System for reducing acid value of hydrolysate in separation and washing process of dimethyl dichlorosilane hydrolysate

Abstract

The utility model relates to a system for reducing the acid value of hydrolysate in the separation and washing process of dimethyl dichlorosilane hydrolysate. Comprising three stages of coalescers, dimethyl dichlorosilane acidic hydrolysate enters the system from the first stage of coalescer, process water enters the system from the third stage of coalescer, the acidic hydrolysate and diluted hydrochloric acid or process water are mixed in each stage of coalescer, oil-water two-phase separation is completed through multiple times of washing and coalescence, and meanwhile the acid value of the hydrolysate is reduced; each stage of coalescer comprises two static mixers connected in series, a group of prefilters and a large coalescer, the coalescer is Z-shaped, and four stages of filter elements are arranged in each stage of coalescer. Through repeated tests, a modified polyvinylidene fluoride filter element of Pall Company is finally selected, and after continuous three-stage coalescer treatment, the acid value of dimethyldichlorosilane hydrolysate can be reduced to 10 PPM or below.

Description

Technical Field

[0001] This invention relates to a system for reducing the acid value of dimethyldichlorosilane hydrolysates during the separation and washing process. This coalescing device significantly reduces the chloride ion content in the hydrolysates while decreasing the amount of makeup water required. It belongs to the field of organosilicon technology. Background Technology

[0002] Currently, most domestic manufacturers of organosilicon monomers use a weak alkali neutralization-water washing and stratification process to produce neutral hydrolysates. This process results in a long residence time for the hydrolysates, involves numerous reaction, storage, and separation devices, and produces neutral hydrolysates with high chloride ion content and high viscosity. Furthermore, the purification process requires the introduction of soda ash to neutralize the hydrolysates, supplemented by boiling and washing with a large amount of process water. During this process, the washing kettle consumes steam and generates a large amount of alkaline wastewater that needs to be treated, which is not conducive to building a resource-saving and environmentally friendly society. Summary of the Invention

[0003] To address the aforementioned technical problems, this utility model provides a system for reducing the acid value of dimethyldichlorosilane hydrolysate during the separation and washing process. The system comprises a continuous multi-stage coalescing device, preferably a three-stage coalescing device. Acidic dimethyldichlorosilane hydrolysate enters the system from the first-stage coalescing device, while process water enters from the third-stage coalescing device. In each stage coalescing device, the acidic hydrolysate is mixed with dilute hydrochloric acid or process water. Through multiple washing and coalescence processes, oil-water phase separation is achieved, simultaneously reducing the acid value of the hydrolysate. Each stage coalescing device includes: two static mixers in series, a pre-filter, and a large coalescing device in a "Z" shape. Each stage coalescing device contains four filter cartridges. Through repeated experiments, a modified polyvinylidene fluoride filter cartridge from Pall Corporation was ultimately selected. After continuous three-stage coalescing treatment, the acid value of dimethyldichlorosilane hydrolysate can be reduced to below 10 PPM. This coalescence device replaces the traditional alkaline washing + water washing method for acidic hydrolysates, significantly reducing wastewater generation while lowering the acid value of the hydrolysates. It avoids the high energy consumption and pollution associated with traditional multi-stage alkaline washing-water washing processes.

[0004] The device includes at least one aggregator unit, which includes a hydrolysate pipeline connected to a static mixer, the static mixer connected to a pre-filter, the pre-filter connected to a coalescer, and the coalescer connected to the finished hydrolysate product area.

[0005] The static mixer consists of two identical static mixers connected in series. The static mixer can thoroughly mix the dimethylsiloxane acidic hydrolysate with water, which helps to reduce the chloride ion content and acid value of the hydrolysate.

[0006] The pre-filter consists of two identical pre-filters connected in series. On one hand, the pre-filter removes impurities from the oil-water mixture, preventing them from clogging the coalescer filter element and protecting the special coalescer filter element from clogging and damage. On the other hand, the pre-filter also reduces emulsification of the mixture.

[0007] In the coalescer, the first transverse unit containing a filter element is connected to the lower part of the second vertical unit containing a filter element, the upper part of the second vertical unit containing a filter element is connected to the third transverse unit containing a filter element, and the third transverse unit containing a filter element is connected to the lower part of the fourth vertical unit containing a filter element.

