阅读说明：本技术 高含铜量高挥发性废酸处理系统及操作方法 (High-copper content and high-volatility waste acid treatment system and operation method ) 是由 单颖会 吴涛 战祥连 林双 陈龙霞 李振铎 于 2021-08-20 设计创作，主要内容包括：本发明属于化工废料处理技术领域,具体涉及一种高含铜量高挥发性废酸处理系统及操作方法,所述系统包括酸雾净化器、供碱系统、供酸系统、反应槽、缓存槽、压滤系统、围堰、排放系统、操控台和中和池,操作方法包括负压反应、降盐分处理、只排清液和双槽交替压滤。本发明不仅能有效防止酸雾或有毒气体逸出破换环境并危害操作者身体健康,还可避免滤液无法达标排放,盐分结晶,阻塞滤布、输送泵或者输送管路等问题。(The invention belongs to the technical field of chemical waste treatment, and particularly relates to a high-copper content and high-volatility waste acid treatment system and an operation method. The invention can not only effectively prevent acid mist or toxic gas from escaping to break the environment and harm the health of operators, but also avoid the problems that the filtrate can not be discharged up to the standard, the salt is crystallized, and the filter cloth, the delivery pump or the delivery pipeline are blocked, etc.)

1. The utility model provides a high copper content high volatility spent acid processing system, includes alkali storage tank (1), stores up useless acid tank (9), reaction tank (4), pressure filter (24) and buffer tank (29), and alkali storage tank (1) all is connected its characterized in that with reaction tank (4) with storing up useless acid tank (9): be connected with water pipe (5) on reaction tank (4), reaction tank (4) are connected with acid mist clarifier (11), aeration pipe I (6) have been laid in reaction tank (4), aeration pipe II (32) have been laid in buffer tank (29), clear solution export (15) on reaction tank (4) are connected with neutralization pond (40), turbid liquid export I (18) on reaction tank (4) and turbid liquid export II (33) of buffer tank (29) all are connected with pressure filter (24), the filtrating export of pressure filter (24) is connected with reaction tank (4) and buffer tank (29) respectively, clear solution discharge port (36) on buffer tank (29) are connected with neutralization pond (40) through precision filter (39).

2. The high copper content high volatility spent acid treatment system of claim 1, wherein: an alkali-leaching pipe (8) with a plurality of alkali-leaching holes is arranged above the inner part of the reaction tank (4), and the alkali-leaching pipe (8) is connected with the alkali storage tank (1).

3. The high copper content high volatility spent acid treatment system of claim 1, wherein: the aeration pipe I (6) is connected with the compressed air pipe (17) through the air throttle valve I (20), and the aeration pipe II (32) is connected with the compressed air pipe (17) through the air throttle valve II (21).

4. The high copper content high volatility spent acid treatment system of claim 1, wherein: the filter press (24) is provided with a material containing groove (25), the material containing groove (25) is provided with a liquid leakage hole (26), and the liquid leakage hole (26) is connected with a reflux opening (22) on the reaction tank (4).

5. The high copper content high volatility spent acid treatment system of claim 1, wherein: the reaction tank (4) is provided with an observation port I (13), a temperature measuring port (7) and a liquid level display interface (12).

6. The high copper content high volatility spent acid treatment system of claim 1, wherein: an observation port II (41) and a pump idling prevention liquid level port (35) are arranged on the buffer tank (29).

7. The high copper content high volatility spent acid treatment system of claim 1, wherein: cofferdams (3) are arranged outside the reaction tank (4) and the buffer tank (29) in a matching way.

