Disc ceramic membrane treatment device for high-solid-content and high-concentration materials

Abstract

The utility model discloses a disc ceramic membrane treatment device for high-solid-content and high-concentration materials. The disc ceramic membrane treatment device comprises a vertical rotary disc ceramic membrane unit, a material tank, a backwashing tank and a control unit, in the concentrating process in the field of high-concentration and high-solid-content materials, the viscosity change span is large, a conventional tubular ceramic membrane system or a rotary membrane system cannot be suitable for conveying the materials with large viscosity change, cross flow cannot be guaranteed, so that the membrane pollution speed is too high due to hole blockage of a tubular ceramic membrane or excessive concentration of an internal cavity, and the membrane pollution speed is too high. Therefore, the effect of high-multiple concentration cannot be achieved. A double-rotor pump conveying system and a constant-pressure control mode are adopted, the defect can be overcome, material conveying is guaranteed, and conveying and filtering in the field of high-concentration and high-viscosity materials can be achieved.

Description

Technical Field

[0001] The utility model specifically relates to a disc ceramic membrane processing device for high-solid content and high-concentration viscosity materials. Background Art

[0002] Inorganic ceramic membranes have the characteristics of high temperature resistance, organic solvent resistance, microbial resistance, good chemical stability, high mechanical strength, narrow pore size distribution, good separation performance, easy cleaning, and long service life. They have been widely used in the fields of food industry, biopharmaceuticals, environmental engineering, chemical industry, petrochemical industry, metallurgical industry, etc. The prior art has gradually developed two types of ceramic membranes in ceramic membrane filtration, one is a tubular ceramic membrane, and the other is a disc-type ceramic membrane (hereinafter referred to as a disc membrane). In the actual manufacturing process, the disc membrane has higher difficulty and cost than the tubular ceramic membrane. In terms of systems and equipment, the tubular ceramic membrane has a simpler sealing method and a simpler industrial-scale integration method, while the disc membrane equipment and system are more difficult to manufacture, more difficult to integrate, and more difficult to operate. In conventional application fields, the production efficiency of the disc membrane will be 3-5 times lower than that of the tubular ceramic membrane, and it is not competitive compared with the tubular ceramic membrane. Therefore, the application of the disc membrane is further limited.

[0003] Tubular ceramic membranes provide shear force on the membrane surface through large cross-flow. In the field of high solid content and high-concentration viscous liquid, the change in viscosity and the sharp change in solid content will cause the pump performance to drop sharply, resulting in blockage of the tubular ceramic membrane and frequent membrane failure. In response to this phenomenon, the rotating disc membrane is more suitable for the field of high solid content and high-concentration viscous liquid because of its larger dirt holding space and the advantages of providing shear force on the membrane surface through rotation to effectively weaken the filter cake layer. CN108939922A discloses a rotary ceramic membrane filtration separation process and device. However, when this process and device are used in the field of high solid content and high-concentration viscous liquid, there will be many dead corners in the equipment, which are easy to breed bacteria, have low operating reliability, poor cleaning recovery, and the cavity volume of the rotary membrane is too large, and the matching is too complicated. The rotary disc ceramic membrane will swing to a certain extent during operation, and disturbances will occur during the fluid flow. The accessories are easy to collide with the rotary disc ceramic membrane and break the rotary disc ceramic membrane. The feasibility of the solution is poor, and high concentration and low efficiency cannot be achieved. Problems such as this are not suitable for the field of high solid content and high-concentration viscous liquid. Utility Model Content

[0004] The utility model aims to overcome the defects of the prior art and provide a disc ceramic membrane treatment device for high solid content and high concentrated viscosity materials and its application.

[0005] The technical solution of the utility model is as follows:

[0006] A disc ceramic membrane treatment device for high solid content and high viscosity materials, comprising a vertical rotating disc ceramic membrane unit, a material tank, a backwash tank and a control unit.

