Continuous vanadium removal device and method for waste catalyst regeneration and activation waste liquid

Abstract

The invention relates to a continuous vanadium removal device and method for waste catalyst regeneration and activation waste liquid. The device comprises a liquid inlet reaction tank, a flocculation tank and a sedimentation tank which are connected in sequence, the liquid inlet reaction tank is communicated with the flocculation tank; the flocculation tank is communicated with the sedimentation tank; wherein the liquid inlet reaction tank is provided with a first dosing pipe and a second dosing pipe, and the first dosing pipe is used for adding a vanadium reducing agent into the liquid inlet reaction tank; the second dosing pipe is used for adding a PH regulator into the liquid inlet reaction tank; a fourth dosing pipe and a fifth dosing pipe are arranged on the flocculation basin, and the fourth dosing pipe is used for adding a flocculating agent into the flocculation basin; the fifth dosing pipe is used for adding a coagulant aid into the flocculation basin. According to the continuous vanadium removal device, vanadium ions in the activated waste liquid can be efficiently removed at low cost, and the vanadium emission index reaches the vanadium industrial pollutant emission standard.

Description

Technical Field

[0001] The present application relates to the field of hazardous waste recycling, and in particular to a device and method for continuously removing vanadium from waste catalyst regeneration and activation waste liquid. Background Art

[0002] At present, the regeneration and utilization of waste flue gas SCR denitrification catalysts requires the process of "ultrasonic cleaning-spray cleaning-chemical cleaning-bubbling cleaning-active material implantation". Most active material implantation processes use wet impregnation. After each waste catalyst module is loaded, the concentration of the activated loading liquid decreases. Therefore, it is necessary to discharge a certain amount of activated loading liquid, and then replenish high-concentration activation liquid to ensure that the concentration of the activated loading liquid remains constant. However, the vanadium content in this part of the discharged loading liquid is about 500-800 mg / L. Traditionally, flocculation precipitation + supernatant ion exchange resin is used to remove vanadium, but this treatment method has low removal efficiency, high cost, and cannot be treated continuously, and cannot meet the vanadium industrial pollutant emission standards (GB 26452-2011).

[0003] In view of the above-mentioned difficulties, the research and development of a continuous vanadium removal device and method for waste catalyst regeneration and activation waste liquid with simple structure, reliable control and continuous operation has important significance and good economic benefits for the whole chain of waste catalyst regeneration to meet emission standards.

[0004] Therefore, it is necessary to design a device and method for continuously removing vanadium from waste catalyst regeneration and activation waste liquid to solve the technical problems mentioned above. Summary of the invention

[0005] Based on this, a continuous vanadium removal device and a vanadium removal method for waste catalyst regeneration and activation waste liquid are provided, which can remove vanadium ions in the activation waste liquid with high efficiency and low cost, and the vanadium emission index meets the vanadium industry pollutant emission standard.

[0006] To solve the above problems, the present application provides a device for continuous vanadium removal from waste liquid for regeneration and activation of spent catalysts, comprising: a liquid inlet reaction tank, a flocculation tank and a sedimentation tank connected in sequence; the liquid inlet reaction tank is connected to the flocculation tank; the flocculation tank is connected to the sedimentation tank; wherein the liquid inlet reaction tank is provided with a first dosing pipe and a second dosing pipe, the first dosing pipe is used for adding a vanadium reducing agent into the liquid inlet reaction tank; the second dosing pipe is used for adding a pH regulator into the liquid inlet reaction tank; the flocculation tank is provided with a fourth dosing pipe and a fifth dosing pipe, the fourth dosing pipe is used for adding a flocculant into the flocculation tank; the fifth dosing pipe is used for adding a coagulant aid into the flocculation tank.

[0007] Preferably, the liquid inlet reaction pool is provided as one or more, and the multiple liquid inlet reaction pools are sequentially connected in series to form a set of reactors. The reactor can be provided as multiple sets, and the multiple sets of reactors can be arranged in parallel.

[0008] Preferably, the liquid inlet reaction pool includes a liquid inlet pool and a reaction pool, and the liquid inlet pool and the reaction pool are connected; the first dosing tube and the second dosing tube are arranged on the liquid inlet pool; the third dosing tube is arranged on the reaction pool, and the third dosing tube is used to add a pH regulator into the reaction pool.

[0009] Preferably, the liquid inlet tank is provided with a first liquid inlet and a first liquid outlet; the first liquid inlet is connected to a liquid inlet regulating valve and a liquid inlet pump through an inlet pipe; the first liquid outlet is connected to the reaction tank; the reaction tank is provided with a second liquid inlet and a second liquid outlet; the second liquid inlet is connected to the first liquid outlet; the second liquid outlet is connected to the flocculation tank; the flocculation tank is provided with a third liquid inlet and a third liquid outlet; the third liquid inlet is connected to the second liquid outlet; the third liquid outlet is connected to the sedimentation tank; the sedimentation tank is provided with a fourth liquid inlet, a fourth liquid outlet and a mud discharge outlet; the fourth liquid inlet is connected to the third liquid outlet.

[0010] Preferably, the ratio of the total volume of the inlet tank and the reaction tank to the inlet flow rate is 30min-60min; the ratio of the total volume of the flocculation tank to the inlet flow rate of the flocculation tank is 15min-45min; the ratio of the total volume of the sedimentation tank to the inlet flow rate of the sedimentation tank is not less than 40min.

[0011] Preferably, the liquid inlet tank is provided with a liquid inlet tank stirrer; the reaction tank is provided with a reaction tank stirrer; the flocculation tank is provided with a flocculation tank stirrer; the sedimentation tank is provided with a sedimentation tank scraper; wherein the liquid inlet tank stirrer, the reaction tank stirrer, the flocculation tank stirrer and the sedimentation tank scraper can all adopt double-layer stirring or single-layer stirring;

[0012] Preferably, the motor speeds of the liquid inlet tank agitator and the reaction tank agitator are controlled at 300r / min-1500r / min; the motor speed of the flocculation tank agitator is controlled at 200r / min-500r / min; and the motor speed of the sedimentation tank scraper is controlled at 5r / min-15r / min.

[0013] Preferably, the first dosing pipe is provided with a first dosing pump and a first dosing control valve; the second dosing pipe is provided with a second dosing pump and a second dosing control valve; the third dosing pipe is provided with a third dosing pump and a third dosing control valve; the fourth dosing pipe is provided with a fourth dosing pump and a fourth dosing control valve; the fifth dosing pipe is provided with a fifth dosing pump and a fifth dosing control valve.