8. A method for operating a high copper content high volatility spent acid treatment system as claimed in any one of claims 1 to 7, wherein: the operation steps are as follows:

(1) under the negative pressure environment, waste acid is introduced into the reaction tank, liquid alkali is poured into the reaction tank under the aeration condition for neutralization reaction, and after the reaction is finished, the aeration and alkali pouring are stopped for sedimentation;

(2) discharging the supernatant into a neutralization tank after sedimentation, adding water through a water pipe to dilute the precipitate, discharging the diluted supernatant into the neutralization tank, and then aerating to fully disperse the precipitate;

(3) conveying the sediment turbid liquid in the reaction tank to a filter press for filter pressing, and feeding the filtrate into a buffer tank;

(4) aerating the buffer tank, conveying the sediment turbid liquid in the buffer tank to a filter press for filter pressing, and allowing the filtrate to enter the reaction;

(5) and (4) repeating the operation of the step (3) and the operation of the step (4) for one time or more, filtering the clear liquid in the buffer tank by a precision filter, then feeding the clear liquid into a neutralization tank, and neutralizing the liquid in the neutralization tank to discharge the liquid after reaching the standard.

9. The method of operating a high copper content high volatility spent acid treatment system of claim 8, wherein: the filter precision of the filter cloth of the filter press is 2-20 mu m, and the filter precision of the filter element of the precision filter is 0.2-1 mu m.

10. The method of operating a high copper content high volatility spent acid treatment system of claim 8, wherein: when the liquid alkali is poured for neutralization reaction, stopping pouring alkali when the temperature reaches 80 ℃, and continuing to pour alkali after the temperature is reduced to 60 ℃; when the blue flocculent precipitate is found to be generated in the reaction tank, the alkali is poured in a point-moving mode, and the alkali pouring is stopped when the precipitate in the reaction tank is changed into black particles, so that the reaction is completed.

Technical Field

The invention belongs to the technical field of chemical waste treatment, and particularly relates to a high-copper content and high-volatility waste acid treatment system and an operation method.

Background

At present, a large amount of acid mist and even toxic gas escape to damage the environment and harm the body health of operators in the treatment process of waste acid with high copper content and high volatility; the filter cloth is not completely intercepted and cannot be discharged up to the standard; salt crystallization, blockage of filter cloth, conveying pump or conveying pipeline and the like.

CN 201824566283.6 discloses a high volatility abandonment mixed acid processing system of copper content, filters through the mode of circulation reciprocating, has solved the problem that the strong corrosive acid mist escapes and destroys the environment, harm the human body to and waste water discharge is not up to standard. However, in the using process, the problems that the filter cloth is not completely intercepted, the salt is crystallized, the filter cloth, a conveying pump or a conveying pipeline are blocked, and the drainage does not reach the standard exist.

Disclosure of Invention

The technical problem to be solved by the invention is as follows: the defects of the prior art are overcome, and the high-copper content and high-volatility waste acid treatment system and the operation method are provided, so that not only can acid mist or toxic gas be effectively prevented from escaping to break the environment and harm the body health of an operator, but also the problems that filtrate cannot reach the standard to be discharged, salt is crystallized, filter cloth, a conveying pump or a conveying pipeline is blocked and the like can be avoided.

In order to solve the technical problems, the invention adopts the following technical scheme:

the high-copper content and high-volatility waste acid treatment system comprises an acid mist purifier, an alkali supply system, an acid supply system, a reaction tank, a cache tank, a filter pressing system, a cofferdam, a discharge system, a control platform and a neutralization pond.

The acid mist purifier is communicated with the reaction tank through a pipeline, acid mist and toxic gas generated in the reaction process are taken away under the action of negative pressure, and the pipeline has strong acid resistance.

The alkali supply system consists of an alkali storage tank, an alkali supply pump, an alkali pouring pipe and a pipeline. Wherein, the alkali-leaching pipe is arranged above the reaction tank, the alkali supply pump, the alkali-leaching pipe and the pipeline are alkali-resistant, the alkali storage tank and the alkali supply pump as well as the alkali supply pump and the alkali-leaching pipe are communicated through the pipeline, and the alkali-leaching pipe is provided with a series of alkali-leaching holes.

