Treatment device for waste lithium battery NMP slurry recovery wastewater

Abstract

The utility model provides a treatment device for waste lithium battery NMP slurry recovery wastewater. The treatment device comprises a homogeneous adjustment assembly, a heavy-removing coagulating sedimentation assembly, a sand filtration assembly, an electro-catalysis assembly, a phosphorus-removing coagulating sedimentation assembly and a biochemical reaction assembly. The water inlet end of the heavy-removing coagulating sedimentation assembly is communicated with the water outlet end of the homogeneous adjusting assembly. And the water inlet end of the sand filter assembly is communicated with the water outlet end of the heavy-removing coagulating sedimentation assembly. The electro-catalysis assembly comprises an electro-catalysis reactor, the electro-catalysis reactor is provided with an electro-catalysis reaction dosing area and an electro-catalysis reaction electrolysis area which are communicated with each other, and the water inlet end of the electro-catalysis reaction dosing area is communicated with the water outlet end of the sand filter assembly. The water inlet end of the dephosphorization coagulating sedimentation assembly is communicated with the water outlet end of the electro-catalysis reaction electrolysis area. The water inlet end of the biochemical reaction assembly is communicated with the water outlet end of the dephosphorization coagulating sedimentation assembly.

Description

Technical Field

[0001] The present invention relates to the field of lithium battery wastewater treatment, and in particular to a treatment device for wastewater recovered from NMP slurry of waste lithium batteries. Background Art

[0002] After disassembly and crushing, waste lithium batteries need to be recycled as the solvent NMP in the battery batching process to achieve the purpose of recycling and saving costs. In the process of recycling NMP, high concentrations of COD, ammonia nitrogen, TP, and SO4 are generated. 2- This wastewater is difficult to degrade and has poor biodegradability, so it must be treated before it can be discharged in compliance with discharge standards.

[0003] For example, the Chinese patent with patent number CN202320890202.2 proposes a treatment system for lithium battery positive electrode material production wastewater, including a sedimentation and coagulation device, a filtration device, a catalytic oxidation device and a biochemical treatment device. Through the sedimentation and coagulation device, the filtration device and the catalytic oxidation device, the content of heavy metals, fluorine, organic phosphorus and other biochemically toxic substances in the wastewater is reduced, and the biodegradability of the wastewater is increased; the wastewater pollutants are further removed by the subsequent high-efficiency biochemical treatment device. The system treatment target is highly targeted, the process design is reasonable, the treatment effect is stable and efficient, and the process scalability is good. This system solves the problems of unstable sewage treatment effect, high operating cost, and inability to effectively remove pollutants such as fluoride ions and organic phosphorus in wastewater in the prior art.

[0004] However, the technical solution of the above patent has the following problems:

[0005] First, the catalytic oxidation device uses a packed ozone catalytic oxidation tower, which needs to be equipped with corresponding ozone preparation equipment and air compression equipment. This makes the wastewater treatment process of the catalytic oxidation device more complicated, and the ozone catalytic oxidation of organic matter treatment efficiency is low; secondly, the organic phosphorus in the wastewater is converted into orthophosphate by the catalytic oxidation tower and needs to be returned to the sedimentation and coagulation device for coagulation and sedimentation treatment to reduce the orthophosphate content in the wastewater. If the organic phosphorus content in the wastewater is high, the same batch of wastewater will be returned to the sedimentation and coagulation device multiple times during the treatment process, resulting in the inability of subsequent devices to operate normally, affecting the treatment efficiency of the entire wastewater treatment system. Utility Model Content

[0006] The purpose of the present invention is to overcome the shortcomings of the prior art and provide a treatment device for recycling waste water from NMP slurry of waste lithium batteries with high waste water treatment efficiency.

[0007] The purpose of this disclosure is achieved through the following technical solutions:

[0008] A treatment device for waste water from NMP slurry recovery of waste lithium batteries, comprising:

[0009] Homogenizing adjustment component;

[0010] A weight removal coagulation and sedimentation component, wherein the water inlet end of the weight removal coagulation and sedimentation component is connected to the water outlet end of the homogenization and adjustment component;

[0011] A sand filter assembly, wherein the water inlet end of the sand filter assembly is connected to the water outlet end of the weight removal coagulation sedimentation assembly;

[0012] An electrocatalytic component, the electrocatalytic component comprising an electrocatalytic reactor, the electrocatalytic reactor being provided with an electrocatalytic reaction dosing area and an electrocatalytic reaction electrolysis area which are connected to each other, and the water inlet end of the electrocatalytic reaction dosing area is connected to the water outlet end of the sand filter component;

[0013] A phosphorus removal coagulation and sedimentation component, wherein the water inlet end of the phosphorus removal coagulation and sedimentation component is connected to the water outlet end of the electrocatalytic reaction electrolysis zone;

[0014] A biochemical reaction component, wherein the water inlet end of the biochemical reaction component is connected to the water outlet end of the phosphorus removal coagulation and sedimentation component.

[0015] In one embodiment, the homogenization adjustment component includes a homogenization adjustment tank, the water outlet of the homogenization adjustment tank is connected to the water inlet of the weight removal coagulation sedimentation component, and the water inlet of the homogenization adjustment tank is connected to the water outlet of the NMP recovery wastewater discharge component.

[0016] In one embodiment, the weight removal coagulation and sedimentation component includes a weight removal coagulation and sedimentation reaction tank, and the weight removal coagulation and sedimentation reaction tank is provided with a first weight removal coagulation reaction zone, a second weight removal coagulation reaction zone, a third weight removal coagulation reaction zone, a weight removal inclined tube sedimentation zone and a weight removal wastewater outlet zone which are sequentially connected along the water inlet direction, the water inlet end of the first weight removal coagulation reaction zone is connected to the water outlet end of the homogenization adjustment tank, and the water outlet end of the weight removal wastewater outlet zone is connected to the water inlet end of the sand filter component.

[0017] In one embodiment, the sand filter assembly includes at least one sand filter tank and a sand filter water outlet tank, the first water inlet end of each sand filter tank is connected to the water outlet end of the de-heavy wastewater outlet area, the first water outlet end of each sand filter tank is connected to the water inlet end of the sand filter water outlet tank, the second water outlet end of each sand filter tank is connected to the water inlet end of the first de-heavy coagulation reaction zone, and the water outlet end of the sand filter water outlet tank is respectively connected to the second water inlet ends of multiple sand filter tanks and the water inlet end of the electrocatalytic reaction dosing zone.