[0007] A vertical rotating disc ceramic membrane unit comprises a membrane unit cavity, a rotating hollow shaft, a plurality of rotating disc ceramic membranes arranged in the membrane unit cavity and a driving assembly; a membrane unit feed port is arranged at the lower part of the membrane unit cavity, and a reflux outlet is arranged at the upper part; the rotating hollow shaft is vertically arranged in the membrane unit cavity, a plurality of rotating disc ceramic membranes are arranged in parallel with the sealing sleeve at the upper part, and the inner cavity of the rotating hollow shaft is communicated with the internal flow channels of the plurality of rotating disc ceramic membranes; the driving assembly drives and connects the lower part of the rotating hollow shaft;

[0008] The material tank has a first liquid level sensor and a viscometer, a peripheral wall of which is provided with a heat-insulating jacket connected to a constant temperature tank, a discharge port at the bottom, and a feed port at the top.

[0009] The backwash tank has a second liquid level sensor, a backwash outlet is provided at the bottom, and a permeate inlet is provided at the top.

[0010] The discharge port of the material tank is connected to the feed port of the membrane unit cavity through a first automatic valve, a rotor pump group and a first pressure sensor in sequence. The rotor pump group includes a first rotor pump and a second rotor pump arranged in parallel. The first rotor pump is a low-clearance rotor and high-speed rotor pump, and the second rotor pump is a high-clearance rotor and low-speed rotor pump; the reflux outlet of the membrane unit cavity is connected to the feed port of the material tank through a second pressure sensor and a first regulating valve, and the external gas source is connected to the reflux outlet of the membrane unit cavity through a second automatic valve, and is connected to the feed port of the material tank through the second pressure sensor and the first regulating valve. ; The inner cavity of the rotating hollow shaft is connected to the permeate inlet of the backwash tank through the third pressure sensor, the second regulating valve and the third automatic valve in sequence, and is connected to the subsequent process through the third pressure sensor, the second regulating valve and the fourth automatic valve in sequence; the backwash outlet of the backwash tank is connected to the inner cavity of the rotating hollow shaft through a backwash pump and a fifth automatic valve and the third pressure sensor; the control unit is electrically connected to the above-mentioned first to fifth automatic valves, the first regulating valve, the second regulating valve, the first to third pressure sensors, the first to second liquid level sensors, the viscometer, the rotor pump group, the backwash pump and the drive assembly respectively;

[0011] The second pressure sensor is interlocked with the first rotor pump and the second rotor pump, and the control unit enables the first rotor pump and the second rotor pump to adjust their operating frequencies according to the pressure value obtained by the second pressure sensor, thereby adapting to changes in material viscosity; the viscometer is interlocked with the first rotor pump and the second rotor pump, and the control unit realizes the switching of the first rotor pump and the second rotor pump according to the data obtained by the viscometer; the backwash pump is interlocked with the first and second liquid level sensors and the third pressure sensor, and the control unit controls the on-off of the backwash process according to the liquid level data obtained by the first and second liquid level sensors, and realizes constant pressure backwashing according to the pressure value obtained by the third pressure sensor.

[0012] In a preferred embodiment of the present utility model, the driving assembly includes a driving motor and a transmission mechanism arranged at the lower part of the rotating hollow shaft which are connected in sequence, and the control unit is electrically connected to the driving motor.

[0013] In a preferred embodiment of the present invention, the discharge port of the material tank is connected to the waste discharge process via a sixth automatic valve, and the control unit is electrically connected to the sixth automatic valve.

[0014] In a preferred embodiment of the present invention, the feed port of the membrane unit cavity is connected to the waste discharge process via a seventh automatic valve, and the control unit is electrically connected to the seventh automatic valve.

[0015] In a preferred embodiment of the present invention, the backwash outlet of the backwash tank is connected to the waste discharge process through an eighth automatic valve, and the control unit is electrically connected to the eighth automatic valve.

[0016] In a preferred embodiment of the present invention, the discharge port of the material tank, the feed port of the membrane unit cavity and the backwash outlet of the backwash tank are connected to the waste discharge process through the sixth automatic valve, the seventh automatic valve and the eighth automatic valve respectively, and the control unit is electrically connected to the sixth to eighth automatic valves.