The acid supply system consists of a waste acid storage tank, an acid supply pump and a pipeline. Wherein, store up useless acid tank, supply acid pump and pipeline strong acid resistance, store up useless acid tank and supply acid pump and reaction tank all through the pipeline intercommunication.

The feed pumps used in the invention are resistant to strong acid and strong alkali, the lift is 2-50 m, and the flow is 0.5-8 m³/h。

The reaction tank is resistant to strong acid and strong alkali, and an observation port I (with a cover plate), an acid inlet, an alkali inlet, an exhaust port, a temperature measuring port, a liquid level display interface, a backflow port (also serving as a filtrate inlet), an aeration air inlet, a water inlet, a turbid liquid outlet I and a clear liquid outlet are reserved on the upper portion of the tank body. The clear liquid outlet is arranged at the middle lower part of the reaction tank in the vertical direction and is communicated with the neutralization tank through a pipeline, and a control valve is arranged at the clear liquid outlet. An aeration pipe I is distributed in the reaction tank, a plurality of rows of aeration holes are formed in the aeration pipe I, and the aeration pipe is communicated with a compressed air pipeline. The temperature measuring port is inserted with an acid-base corrosion resistant thermocouple, and the display can directly read the temperature value.

The buffer tank is resistant to strong acid and strong alkali, and the tank body is provided with an observation port II (with a cover plate), a filtrate inlet, a turbid liquid outlet II, a clear liquid discharge port and an anti-pump idling liquid level port. And an aeration pipe II is distributed in the cache groove, a series of aeration holes are formed in the aeration pipe II, and the aeration pipe II is communicated with a compressed air pipeline. The clear liquid discharge port is arranged at the middle lower part of the vertical direction of the buffer tank and is communicated with the discharge pump, the precision filter and the neutralization tank through pipelines, and a control valve is arranged at the clear liquid discharge port.

The filter pressing system consists of a filter pressing platform, a filter press, a pneumatic diaphragm pump, a material containing groove and a pipeline. The filter press has an automatic pressure maintaining function, and the filter press table, the pneumatic diaphragm pump, the material containing groove, the filter press parts and the pipeline are resistant to strong alkali corrosion. The filtering precision (2-20) mu m of the filter cloth of the filter press. The liquid leakage holes are distributed on the material containing groove, filtrate seeped out from the filter cloth flows back to the reaction tank along the pipeline, the pneumatic diaphragm pump is communicated with the compressed air pipeline, the filter press is communicated with the reaction tank and the buffer tank through the pipeline, and the liquid in the reaction tank or the buffer tank can be respectively filtered and pressed through the switch of the valve. When liquid in the filter pressing reaction tank is filtered, the filtrate enters the buffer tank, and when liquid in the filter pressing buffer tank is filtered, the filtrate enters the reaction tank.

The cofferdam is resistant to strong acid and alkali corrosion, the reaction tank and the buffer tank are both provided with cofferdams, and anti-corrosive liquid leaks to the environment.

The discharge system consists of a discharge pump (the discharge pump is provided with an anti-idle rotation device), a precision filter and a pipeline, and the filtering precision of a filter element of the precision filter is (0.2-1) mu m.

The control platform can display the temperature of the liquid in the reaction tank, can control power switches of the acid mist purifier, the alkali supply pump, the acid supply pump, the filter press and the discharge pump, and can control air supply and water supply switches of each compressed air pipeline. Wherein, the power switch of the alkali supply pump has inching control function.

The neutralization pond has the function of adjusting acidic or alkaline liquid, and can be used for manual feeding neutralization and automatic feeding neutralization.