[0018] In one embodiment, the electrocatalytic component further includes a pH adjusting tank, the water inlet of the pH adjusting tank is connected to the water outlet of the deheavy wastewater outlet area, and the water outlet of the pH adjusting tank is respectively connected to the water inlet of the plurality of sand filter tanks.

[0019] In one embodiment, the phosphorus removal coagulation and sedimentation component includes a phosphorus removal coagulation and sedimentation reaction tank, which is provided with a first phosphorus removal coagulation reaction zone, a second phosphorus removal coagulation reaction zone, a third phosphorus removal coagulation reaction zone, a fourth phosphorus removal coagulation reaction zone, a phosphorus removal inclined tube sedimentation zone and a phosphorus removal wastewater outlet zone which are sequentially connected along the water inlet direction, the water inlet end of the first phosphorus removal coagulation reaction zone is connected to the water outlet end of the electrocatalytic reaction electrolysis zone, and the water outlet end of the phosphorus removal wastewater outlet zone is connected to the water inlet end of the biochemical reaction component.

[0020] In one embodiment, the biochemical reaction component includes a biochemical reactor and a biochemical reaction effluent tank. The biochemical reactor is provided with an anaerobic reaction zone, an anoxic reaction zone, an aerobic reaction zone and a secondary sedimentation tank which are sequentially connected along the water inlet direction. The water inlet end of the anaerobic reaction zone is connected to the water outlet end of the phosphorus removal wastewater effluent zone, and the water outlet end of the secondary sedimentation tank is respectively connected to the water inlet end of the anaerobic reaction zone, the water inlet end of the anoxic reaction zone and the water inlet end of the biochemical reaction effluent tank.

[0021] In one embodiment, the biochemical reaction assembly further includes a neutralization reaction tank and a plate heat exchanger, the water inlet end of the neutralization reaction tank is connected to the water outlet end of the dephosphorization wastewater outlet area, the water outlet end of the neutralization reaction tank is respectively connected to the water inlet end of the plate heat exchanger and the water inlet end of the anaerobic reaction area, and the water outlet end of the plate heat exchanger is connected to the water inlet end of the anaerobic reaction area.

[0022] In one of the embodiments, the treatment device further comprises a wastewater discharge tank, and a water inlet end of the wastewater discharge tank is connected to a water outlet end of the biochemical reaction water outlet tank.

[0023] In one of the embodiments, a first sludge hopper is provided at the bottom of the weight removal inclined tube sedimentation zone;

[0024] A second sludge hopper is provided at the bottom of the phosphorus removal inclined tube sedimentation zone;

[0025] A third sludge hopper is arranged at the bottom of the secondary sedimentation tank.

[0026] Compared with the prior art, the present invention has at least the following advantages:

[0027] 1. The wastewater from NMP slurry recovery from used lithium batteries treated by the homogenizing and regulating component is transported to the weight removal coagulation and sedimentation component for coagulation and sedimentation reaction, which can not only effectively remove heavy metals in the wastewater, but also remove most of the suspended matter in the wastewater. The wastewater treated by the weight removal coagulation and sedimentation component is transported to the sand filter component, and the suspended matter in the wastewater is further removed by the sand filter component, which can reduce the effluent turbidity in the wastewater.

[0028] 2. The wastewater treated by the sand filter assembly is transported to the electrocatalytic reaction dosing area, sodium sulfate is added to the electrocatalytic reaction area and fully mixed with the wastewater, and then flows into the electrocatalytic reaction electrolysis area for electrocatalytic reaction, that is, the hydroxyl radicals and active oxygen radicals generated by the electrolysis reaction are used to decompose macromolecular organic matter into small molecular inorganic matter, nitrogen-containing compounds are decomposed and converted into nitrogen, and organic phosphorus is converted into phosphate ions, which not only effectively improves the biodegradability of the wastewater, but also reduces the COD value of the wastewater, and simplifies the treatment process of catalytic oxidation of wastewater. Further, the wastewater treated by the electrocatalytic reactor is transported to the phosphorus removal coagulation and precipitation assembly, and the sulfate ions and phosphate ions in the wastewater are removed by the phosphorus removal coagulation and precipitation assembly, so that the concentration of sulfate ions and phosphate ions in the wastewater can be effectively reduced, thereby effectively reducing the TP value of the wastewater. At the same time, the wastewater treated by the electrocatalytic reactor does not need to be refluxed, which ensures the continuous operation of the treatment device for recycling wastewater from NMP slurry of waste lithium batteries, thereby effectively improving the wastewater treatment efficiency of the treatment device for recycling wastewater from NMP slurry of waste lithium batteries.

[0029] 3. The wastewater treated by the phosphorus removal coagulation and sedimentation component is transported to the biochemical reaction component, and the wastewater is subjected to phosphorus removal and nitrogen removal operations through the biochemical reaction component, which can effectively reduce the TP value and ammonia nitrogen concentration of the wastewater, thereby effectively improving the wastewater treatment effect of the waste lithium battery NMP slurry recovery wastewater treatment device. BRIEF DESCRIPTION OF THE DRAWINGS

[0030] In order to more clearly illustrate the technical solutions of the embodiments of the present disclosure, the drawings required for use in the embodiments will be briefly introduced below. It should be understood that the following drawings only show certain embodiments of the present disclosure and therefore should not be regarded as limiting the scope. For ordinary technicians in this field, other related drawings can be obtained based on these drawings without paying creative work.