[0017] In a preferred embodiment of the present invention, the feed port of the material tank has a feed pipe extending into the lower part of the inner cavity of the material tank.

[0018] Further preferably, the lower end of the feed pipe has an elbow facing the inner wall of the tank.

[0019] The beneficial effects of the utility model are:

[0020] 1. In the field of high-viscosity and high-solid content materials, the viscosity changes greatly during the concentration process. The conventional tubular ceramic membrane system or rotary membrane system is not suitable for conveying materials with large viscosity changes, and cannot guarantee the cross-flow rate, resulting in the blocking of the tubular ceramic membrane or the excessive concentration of the internal cavity causing the membrane to be polluted too quickly, thus failing to achieve the effect of high-multiple concentration. The utility model adopts a dual-rotor pump conveying system and a matching constant pressure control method to overcome this defect, ensure material conveying, and realize conveying and filtration in the field of high-viscosity materials.

[0021] 2. The utility model can adopt forward washing and backwashing in coordination, which greatly removes the contamination layer on the membrane surface during the water washing stage, and promptly removes it from the membrane surface through rotating centrifugation and cross flow, which reduces the consumption of reagents to a certain extent. At the same time, during the drug washing, filtration, forward washing and backwashing are also used for combined cleaning. The contact between the rotating disc ceramic membrane and the reagent is greatly enhanced. Therefore, this cleaning method can greatly save the amount of reagents, and at the same time, the cleaning temperature can be appropriately reduced (membrane pollutants are removed more cleanly during the water washing stage); the temperature generally accelerates the dissolution of pollutants and increases the reaction rate between pollutants and reagents, so the amount of reagents can be greatly saved and the energy consumption of heating can be reduced.

[0022] 3. The utility model can use gas-assisted sewage discharge, which is conducive to the rapid discharge of pollutants. The internal structure of the cavity is simple, and there is no need to add additional components in the cavity to create more sanitary dead corners. BRIEF DESCRIPTION OF THE DRAWINGS

[0023] Figure 1 It is a structural schematic diagram of the high solid content and high concentration viscosity material disc ceramic membrane processing device of the utility model. DETAILED DESCRIPTION

[0024] The technical solution of the present utility model is further illustrated and described below through specific implementation modes in combination with the accompanying drawings.

[0025] Example 1

[0026] like Figure 1 As shown, a high solid content and high viscosity material disc ceramic membrane treatment device includes a vertical rotating disc ceramic membrane unit 1, a material tank 2, a backwash tank 3 and a control unit (not shown in the figure).

[0027] A vertical rotating disc ceramic membrane unit 1 comprises a membrane unit cavity 10, a rotating hollow shaft 11, a plurality of rotating disc ceramic membranes 12 arranged in the membrane unit cavity 10 and a driving assembly 13; a membrane unit feed port 101 is arranged at the lower part of the membrane unit cavity 10, and a reflux outlet 102 is arranged at the upper part. Preferably, a glass sight glass (not shown in the figure) is arranged at the upper part of the membrane unit cavity 10 to facilitate observation of the operation and cleaning conditions of the rotating disc ceramic membrane 12; the rotating hollow shaft 11 is vertically arranged in the membrane unit cavity 10, and a plurality of rotating disc ceramic membranes 12 are arranged in parallel with the sealing sleeve at the upper part thereof, and the inner cavity of the rotating hollow shaft 11 is connected to the internal flow channel of the plurality of rotating disc ceramic membranes 12; the driving assembly 13 drives the lower part of the rotating hollow shaft 11; the driving assembly 13 comprises a driving motor 131 and a transmission mechanism 132 arranged at the lower part of the rotating hollow shaft 11 which are connected in sequence.

[0028] The material tank 2 has a first liquid level sensor 21 and a viscometer 22, a peripheral wall of which is provided with a heat-insulating jacket 23 connected to a thermostatic bath, a lower portion of which is provided with a discharge port 24, and an upper portion of which is provided with a feed port 25, the feed port 25 having a feed pipe 26 extending into the lower portion of the inner cavity of the material tank 2, and the lower end of the feed pipe 26 having a 45-degree elbow 260 facing the inner wall of the material tank 2 (this design is conducive to preventing liquid impact and preventing a large amount of foam from being generated);

[0029] The backwash tank 3 has a second liquid level sensor 31, a backwash outlet 32 ​​is provided at the bottom, and a permeate inlet 33 is provided at the top.