[0008] The filter element in the first transverse unit containing the filter element is disposed in the middle of the first transverse unit containing the filter element, and cavities are formed at both ends of the first transverse unit containing the filter element. The front cavity is a buffer zone into which the hydrolyzed mixture after being filtered by the pre-filter enters, so that the hydrolyzed mixture can be aggregated and separated by the first filter element and enter the end cavity.

[0009] The filter element in the second vertical unit containing the filter element is disposed in the middle of the second vertical unit containing the filter element, and cavities are formed at the upper and lower ends of the second vertical unit containing the filter element. In some embodiments, it can be seen that the middle part refers to the interior, and the position of the filter element is such that there are cavities at both ends, and the volume of the cavities may be the same or different.

[0010] The first transverse unit containing the filter element is connected to the lower cavity of the second vertical unit containing the filter element.

[0011] In some embodiments, it can be understood that after being aggregated and filtered by the first transverse unit containing a filter element, the material enters the lower cavity of the second vertical unit containing a filter element from the end cavity of the first transverse unit containing a filter element. After the hydrolyzed mixture gradually aggregates, it is filtered upwards from the filter element in the second vertical unit containing a filter element, and the filtered material enters the upper cavity of the second vertical unit containing a filter element.

[0012] In some embodiments, it can be understood that the length of the second vertical unit containing the filter element is much greater than the length of the first horizontal unit containing the filter element, such as 10-50 times the length. The length of the lower cavity of the second vertical unit containing the filter element is much greater than the length of the first horizontal unit containing the filter element, such as 5-20 times the length, to achieve a sufficiently long buffer time and buffer zone, so that the hydrolyzed mixture that is filtered by the first horizontal unit containing the filter element accumulates and settles in the lower cavity, and oil-water separation is achieved, with the water phase settling and the oil phase floating, and the oil phase being filtered through the filter element under the action of the water phase.

[0013] In some embodiments, it can be understood that the length of the upper cavity of the second vertical unit containing the filter element is much greater than the length of the third horizontal unit containing the filter element, such as 5-20 times, to achieve a sufficiently long buffer time and buffer zone, so that the oil phase filtered in the second vertical unit containing the filter element overflows and slowly enters the third horizontal unit containing the filter element.

[0014] The filter element in the third transverse unit containing the filter element is disposed in the middle of the third transverse unit containing the filter element, and cavities are formed at both ends of the third transverse unit containing the filter element; wherein, one end cavity is connected to the upper cavity of the second vertical unit containing the filter element, and the other end cavity is connected to the fourth vertical unit containing the filter element.

[0015] In some embodiments, it can be understood that a cavity at one end receives the hydrolyzed mixture overflowing from the upper cavity of the second vertical unit containing a filter element, filters it through the filter element, and then enters the cavity at the end.

[0016] The first transverse unit containing a filter element and the third transverse unit containing a filter element can have the same size and the same filter element position.

[0017] The filter element in the fourth vertical unit containing the filter element is disposed at the upper part of the fourth vertical unit containing the filter element, and a cavity is formed at the lower part of the fourth vertical unit containing the filter element. Then, the cavity at the other end of the third horizontal unit containing the filter element is connected to the lower cavity of the fourth vertical unit containing the filter element.

[0018] In some embodiments, it can be understood that the hydrolyzed mixture from the third transverse unit containing the filter element enters the lower cavity of the fourth vertical unit containing the filter element. The volume of the lower cavity is larger than that of the cavity of the third transverse unit containing the filter element, such as 1-10 times. The lower cavity serves as a buffer to achieve the further separation of oil and water in the hydrolyzed mixture.

[0019] The filter element is selected from polyolefin special filter elements.

[0020] In the technical solution of this utility model, the coalescer innovatively adopts a "Z" structure, and a single coalescer can accommodate four special filter elements, making efficient use of equipment volume. The coalescer of this device adopts a "Z" shaped structure, which can accommodate four filter elements, maximizing the use of equipment space, reducing the number of equipment, and saving equipment footprint. The "Z" shaped structure has two settling zones, which facilitates the control of gravity sedimentation separation of oil and water.

[0021] The bottom of the cavity of the second vertical unit containing the filter element is connected to the hydrolysate pipeline via a pipe. This pipeline is equipped with a process water inlet pipe and / or a return acid inlet pipe, forming a circulating separation and chloride ion removal device.