[0014] Preferably, the liquid inlet pipe is also provided with a liquid inlet flowmeter; the first dosing pipe is also provided with a dosing flowmeter; the liquid inlet tank is provided with a first Ph meter for detecting the Ph value of the liquid inlet and controlling it at 2-4; the flocculation tank is provided with a second Ph meter for detecting the Ph value of the flocculation tank and controlling it at 7-9; the sedimentation tank is provided with a mud level meter.

[0015] Preferably, the bottom of the sedimentation tank is configured as a conical bucket structure; and the mud discharge port is arranged at the lower part of the tank wall of the conical bucket structure.

[0016] Preferably, an inclined tube sedimentation device is further provided in the sedimentation tank; the inclined tube sedimentation device is arranged above the conical bucket structure, and an inclined tube filler is used inside.

[0017] The present application also provides a vanadium removal method using a waste catalyst regeneration and activation waste liquid vanadium removal device, comprising the following steps:

[0018] Step 1: Start the liquid inlet pump and adjust the liquid inlet regulating valve;

[0019] Step 2: Gradually increase the opening of the liquid inlet regulating valve until the reading of the liquid inlet flow meter reaches the set flow rate, and record the flow meter reading v0 m at this time 3 / h; inductively coupled plasma was used to detect the vanadium ion concentration in the waste liquid of the spent catalyst regeneration and activation, recorded as n0 mg / L, and the relative molecular weight of vanadium, recorded as M V g / mol; at this time, the amount of vanadium ions in the influent liquid q0 (mol / h) is:

[0020]

[0021] Step 3: Start the second dosing pump and adjust the second dosing control valve;

[0022] Step 4: Gradually increase the opening of the second dosing control valve to make the reading of the first Ph meter reach 2-4;

[0023] Step 5: Start the first dosing pump and adjust the first dosing control valve;

[0024] Step 6: Gradually increase the opening of the first dosing control valve to make the reading of the dosing flow meter reach the set flow rate, and record the flow meter reading v2 m 3 / h, this part of the reagent uses vanadium reducing agent, the relative molecular weight of vanadium reducing agent is Mg / mol, and the configured mass concentration is C, then the amount of vanadium reducing agent in the original solution is q1 (mol / h):

[0025]

[0026] Step 7: Start the third dosing pump, adjust the third dosing control valve, start the fourth dosing pump, adjust the fourth dosing control valve, start the fifth dosing pump, and adjust the fifth dosing control valve;

[0027] Step 8: gradually increase the opening of the third dosing control valve to adjust the second Ph meter reading to 7-9; gradually increase the opening of the fourth dosing control valve and the fifth dosing control valve. When uniform floccules appear and the sedimentation speed is fast, stop adjusting the fourth dosing control valve and the fifth dosing control valve;

[0028] Step 9: Take a sample from the effluent of the fourth outlet of the sedimentation tank, and use inductively coupled plasma to detect the vanadium ion concentration of the effluent of the sedimentation tank, recorded as n1 mg / L. At this time, the vanadium removal efficiency is:

[0029]

[0030] Step 10: If the water vanadium ion concentration detected in step 9 is less than the target value, repeat steps 6 to 9 to increase the flow setting value of the vanadium reducing agent.

[0031] Preferably, the method further includes the following steps: controlling the start and stop of the mud discharge pump and the opening of the mud discharge control valve according to the reading of the mud level meter; and controlling the mud level in the sedimentation tank to be between 1 / 3 and 2 / 3 of the height of the tank body from the bottom.

[0032] Beneficial effects:

[0033] The activated waste liquid to be treated is discharged into the liquid inlet reaction tank, and a vanadium reducing agent is added to the liquid inlet reaction tank through the first dosing pipe, and a pH regulator is added to the liquid inlet reaction tank through the second dosing pipe, so that the vanadium reducing agent can react with the activated waste liquid under appropriate conditions. The waste liquid after the reaction flows to the flocculation tank, and a flocculant is added to the flocculation tank through the fourth dosing pipe, and a coagulant aid is added to the flocculation tank through the fifth dosing pipe. When uniform floccules appear in the flocculation tank and the sedimentation speed is fast, the dosing is stopped, and the precipitated impurities flow to the sedimentation tank. It can be understood that the vanadium reducing agent and the activated waste liquid react under appropriate conditions. The vanadium +5 in the activated liquid is reduced to vanadium +4 by a chemical reaction, and forms fine complex particles with the vanadium reducing agent under alkaline conditions. The flocculant condenses these fine particles to form a flocculant, and the coagulant aid helps to improve the coagulation effect. Therefore, the continuous vanadium removal device for waste catalyst regeneration and activation waste liquid is suitable for the regeneration and utilization process of waste denitrification catalysts, and has the advantages of simple system structure, high continuous reliability, high removal rate, etc. It can achieve efficient vanadium removal from waste catalyst regeneration and activation waste liquid, ensure the stable and standard discharge of heavy metal ion vanadium in the wastewater during the waste catalyst regeneration process, low operating cost, and good economic and environmental benefits. BRIEF DESCRIPTION OF THE DRAWINGS

[0034] Figure 1 It is a schematic diagram of the structure of the device for continuous vanadium removal from waste liquid for regeneration and activation of spent catalyst in this embodiment.

[0035] Figure numerals: 10, liquid inlet reaction tank; 11, liquid inlet tank; 111, first liquid inlet; 112, first liquid outlet; 113, liquid inlet pipeline; 114, liquid inlet regulating valve; 115, liquid inlet pump; 12, reaction tank; 121, second liquid inlet; 122, second liquid outlet; 20, flocculation tank; 21, third liquid inlet; 22, third liquid inlet; 30, sedimentation tank; 31, fourth liquid inlet; 32, fourth liquid outlet; 33, fourth liquid outlet; 34, mud discharge pipe; 35, mud discharge control valve; 36, mud discharge pump; 37, cone bucket structure; 38, cone bucket structure; 39, liquid outlet pipe; 391, liquid outlet flow meter; 41, first dosing pipe; 411, first dosing pump; 412, first dosing control valve; 42, second dosing pipe; 421, second dosing pump; 422, second dosing control valve; 43, third dosing pipe; 431, third dosing pump; 432, first three dosing control valves; 44, fourth dosing pipe; 441, fourth dosing pump; 442, fourth dosing control valve; 45, fifth dosing pipe; 451, fifth dosing pump; 452, fifth dosing control valve; 51, inlet tank agitator; 511, first agitation motor; 512, first agitation shaft; 513, first agitation blade; 52, reaction tank agitator; 521, second agitation motor; 522, second agitation shaft; 523, second agitation Blade; 53, flocculation tank agitator; 531, the third agitator motor; 532, the third agitator shaft; 533, the third agitator blade; 54, sedimentation tank scraper; 541, the fourth agitator motor; 542, the fourth agitator shaft; 543, the scraper; 61, the liquid inlet flow meter; 62, the dosing flow meter; 63, the first Ph meter; 64, the second Ph meter; 65, the mud level meter; 71, the first partition; 72, the second partition; 73, the third partition. DETAILED DESCRIPTION