[0030] The discharge port 24 of the material tank 2 is connected to the membrane unit feed port 101 of the membrane unit cavity 10 through a first automatic valve 51, a rotor pump group 4 and a first pressure sensor 61 in sequence. The rotor pump group 4 includes a first rotor pump 41 and a second rotor pump 42 arranged in parallel. The first rotor pump 41 is a low-clearance rotor high-speed rotor pump, and the second rotor pump 42 is a high-clearance rotor low-speed rotor pump;

[0031] The reflux outlet 102 of the membrane unit cavity 10 is connected to the feed inlet 25 of the material tank 2 through a second pressure sensor 62 and a first regulating valve 71, and the external gas source is connected to the reflux outlet 102 of the membrane unit cavity through a second automatic valve 52, and is connected to the feed inlet 25 of the material tank 2 through the second pressure sensor 62 and the first regulating valve 71; the inner cavity of the rotating hollow shaft 11 is connected to the permeate inlet 3 of the backwash tank 3 through the third pressure sensor 63, the second regulating valve 72 and the third automatic valve 53 in sequence. 3, and connected to the subsequent process through the third pressure sensor 63, the second regulating valve 72 and the fourth automatic valve 54 in sequence; the backwash outlet 32 ​​of the backwash tank 3 is connected to the inner cavity of the rotating hollow shaft 11 through a backwash pump 8 and a fifth automatic valve 55 and the third pressure sensor 63; the discharge port 24 of the material tank 2, the feed port 25 of the membrane unit cavity 10 and the backwash outlet 32 ​​of the backwash tank 3 are connected to the waste discharge process through the sixth automatic valve 56, the seventh automatic valve 57 and the eighth automatic valve 58 respectively;

[0032] The control unit is electrically connected to the first to eighth automatic valves 51-58, the first regulating valve 71, the second regulating valve 72, the first to third pressure sensors 61-63, the first liquid level sensor 21, the second liquid level sensor 31, the viscometer 22, the rotor pump group 4, the backwash pump 8 and the drive motor 131 of the drive assembly 13 respectively;

[0033] The second pressure sensor 62 is interlocked with the first rotor pump 41 and the second rotor pump 42. The control unit enables the first rotor pump 41 and the second rotor pump 42 to adjust their operating frequencies according to the pressure value obtained by the second pressure sensor 62, thereby adapting to changes in material viscosity; the viscometer 22 is interlocked with the first rotor pump 41 and the second rotor pump 42. The control unit realizes the switching of the first rotor pump 41 and the second rotor pump 42 according to the data obtained by the viscometer 22; the backwash pump 8 is interlocked with the first and second liquid level sensors 31 and the third pressure sensor 63. The control unit controls the on-off of the backwash process according to the liquid level data obtained by the first and second liquid level sensors 31, and realizes constant pressure backwashing according to the pressure value obtained by the third pressure sensor 63.

[0034] Preferably, the two ends of the second pressure sensor 62 are respectively provided with a first flow meter 621 and a first pressure gauge 622, the two ends of the third pressure sensor 63 are respectively provided with a second flow meter 631 and a second pressure gauge 632, and the discharge end of the rotor pump group 4 is provided with a third pressure gauge 43. The second flow meter 631 needs to have a two-way flow, and there is no obvious pressure loss when flowing through.