[0031] Figure 1 This is a schematic diagram of the structure of a treatment device for recycling waste water from NMP slurry of waste lithium batteries in one embodiment;

[0032] Figure 2 for Figure 1 A partial structural schematic diagram of a weight removal coagulation and sedimentation component of a treatment device for recycling waste water from NMP slurry of used lithium batteries is shown;

[0033] Figure 3 for Figure 1 A schematic diagram of the partial structure of a sand filter assembly of a treatment device for recycling waste water from NMP slurry of used lithium batteries is shown;

[0034] Figure 4 for Figure 1A schematic diagram of the partial structure of the electrocatalytic component of the treatment device for recycling waste water from NMP slurry of used lithium batteries is shown;

[0035] Figure 5 for Figure 1 A schematic diagram of the partial structure of the phosphorus removal coagulation and sedimentation component of the treatment device for recycling waste water from NMP slurry of used lithium batteries is shown;

[0036] Figure 6 for Figure 1 A schematic diagram of the partial structure of the biochemical reaction components of the treatment device for recycling waste water from NMP slurry of used lithium batteries is shown;

[0037] Figure symbols: Treatment device 10 for recycling waste water from NMP slurry of used lithium batteries; homogenization adjustment component 100; homogenization adjustment tank 110; weight removal coagulation and sedimentation component 200; weight removal coagulation and sedimentation reaction tank 210; first weight removal coagulation reaction zone 211; second weight removal coagulation reaction zone 212; third weight removal coagulation reaction zone 213; weight removal inclined tube sedimentation zone 214; weight removal wastewater effluent zone 215; first sludge hopper 220; sand filter component 300; sand filter tank 310; sand filter effluent tank 320; electrocatalytic component 400; electrocatalytic reactor 410; electrocatalytic reaction dosing zone 411; electrocatalytic reaction electrolysis zone 412; pH adjustment Tank 420; phosphorus removal coagulation and sedimentation component 500; phosphorus removal coagulation and sedimentation reaction tank 510; first phosphorus removal coagulation reaction zone 511; second phosphorus removal coagulation reaction zone 512; third phosphorus removal coagulation reaction zone 513; fourth phosphorus removal coagulation reaction zone 514; phosphorus removal inclined tube sedimentation zone 515; phosphorus removal wastewater effluent zone 516; second sludge hopper 520; biochemical reaction component 600; biochemical reactor 610; anaerobic reaction zone 611; anoxic reaction zone 612; aerobic reaction zone 613; second sedimentation tank 614; biochemical reaction effluent tank 620; neutralization reaction tank 630; plate heat exchanger 640; third sludge hopper 650; wastewater discharge tank 700. DETAILED DESCRIPTION

[0038] In order to facilitate the understanding of the present disclosure, the present disclosure will be described more fully below with reference to the relevant drawings. The preferred embodiments of the present disclosure are given in the drawings. However, the present disclosure can be implemented in many different forms and is not limited to the embodiments described herein. On the contrary, the purpose of providing these embodiments is to make the disclosure of the present disclosure more thoroughly and comprehensively understood.

[0039] It should be noted that when an element is referred to as being "fixed to" another element, it may be directly on the other element or there may be a central element. When an element is considered to be "connected to" another element, it may be directly connected to the other element or there may be a central element at the same time. The terms "vertical", "horizontal", "left", "right" and similar expressions used herein are for illustrative purposes only and do not represent the only implementation method.

[0040] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as those commonly understood by those skilled in the art of the present disclosure. The terms used herein in the specification of the present disclosure are only for the purpose of describing specific embodiments and are not intended to limit the present disclosure. The term "and / or" used herein includes any and all combinations of one or more related listed items.

[0041] See also Figures 1 to 6 In order to better understand the waste lithium battery NMP slurry recovery wastewater treatment device 10 disclosed in the present invention, the waste lithium battery NMP slurry recovery wastewater treatment device 10 is further explained below:

[0042] The treatment device 10 for recycling wastewater from NMP slurry of waste lithium batteries in one embodiment includes a homogenizing and regulating component 100, a weight removal coagulation and sedimentation component 200, a sand filter component 300, an electrocatalytic component 400, a phosphorus removal coagulation and sedimentation component 500 and a biochemical reaction component 600. The water inlet end of the weight removal coagulation and sedimentation component 200 is connected to the water outlet end of the homogenizing and regulating component 100. The water inlet end of the sand filter component 300 is connected to the water outlet end of the weight removal coagulation and sedimentation component 200. The electrocatalytic component 400 includes an electrocatalytic reactor 410, which is provided with an electrocatalytic reaction dosing area 411 and an electrocatalytic reaction electrolysis area 412 connected to each other, and the water inlet end of the electrocatalytic reaction dosing area 411 is connected to the water outlet end of the sand filter component 300. The water inlet end of the phosphorus removal coagulation and sedimentation component 500 is connected to the water outlet end of the electrocatalytic reaction electrolysis area 412. The water inlet of the biochemical reaction component 600 is communicated with the water outlet of the phosphorus removal coagulation and sedimentation component 500 .

[0043] In this embodiment, the waste water from the NMP slurry recovery of used lithium batteries after being treated by the homogenizing and regulating component 100 is transported to the weight removal coagulation and sedimentation component 200 for coagulation and sedimentation reaction, which can not only effectively remove heavy metals in the waste water, but also remove most of the suspended matter in the waste water. The waste water treated by the weight removal coagulation and sedimentation component 200 is transported to the sand filter component 300, and the suspended matter in the waste water is further removed by the sand filter component 300, so that the effluent turbidity in the waste water can be reduced.

[0044] Furthermore, the wastewater treated by the sand filter assembly 300 is transported to the electrocatalytic reaction dosing zone 411, sodium sulfate is added to the electrocatalytic reaction zone and fully mixed with the wastewater before flowing into the electrocatalytic reaction electrolysis zone 412 for electrocatalytic reaction, that is, the hydroxyl radicals and active oxygen radicals generated by the electrolysis reaction are used to decompose large molecular organic matter into small molecular inorganic matter, nitrogen-containing compounds are decomposed and converted into nitrogen, and organic phosphorus is converted into phosphate ions, which not only effectively improves the biodegradability of the wastewater, but also reduces the COD value of the wastewater, while also simplifying the treatment process of catalytic oxidation of the wastewater. Furthermore, the wastewater treated by the electrocatalytic reactor 410 is transported to the phosphorus removal coagulation and sedimentation component 500, and the sulfate ions and phosphate ions in the wastewater are removed by the phosphorus removal coagulation and sedimentation component 500, which can effectively reduce the concentration of sulfate ions and phosphate ions in the wastewater, thereby effectively reducing the TP value of the wastewater. At the same time, the wastewater treated by the electrocatalytic reactor 410 does not need to be refluxed, thereby ensuring the continuous operation of the treatment device 10 for recovering NMP slurry wastewater from waste lithium batteries, thereby effectively improving the wastewater treatment efficiency of the treatment device 10 for recovering NMP slurry wastewater from waste lithium batteries.