[0036] In order to make the purpose, technical solution and advantages of the present application more clearly understood, the present application is further described in detail below in conjunction with the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are only used to explain the present application and are not used to limit the present application.

[0037] It should be noted that the illustrations provided in this embodiment only illustrate the basic concept of the present application in a schematic manner, and therefore the drawings only show components related to the present application rather than being drawn according to the number, shape and size of components in actual implementation. In actual implementation, the type, quantity and proportion of each component may be changed arbitrarily, and the component layout may also be more complicated.

[0038] The directions or positional relationships indicated by the terms "upper", "lower", "left", "right", "middle", "longitudinal", "lateral", "horizontal", "inner", "outer", "radial", "circumferential" and the like in this specification are based on the directions or positional relationships shown in the drawings and are only for the convenience of simplifying the description. They do not indicate or imply that the devices or elements referred to must have a specific direction, be constructed and operate in a specific direction, and therefore cannot be understood as limiting the present application. In addition, the terms "first" and "second" are used for descriptive purposes only and cannot be understood as indicating or implying relative importance.

[0039] The embodiment of the present application provides a continuous vanadium removal device and a vanadium removal method for waste catalyst regeneration and activation waste liquid. The present application has the advantages of simple system structure, high continuous reliability, and high removal rate. It can achieve efficient vanadium removal from waste catalyst regeneration and activation waste liquid, ensure the stable and standard discharge of heavy metal vanadium ions in the wastewater during the waste catalyst regeneration process, have low operating costs, and have good economic and environmental benefits.

[0040] The following is a detailed description of a waste catalyst regeneration and activation waste liquid continuous vanadium removal device provided in this embodiment in conjunction with the accompanying drawings. Figure 1 As shown, the device includes: an inlet reaction tank 10, a flocculation tank 20 and a sedimentation tank 30 connected in sequence; the inlet reaction tank 10 is connected to the flocculation tank 20, and the flocculation tank 20 is connected to the sedimentation tank 30; wherein, the inlet reaction tank 10 is provided with a first dosing pipe 41 and a second dosing pipe 42, the first dosing pipe 41 is used to add a vanadium reducing agent into the inlet reaction tank 10, and the second dosing pipe 42 is used to add a pH regulator into the inlet reaction tank 10; the flocculation tank 20 is provided with a fourth dosing pipe 44 and a fifth dosing pipe 45, the fourth dosing pipe 44 is used to add a flocculant into the flocculation tank 20; the fifth dosing pipe 45 is used to add a coagulant aid into the flocculation tank 20.

[0041] In the present embodiment, a continuous vanadium removal device for waste catalyst regeneration and activation waste liquid is formed by sequentially connecting the inlet reaction tank 10, the flocculation tank 20 and the sedimentation tank 30. A pH regulator is added into the inlet reaction tank 10 through the second dosing pipe 42. The pH value of the inlet reaction tank 10 is adjusted to the specified requirement by the pH regulator. Then, a vanadium reducing agent is added into the inlet reaction tank 10 through the first dosing pipe 41. The vanadium reducing agent reacts with the activated waste liquid. The waste liquid after the reaction flows to the flocculation tank 20. In the flocculation tank 20, a flocculant is added into the flocculation tank 20 through the fourth dosing pipe 44. A coagulant aid is added into the flocculation tank 20 through the fifth dosing pipe 45. When uniform floccules appear in the flocculation tank 20 and the sedimentation speed is fast, the dosing is stopped. The impurities after the precipitation flow into the sedimentation tank 30. Therefore, the continuous vanadium removal device for waste catalyst regeneration and activation waste liquid in the present embodiment can remove vanadium ions in the activated waste liquid with high efficiency and low cost, and the vanadium emission index meets the vanadium industry pollutant emission standard.

[0042] In this embodiment, it should be noted that the liquid inlet reaction pool 10 can be set to one or more, and multiple liquid inlet reaction pools 10 are sequentially connected in series to form a set of reactors. The reactor can be set to multiple sets, and multiple sets of reactors can be set in parallel. Therefore, this setting method in this embodiment can increase the processing capacity.

[0043] In some embodiments, the liquid inlet reaction tank 10 includes a liquid inlet tank 11 and a reaction tank 12. The liquid inlet tank 11 and the reaction tank 12 can be two independent tank bodies, or the reaction tank 12 can be omitted. The liquid inlet tank 11 also serves as the reaction tank 12. In this embodiment, the liquid inlet tank 11 and the reaction tank 12 are separated as an example for explanation, and the liquid inlet tank 11, the reaction tank 12, the flocculation tank 20, and the sedimentation tank 30 can be cylindrical tank bodies or square tank bodies. The specific arrangement is not specifically limited in this embodiment.

[0044] In some embodiments, the liquid inlet pool 11 and the reaction pool 12 are separated by welding a first partition 71, and the liquid inlet pool 11 is provided with a first liquid inlet 111 and a first liquid outlet 112, the first liquid inlet 111 is arranged on the top side wall of the liquid inlet pool 11, and the first liquid inlet 111 is connected to a liquid inlet regulating valve 114 and a liquid inlet pump 115 through a liquid inlet pipe 113, and a liquid inlet flowmeter 61 is also arranged on the liquid inlet pipe 113, that is, the liquid inlet pump 115, the liquid inlet regulating valve 114 and the liquid inlet flowmeter 61 are arranged on the liquid inlet pipe 113 from left to right, the liquid inlet flowmeter 61 is arranged between the liquid inlet regulating valve 114 and the first liquid inlet 111, to control the liquid inlet flow, and the first liquid outlet 112 is arranged on the bottom side wall of the liquid inlet pool 11, that is, the lower part of the first partition 71. The reaction tank 12 is provided with a second liquid inlet 121 and a second liquid outlet 122. The second liquid inlet 121 is arranged on the bottom side wall of the reaction tank 12, that is, the lower part of the first partition 71, and is connected with the first liquid outlet 112 of the liquid inlet tank 11. It can be understood that the first liquid outlet 112 and the second liquid inlet 121 are both opened at the lower part of the first partition 71 and are in the same position. The second liquid outlet 122 of the reaction tank 12 is arranged on the top side wall of the reaction tank 12, that is, the top of the first partition 71, and is connected with the flocculation tank 20.