[0035] For high viscosity and high solid content materials, especially for materials with large viscosity variation span during the concentration process, the first rotor pump 41 can be started at first to ensure the transportation of low viscosity materials of 20-3000cP. When the viscosity increases to 3000cP, the first rotor pump 41 is stopped and the second rotor pump 42 is started to ensure the transportation of high viscosity materials. For the rotary membrane system, the flux is large at the beginning, and then as the viscosity and concentration multiple increase, the flux gradually decreases. In this process, the required cross-flow flow rate can decrease. However, for the rotor pump, different rotor pumps are required for the transportation of low viscosity and high viscosity materials. The second rotor pump 42 with high clearance and low speed is suitable for high viscosity, but not for low viscosity materials. It cannot meet the flow and pressure requirements under low viscosity. The low viscosity rotor pump may be overloaded or unable to transport high viscosity when reaching a certain viscosity. Therefore, for this situation, the first rotor pump 41 is started first to ensure its flow and pressure. When a certain viscosity is reached, the first rotor pump 41 is stopped and the second rotor pump 42 is started. In this process, constant pressure filtration is always maintained. As the viscosity increases, the filtration pressure may increase. The first rotor pump and the second rotor pump 42 are interlocked with the pressure sensor and use a frequency reduction method instead of reducing the pressure by the valve opening. The switching of the first rotor pump 41 and the second rotor pump 42 is interlocked with the viscometer 22, and the first rotor pump 41 and the second rotor pump 42 are switched according to the viscosity.

[0036] The working steps of this embodiment can be divided into conveying and filtering, sewage discharge, forward washing and backwashing coordination, water washing and chemical washing, as follows:

[0037] Conveying and filtering: The control unit is used to open the automatic valves except the second automatic valve 52 and the fourth to eighth automatic valves 58, set the frequency, start the first rotor pump 41, and then set the opening of the first regulating valve 71 to reach the set filtering pressure (the first pressure gauge 622 and the second pressure sensor 62). Under the pressure drive, the permeate is transmitted to the post-process interface or collected and stored in the post-process section. During the conveying and filtering process, the viscosity of the liquid in the tank 2 continues to increase, and the flow rate (first flowmeter 621) and pressure (first pressure gauge 622 and second pressure sensor 62) delivered by the rotor pump group 4 will increase. Therefore, the frequency of the first rotor pump 41 is reduced to perform constant pressure filtering. The second pressure sensor 62 and the first rotor pump 41 are interlocked to ensure that the first rotor pump 41 is within the use viscosity range. The viscosity is monitored by the viscometer 22. When the viscosity reaches a certain level, it is switched to the second rotor pump 42, and the frequency of the second rotor pump 42 is reduced to perform constant pressure filtering. In this way, the stable operation of the conveying system can be guaranteed when the viscosity changes greatly during filtration. If this control is not done, the pump may be damaged or insufficient cross-flow may be provided, causing the rotating membrane to foul faster and failing to achieve the goal of high concentration or high recovery rate.

[0038] Drainage: After the conveying and filtering is completed, stop the rotor pump group 4, open the second automatic valve 52, the sixth to eighth automatic valves 56-58 through the control unit, close the first automatic valve 51, the third automatic valve 53, the fourth automatic valve 54, and the fifth automatic valve 55, and discharge all the residual liquid in the material tank 2, the membrane unit cavity 10 and the backwash tank 3 through external gas source assistance and gravity discharge, which is conducive to subsequent cleaning work. Because after concentration, the viscosity of the material is often very high, and the gravity outflow speed is slow, gas assistance can be used to quickly discharge the material.

[0039] Forward and backwash coordination: Check the liquid level 2 of the material tank and the liquid level 3 of the backwash tank, ensure the operation of the first rotor pump 41, the second rotor pump 42 and the backwash pump 8, open the first automatic valve 51, the first regulating valve 71, the third automatic valve 53, the fifth automatic valve 55 through the control unit, close the second automatic valve 52, the fourth automatic valve 54 and the sixth to eighth automatic valves 56-58, start forward and backwash coordination, at this time, it is necessary to ensure that the opening of the first regulating valve 71 is 100%, and the concentrated liquid reflux pipeline cannot be pressed, so that the pressure of the first pressure gauge 622 and the second pressure sensor 62 is 0, and the backwash pump 8 is interlocked with the third pressure sensor 63, and the backwash is performed at a constant pressure, and the backwash pressure is controlled not to exceed 2.5 bar to prevent the rotating disc ceramic membrane 12 from breaking due to excessive pressure. At the same time, the first rotor pump 41 and the second rotor pump 42 are turned on for circulating flushing, which can be regarded as forward flushing. Therefore, the cleaning method of this stage is different from the conventional flushing and pump backwashing. The two are combined. Pump backwashing can loosen the connection between the attached membrane fouling layer and the rotating disc ceramic membrane 12, and then the entire membrane fouling layer can be easily peeled off and taken away from the rotating membrane component cavity under the action of the rotating centrifugal force and the flow of the feeding system. Note that if you need to achieve a better forward flushing and backwashing effect, you must ensure that the concentrated liquid return pipe cannot be pressurized, and the pressure of the first pressure gauge 622 and the second pressure sensor 62 is 0. If there is pressure, it will affect the backwashing effect.