[0022] When the device used for reducing acid value during the separation and washing process of dimethyldichlorosilane hydrolysate contains a multi-stage aggregator, each aggregator is connected in series, and the structure of each aggregator is substantially the same as that understood by those skilled in the art. In each aggregator, the bottom of the second vertical unit containing a filter element is connected to the discharge pipe of the previous stage hydrolysate via a pipe; simultaneously, in the last aggregator, the bottom of the second vertical unit containing a filter element is connected to the discharge pipe of the previous stage hydrolysate via a pipe, and a process water inlet pipe and / or a return acid inlet pipe are provided, forming a circulating separation and removal device for chloride ions.

[0023] Taking the multi-stage aggregator device as an example of a three-stage aggregator device connected in series; the bottom of the second vertical unit containing the filter element in the third-stage aggregator device is connected to the second-stage hydrolysate feed pipe via a pipe; the bottom of the second vertical unit containing the filter element in the second-stage aggregator device is connected to the first-stage hydrolysate feed pipe via a pipe.

[0024] An interface gauge is used to control the liquid level at the bottom of the coalescer, ensuring that the acid interface at the bottom is sufficiently low to prevent it from being carried to the next stage coalescer with the hydrolysate, thereby improving coalescence efficiency, stabilizing process control, and ensuring uniform product quality. Sight glasses on the pipes between each process and on the equipment itself allow for direct observation of the morphology of dimethyldichlorosilane hydrolysis products within the system, enabling timely adjustments to parameters such as the oil-water interface and acid replenishment flow rate.

[0025] Meanwhile, at the bottom of the second vertical unit containing the filter element in the third-stage aggregator device, a process water inlet pipe and / or a return acid inlet pipe are installed on the second-stage hydrolysate discharge pipe via a pipeline, forming a device for circulating separation and removal of chloride ions.

[0026] The acidic hydrolysate in the first and third transverse units containing filter elements enters from the inside of the filter element and exits from the outside.

[0027] In the second and fourth vertical units containing filter elements, acidic hydrolysates enter from the outside of the filter element and exit from the inside.

[0028] Differential pressure transmitters are installed at the front and rear ends of the first transverse unit containing the filter element and the third transverse unit containing the filter element. Differential pressure transmitters are also installed before and after the pre-filter. This allows for intuitive judgment and timely switching of equipment and replacement of filter bags, which ensures the stable operation of the entire oil-water separation device.

[0029] In addition to the aforementioned apparatus, this invention also provides a method for reducing the acid value of dimethyldichlorosilane hydrolysate during the separation and washing process. This method employs a coalescence liquid-liquid separation technique. In this apparatus, the hydrolysate is washed downstream by process water, while the settled aqueous phase washes the hydrolysate upstream. The process using the aforementioned apparatus, in a separation and purification process comprising only a single-stage aggregator, includes the following steps:

[0030] The dimethyldichlorosiloxane hydrolysate and the aqueous phase enter a static mixer. After thorough mixing, the mixture enters a pre-filter for filtration. After filtration, it enters a coalescer. First, it is washed and coalesced in the first horizontal unit containing a filter element. Then, the hydrolysate moves upward through the second vertical unit containing a filter element for repeated coalescing and separation. The separated aqueous phase accumulates in the lower cavities of the first horizontal unit and the second vertical unit containing a filter element and is pumped to the previous stage coalescer for washing. The hydrolysate separated by the second filter element continues to coalesce and separate in the third and fourth filter elements. The separated aqueous phase accumulates in the lower cavities of the third horizontal unit and the fourth vertical unit containing a filter element. The hydrolysate separated by the fourth filter element flows out of the equipment from the top outlet of the coalescer, resulting in purified dimethyldichlorosiloxane hydrolysate.

[0031] The acid value of the dimethyldichlorosilane acid hydrolysate before entering the coalescer is approximately 0.15~0.5%.

[0032] When the coalescing unit is a multi-stage coalescing unit connected in series, the purified dimethyldichlorosilane hydrolysate is mixed again with the aqueous phase (which includes back acid, process water, and circulating dilute acid) and then enters the next stage coalescing unit. Specifically, it enters the static mixer in the next stage coalescing unit for coalescence separation again, and obtains purified dimethyldichlorosilane hydrolysate again. This process of mixing the purified dimethyldichlorosilane hydrolysate with the aqueous phase and entering the coalescence separation process realizes the coalescence liquid-liquid separation technology.