The operation method of the high-copper content and high-volatility waste acid treatment system comprises negative pressure reaction, salinity reduction treatment, only clear liquid discharge and double-tank alternate filter pressing. The negative pressure reaction operation is to perform neutralization reaction in a negative pressure environment, and the acid mist purifier takes away generated acid mist or toxic gas, so that the problems of environmental pollution and personnel injury are solved; the salinity reducing treatment operation comprises the steps of standing for a period of time after complete reaction, discharging most of clear liquid through a reaction tank after precipitates are settled to the bottom of the tank, then adding tap water to dilute the liquid in the reaction tank, discharging the clear liquid again after settlement, greatly reducing the salinity concentration in the liquid after dilution for several times, and solving the problem caused by salinity crystallization; the clear liquid discharging operation is carried out, only clear liquid is discharged before and after filter pressing, and a small amount of precipitate left after filter pressing is left in the tank body; double flute filter-pressing operation in turn, the turbid liquid in filter-pressing reaction tank or the buffer tank respectively can be through the switch of control valve, to reaction tank and buffer tank filter-pressing in turn, to the whole aeration of the cell body of filter-pressing during the filter-pressing, press out most precipitate through the mode of reciprocating filter-pressing in turn in reaction tank and buffer tank, at last will contain a small amount of precipitate liquid and subside in the buffer tank, the precipitate is retained in the buffer tank, filter through precision filter through the discharge pump and discharge upper portion clear liquid, the problem of unable discharge to reach standard has been solved.

Compared with the prior art, the invention has the following beneficial effects:

the invention solves the problems that acid mist or toxic gas escapes to break the exchange environment and harm the body health of operators, filtrate can not be discharged up to the standard, salt is crystallized, filter cloth, a conveying pump or a conveying pipeline is blocked, and the like.

Drawings

FIG. 1 is a schematic diagram of a high copper content high volatility spent acid treatment system according to the present invention;

in the figure: 1. an alkali storage tank; 2. an alkali supply pump; 3. cofferdam; 4. a reaction tank; 5. a water pipe; 6. an aeration pipe I; 7. a temperature measuring port; 8. an alkali spraying pipe; 9. a waste acid storage tank; 10. an acid supply pump; 11. an acid mist purifier; 12. a liquid level display interface; 13. an observation port I; 14. an operation table; 15. a clear liquid outlet; 16. a valve I; 17. a compressed air pipe; 18. a turbid liquid outlet I; 19. a valve II; 20. an air throttle valve I; 21. an air throttle valve II; 22. a return port; 23. a filter pressing table; 24. a filter press; 25. a material containing groove; 26. a weep hole; 27. a pneumatic diaphragm pump; 28. a valve III; 29. a buffer tank; 30. a valve IV; 31. a filtrate inlet; 32. an aeration pipe II; 33. a turbid liquid outlet II; 34. a valve V; 35. a pump idle rotation prevention liquid level port; 36. a clear liquid discharge port; 37. a valve VI; 38. a discharge pump; 39. a precision filter; 40. a neutralization pond; 41. and a viewing port II.

Detailed Description

The invention is further described below with reference to the accompanying drawings and examples.

Example 1

The processing object is as follows: the high-concentration nitric acid is mixed with sulfuric acid and hydrochloric acid in a certain proportion, wherein the sulfuric acid and the hydrochloric acid contain a large amount of copper ions, and the total acid amount of the mixed acid is about 550g/L (as H)₂SO₄Copper salts are crystallized out, and a large amount of acid mist and red gas are generated in the process of stirring or treating waste liquid.

The treatment scheme is as follows: by adopting the treatment system, NaOH solution with mass concentration of 31% is used for neutralization, a large amount of CuO precipitate is generated in the solution after the neutralization is finished, and clear liquid is discharged after the precipitate is subjected to filter pressing. The compressed air used in the treatment process was about 0.6 MPa.

As shown in FIG. 1, a small system for processing high-copper content high-volatility mixed acid is manufactured.

1) The power of the acid mist purifier 11 is 0.75kW, and the acid mist purifier is communicated with the reaction tank 4 by a DN50PP pipe.