[0045] In some embodiments, the flocculation tank 20 and the reaction tank 12 are separated by welding a second partition 72. The flocculation tank 20 is provided with a third liquid inlet 21 and a third liquid outlet 22. The third liquid inlet 21 is arranged on the top side wall of the flocculation tank 20, that is, the upper part of the second partition 72, and is connected to the second liquid outlet 122 of the reaction tank 12. It can be understood that the second liquid outlet 122 and the third liquid inlet 21 are both opened on the upper part of the second partition 72 and are in the same position. The third liquid outlet 22 of the flocculation tank 20 is arranged on the bottom side wall of the flocculation tank 20, that is, the bottom of the second partition 72, and is connected to the bottom of the sedimentation tank 30.

[0046] In some embodiments, the sedimentation tank 30 and the flocculation tank 20 are separated by welding the third partition 73. The sedimentation tank 30 is provided with a fourth liquid inlet 31, a fourth liquid outlet 32 ​​and a mud outlet 33. The fourth liquid inlet 31 is provided at the bottom side wall of the sedimentation tank 30, that is, at the lower part of the third partition 73, and is connected to the third liquid outlet 22 of the flocculation tank 20. It can be understood that the third liquid outlet 22 and the fourth liquid inlet 31 are both provided at the lower part of the third partition 73 and are in the same position. The fourth liquid outlet 32 ​​is provided at the top side wall of the sedimentation tank 30, and the fourth liquid outlet 32 ​​is connected to the liquid outlet flowmeter 391 through the liquid outlet pipe 39. The mud outlet 33 is provided at the bottom side wall of the sedimentation tank 30, and the mud outlet 33 is connected to the mud discharge control valve 35 and the mud discharge pump 36 through the mud discharge pipe 34, that is, the mud discharge control valve 35 and the mud discharge pump 36 are provided on the mud discharge pipe 34 in sequence from left to right.

[0047] In one example, the bottom of the sedimentation tank 30 is configured as a conical bucket structure 37 to facilitate the sedimentation of sludge. The sludge discharge port 33 is arranged at the lower part of the tank wall of the conical bucket structure 37, and an inclined tube sedimentation device 38 is also provided in the sedimentation tank 30. The inclined tube sedimentation device 38 is arranged above the conical bucket structure 37, and PP inclined tube filler is used inside. The inclined tube filler is placed on a steel structure support welded to the tank wall. The function of the inclined tube filler is to accelerate the separation of mud and water and improve the mud and water separation effect. The sludge and water are separated in the inclined tube filler. During the separation process, the sludge flows downward and the water flows upward through the action of the inclined tube, thereby achieving a rapid separation effect.

[0048] In this embodiment, it should also be noted that the ratio of the total volume of the liquid inlet tank 11 and the reaction tank 12 to the liquid inlet flow rate is 30min-60min, preferably 30min; the ratio of the total volume of the flocculation tank 20 to the liquid inlet flow rate of the flocculation tank 20 should be 15min-45min, preferably 15min; the ratio of the total volume of the sedimentation tank 30 to the liquid inlet flow rate of the sedimentation tank 30 is not less than 40min, preferably 40min.

[0049] In the present embodiment, it should also be noted that a first dosing pipe 41 and a second dosing pipe 42 are arranged on the liquid inlet pool 11, and a first dosing pump 411, a first dosing control valve 412 and a dosing flowmeter 62 are arranged on the first dosing pipe 41. It can be understood that the first dosing pump 411, the first dosing control valve 412 and the dosing flowmeter 62 are arranged on the first dosing pipe 41 from left to right in sequence, and the first dosing pipe 41 conveys a vanadium reducing agent, which can be oxalic acid, ferrous sulfate, ferrous chloride, nano iron powder, etc. The best agents are nano iron powder and ferrous sulfate; the first dosing control valve 412 can control the valve opening and then adjust the delivery flow of the vanadium reducing agent, and the dosing flowmeter 62 is arranged between the liquid inlet regulating valve 114 and the dosing port to control the liquid addition flow. The second dosing pipe 42 is provided with a second dosing pump 421 and a second dosing control valve 422. The second dosing pipe 42 delivers a PH regulator for adjusting the PH value of the solution, which can be dilute sulfuric acid, dilute hydrochloric acid, etc. The best regulator is dilute sulfuric acid; the second dosing control valve 422 can control the valve opening and then adjust the delivery flow of the PH regulator. Preferably, a first Ph meter 63 is provided in the inlet pool 11, and the first Ph meter 63 is arranged in the middle of the inlet pool 11 to adjust the inlet Ph value of the inlet pool 11, such as controlling it at 2-4.

[0050] The reaction tank 12 is provided with a third dosing pipe 43, on which a third dosing pump 431 and a third dosing control valve 432 are provided. The third dosing pipe 43 delivers a PH regulator for adjusting the PH value of the solution, which may be sodium hydroxide, sodium carbonate, calcium hydroxide, etc., and the best regulator is calcium hydroxide; the third dosing control valve 432 can control the opening of the valve and then adjust the delivery flow of the PH regulator.

[0051] The flocculation tank 20 is provided with a fourth dosing pipe 44 and a fifth dosing pipe 45. The fourth dosing pipe 44 is provided with a fourth dosing pump 441 and a fourth dosing control valve 442. The fourth dosing pipe 44 delivers a flocculant, which can be cationic polyacrylamide, anionic polyacrylamide, or nonionic polyacrylamide, with a molecular weight of 6-12 million. The best flocculant is cationic polyacrylamide with a molecular weight of 12 million. The fourth dosing control valve 442 can control the valve opening to adjust the flocculant delivery flow rate. The fifth dosing pipe 45 is provided with a fifth dosing pump 451 and a fifth dosing control valve 452. The fifth dosing pipe 45 delivers a coagulant, which can be polyaluminum chloride, ferric sulfate, etc. The fifth dosing control valve 452 can control the valve opening to adjust the coagulant delivery flow rate. Preferably, a second Ph meter 64 is provided in the flocculation tank 20, and the second Ph meter 64 is arranged in the middle of the flocculation tank 20 to adjust the liquid Ph value of the flocculation tank 20 to be controlled at 7-9.