[0033] The coalescing unit consists of three stages connected in series. Process water is pumped into the inlet of the third-stage coalescing unit. Once a certain liquid level is reached at the bottom of the connection between the first and second filter elements in the third-stage coalescing unit, the third-stage circulation pump is started to replenish water to the second-stage coalescing unit. Once a certain liquid level is reached at the bottom of the connection between the first and second filter elements in the second-stage coalescing unit, the second-stage circulation pump is started to replenish water to the first-stage coalescing unit. Once a certain liquid level is reached at the bottom of the connection between the first and second filter elements in the first-stage coalescing unit, the first-stage circulation pump is started to replenish water to the front-end system for reaction with dimethyldichlorosilane. The dimethyldichlorosilane acidic hydrolysate produced by the reaction is filtered through a pre-filter and enters the coalescing unit for multiple oil-water separations. The hydrolysate from the coalescing unit then enters the second-stage and third-stage coalescing units for further processing to obtain purified dimethyldichlorosilane hydrolysate.

[0034] The process water replenishment to dimethyl methacrylate (DMMA) in the third-stage coalescer unit is in a volume ratio of 0.2 to 0.3:1.

[0035] The pressure difference of the pre-filter is <50 kPa, and the pressure difference between the first and third filter elements is <100 kPa.

[0036] After separation and washing using the method described above, the acid value of the hydrolysate is less than 10 ppm, more preferably less than 5 ppm, and even more preferably less than 1 ppm.

[0037] In the technical solution of this utility model, one aspect is to use an interface gauge to control the liquid level at the bottom of the coalescer, ensuring that the bottom acid interface is sufficiently low and will not be carried to the next stage coalescer with the hydrolysate, thereby improving coalescence efficiency, stabilizing process control, and ensuring uniform product quality.

[0038] By calculating and matching the height of the boundary gauge and the water supply flow of the five-ring system with the current feed flow rate, the residence time of the hydrolysis products can be controlled to make the product quality more stable. Secondly, the pressure difference before and after each filter and coalescer filter element should be monitored, and the filter should be switched and the filter bag replaced in time to prevent impurities from being carried into the equipment and causing filter element blockage and damage. Thirdly, the equipment and pipeline sight glasses should be observed to determine the current status of the hydrolysis products by observing their color and morphology, and the parameters such as reaction boundary and water supply should be adjusted in time.

[0039] The test results show that the acid value can be reduced to 70% of the raw material liquid after treatment by a three-stage coalescer, to 90-98% after treatment by a four-stage coalescer, and to 98-99.99% after treatment by a five-stage coalescer. Attached Figure Description

[0040] Figure 1 This is a schematic diagram of the structure of the first-stage aggregator device.

[0041] Figure 2 This is a schematic diagram of a three-stage aggregator device.

[0042] The system includes: 1. Hydrolysate pipeline; 2. Static mixer; 3. Pre-filter; 4. Coalescer; 5. First horizontal unit containing filter element 4-1; 6. Second vertical unit containing filter element 4-2; 7. Third horizontal unit containing filter element 4-3; 8. Fourth vertical unit containing filter element 4-4; 9. Level gauge; 10. Differential pressure gauge; 11. Process water; 2. Acidic hydrolysate; 3. Finished product hydrolysate; 4. Dilute acid (or acid discharge). The shaded areas indicate the filter element installation locations. Detailed Implementation

[0043] Example 1

[0044] An apparatus for reducing the acid value of dimethyldichlorosilane hydrolysate during the separation and washing process, the apparatus comprising a primary aggregator device, such as... Figure 1 As shown, the agglomerator device includes a hydrolysate pipeline 1 connected to a static mixer 2, a static mixer 2 connected to a pre-filter 3, a pre-filter 3 connected to a coalescer 4, and a coalescer 4 connected to a clean hydrolysate product area.

[0045] In the coalescer 4, the lower part of the first horizontal unit 4-1 containing the filter element is connected to the lower part of the second vertical unit 4-2 containing the filter element, the upper part of the second vertical unit 4-2 containing the filter element is connected to the third horizontal unit 4-3 containing the filter element, and the lower part of the third horizontal unit 4-3 containing the filter element is connected to the lower part of the fourth vertical unit 4-4 containing the filter element.