2) The alkali storage tank 1 in the alkali supply system is 3000L; 2 delivery head of alkali supply pump 8m, flow 1.5m³H; the alkali leaching pipe 8 is DN50PP pipe, two rows of alkali leaching holes with diameter of 5mm are arranged at intervals of 10cm along the horizontal downward 45-degree direction of the central line of the alkali leaching pipe 8, the alkali leaching pipe 8 is fixed at the upper part in the length direction of the reaction tank 4, and the alkali leaching pipe 8 is communicated with the liquid alkali conveying pipeline; and pipelines communicated with the alkali storage tank 1, the alkali supply pump 2 and the alkali pouring pipe 8 are DN32PP pipes.

3) The waste acid storage tank 9 in the acid supply system is a 1000L industrial acid storage barrel; the acid supply pump 10 has a lift of 8m and a flow of 1.5m³H; pipelines for communicating the waste acid storage tank 9, the acid supply pump 10 and the reaction tank 4 are DN32PP pipes.

4) The reaction tank 4 has the external dimension of 2m multiplied by 3m multiplied by 1m, the thickness of 20mm, the material is PP, and an observation port I13 (with a cover plate) of 30cm multiplied by 30cm is reserved on the upper cover; an acid inlet phi 32mm, an alkali inlet phi 32mm, an exhaust outlet phi 50mm, a temperature measuring port 7 phi 20mm, a liquid level display interface 12 phi 30mm, a reflux port 22 (also used as a filtrate inlet) phi 32mm, an aeration air inlet phi 32mm, a water inlet phi 32mm, a turbid liquid outlet I18 phi 50mm and a clear liquid outlet 15 phi 32 mm. The turbid liquid outlet I18 is close to the bottom of the tank as much as possible, the clear liquid outlet 15 is arranged at the position which is 30cm away from the bottom of the reaction tank 4 in the vertical direction and is communicated with the neutralization tank 40 through a pipeline, and the clear liquid outlet 15 is provided with a control valve I16. Aeration pipe I6 is DN32PP pipe, arranges the bottom in reaction tank 4 in, and aeration pipe I6 top is every 10cm single row phi 5 mm's aeration hole, and aeration pipe I6 and compressed air pipe 17 intercommunication. A Pt100 thermocouple, a display can directly read the temperature value.

5) The buffer tank 29 has the overall dimension of 2m multiplied by 3m multiplied by 1m, the thickness of 20mm, the material is PP, an observation port II 41 (with a cover plate) of 30cm multiplied by 30cm is reserved on the upper cover, the filtrate inlet is 31 phi 32mm, the turbid liquid outlet is II 33 phi 50mm, the clear liquid discharge port is 36 phi 32mm, and the anti-pump idling liquid level port is 35 phi 20 mm. And an aeration pipe II 32DN32PP pipe is arranged at the bottom of the buffer tank 29, aeration holes with the diameter of 5mm are singly arranged at intervals of 10cm above the aeration pipe II 32, and the aeration pipe II 32 is communicated with the compressed air pipe 17. The clear liquid discharge port 36 phi 32mm, the control valve VI 37 is arranged at the clear liquid discharge port 36, the clear liquid discharge port 36 is 20cm away from the bottom of the buffer tank 29, and the buffer tank 29 is communicated with the discharge pump 38 through a DN32PP pipe. The turbid liquid outlet II 33 is 5cm away from the bottom of the buffer tank 29, and the filtrate conveying pipe orifice enters the buffer tank 29 by 5 cm.

6) A filter pressing table 23 in the filter pressing system is 5m multiplied by 1.5m multiplied by 0.5m, and acid and alkali resistant marble is paved on the filter pressing table; 24 filter area of the filter press is 8m²The volume of the filter chamber (120 +/-5) L has an automatic pressure maintaining function, the discharge form of filtrate is a dark flow, and the filter precision is 10 mu m of terylene filter cloth; the pneumatic diaphragm pump 27 is communicated with a compressed air pipeline, the lift is 50 meters, and the flow is about 5m³H; the material containing groove 25 is made of PP and is provided with a liquid leakage hole 26. The turbid liquid conveying pipe is DN50PP pipe, and the other conveying liquid pipelines are DN32PP pipes.