[0045] Furthermore, the wastewater treated by the phosphorus removal coagulation and sedimentation component 500 is transported to the biochemical reaction component 600, and the wastewater is subjected to phosphorus removal and nitrogen removal operations through the biochemical reaction component 600, which can effectively reduce the TP value and ammonia nitrogen concentration of the wastewater, thereby effectively improving the wastewater treatment effect of the waste lithium battery NMP slurry recovery wastewater treatment device 10.

[0046] It should be noted that the material of the anode plate of the electrocatalytic reactor 410 is boron-doped diamond material, and the material of the cathode plate is titanium material, so that hydroxyl radicals and reactive oxygen radicals can be generated by electrolysis reaction, and hydroxyl radicals and reactive oxygen radicals as oxidants can decompose macromolecular organic matter into small molecule inorganic matter, decompose nitrogen-containing compounds into nitrogen, and convert organic phosphorus into phosphate ions, which not only effectively improves the biodegradability of wastewater, but also reduces the COD value of wastewater. Furthermore, the treatment process of catalytic oxidation of wastewater can be achieved only by powering on and adding drugs, which simplifies the wastewater treatment process, reduces the cost of wastewater treatment while ensuring good organic matter treatment efficiency.

[0047] It should be additionally explained that a vertical mixer is provided in the electrocatalytic reaction dosing area 411 to ensure that the wastewater and sodium sulfate in the electrocatalytic reaction dosing area 411 can be fully mixed.

[0048] like Figure 1 and Figure 2As shown, in one embodiment, the homogenization adjustment component 100 includes a homogenization adjustment tank 110, the outlet end of the homogenization adjustment tank 110 is connected to the inlet end of the weight removal coagulation sedimentation component 200, and the inlet end of the homogenization adjustment tank 110 is connected to the outlet end of the NMP recovery wastewater discharge component. It can be understood that the wastewater recovered from the NMP slurry of the waste lithium battery is transported to the homogenization adjustment tank 110 through the NMP recovery wastewater discharge component for pretreatment, that is, the wastewater recovered from the NMP slurry of the waste lithium battery is subjected to a homogenization adjustment operation to make the wastewater more uniform.

[0049] like Figure 2 As shown, in one embodiment, the de-weighting coagulation and sedimentation component 200 includes a de-weighting coagulation and sedimentation reaction tank 210, and the de-weighting coagulation and sedimentation reaction tank 210 is provided with a first de-weighting coagulation reaction zone 211, a second de-weighting coagulation reaction zone 212, a third de-weighting coagulation reaction zone 213, a de-weighting inclined tube sedimentation zone 214 and a de-weighting wastewater outlet zone 215 which are sequentially connected along the water inlet direction, and the water inlet end of the first de-weighting coagulation reaction zone 211 is connected to the water outlet end of the homogenization adjustment tank 110, and the water outlet end of the de-weighting wastewater outlet zone 215 is connected to the water inlet end of the sand filter component 300. It should be noted that, first, the wastewater is pumped into the first de-weighting coagulation reaction zone 211 by the homogenization adjustment tank 110, and a 5-10% sodium hydroxide solution is added to the first de-weighting coagulation reaction zone 211 to control the pH value between 9.5 and 11.0, and then the wastewater is fully mixed. Secondly, the wastewater flows from the first weight removal coagulation reaction zone 211 into the second weight removal coagulation reaction zone 212, 5-10% polyaluminium chloride is added to the second weight removal coagulation reaction zone 212, and the wastewater is fully mixed. Then, the wastewater flows from the second weight removal coagulation reaction zone 212 into the third weight removal coagulation reaction zone 213, 0.5-1% anionic polyacrylamide is added to the third weight removal coagulation reaction zone 213 for flocculation precipitation, and the wastewater is fully mixed to form sludge wastewater. Finally, the sludge wastewater flows from the bottom of the third weight removal coagulation reaction zone 213 to the weight removal inclined pipe sedimentation zone 214, the weight removal sediment sinks to the bottom along the inclined pipe and is discharged from the sewage discharge assembly connected to the sewage discharge port at the bottom, and the supernatant of the weight removal inclined pipe sedimentation zone 214 flows into the weight removal wastewater outlet zone 215, so that the heavy metals and suspended matter in the wastewater can be effectively removed.

[0050] It should be noted that vertical mixers are provided in the first weight removal and coagulation reaction zone 211 , the second weight removal and coagulation reaction zone 212 , and the third weight removal and coagulation reaction zone 213 , so that the wastewater can be fully mixed.

[0051] Furthermore, in other embodiments, the deweighted precipitate is discharged to a filter press through a sewage discharge component for filtration, and the filtrate is returned to the first deweighting coagulation reaction zone 211 for circulation treatment, while the filter residue is uniformly recovered and treated.

[0052] like Figure 1 and Figure 3 As shown, in one embodiment, the sand filter assembly 300 includes at least one sand filter tank 310 and a sand filter water outlet tank 320, the first water inlet end of each of the sand filter tanks 310 is connected to the water outlet end of the de-weighting wastewater outlet area 215, the first water outlet end of each of the sand filter tanks 310 is connected to the water inlet end of the sand filter water outlet tank 320, the second water outlet end of each of the sand filter tanks 310 is connected to the water inlet end of the first de-weighting coagulation reaction area 211, and the water outlet end of the sand filter water outlet tank 320 is respectively connected to the second water inlet ends of multiple sand filter tanks 310 and the water inlet end of the electrocatalytic reaction dosing area 411. It should be noted that the sand filter tank 310 can further remove suspended matter in the wastewater and reduce the turbidity of the wastewater outlet, and multiple sand filter tanks 310 can serve as a backup to avoid the shutdown of the treatment device when a single sand filter tank 310 is blocked, thereby ensuring that the wastewater treatment device can operate continuously, thereby ensuring that the treatment device 10 for recycling NMP slurry wastewater from waste lithium batteries has a higher wastewater treatment efficiency.