[0046] The filter element in the first transverse unit 4-1 containing the filter element is disposed in the middle of the first transverse unit 4-1 containing the filter element, and cavities are formed at both ends of the first transverse unit 4-1 containing the filter element.

[0047] The filter element in the second vertical unit 4-2 containing the filter element is disposed in the middle of the second vertical unit 4-2 containing the filter element, and cavities are formed at the upper and lower ends of the second vertical unit 4-2 containing the filter element.

[0048] The first transverse unit 4-1 containing a filter element is connected to the lower cavity of the second vertical unit 4-2 containing a filter element; the length of the second vertical unit 4-2 containing a filter element is greater than that of the first transverse unit 4-1 containing a filter element.

[0049] The filter element in the third transverse unit 4-3 containing the filter element is disposed in the middle of the third transverse unit 4-3 containing the filter element, and cavities are formed at both ends of the third transverse unit 4-3 containing the filter element; wherein, one end cavity is connected to the upper cavity of the second vertical unit 4-2 containing the filter element, and the other end cavity is connected to the fourth vertical unit 4-4 containing the filter element.

[0050] The filter element in the fourth vertical unit 4-4 containing the filter element is disposed at the upper part of the fourth vertical unit 4-4 containing the filter element, and a cavity is formed at the lower part of the fourth vertical unit 4-4 containing the filter element. Then, the cavity at the other end of the third horizontal unit 4-3 containing the filter element is connected to the lower cavity of the fourth vertical unit 4-4 containing the filter element.

[0051] The filter element is selected from Pall's modified polyvinylidene fluoride filter element.

[0052] The bottom of the second vertical unit 4-2 containing the filter element is connected to the hydrolysate pipe 1 via a pipe;

[0053] The pipeline is equipped with a process water inlet pipe and / or a return acid inlet pipe, forming a device for circulating separation and removal of chloride ions.

[0054] Differential pressure transmitters are provided at the front and rear ends of the first horizontal unit 4-1 containing a filter element, the second vertical unit 4-2 containing a filter element, the third horizontal unit 4-3 containing a filter element, and the fourth vertical unit 4-4 containing a filter element.

[0055] Example 2

[0056] An apparatus for reducing the acid value of dimethyldichlorosilane hydrolysate during the separation and washing process, the apparatus comprising a three-stage aggregator device, such as... Figure 2 As shown, the agglomerator device includes a hydrolysate pipeline 1 connected to a static mixer 2, a static mixer 2 connected to a pre-filter 3, a pre-filter 3 connected to a coalescer 4, and a coalescer 4 connected to a clean hydrolysate product area.

[0057] In the coalescer 4, the lower part of the first horizontal unit 4-1 containing the filter element is connected to the lower part of the second vertical unit 4-2 containing the filter element, the upper part of the second vertical unit 4-2 containing the filter element is connected to the third horizontal unit 4-3 containing the filter element, and the lower part of the third horizontal unit 4-3 containing the filter element is connected to the lower part of the fourth vertical unit 4-4 containing the filter element.

[0058] The filter element in the first transverse unit 4-1 containing the filter element is disposed in the middle of the first transverse unit 4-1 containing the filter element, and cavities are formed at both ends of the first transverse unit 4-1 containing the filter element.

[0059] The filter element in the second vertical unit 4-2 containing the filter element is disposed in the middle of the second vertical unit 4-2 containing the filter element, and cavities are formed at the upper and lower ends of the second vertical unit 4-2 containing the filter element.

[0060] The first transverse unit 4-1 containing a filter element is connected to the lower cavity of the second vertical unit 4-2 containing a filter element; the length of the second vertical unit 4-2 containing a filter element is greater than that of the first transverse unit 4-1 containing a filter element.

[0061] The filter element in the third transverse unit 4-3 containing the filter element is disposed in the middle of the third transverse unit 4-3 containing the filter element, and cavities are formed at both ends of the third transverse unit 4-3 containing the filter element; wherein, one end cavity is connected to the upper cavity of the second vertical unit 4-2 containing the filter element, and the other end cavity is connected to the fourth vertical unit 4-4 containing the filter element.