7) The cofferdams 3 of the reaction tank 4 and the buffer tank 29 are made of 10cm thick marble materials, and the size of the cofferdams 3 is 5m multiplied by 4m multiplied by 0.6 m.

8) The discharge pump 38 in the discharge system has a lift of 8m and a flow of 1.5m³The filtration precision of the precision filter 39 is 1 mu m, the filter element material is terylene, and a pipeline used for communicating the discharge pump, the precision filter 39 and the neutralization tank 40 is DN32PP pipe.

9) The console 14 is provided with a temperature display, a power switch of the acid mist purifier 11, the alkali supply pump 2, the acid supply pump 10, the filter press 24 and the discharge pump 38, and a compressed air and water supply switch. Wherein, the power switch of the alkali supply pump 2 has inching control function.

10) The neutralization tank 40 is a low-level tank, guard rails are arranged on the periphery of the tank, PTFE plates with the thickness of 20mm are lined in the tank, and liquid can be left in the tank by itself and has the size of 3m multiplied by 1 m.

11) In the invention, only the key valve body, namely the ball valve, is called a valve for short, and whether the non-key valve body is installed or not is processed as appropriate.

12) The incomplete matters are treated according to the conventional operation, such as the selection of ball valves, the specific position of non-critical pipelines and the like.

13) The specific operation steps are as follows (refer to the attached figure 1):

(1) and confirming that all valves are in a closed state, closing the switch of the acid mist purifier 11 to enable the interior of the reaction tank 4 to reach a certain negative pressure state, keeping the acid mist purifier 11 in a working state before the reaction is finished, and closing the acid mist purifier 11 before filter pressing operation.

(2) The power switch of the acid supply pump 10 is closed at the console 14, the waste acid enters the reaction tank 4 through the acid supply pump 10, and the power switch of the acid supply pump 10 is closed when the waste acid reaches about 1/3 height of the reaction tank 4 as viewed by the liquid level indicator.

(3) At the console 14, the throttle valve I20 is opened, and compressed air enters the aeration pipe I6 in the reaction tank 4 from the air supply station along the compressed air pipe line, the throttle valve I20 and the aeration port, and enters the reaction tank 4 through the aeration hole on the aeration pipe I6 for aeration.

(4) A power switch of an alkali supply pump 2 is closed at a control table 14, liquid alkali enters an alkali sprinkling pipe 8 in a reaction tank 4 through the alkali supply pump 2, the liquid alkali enters the reaction tank 4 through an alkali sprinkling hole in the alkali sprinkling pipe 8 in a sprinkling mode to perform a neutralization reaction with waste acid, and a temperature value and a liquid state in the reaction tank 4 are observed during alkali sprinkling. Stopping leaching alkali when the temperature reaches 80 ℃, and continuing leaching alkali after the temperature is reduced to 60 ℃; when the blue flocculent precipitate is found to be generated in the reaction tank 4, the operation is switched to the inching switch for controlling the alkali supply pump 2, the inching mode is adopted for pouring alkali, and the alkali pouring is stopped when the precipitate in the reaction tank 4 is changed into black particles, so that the reaction is complete. The air throttle I20 is closed to stop aeration.

(5) And settling for 30min, wherein the precipitate is completely settled, and the height of the precipitate is lower than the 15-height of the clear liquid outlet. The valve I16 is opened, the supernatant flows along the supernatant outlet 15 and the valve I16 into the neutralization tank 40, and the supernatant is discharged to complete the valve I16.

(6) And opening a switch of a water supply pipe 5 at the control platform 14, enabling tap water to enter the reaction tank 4, closing the water supply switch after the reaction tank 4 is basically filled with liquid, opening a valve I16 after sedimentation is carried out for 15min, enabling supernatant to automatically flow into the neutralization tank 40 along a clear liquid outlet 15 and the valve I16, and completely discharging the supernatant out of the valve I16. After this operation was repeated twice, the salt content in the clear solution was less than 1/10 which was the salt content after the preliminary reaction, and the pressure filtration was started.