[0053] It should be added that the sand filter tank 310 is filled with 8-16 mm quartz sand, 4-8 mm quartz sand, 2-4 mm quartz sand, 1-2 mm quartz sand, 0.5-1 mm quartz sand, 2-4 mm anthracite, and 1-2 mm anthracite from bottom to top, and an exhaust valve is provided at the top of the sand filter tank 310, and an emptying valve is provided at the bottom of the sand filter tank 310. Further, in other embodiments, the sand filter tank 310 is also provided with a backwashing pipeline and an air washing pipeline, and the sand filter tank 310 is backwashed through the backwashing pipeline box and the air washing pipeline, the backwashing water is provided by the sand filter water tank 320, and the compressed air for air washing is provided by the air compressor.

[0054] like Figures 1 to 3 As shown, in one embodiment, the electrocatalytic assembly 400 further includes a pH adjustment tank 420, the water inlet of the pH adjustment tank 420 is connected to the water outlet of the de-heavy wastewater outlet area 215, and the water outlet of the pH adjustment tank 420 is respectively connected to the water inlet of the plurality of sand filter tanks 310. It is understood that in order to achieve the optimal pH condition of the electrocatalytic oxidation reaction, the wastewater is transported from the de-heavy wastewater outlet area 215 to the pH adjustment tank 420, and 5-10% sulfuric acid is added to the pH adjustment tank 420 to adjust the pH value to between 7.0 and 8.0.

[0055] like Figure 1 , Figure 4 and Figure 5As shown, in one embodiment, the phosphorus removal coagulation and sedimentation assembly 500 includes a phosphorus removal coagulation and sedimentation reaction tank 510, and the phosphorus removal coagulation and sedimentation reaction tank 510 is provided with a first phosphorus removal coagulation reaction zone 511, a second phosphorus removal coagulation reaction zone 512, a third phosphorus removal coagulation reaction zone 513, a fourth phosphorus removal coagulation reaction zone 514, a phosphorus removal inclined tube sedimentation zone 515 and a phosphorus removal wastewater outlet zone 516 which are sequentially connected along the water inlet direction, and the water inlet end of the first phosphorus removal coagulation reaction zone 511 is connected to the water outlet end of the electrocatalytic reaction electrolysis zone 412, and the water outlet end of the phosphorus removal wastewater outlet zone 516 is connected to the water inlet end of the biochemical reaction assembly 600. It should be noted that the wastewater is transported from the electrocatalytic reaction electrolysis zone 412 to the first phosphorus removal coagulation reaction zone 511, and 5-10% calcium hydroxide solution is added to the first phosphorus removal coagulation reaction zone 511 to fully mix with the wastewater, so as to remove sulfate ions and phosphate ions in the wastewater. Wastewater flows from the first phosphorus removal coagulation reaction zone 511 into the second phosphorus removal coagulation reaction zone 512. A 5-10% sodium carbonate solution is added to the second phosphorus removal coagulation reaction zone 512 to mix the wastewater thoroughly, which can remove calcium ions in the wastewater. Wastewater flows from the second phosphorus removal coagulation reaction zone 512 into the third phosphorus removal coagulation reaction zone 513. A 5-10% polyaluminium chloride is added to the third phosphorus removal coagulation reaction zone 513 to mix the wastewater thoroughly, and the polyaluminium chloride plays a coagulant effect. Wastewater flows from the third phosphorus removal coagulation reaction zone 513 into the fourth phosphorus removal coagulation reaction zone 514. A 0.5-1% anionic polyacrylamide is added to the fourth phosphorus removal coagulation reaction zone 514 to mix the wastewater thoroughly, so that the sediment in the wastewater flocculates into agglomerates to form sludge wastewater. The sludge wastewater flows into the phosphorus removal inclined tube sedimentation zone 515 from the bottom of the fourth phosphorus removal coagulation reaction zone 514, and the phosphorus removal precipitate sinks to the bottom along the inclined tube and is discharged from the sewage discharge assembly connected to the sewage outlet at the bottom, while the supernatant of the phosphorus removal inclined tube sedimentation zone 515 flows into the phosphorus removal wastewater outlet zone 516, so that the sulfate ions and phosphate ions in the wastewater can be effectively removed, and the calcium ions introduced by calcium sulfate can also be removed.

[0056] It should be noted that vertical mixers are installed in the first phosphorus removal coagulation reaction zone 511 , the second phosphorus removal coagulation reaction zone 512 , the third phosphorus removal coagulation reaction zone 513 , and the fourth phosphorus removal coagulation reaction zone 514 , so that the wastewater can be fully mixed.

[0057] Furthermore, in other embodiments, the dephosphorization precipitate is discharged to a filter press through a sewage discharge component for filtration, and the filtrate is returned to the first dephosphorization coagulation reaction zone 511 for circulation treatment, and the filter residue is uniformly recovered and treated.

[0058] like Figure 1 , Figure 5 and Figure 6As shown, in one embodiment, the biochemical reaction assembly 600 includes a biochemical reactor 610 and a biochemical reaction outlet tank 620. The biochemical reactor 610 is provided with an anaerobic reaction zone 611, an anoxic reaction zone 612, an aerobic reaction zone 613 and a secondary sedimentation tank 614 which are sequentially connected along the water inlet direction. The water inlet end of the anaerobic reaction zone 611 is connected to the water outlet end of the phosphorus removal wastewater outlet zone 516, and the water outlet end of the secondary sedimentation tank 614 is respectively connected to the water inlet end of the anaerobic reaction zone 611, the water inlet end of the anoxic reaction zone 612 and the water inlet end of the biochemical reaction outlet tank 620. It should be noted that the wastewater is transported to the anaerobic reaction zone 611, phosphorus is released under the action of the phosphorus-releasing bacteria in the anaerobic reaction zone 611, and the phosphorus released anaerobically is absorbed and treated under the action of the polyphosphate bacteria in the aerobic reaction zone 613 and discharged with the bottom mud, thereby reducing the TP value of the wastewater. Under the action of nitrifying bacteria in the anaerobic reaction zone 611 and the aerobic reaction zone 613, organic nitrogen compounds are decomposed into NO 2- and NO 3- Under the action of denitrifying bacteria in the anoxic reaction zone 612, NO 2- and NO 3- The wastewater is reduced to nitrogen gas, thereby reducing the ammonia nitrogen content of the wastewater, and the organic matter remaining in the wastewater is degraded and converted into small molecular organic matter by the action of facultative bacteria and anaerobic bacteria in the anaerobic reaction zone 611, and the small molecular organic matter is decomposed in the aerobic reaction zone 613, further reducing the COD value of the wastewater. The wastewater after aerobic treatment enters the secondary sedimentation tank 614 for sedimentation treatment, and the supernatant of the secondary sedimentation tank 614 flows into the biochemical reaction water outlet tank 620, and the biochemical precipitate is discharged from the sewage discharge component connected to the sewage discharge port at the bottom of the secondary sedimentation tank 614.