[0062] The filter element in the fourth vertical unit 4-4 containing the filter element is disposed at the upper part of the fourth vertical unit 4-4 containing the filter element, and a cavity is formed at the lower part of the fourth vertical unit 4-4 containing the filter element. Then, the cavity at the other end of the third horizontal unit 4-3 containing the filter element is connected to the lower cavity of the fourth vertical unit 4-4 containing the filter element.

[0063] The filter element is made of modified PVDF.

[0064] The above describes the overall structure of the primary aggregator device. The primary aggregator device is connected in series with the secondary aggregator device, and the secondary aggregator device is connected in series with the tertiary aggregator device. The primary aggregator device, the secondary aggregator device, and the tertiary aggregator device contain the same structural components.

[0065] The fourth vertical unit containing a filter element in the primary aggregator device is connected to the static mixer in the secondary aggregator device to form a connector; the fourth vertical unit containing a filter element in the secondary aggregator device is connected to the static mixer in the tertiary aggregator device to form a connector; the top of the fourth vertical unit containing a filter element in the tertiary aggregator device is treated to obtain clean hydrolysate; thus forming a series connection.

[0066] The second vertical unit containing a filter element of the three-stage aggregator device is connected to the static mixer of the three-stage aggregator device via a pipe to form a return material cycle; the second vertical unit containing a filter element of the two-stage aggregator device is connected to the static mixer of the two-stage aggregator device via a pipe to form a return material cycle; the second vertical unit containing a filter element of the one-stage aggregator device is connected to the static mixer of the one-stage aggregator device via a pipe to form a return material cycle.

[0067] It would be meaningless for someone skilled in the art to know that a circulating pump is connected to the pipeline.

[0068] Example 3

[0069] A method for reducing acid value during the separation and washing process of dimethyldichlorosilane hydrolysate, wherein the apparatus of Example 2 performs the following process:

[0070] After process water is pumped into the tertiary coalescer unit until the equipment is full, the tertiary circulation pump is started to circulate the water and simultaneously begin returning water to the secondary coalescer unit. Once the secondary coalescer unit is full, water is returned to the primary coalescer unit. After the primary coalescer unit is full, acidic dimethyldichlorosilane hydrolysate is pumped in and mixed with the water phase from the secondary coalescer unit at a volume ratio of 3:1. This mixture is then fed into a series of two-stage static mixers for thorough mixing and extraction. After extraction, the mixture is filtered through a pre-filter and then enters the coalescer unit for multiple oil-water separations. The hydrolysate from the coalescer unit then sequentially enters the secondary and tertiary coalescer units for further processing. Upon reaching the inlet of the static mixer in the tertiary coalescer unit, it mixes with process water from outside the unit and its own circulating acid before undergoing oil-water separation within the coalescer unit. This process significantly reduces the chloride ion content in the hydrolysate.

[0071] In the aforementioned primary, secondary, and tertiary coalescing devices, the hydrolysate from the premixer first undergoes oil-water separation in the first horizontal unit containing a filter element. The acid deposited at the bottom is pumped to the next stage. The hydrolysate then passes upwards through the second vertical unit containing a filter element, repeating the oleic acid separation process. After passing through the vertical filter element, the hydrolysate reaches the top of the coalescer, where it coalesces and undergoes oil-water separation in the third horizontal unit and the fourth vertical unit containing a filter element at the top. The mixture flows out of the equipment from the coalescer outlet after passing through four filter elements for coalescing and separation, yielding purified dimethyldichlorosilane hydrolysate. Each special filter element in the coalescer is equipped with a differential pressure transmitter before and after it, and pressure gauges are also installed before and after the pre-filter.

[0072] After separation and washing using the method described above, the chloride ion content after treatment by a primary coalescer device is 500-1000 PPM; the chloride ion content after treatment by a secondary coalescer device is 50-100 PPM; and the chloride ion content after treatment by a tertiary coalescer device is 5 ppm.

Claims

1. A system for reducing the acid value of dimethyldichlorosilane hydrolysate during the separation and washing process, characterized in that, The system includes at least one aggregator device, which includes a hydrolysate feed pipe (1) connected to a static mixer (2), the static mixer (2) connected to a pre-filter (3), the pre-filter (3) connected to a coalescer (4), and the coalescer (4) connected to the finished hydrolysate product area.

