachloride is discharged from the top of the tower, condensed by the heavy removal tower condenser 612, and then enters the heavy removal reflux tank 613. At this time, the quality of silicon tetrachloride in the heavy removal reflux tank 613 meets the production requirements and can be directly discharged into the storage tank for later use.

[0062] Furthermore, the top temperature of the deweight recovery tower 61 is controlled between 40-60℃, the bottom temperature between 80-100℃, the top pressure between 0.10-0.30 MPaG, the feed flow rate between 200-600 kg / h, and the reflux flow rate between 700-1200 kg / h; the reflux ratio is controlled between 1.0-2.0; the medium temperature of the deweight recovery kettle heater 611 is controlled between 80-100℃, the medium pressure between 0.10-0.50 MPaG, the heating steam temperature between 70-120℃, the steam pressure between 0.20-1.00 MPaG, and the bottom discharge rate between 20-80 kg / h; the rotary drum overflow tank 64... The internal temperature is controlled between 30-70℃, the pressure between 10-50 kPaG, and the liquid level in the tank is controlled between 30-70%; the medium inlet temperature of the de-weighting tower condenser 612 is controlled between 20-50℃, the medium inlet pressure is controlled between 0.10-0.50 MPaG, the circulating water inlet temperature is 32℃, the outlet temperature is 38℃, the inlet pressure is controlled between 0.10-0.50 MPaG, the outlet pressure is controlled between 0.10-0.50 MPaG, and the circulating water flow rate is controlled between 5-30 m3 / h; the temperature of the de-weighting reflux tank 613 is controlled between 30-50℃, the pressure is controlled between 0.10-0.50 MPaG, and the liquid level in the tank is controlled between 30-70%. This system can effectively separate solids and liquids in slurry to obtain solid waste and liquid chlorosilanes. The solid waste can be effectively treated, while the liquid chlorosilanes can be reused in the cold hydrogenation process.

Claims

1. A slurry treatment system for a cold hydrogenation synthesis process, characterized in that, The feeding unit (1) is capable of preliminary filtration, and is connected to the filtrate recovery tank (3) and the rotary drum filter (2) to process solid and liquid phases respectively; The rotary drum filter (2) performs secondary filtration. It is connected to the drying unit (7) to process solids and is also connected to the separation unit (4) for gas-liquid separation. The separation unit (4) is connected to the condensation unit (5) to liquefy gases. The condensation unit (5) is connected to the filtrate recovery tank (3) and the drying unit (7). A composite unit (6) is connected between the filtrate recovery tank (3) and the rotary drum filter (2) to provide filter material and perform liquid phase treatment. The filtrate recovery tank (3) is connected to the separation unit (4).

2. The slurry treatment system for a cold hydrogenation synthesis process according to claim 1, characterized in that, The feeding unit (1) includes a slurry mixing tank (11) and a slurry filter (12) connected in sequence. The slurry filter (12) is connected to a rotary drum filter (2) and a filtrate recovery tank (3).

3. The slurry treatment system for a cold hydrogenation synthesis process according to claim 1, characterized in that, The separation unit (4) includes a vacuum cooler (41), a vacuum filtration unit (42), and a gas-liquid separator (43) connected in sequence. The vacuum cooler (41) is connected to the drum filter (2), the gas-liquid separator (43) is connected to the filtrate recovery tank (3), and the vacuum filtration unit (42) is connected to the condensation unit (5).

4. The slurry treatment system for a cold hydrogenation synthesis process according to claim 1, characterized in that, The condensation unit (5) includes a primary recovery condenser (51) and a secondary recovery condenser (52) connected in sequence. The primary recovery condenser (51) is connected to the drying unit (7) and the separation unit (4), and the secondary recovery condenser (52) is connected to the waste gas treatment unit.

5. The slurry treatment system for a cold hydrogenation synthesis process according to claim 1, characterized in that, The composite unit (6) includes a deweight recovery tower (61), which is connected to a drum filter (2) and a filtrate recovery tank (3).

6. The slurry treatment system for a cold hydrogenation synthesis process according to claim 5, characterized in that, The bottom of the de-weight recovery tower (61) is provided with a de-weight kettle heater (611), and the top is provided with a de-weight tower condenser (612) and a de-weight reflux tank (613) connected thereto. The de-weighting kettle heater (611) is connected to the drum filter (2) via the drum overflow tank (64), and the de-weighting return tank (613) is connected to a storage tank.

7. The slurry treatment system for a cold hydrogenation synthesis process according to claim 1, characterized in that, The composite unit (6) includes a diatomaceous earth mixing tank (62) and a diatomaceous earth adding tank (63) connected in sequence. The diatomaceous earth mixing tank (62) is connected to the separation unit (4) and the drum filter (2).

8. The slurry treatment system for a cold hydrogenation synthesis process according to claim 1, characterized in that, The drying unit (7) includes a rake dryer (71) and a dry residue ton bag packaging machine (72) connected in sequence. The rake dryer (71) is connected to the drum filter (2) and the condenser unit (5).

9. A slurry treatment system for a cold hydrogenation synthesis process according to claim 8, characterized in that, The rake dryer (71) is equipped with a drying filter (711) and a drying exhaust fan (712) connected in sequence inside, and the drying exhaust fan (712) is connected to the condensation unit (5).

10. A slurry treatment system for a cold hydrogenation synthesis process according to claim 8, characterized in that, The dry slag ton bag packaging machine (72) is equipped with a dry slag tank (721), a lime tank (722) and a neutralization spiral (723), and the dry slag tank (721) is connected to a rake dryer (71).

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