[0059] Furthermore, in other embodiments, the biochemical precipitate is discharged to the filter press through the sewage discharge component for filtration, the filtrate is returned to the anaerobic reaction zone 611 for circulation treatment, and the filter residue is uniformly recovered and treated.

[0060] like Figure 1 , Figure 5 and Figure 6As shown, in one embodiment, the biochemical reaction assembly 600 further includes a neutralization reaction tank 630 and a plate heat exchanger 640, the water inlet end of the neutralization reaction tank 630 is connected to the water outlet end of the dephosphorization wastewater outlet area 516, the water outlet end of the neutralization reaction tank 630 is respectively connected to the water inlet end of the plate heat exchanger 640 and the water inlet end of the anaerobic reaction area 611, and the water outlet end of the plate heat exchanger 640 is connected to the water inlet end of the anaerobic reaction area 611. It can be understood that the wastewater flows into the neutralization reaction tank 630 from the dephosphorization wastewater outlet area 516, and 5-10% sulfuric acid is added to the neutralization reaction tank 630 to adjust the pH value of the wastewater to between 6.5 and 8.5 to meet the water inlet conditions of the biochemical reaction assembly 600. The wastewater flows from the neutralization reaction tank 630 into the plate heat exchanger 640 for heat exchange, so that the water temperature of the wastewater is 25-40° C. to meet the water inlet condition of the biochemical reaction assembly 600 .

[0061] like Figure 1 and Figure 6 As shown, in one embodiment, the treatment device 10 further includes a wastewater discharge tank 700, and the water inlet end of the wastewater discharge tank 700 is connected to the water outlet end of the biochemical reaction water outlet tank 620. It can be understood that the treated wastewater flows from the biochemical reaction water outlet tank 620 into the wastewater discharge tank 700, and the pH value of the wastewater in the wastewater discharge tank 700 is adjusted to be between 6 and 9. If the wastewater measurement result meets the third-level standard of the "Comprehensive Sewage Discharge Standard" GB8978-1996, it is discharged to the downstream process, and if it does not meet the standard, it is returned to the homogenization adjustment tank 110 for circulation treatment.

[0062] like Figure 2 , Figure 5 and Figure 6 As shown, in one embodiment, a first sludge hopper 220 is provided at the bottom of the weight removal inclined tube sedimentation zone 214. A second sludge hopper 520 is provided at the bottom of the phosphorus removal inclined tube sedimentation zone 515. A third sludge hopper 650 is provided at the bottom of the secondary sedimentation tank 614. It can be understood that by providing sludge hoppers in the weight removal inclined tube sedimentation zone 214, the phosphorus removal inclined tube sedimentation zone 515 and the secondary sedimentation tank 614, it is convenient to collect and process the sediment in the sludge wastewater.

[0063] See also Figures 1 to 6 In one embodiment, the operation process of the treatment device 10 for recycling waste water from NMP slurry of waste lithium batteries is as follows:

[0064] Target wastewater: wastewater recovered from NMP distillation of waste lithium batteries. The main pollutants in the wastewater are COD8000~16000mg / L, NH3-N100~500mg / L, TP30~360mg / L, and heavy metal concentration 10~15mg / L.

[0065] 1. The wastewater first enters the homogenization adjustment tank 110 for homogenization adjustment of water quality and quantity. At this time, the pH value of the wastewater is 6 to 8;

[0066] 2. Wastewater is pumped from the homogenization adjustment tank 110 into the first de-weighting coagulation reaction zone 211. A 5-10% sodium hydroxide solution is added to the first de-weighting coagulation reaction zone 211 to control the pH value to 9.5-11.0. The reaction zone is equipped with a vertical mixer to stir the material at a uniform speed. The reaction time of this process is 30 minutes. By measuring the heavy metal ion content in the de-weighting inclined tube sedimentation zone 214, the amount of sodium hydroxide added is adjusted to ensure that the heavy metal content is ≤1mg / L to avoid the OH generated during the reaction with the electrocatalytic oxidation reactor. - The generated precipitate causes the electrocatalytic oxidation reactor to be blocked and affects the biochemical reaction component 600 at the rear end;

[0067] 3. The wastewater flows from the first weight removal coagulation reaction zone 211 to the second weight removal coagulation reaction zone 212 by gravity. 5-10% polyaluminium chloride is added to the second weight removal coagulation reaction zone 212 as a coagulant. The reaction zone is equipped with a vertical mixer to stir the material at a uniform speed. The reaction time of this process is 10-20 minutes.

[0068] 4. The wastewater flows from the second weight removal coagulation reaction zone 212 to the third weight removal coagulation reaction zone 213. 0.5-1% anionic polyacrylamide is added to the third weight removal coagulation reaction zone 213 for flocculation. The reaction zone is equipped with a vertical mixer to stir the material at a uniform speed. The reaction time of this process is 10-20 minutes.

[0069] 5. Wastewater flows from the bottom of the third weight removal coagulation reaction zone 213 into the weight removal inclined tube sedimentation zone 214 by gravity. The sediment sinks along the inclined tube to the first sludge hopper 220 at the bottom. Under the action of an external pump, it is pumped from the mud outlet pipeline to the filter press for filtration. The filtrate is then returned to the first weight removal coagulation reaction zone 211 for treatment, and the sludge is transported to a qualified unit for disposal.