2. The system for reducing the acid value of dimethyldichlorosilane hydrolysate during the separation and washing process according to claim 1, characterized in that, In the coalescer (4), the first transverse unit (4-1) containing a filter element is connected to the lower part of the second vertical unit (4-2) containing a filter element, the upper part of the second vertical unit (4-2) containing a filter element is connected to the third transverse unit (4-3) containing a filter element, and the third transverse unit (4-3) containing a filter element is connected to the lower part of the fourth vertical unit (4-4) containing a filter element.

3. The system for reducing the acid value of dimethyldichlorosilane hydrolysate during the separation and washing process according to claim 2, characterized in that, The filter element in the first transverse unit (4-1) containing the filter element is disposed in the middle of the first transverse unit (4-1) containing the filter element, and cavities are formed at both ends of the first transverse unit (4-1) containing the filter element.

4. The system for reducing the acid value of dimethyldichlorosilane hydrolysate during the separation and washing process according to claim 3, characterized in that, The filter element in the second vertical unit (4-2) containing the filter element is disposed in the middle of the second vertical unit (4-2) containing the filter element, and cavities are formed at the upper and lower ends of the second vertical unit (4-2) containing the filter element; one end cavity of the first horizontal unit (4-1) containing the filter element is connected to the lower end cavity of the second vertical unit (4-2) containing the filter element.

5. The system for reducing the acid value of dimethyldichlorosilane hydrolysate during the separation and washing process according to claim 4, characterized in that, The filter element in the third transverse unit (4-3) containing the filter element is located in the middle of the third transverse unit (4-3) containing the filter element, and cavities are formed at both ends of the third transverse unit (4-3) containing the filter element; wherein, one end cavity is connected to the upper cavity of the second vertical unit (4-2) containing the filter element, and the other end cavity is connected to the fourth vertical unit (4-4) containing the filter element.

6. The system for reducing the acid value of dimethyldichlorosilane hydrolysate during the separation and washing process according to claim 5, characterized in that, The filter element in the fourth vertical unit (4-4) containing the filter element is located at the upper part of the fourth vertical unit (4-4) containing the filter element, and a cavity is formed at the lower part of the fourth vertical unit (4-4) containing the filter element. Then, the cavity at the other end of the third horizontal unit (4-3) containing the filter element is connected to the lower cavity of the fourth vertical unit (4-4) containing the filter element.

7. The system for reducing the acid value of dimethyldichlorosilane hydrolysate during the separation and washing process according to claim 1, characterized in that, The bottom of the second vertical unit (4-2) containing the filter element is connected to the hydrolysate feed pipe (1) via a pipe to form a device for circulating washing to reduce the acid value of the hydrolysate.

8. The system for reducing the acid value of dimethyldichlorosilane hydrolysate during the separation and washing process according to claim 1, characterized in that, When the device is a multi-stage aggregator device, each stage aggregator device is connected in series. In each stage aggregator device, the top of the fourth vertical unit containing a filter element is connected via a pipe to the port hydrolysate feed pipe of the first horizontal unit containing a filter element of the next stage aggregator for conveying acidic hydrolysate. The bottom of the second vertical unit containing the filter element is connected to the discharge pipe of the previous stage coalescer via a pipe to transport dilute hydrochloric acid. The bottom of the second vertical unit containing a filter element in the last stage aggregator device is connected to the discharge pipe of the previous stage hydrolysate via a pipe, and a process water inlet pipe is installed to form a device for circulating washing to reduce the acid value of the hydrolysate.

9. The system for reducing the acid value of dimethyldichlorosilane hydrolysate during the separation and washing process according to claim 8, characterized in that, The multi-stage aggregator device consists of three aggregator devices connected in series.

10. The system for reducing the acid value of dimethyldichlorosilane hydrolysate during the separation and washing process according to claim 2, characterized in that, The acidic hydrolysate from the first transverse unit (4-1) containing the filter element and the third transverse unit (4-3) containing the filter element enters from the inside of the filter element and exits from the outside. In the second vertical unit (4-2) containing a filter element and the fourth vertical unit (4-4) containing a filter element, acidic hydrolysates enter from the outside of the filter element and exit from the inside. Differential pressure transmitters are provided at the front and rear ends of the first transverse unit (4-1) containing a filter element and the third transverse unit (4-3) containing a filter element.

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