[0040] Water washing: pure water is injected into both the material tank 2 and the backwash tank 3. The pure water injected into the material tank 2 only needs to meet the minimum circulation volume. The above-mentioned forward washing and backwashing coordination are started. At the same time, the initial water level in the material tank 2 cannot be too high. During backwashing, the backwash pump 8 will bring the water in the backwash tank 3 to the material tank 2. Therefore, it is easy to find that the water level of the material tank 2 will rise during water washing. Therefore, the entire backwash pump 8 needs to be interlocked with the material tank 2, and the backwashing is stopped when the target liquid level is reached. The liquid level of the backwash tank 3 is also interlocked with the backwash pump 8. When the liquid level drops to a certain level, the backwashing is stopped. The forward washing and backwashing are coordinated for 5-10 minutes, and the sewage is discharged. Then it is repeated 2-5 times. When the pure water in the material tank 2 is colorless, the water washing is completed and the drug washing stage is entered.

[0041] Drug washing: prepare a certain concentration of cleaning agent in the material tank 2, and then start the conveying and filtering. It is slightly different from the permeate in the conveying and filtering stage to the post-process section. The permeate in this stage flows to the backwash tank 3 for collection (open the third automatic valve 53, close the fourth automatic valve 54), adjust the filtration pressure, the first pressure gauge 622 pressure shows 1-2bar, adjust the valve opening of the second regulating valve 72, so that the second pressure gauge 632 can reach 0-0.5bar, and the pressure of the dialysate pipeline is conducive to the filling of the inner cavity of the rotating disc ceramic membrane 12 with the agent, which is conducive to cleaning. After filtering for 10-15 minutes, the control unit automatically starts the above-mentioned forward washing and backwashing coordination, and all the permeate collected by filtration is backwashed back into the material tank 2, and circulated 3-5 times. In this process, the temperature of the cleaning agent can be controlled at 35-60℃ through the insulation jacket 23 in the material tank 2, which is more effective. In general, the rotating disc ceramic membrane 12 can be cleaned and restored with 1-2% alkali. If it cannot be restored, 0.3-1% sodium hypochlorite can be added for mixed use. If there is heavy metal or scale pollution, it can be cleaned and restored with an acid cleaning agent. When changing the type of cleaning, the previous cleaning agent must be cleaned. The chemical washing stage is different from the existing common methods. There is filtration, forward flushing and backwashing to carry out chemical washing in coordination, and the cleaning effect will be better.

[0042] The above is only a preferred embodiment of the present invention, and therefore cannot be used to limit the scope of implementation of the present invention. That is, equivalent changes and modifications made according to the patent scope of the present invention and the content of the specification should still fall within the scope covered by the present invention.