[0070] 6. The supernatant of the gravity removal inclined tube sedimentation area 214 overflows to the gravity removal wastewater outlet area 215;

[0071] 7. The wastewater is pumped from the de-gravimetric wastewater outlet area 215 into the pH adjustment tank 420, and 5-10% sulfuric acid is added to adjust the pH to 7.0-8.0 to achieve the optimal pH condition for the electrocatalytic oxidation reaction;

[0072] 8. After adjusting the pH, the wastewater is pumped into the sand filter tank 310 for filtration to further remove suspended solids in the water and reduce the turbidity of the effluent. The effluent SS is ≤15mg / L. The sand filter tank 310 is used in a standby manner. The sand filter tank 310 is filled with 8-16mm quartz sand, 4-8mm quartz sand, 2-4mm quartz sand, 1-2mm quartz sand, 0.5-1mm quartz sand, 2-4mm anthracite, and 1-2mm anthracite from bottom to top. There is an exhaust valve at the top of the sand filter tank 310 and an emptying valve at the bottom of the sand filter tank 310. In addition, the sand filter tank 310 contains a backwashing pipeline and an air washing pipeline for backwashing. The backwashing water is provided by the sand filter water tank 320, and the compressed air for air washing is provided by the air compressor. When the inlet and outlet water pressure difference is ≥0.2MPa, the sand filter tank 310 enters the backwashing procedure;

[0073] 9. The water from the sand filter tank 310 enters the sand filter water tank 320 and is then pumped into the electrocatalytic reaction dosing area 411. The electrocatalytic reaction dosing area 411 is provided with a vertical agitator. Industrial sodium sulfate is added as an electrolyte for electrocatalytic oxidation. The addition amount is 1 to 4 g / L and the reaction time is 5 to 20 min.

[0074] 10. After adding the electrolyte, the wastewater flows by gravity into the electrocatalytic reaction electrolysis zone 412 for treatment. The cathode plate of the electrocatalytic oxidation reaction electrolysis zone is made of titanium, and the anode plate is made of boron-doped diamond. The plate spacing is 2mm. The top of the electrocatalytic oxidation reaction electrolysis is provided with an exhaust gas outlet pipeline, the bottom of the electrocatalytic oxidation reaction electrolysis is provided with an emptying pipeline, and the outlet of the electrocatalytic oxidation reaction electrolysis is provided with a reflux pipeline. In addition, a pickling unit is also provided, which is connected to the electrocatalytic oxidation reactor through a pipeline, and the acid is 5-10% dilute hydrochloric acid or citric acid. The current density during electrolysis is 20-80mA / cm 2 , using the oxidants such as ·OH and ·O generated by the reaction to decompose macromolecular organic matter into small molecular inorganic matter, convert organic phosphorus into phosphate, improve the biodegradability and degradation performance of wastewater, and decompose nitrogen-containing compounds into nitrogen gas. The reaction time is 60 to 90 minutes. The effluent COD is ≤800mg / L, and NH3-N is ≤35mg / L;

[0075] 11. The effluent from the electrolytic zone 412 enters the first phosphorus removal coagulation reaction zone 511. A 5-10% calcium hydroxide solution is added to the first phosphorus removal coagulation reaction zone 511 to remove SO4 in the wastewater. 2- and PO4 3- The dosage is 1.2 to 1.5 times of the theoretical value. The reaction zone is equipped with a vertical mixer to stir the materials at a uniform speed. The reaction time of this process is 30 minutes. 2- and PO4 3- content, adjust the amount of calcium hydroxide added to ensure SO4 2- Content ≤1000mg / L, PO43- The content is ≤8mg / L, so as not to affect the biochemical reaction component 600 at the back end;

[0076] 12. The wastewater from the first phosphorus removal coagulation reaction zone 511 flows into the second phosphorus removal coagulation reaction zone 512 by gravity. A 5-10% sodium carbonate solution is added to the second phosphorus removal coagulation reaction zone 512 to remove Ca in the wastewater. 2+ The dosage is 1.2 to 1.5 times the theoretical value. The reaction zone is equipped with a vertical mixer to stir the materials at a uniform speed. The reaction time of this process is 30 minutes.

[0077] 13. The wastewater from the second phosphorus removal coagulation reaction zone 512 flows into the third phosphorus removal coagulation reaction zone 513 by gravity. 5-10% polyaluminium chloride is added to the third phosphorus removal coagulation reaction zone 513 for coagulation assistance. The reaction zone is equipped with a vertical mixer to stir the materials at a uniform speed. The reaction time of this process is 10-20 minutes.

[0078] 14. The wastewater from the third phosphorus removal coagulation reaction zone 513 flows by gravity into the fourth phosphorus removal coagulation reaction zone 514. 0.5-1% anionic polyacrylamide is added to the fourth phosphorus removal coagulation reaction zone 514 for flocculation precipitation. The reaction zone is equipped with a vertical mixer to stir the material at a uniform speed. The reaction time of this process is 10-20 minutes.

[0079] 15. Wastewater flows from the bottom of the fourth phosphorus removal coagulation reaction zone 514 into the phosphorus removal inclined tube sedimentation zone 515 by gravity. The sediment sinks along the inclined tube to the second sludge hopper 520 at the bottom. Under the action of the external pump, it is pumped from the mud outlet pipeline to the filter press for filtration. The filtrate is then returned to the first phosphorus removal coagulation reaction zone 511 for treatment. The sludge is transported to a qualified unit for disposal. The supernatant of the inclined tube sedimentation tank overflows to the phosphorus removal wastewater outlet zone 516.