[0052] A mud level meter 65 is provided in the sedimentation tank 30 . The mud level meter 65 is arranged at the upper part of the sedimentation tank 30 to adjust the sludge height in the sedimentation tank 30 .

[0053] In this embodiment, it should also be noted that a liquid inlet tank stirrer 51 is provided in the liquid inlet tank 11, a reaction tank stirrer 52 is provided in the reaction tank 12, a flocculation tank stirrer 53 is provided in the flocculation tank 20, and a sedimentation tank scraper 54 is provided in the sedimentation tank 30; wherein, the liquid inlet tank stirrer 51, the reaction tank stirrer 52, the flocculation tank stirrer 53 and the sedimentation tank scraper 54 can all adopt double-layer stirring or single-layer stirring, which is determined according to the height of the tank body. If the tank body height is less than 1.5m, single-layer stirring is preferably adopted; if the tank body height is greater than 1.5m, double-layer stirring is preferably adopted; the material of the part in contact with water should be stainless steel, PP, carbon steel lined with glass flake anti-corrosion or carbon steel lined with plastic.

[0054] In one example, the liquid inlet pool stirrer 51 is composed of a first stirring motor 511, a first stirring shaft 512, and a first stirring blade 513 from top to bottom; the first stirring motor 511 is arranged at the upper top of the liquid inlet pool 11, and the first stirring shaft 512 is vertically arranged in the liquid inlet pool 11. The upper end of the first stirring shaft 512 is coaxially connected with the output shaft of the first stirring motor 511, and the first stirring blade 513 is arranged on the first stirring shaft 512. The first stirring blade 513 can be arranged as one group or two groups. When set as two groups, the two groups of first stirring blades 513 can be arranged at intervals on the first stirring shaft 512, one group of first stirring blades 513 is arranged on the upper part of the first stirring shaft 512, and one group of first stirring blades 513 is arranged on the lower part of the first stirring shaft 512, thereby forming double-layer stirring.

[0055] In one example, the reaction tank stirrer 52 is composed of a second stirring motor 521, a second stirring shaft 522, and a second stirring blade 523 from top to bottom; the second stirring motor 521 is arranged at the upper top of the reaction tank 12, and the second stirring shaft 522 is vertically arranged in the reaction tank 12, the upper end of the second stirring shaft 522 is coaxially connected with the output shaft of the second stirring motor 521, and the second stirring blade 523 is arranged on the second stirring shaft 522, and the second stirring blade 523 can be arranged as one group or two groups. When set as two groups, the two groups of second stirring blades 523 can be arranged at intervals on the second stirring shaft 522, one group of second stirring blades 523 is arranged on the upper part of the second stirring shaft 522, and one group of second stirring blades 523 is arranged on the lower part of the second stirring shaft 522, thereby forming double-layer stirring.

[0056] In one example, the flocculation tank mixer 53 is composed of a third stirring motor 531, a third stirring shaft 532, and a third stirring blade 533 from top to bottom; the third stirring motor 531 is arranged at the upper top of the flocculation tank 20, and the third stirring shaft 532 is vertically arranged in the flocculation tank 20, and the upper end of the third stirring shaft 532 is coaxially connected with the output shaft of the third stirring motor 531, and the third stirring blade 533 is arranged on the third stirring shaft 532. The third stirring blade 533 can be set as one group or two groups. When set as two groups, two groups of third stirring blades 533 can be set at intervals on the third stirring shaft 532, one group of third stirring blades 533 is set at the upper part of the third stirring shaft 532, and one group of third stirring blades 533 is set at the lower part of the third stirring shaft 532, thereby forming double-layer stirring.

[0057] In one example, the sedimentation tank scraper 54 is composed of a fourth stirring motor 541, a fourth stirring shaft 542, and a scraper 543 from top to bottom; the fourth stirring motor 541 is arranged at the upper top of the sedimentation tank 30, and the fourth stirring shaft 542 is vertically arranged in the sedimentation tank 30, the upper end of the fourth stirring shaft 542 is coaxially connected with the output shaft of the fourth stirring motor 541, and the scraper 543 is arranged at the bottom of the fourth stirring shaft 542.

[0058] It should also be noted that the speed of the first stirring motor 511 of the liquid inlet tank stirrer 51 and the second stirring motor 521 of the reaction tank stirrer 52 are controlled at 300r / min-1500r / min. In order to ensure sufficient reaction, the optimal speed should be 980r / min; the speed of the third stirring motor 531 of the flocculation tank stirrer 53 is controlled at 200r / min-500r / min. In order to ensure the blooming effect, the optimal speed should be 300r / min; the speed of the fourth stirring motor 541 of the sedimentation tank scraper 54 is controlled at 5r / min-15r / min. In order to ensure that the mud hangs on the wall and builds a bridge, the optimal speed should be 10r / min.

[0059] In an embodiment of the present application, a vanadium removal method using a waste catalyst regeneration and activation waste liquid vanadium removal device is also provided, comprising the following steps:

[0060] Step 1: Start the liquid inlet pump 115 and adjust the liquid inlet regulating valve 114;

[0061] Step 2: Gradually increase the opening of the liquid inlet regulating valve 114 to make the reading of the liquid inlet flow meter 61 reach the set flow rate, and record the flow meter reading v0m at this time 3 / h; inductively coupled plasma (ICP) was used to detect the vanadium ion concentration in the waste liquid of the spent catalyst regeneration and activation, recorded as n0 mg / L, and the relative molecular weight of vanadium, recorded as M V g / mol; at this time, the amount of vanadium ions in the influent liquid q0 (mol / h) is:

[0062]

[0063] Step 3: Start the second dosing pump 421 and adjust the second dosing control valve 422;

[0064] Step 4: gradually increase the opening of the second dosing control valve 422 to adjust the first Ph meter 63 to a reading of 2-4;

[0065] Step 5: Start the first dosing pump 411 and adjust the first dosing control valve 412;