(7) Opening an air throttle valve I20 at the control console 14, leading compressed air to enter an aeration pipe I6 in the reaction tank 4 from an air supply station along a compressed air pipe pipeline, the air throttle valve I20 and an aeration port, and leading the compressed air to enter the reaction tank 4 through an aeration hole on the aeration pipe I6 for aeration so as to fully disperse the precipitate in clear liquid for filter pressing; a locking switch of the filter press 24 is opened at the control platform 14 (filter cloth is placed), and the locking switch is closed after the filter press 24 is locked (the filter press 24 has a pressure maintaining function); the air operated diaphragm pump 27 is opened at the console 14, and the air operated diaphragm pump 27 starts to operate (the pump can be operated empty); under the normal operation of the pneumatic diaphragm pump 27, the valve II 19 is opened, the turbid liquid in the reaction tank 4 enters the filter press 24 through the turbid liquid outlet I18 and the pneumatic diaphragm pump 27, most of precipitates are intercepted by the filter cloth, and most of the filtrate with a certain amount of precipitates enters the buffer tank 29 through the valve IV 30 and the filtrate inlet 31 on the buffer tank 29 in a dark flow mode. A part of the filter liquid seeped through the filter cloth drips onto the material containing groove 25 and enters the reaction tank 4 through the liquid leakage hole 26 on the material containing groove 25 and the return opening 22 on the reaction tank 4.

(8) The air throttle valve I20 is closed, aeration to the reaction tank 4 is stopped, the air throttle valve II 21 is opened, compressed air enters the aeration pipe II 32 in the buffer tank 29 from the air supply station along the compressed air pipe pipeline, the air throttle valve II 21 and the aeration port, enters the buffer tank 29 through the aeration hole in the aeration pipe II 32 for aeration, the valve II 19 and the valve IV 30 are closed, the valves V34 and III 28 are opened, turbid liquid in the buffer tank 29 enters the filter press 24 through the turbid liquid outlet II 33 pneumatic diaphragm pump 27, sediment is intercepted by filter cloth, most of filter liquid with part of sediment enters the reaction tank 4 through the valve III 28, one part of filter liquid seeped out through the filter cloth drops onto the material containing tank 25, and enters the return port 22 in the reaction tank 4 through the liquid leakage hole 26 in the material containing tank 25.

(9) The filter pressing operation is stopped after the filter pressing operation is performed again with reference to the operation of steps (7) and (8), and at this time, the turbid liquid is in the buffer tank 29 and the content of the precipitate is small. The pneumatic diaphragm pump 27 was closed, and aeration was stopped in each of the reaction tank 4 and the buffer tank 29, and the valves II 19, V34, III 28, and IV 30 were also closed.

(10) After 15min of sedimentation, a small amount of sediment is fully settled, the height of the sediment is lower than that of the clear liquid discharge port 36, the valve VI 37 is opened, the discharge pump 38 is started at the console 14, and clear liquid (containing a very small amount of sediment particles) in the buffer tank 29 enters the neutralization tank 40 through the clear liquid discharge port 36, the valve VI 37, the discharge pump 38 and the precision filter 39. A small amount of turbid liquid remains in the buffer tank 29 after the discharge.

(11) After the clear liquid in the buffer tank 29 is discharged, the discharge pump 38 and the valve VI 37 are closed. The liquid in the neutralization tank 40 is discharged after reaching the standard after neutralization.

(12) After the treatment is finished, all the kinetic energy switches and valves are ensured to be in a closed state, and after 24 hours, the filter press 24 is opened to clean sediments.

Of course, the foregoing is only a preferred embodiment of the invention and should not be taken as limiting the scope of the embodiments of the invention. The present invention is not limited to the above examples, and equivalent changes and modifications made by those skilled in the art within the spirit and scope of the present invention should be construed as being included in the scope of the present invention.