Claims

1. A disc ceramic membrane treatment device for high solid content and high viscosity materials, characterized by: It includes a vertical rotating disc ceramic membrane unit, a material tank, a backwash tank and a control unit. A vertical rotating disc ceramic membrane unit comprises a membrane unit cavity, a rotating hollow shaft, a plurality of rotating disc ceramic membranes arranged in the membrane unit cavity and a driving assembly; a membrane unit feed port is arranged at the lower part of the membrane unit cavity, and a reflux outlet is arranged at the upper part; the rotating hollow shaft is vertically arranged in the membrane unit cavity, a plurality of rotating disc ceramic membranes are arranged in parallel with the sealing sleeve at the upper part, and the inner cavity of the rotating hollow shaft is communicated with the internal flow channels of the plurality of rotating disc ceramic membranes; the driving assembly drives and connects the lower part of the rotating hollow shaft; The material tank has a first liquid level sensor and a viscometer, a peripheral wall of which is provided with a heat-insulating jacket connected to a constant temperature tank, a discharge port at the bottom, and a feed port at the top. The backwash tank has a second liquid level sensor, a backwash outlet is arranged at the bottom, and a permeate inlet is arranged at the top. The discharge port of the material tank is connected to the feed port of the membrane unit cavity through a first automatic valve, a rotor pump group and a first pressure sensor in sequence. The rotor pump group includes a first rotor pump and a second rotor pump arranged in parallel. The first rotor pump is a low-clearance rotor and high-speed rotor pump, and the second rotor pump is a high-clearance rotor and low-speed rotor pump; the reflux outlet of the membrane unit cavity is connected to the feed port of the material tank through a second pressure sensor and a first regulating valve, and the external air source is connected to the reflux outlet of the membrane unit cavity through a second automatic valve, and is connected to the reflux outlet of the membrane unit cavity through the second pressure sensor. The force sensor and the first regulating valve are connected to the feed port of the material tank; the inner cavity of the rotating hollow shaft is connected to the permeate inlet of the backwash tank through the third pressure sensor, the second regulating valve and the third automatic valve in sequence, and is connected to the subsequent process through the third pressure sensor, the second regulating valve and the fourth automatic valve in sequence; the backwash outlet of the backwash tank is connected to the inner cavity of the rotating hollow shaft through a backwash pump and a fifth automatic valve and the third pressure sensor; the control unit is electrically connected to the above-mentioned first to fifth automatic valves, the first to second regulating valves, the first to third pressure sensors, the first to second liquid level sensors, the viscometer, the rotor pump group, the backwash pump and the drive assembly respectively; The second pressure sensor is interlocked with the first rotor pump and the second rotor pump; the viscometer is interlocked with the first rotor pump and the second rotor pump; the backwash pump is interlocked with the first and second liquid level sensors and the third pressure sensor.

2. A disc ceramic membrane treatment device for high solid content and high viscosity materials as claimed in claim 1, characterized in that: The driving assembly includes a driving motor and a transmission mechanism arranged at the lower part of the rotating hollow shaft which are connected in sequence, and the control unit is electrically connected to the driving motor.

3. A high solid content and high viscosity material disc ceramic membrane treatment device as claimed in claim 1, characterized in that: The material outlet of the material tank is connected to the waste discharge process through a sixth automatic valve, and the control unit is electrically connected to the sixth automatic valve.

4. A disc ceramic membrane treatment device for high solid content and high viscosity materials as claimed in claim 1, characterized in that: The feed port of the membrane unit cavity is connected to the waste discharge process through a seventh automatic valve, and the control unit is electrically connected to the seventh automatic valve.

5. A disc ceramic membrane treatment device for high solid content and high viscosity materials as claimed in claim 1, characterized in that: The backwash outlet of the backwash tank is connected to the waste discharge process through an eighth automatic valve, and the control unit is electrically connected to the eighth automatic valve.

6. A disc ceramic membrane treatment device for high solid content and high viscosity materials as claimed in claim 1, characterized in that: The discharge port of the material tank, the feed port of the membrane unit cavity and the backwash outlet of the backwash tank are connected to the waste discharge process through the sixth automatic valve, the seventh automatic valve and the eighth automatic valve respectively, and the control unit is electrically connected to the sixth to eighth automatic valves.

7. A disc ceramic membrane treatment device for high solid content and high viscosity materials as claimed in claim 1, characterized in that: The feed port of the material tank has a feed pipe extending into the lower part of the inner cavity of the material tank.

8. A disc ceramic membrane treatment device for high solid content and high viscosity materials as claimed in claim 7, characterized in that: The lower end of the feed pipe is provided with an elbow facing the inner wall of the material tank.

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