[0066] Step 6: Gradually increase the opening of the first dosing control valve 412 to adjust the dosing flow meter 62 to the set flow rate, and record the flow meter reading v2 m at this time 3 / h; this part of the reagent uses vanadium reducing agent, the relative molecular weight of vanadium reducing agent is Mg / mol, and the configured mass concentration is C, then the amount of vanadium reducing agent in the original solution is q1 (mol / h):

[0067]

[0068] Step 7: Start the third dosing pump 431, adjust the third dosing control valve 432, start the fourth dosing pump 441, adjust the fourth dosing control valve 442, start the fifth dosing pump 451, and adjust the fifth dosing control valve 452;

[0069] Step 8: gradually increase the opening of the third dosing control valve 432 to adjust the reading of the second Ph meter 64 to 7-9; gradually increase the opening of the fourth dosing control valve 442 and the fifth dosing control valve 452. When uniform floccules appear in the flocculation tank 20 and the sedimentation speed is fast, stop adjusting the fourth dosing control valve 442 and the fifth dosing control valve 452;

[0070] Step 9: Take a sample from the effluent of the fourth liquid outlet 322 of the sedimentation tank 30, and use inductively coupled plasma (ICP) to detect the vanadium ion concentration of the effluent of the sedimentation tank 30, which is recorded as n1 mg / L. At this time, the vanadium removal efficiency is:

[0071]

[0072] Step 10: If the water vanadium ion concentration detected in step 9 is less than the target value, repeat steps 6 to 9 to increase the flow setting value of the vanadium reducing agent; in addition, the start and stop of the mud pump 36 and the opening of the mud control valve 35 are controlled according to the reading of the mud level meter 65 to control the mud level of the sedimentation tank 30 between 1 / 3 and 2 / 3 of the height of the tank body from the bottom.

[0073] The disclosure of this embodiment is described below through Examples 1-4:

[0074] Embodiment 1:

[0075] Given conditions: activated waste liquid inlet flow rate 0.5m 3 / h, the vanadium content of the activated waste liquid is 800 mg / L, and the Ph of the activated waste liquid is 3.5.

[0076] Implementation target: outlet concentration is controlled at 1 mg / L.

[0077] Implementation steps:

[0078] Step 1: Start the liquid inlet pump 115 and adjust the liquid inlet regulating valve 114;

[0079] Step 2: Gradually increase the opening of the liquid inlet regulating valve 114 so that the reading of the liquid inlet flow meter 61 reaches 0.5m 3 / h; using inductively coupled plasma (ICP), the vanadium ion concentration in the waste liquid of the spent catalyst regeneration activation was detected to be 800 mg / L; then according to formula (1), the vanadium ion content in the inlet liquid was calculated to be 7.84 mol / h.

[0080] Step 3: Start the second dosing pump 421 and adjust the second dosing control valve 422;

[0081] Step 4: gradually increase the opening of the second dosing control valve 422 to adjust the first Ph meter 63 to read 3;

[0082] Step 5: Start the first dosing pump 411 and adjust the first dosing control valve 412;

[0083] Step 6: Gradually increase the opening of the first dosing control valve 412 to adjust the dosing flow meter 62 to the set flow rate, and record the flow meter reading at this time as 0.0654m 3 / h; This part of the reagent uses ferrous sulfate solution with a concentration of 20%, and the amount of ferrous ions in the reagent is 47.04 mol / h;

[0084] Step 7: Start the third dosing pump 431, adjust the third dosing control valve 432, start the fourth dosing pump 441, adjust the fourth dosing control valve 442, start the fifth dosing pump 451, and adjust the fifth dosing control valve 452;

[0085] Step 8: gradually increase the opening of the third dosing control valve 432 to adjust the reading of the second Ph meter 64 to 8; gradually increase the opening of the fourth dosing control valve 442 and the fifth dosing control valve 452. When uniform floccules appear in the flocculation tank 20 and the sedimentation speed is fast, stop adjusting the fourth dosing control valve 442 and the fifth dosing control valve 452;

[0086] Step 9: Take a sample from the effluent of the fourth liquid outlet 322 of the sedimentation tank 30, and use inductively coupled plasma (ICP) to detect the vanadium ion concentration of the effluent of the sedimentation tank 30, which is 0.88 mg / L. Then the vanadium removal efficiency is 99.89%.

[0087] Example 2: (Compared with Example 1, the vanadium content of the activated waste liquid is reduced to 300 mg / L)

[0088] Implementation conditions: Given conditions: Activated waste liquid inlet flow rate 0.5m 3 / h, the vanadium content of the activated waste liquid is 300 mg / L, and the Ph of the activated waste liquid is 3.5.

[0089] Implementation target: outlet concentration is controlled at 1 mg / L.

[0090] Implementation steps: Same as Example 1.

[0091] Step 1: Same as Example 1.

[0092] Step 2: Gradually increase the opening of the liquid inlet regulating valve 114 to make the reading of the liquid inlet flow meter 61 reach 0.5m 3 / h; using inductively coupled plasma (ICP), the vanadium ion concentration in the waste liquid of the spent catalyst regeneration activation was detected to be 300 mg / L; then according to formula (1), the vanadium ion content in the inlet liquid was calculated to be 2.94 mol / h.

[0093] Steps 3 to 5 are the same as in Example 1.

[0094] Step 6: Gradually increase the opening of the first dosing control valve 412 to adjust the dosing flow meter 62 to the set flow rate, and record the flow meter reading at this time as 0.0123m 3 / h; this part of the agent uses ferrous sulfate solution with a concentration of 20%, and the amount of ferrous ions in the agent is 8.82 mol / h.

[0095] Steps 7 and 8 are the same as those in Example 1.

[0096] Step 9: Sampling the effluent from the fourth liquid outlet 322 of the sedimentation tank 30, and using inductively coupled plasma (ICP) to detect the vanadium ion concentration of the effluent from the sedimentation tank 30 is 0.76 mg / L, so the vanadium removal efficiency is 99.75%.

[0097] Example 3: (Compared with Example 1, the activation waste liquid inlet flow rate is increased to 1.0m 3 / h)

[0098] Given conditions: activated waste liquid inlet flow rate 1.0m 3 / h, the vanadium content of the activated waste liquid is 800 mg / L, and the Ph of the activated waste liquid is 3.5.

[0099] Implementation target: outlet concentration is controlled at 1 mg / L.

[0100] Implementation steps: Same as Example 1.

[0101] Step 1: Same as Example 1;

[0102] Step 2: Gradually increase the opening of the liquid inlet regulating valve 114 to make the reading of the liquid inlet flow meter 61 reach 1.0m 3 / h; using inductively coupled plasma (ICP), the vanadium ion concentration in the waste liquid of the spent catalyst regeneration activation was detected to be 800 mg / L; then according to formula (1), the vanadium ion content in the inlet liquid was calculated to be 15.68 mol / h.

[0103] Steps 3 to 5 are the same as in Example 1.

[0104] Step 6: Gradually increase the opening of the first dosing control valve 412 to adjust the dosing flow meter 62 to the set flow rate, and record the flow meter reading at this time as 0.1308m 3 / h; This part of the reagent uses ferrous sulfate solution with a concentration of 20%, and the amount of ferrous ions in the reagent is 94.08 mol / h;

[0105] Step 7 to Step 8: Same as Example 1.

[0106] Step 9: Sampling the effluent from the fourth liquid outlet 322 of the sedimentation tank 30, and using inductively coupled plasma (ICP) to detect the vanadium ion concentration of the effluent from the sedimentation tank 30 is 1.54 mg / L, so the vanadium removal efficiency is 99.80%.

[0107] Step 10: Repeat steps 6 to 9. Gradually increase the opening of the first dosing control valve 412 to adjust the dosing flow meter 62 to the set flow rate. Record the flow meter reading at this time as 0.1542m 3 / h; this part of the reagent uses ferrous sulfate solution with a concentration of 20%, and the amount of ferrous ions in the reagent is 108.19 mol / h; a sample is taken from the effluent of the fourth liquid outlet 322 of the sedimentation tank 30, and the vanadium ion concentration of the effluent of the sedimentation tank 30 is detected by inductively coupled plasma (ICP) to be 0.79 mg / L. Then the vanadium removal efficiency is 99.90%.

[0108] Example 4: (Compared with Example 1, the flow rate of the pH regulator in Steps 3 and 4 is adjusted so that the pH of the activated waste liquid in the liquid inlet pool 11 is maintained at 2)

[0109] Implementation conditions: Given conditions: Activated waste liquid inlet flow rate 0.5m 3 / h, the vanadium content of the activated waste liquid is 800 mg / L, and the Ph of the activated waste liquid is 3.5.

[0110] Implementation target: outlet concentration is controlled at 1 mg / L.

[0111] Implementation steps: Same as Example 1.

[0112] Step 1 to Step 3: Same as Example 1.

[0113] Step 4: gradually increase the opening of the second dosing control valve 422 to adjust the first Ph meter 63 to a reading of 2;

[0114] Step 3 to Step 8: Same as Example 1.

[0115] Step 9: Sampling the effluent from the fourth liquid outlet 322 of the sedimentation tank 30, and using inductively coupled plasma (ICP) to detect the vanadium ion concentration of the effluent from the sedimentation tank 30 is 0.72 mg / L, so the vanadium removal efficiency is 99.91%.

[0116] The implementation principle of this embodiment is as follows: the activated waste liquid to be treated is discharged into the liquid inlet tank through the liquid inlet pump, a vanadium reducing agent is added into the liquid inlet tank through the first dosing pipe, and a pH adjusting agent is added into the liquid inlet tank through the second dosing pipe to adjust the pH of the liquid inlet tank, so that the vanadium reducing agent can mix and react with the activated waste liquid under appropriate conditions, the waste liquid flows to the reaction tank, a pH adjusting agent is added into the reaction tank through the third dosing pipe to adjust the pH of the waste liquid entering the flocculation tank, the waste liquid flows to the flocculation tank, a flocculant is added into the flocculation tank through the fourth dosing pipe, a coagulant aid is added into the flocculation tank through the fifth dosing pipe, when uniform floccules appear in the flocculation tank and the sedimentation speed is fast, the dosing is stopped, and then the precipitated impurities flow to the sedimentation tank, and the precipitated sludge is discharged through the sludge discharge pump 36.

[0117] The technical features of the above embodiments may be arbitrarily combined. To make the description concise, not all possible combinations of the technical features in the above embodiments are described. However, as long as there is no contradiction in the combination of these technical features, they should be considered to be within the scope of this specification.

[0118] The above-described embodiments only express several implementation methods of the present application, and the descriptions thereof are relatively specific and detailed, but they cannot be construed as limiting the scope of the patent application. It should be pointed out that, for a person of ordinary skill in the art, several variations and improvements can be made without departing from the concept of the present application, and these all belong to the protection scope of the present application. Therefore, the protection scope of the patent application shall be subject to the attached claims.

Claims

1. A device for continuous vanadium removal from waste liquid of waste catalyst regeneration and activation, characterized in that: include: A liquid inlet reaction tank (10), a flocculation tank (20) and a sedimentation tank (30) connected in sequence; The liquid inlet reaction tank (10) is connected to the flocculation tank (20); The flocculation tank (20) is connected to the sedimentation tank (30); The liquid inlet reaction pool (10) is provided with a first dosing pipe (41) and a second dosing pipe (42), wherein the first dosing pipe (41) is used to add a vanadium reducing agent into the liquid inlet reaction pool (10); and the second dosing pipe (42) is used to add a pH regulator into the liquid inlet reaction pool (10); The flocculation tank (20) is provided with a fourth dosing pipe (44) and a fifth dosing pipe (45), wherein the fourth dosing pipe (44) is used to add flocculant into the flocculation tank (20); and the fifth dosing pipe (45) is used to add coagulant aid into the flocculation tank (20).

2. The vanadium removal device according to claim 1, characterized in that: The liquid inlet reaction pool (10) is provided as one or more, and a plurality of the liquid inlet reaction pools (10) are sequentially connected in series to form a set of reactors. The reactors can be provided as multiple sets, and multiple sets of the reactors can be arranged in parallel.

3. The vanadium removal device according to claim 1 or 2, characterized in that: The liquid inlet reaction pool (10) comprises a liquid inlet pool (11) and a reaction pool (12), and the liquid inlet pool (11) and the reaction pool (12) are connected to each other; The first drug-feeding pipe (41) and the second drug-feeding pipe (42) are arranged on the liquid inlet pool (11); The reaction tank (12) is provided with a third dosing pipe (43), and the third dosing pipe (43) is used to add a pH regulator into the reaction tank (12).

4. The vanadium removal device according to claim 3, characterized in that: The liquid inlet pool (11) is provided with a first liquid inlet (111) and a first liquid outlet (112); The first liquid inlet (111) is connected to a liquid inlet regulating valve (114) and a liquid inlet pump (115) via a liquid inlet pipeline (113); The first liquid outlet (112) is connected to the reaction tank (12); The reaction tank (12) is provided with a second liquid inlet (121) and a second liquid outlet (122); The second liquid inlet (121) is in communication with the first liquid outlet (112); The second liquid outlet (122) is connected to the flocculation tank (20); The flocculation tank (20) is provided with a third liquid inlet (21) and a third liquid outlet (22); The third liquid inlet (21) is in communication with the second liquid outlet (122); The third liquid outlet (22) is connected to the sedimentation tank (30); The sedimentation tank (30) is provided with a fourth liquid inlet (31), a fourth liquid outlet (32) and a mud discharge outlet (33); The fourth liquid inlet (31) is connected to the third liquid outlet (22).

5. The vanadium removal device according to claim 3, characterized in that: The ratio of the total volume of the liquid inlet pool (11) and the reaction pool (12) to the liquid inlet flow rate is 30min-60min; The ratio of the total volume of the flocculation tank (20) to the liquid inlet flow rate of the flocculation tank (20) is 15min-45min; The ratio of the total volume of the sedimentation tank (30) to the liquid inlet flow rate of the sedimentation tank (30) is not less than 40min.

6. The vanadium removal device according to claim 3, characterized in that: The liquid inlet pool (11) is provided with a liquid inlet pool agitator (51); A reaction tank agitator (52) is provided in the reaction tank (12); A flocculation tank agitator (53) is provided in the flocculation tank (20); A sedimentation tank scraper (54) is provided in the sedimentation tank (30); Wherein, the agitator (51) of the liquid inlet tank, the agitator (52) of the reaction tank, the agitator (53) of the flocculation tank and the scraper (54) of the sedimentation tank can adopt double-layer agitation or single-layer agitation; and / or, The motor speeds of the liquid inlet tank agitator (51) and the reaction tank agitator (52) are controlled at 300 r / min-1500 r / min; The motor speed of the flocculation tank agitator (53) is controlled at 200r / min-500r / min; The motor speed of the sedimentation tank scraper (54) is controlled at 5 r / min-15 r / min.

7. The vanadium removal device according to claim 3, characterized in that: The first dosing pipe (41) is provided with a first dosing pump (411) and a first dosing control valve (412); The second dosing pipe (42) is provided with a second dosing pump (421) and a second dosing control valve (422); The third dosing pipe (43) is provided with a third dosing pump (431) and a third dosing control valve (432); The fourth dosing pipe (44) is provided with a fourth dosing pump (441) and a fourth dosing control valve (442); The fifth dosing pipe (45) is provided with a fifth dosing pump (451) and a fifth dosing control valve (452); and / or, The liquid inlet pipeline (113) is also provided with a liquid inlet flow meter (61); The first dosing pipe (41) is also provided with a dosing flow meter (62); The inlet pool (11) is provided with a first Ph meter (63) for detecting the Ph value of the inlet liquid and controlling it at 2-4; The flocculation tank (20) is provided with a second Ph meter (64) for detecting the Ph value of the flocculation tank and controlling it at 7-9; A mud level meter (65) is provided in the sedimentation tank (30).

8. The vanadium removal device according to claim 4, characterized in that: The bottom of the sedimentation tank (30) is configured as a conical bucket structure (37); The mud discharge port (33) is arranged at the lower part of the pool wall of the conical bucket structure (37); And or, the sedimentation tank (30) is further provided with an inclined tube sedimentation device (38); The inclined tube sedimentation device (38) is arranged above the conical bucket structure (37), and an inclined tube filler is used inside.

9. A method for removing vanadium using the device for removing vanadium from waste liquid by regeneration and activation of a waste catalyst as claimed in any one of claims 1 to 8, characterized in that: The steps include: Step 1: Start the liquid inlet pump (115) and adjust the liquid inlet regulating valve (114); Step 2: Gradually increase the opening of the liquid inlet regulating valve (114) until the reading of the liquid inlet flow meter (61) reaches the set flow rate, and record the flow meter reading v0 m at this time. 3 / h; inductively coupled plasma was used to detect the vanadium ion concentration in the waste liquid of the spent catalyst regeneration and activation, recorded as n0 mg / L, and the relative molecular weight of vanadium, recorded as M V g / mol; at this time, the amount of vanadium ions in the influent liquid q0 (mol / h) is: Step 3: Start the second dosing pump (421) and adjust the second dosing control valve (422); Step 4: gradually increase the opening of the second dosing control valve (422) to adjust the first Ph meter (63) to a reading of 2-4; Step 5: Start the first dosing pump (411) and adjust the first dosing control valve (412); Step 6: Gradually increase the opening of the first dosing control valve (412) to adjust the dosing flow meter (62) to the set flow rate, and record the flow meter reading v2 m at this time. 3 / h; this part of the reagent uses vanadium reducing agent, the relative molecular weight of vanadium reducing agent is Mg / mol, and the configured mass concentration is C, then the amount of vanadium reducing agent in the original solution is q1 (mol / h): Step 7: Start the third dosing pump (431), adjust the third dosing control valve (432), start the fourth dosing pump (441), adjust the fourth dosing control valve (442), start the fifth dosing pump (451), and adjust the fifth dosing control valve (452); Step 8: gradually increase the opening of the third dosing control valve (432) to adjust the reading of the second Ph meter (64) to 7-9; gradually increase the opening of the fourth dosing control valve (442) and the fifth dosing control valve (452). When uniform floccules appear and the sedimentation speed is fast, stop adjusting the fourth dosing control valve (442) and the fifth dosing control valve (452); Step 9: Sampling the effluent from the fourth liquid outlet (32) of the sedimentation tank (30) and detecting the vanadium ion concentration of the effluent from the sedimentation tank (30) by inductively coupled plasma, recorded as n1 mg / L. At this time, the vanadium removal efficiency is: Step 10: If the water vanadium ion concentration detected in step 9 is less than the target value, repeat steps 6 to 9 to increase the flow setting value of the vanadium reducing agent.

10. The vanadium removal method according to claim 9, characterized in that: The following steps are also included: Controlling the start and stop of the mud discharge pump (36) and the opening of the mud discharge control valve (35) according to the reading of the mud level meter (65); The mud level of the sedimentation tank (30) is controlled to be between 1 / 3 and 2 / 3 of the height of the tank body from the bottom.

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