[0080] 16. The wastewater from the phosphorus removal wastewater outlet area 516 is pumped into the neutralization reaction tank 630, and 5-10% sulfuric acid is added to adjust the pH to 6.5-8.5 to meet the biochemical water inlet conditions;

[0081] 17. The wastewater from the neutralization reaction tank 630 is pumped into the plate heat exchanger 640 for heat exchange, and the water temperature entering the anaerobic reaction zone 611 is maintained at 25-40°C. When the temperature is high in summer, the wastewater can enter the anaerobic reaction zone 611 directly along the bypass pipeline without passing through the plate heat exchanger 640;

[0082] 18. After heat exchange, the wastewater enters the anaerobic reaction zone 611. Two plug flow pumps are installed at the bottom of the anaerobic reaction zone 611 to mix the wastewater. The anaerobic reaction zone 611 is filled with fillers, which is conducive to the biofilm growth of microorganisms. A sealing cover is provided on the top of the anaerobic reaction zone 611 to keep the DO in the anaerobic reaction zone 611 ≤ 0.3 mg / L. At the same time, the anaerobic reaction zone 611 is provided with a tail gas collection system to absorb the methane, hydrogen sulfide and other gases released by decomposition. The reaction pH is controlled to be 6.5-8.5. The wastewater releases phosphorus under the action of phosphorus-releasing bacteria, and decomposes nitrogen-containing compounds into ammonia under the action of nitrifying bacteria such as fungi and actinomycetes. Organic matter is degraded and converted into simple compounds under the action of facultative bacteria and anaerobic bacteria, while releasing energy;

[0083] 19. The wastewater after anaerobic treatment flows by gravity into the anoxic reaction zone 612. Two plug flow pumps are installed at the bottom of the anoxic reaction zone 612 to mix the wastewater. The anoxic reaction zone 612 is filled with fillers, which is conducive to the biofilm growth of microorganisms. A sealing cover is installed on the top of the anoxic reaction zone 612 to keep the DO in the anoxic reaction zone 612 ≤ 0.5 mg / L. At the same time, a tail gas collection system is installed to absorb and treat the tail gas. The reaction pH is controlled to 6.5-8.5. Under the action of denitrifying bacteria, the wastewater converts NO2 - 、NO3 - etc. are reduced to nitrogen, thereby removing ammonia nitrogen;

[0084] 20. After denitrification treatment, the wastewater flows by gravity into the aerobic reaction zone 613. The aerobic reaction zone 613 is equipped with an aeration pipe, and the air source comes from the Roots blower. According to the organic load of the influent, the hydraulic load, etc., the reaction pH is controlled to be 6.5-8.0, the DO is 2-4 mg / L, and the sludge concentration MLSS is 3000-5000 mg / L. The wastewater absorbs and treats the phosphorus released by anaerobes under the action of polyphosphate bacteria, and is discharged from the system with the bottom mud. At the same time, under the action of microorganisms in the aerobic pool, the organic matter that has been decomposed into small molecules is further decomposed to remove COD;

[0085] 21. The wastewater after aerobic treatment flows by gravity into the secondary sedimentation tank 614. A third sludge hopper 650 is provided at the bottom of the secondary sedimentation tank 614, and a sludge outlet and a return pipeline are provided. The sludge is pumped from the sludge outlet to the screw press filter by an external pump, and the filtrate returns to the aerobic reaction zone 613. According to the effluent NH3-N and TP conditions, the wastewater flows back to the anaerobic reaction zone 611 and the anoxic reaction zone 612, and the reflux ratio is 0-200%. The biochemical effluent COD ≤ 100mg / L, NH3-N ≤ 5mg / L, TP ≤ 1mg / L;

[0086] 22. The supernatant first flows into the biochemical reaction effluent tank 620 for storage, and then is transported from the biochemical reaction effluent tank 620 to the external discharge tank. The pH value of the wastewater in the external discharge tank is adjusted to 6-9, and it is determined whether the effluent meets the third-level standard of the "Comprehensive Sewage Discharge Standard" GB8978-1996. If it meets the standard, it is discharged to the downstream sewage treatment plant. If it does not meet the standard, it is returned to the homogenization adjustment tank 110 for circulation treatment.

[0087] Compared with the prior art, the present invention has at least the following advantages:

[0088] 1. The wastewater from NMP slurry recovery from used lithium batteries treated by the homogenizing and regulating component is transported to the weight removal coagulation and sedimentation component for coagulation and sedimentation reaction, which can not only effectively remove heavy metals in the wastewater, but also remove most of the suspended matter in the wastewater. The wastewater treated by the weight removal coagulation and sedimentation component is transported to the sand filter component, and the suspended matter in the wastewater is further removed by the sand filter component, which can reduce the effluent turbidity in the wastewater.

[0089] 2. The wastewater treated by the sand filter assembly is transported to the electrocatalytic reaction dosing area, sodium sulfate is added to the electrocatalytic reaction area and fully mixed with the wastewater, and then flows into the electrocatalytic reaction electrolysis area for electrocatalytic reaction, that is, the hydroxyl radicals and active oxygen radicals generated by the electrolysis reaction are used to decompose macromolecular organic matter into small molecular inorganic matter, nitrogen-containing compounds are decomposed and converted into nitrogen, and organic phosphorus is converted into phosphate ions, which not only effectively improves the biodegradability of the wastewater, but also reduces the COD value of the wastewater, and simplifies the treatment process of catalytic oxidation of wastewater. Further, the wastewater treated by the electrocatalytic reactor is transported to the phosphorus removal coagulation and precipitation assembly, and the sulfate ions and phosphate ions in the wastewater are removed by the phosphorus removal coagulation and precipitation assembly, so that the concentration of sulfate ions and phosphate ions in the wastewater can be effectively reduced, thereby effectively reducing the TP value of the wastewater. At the same time, the wastewater treated by the electrocatalytic reactor does not need to be refluxed, which ensures the continuous operation of the treatment device for recycling wastewater from NMP slurry of waste lithium batteries, thereby effectively improving the wastewater treatment efficiency of the treatment device for recycling wastewater from NMP slurry of waste lithium batteries.

[0090] 3. The wastewater treated by the phosphorus removal coagulation and sedimentation component is transported to the biochemical reaction component, and the wastewater is subjected to phosphorus removal and nitrogen removal operations through the biochemical reaction component, which can effectively reduce the TP value and ammonia nitrogen concentration of the wastewater, thereby effectively improving the wastewater treatment effect of the waste lithium battery NMP slurry recovery wastewater treatment device.

[0091] The above-mentioned embodiments only express several implementation methods of the present disclosure, and the descriptions thereof are relatively specific and detailed, but they cannot be understood as limiting the scope of the disclosed patent. 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 disclosure, and these all belong to the protection scope of the present disclosure. Therefore, the protection scope of the disclosed patent shall be subject to the attached claims.

Claims

1. A treatment device (10) for recycling waste water from NMP slurry of waste lithium batteries, characterized in that: include: Homogenizing and regulating component (100); A weight removal coagulation and sedimentation component (200), wherein the water inlet end of the weight removal coagulation and sedimentation component (200) is connected to the water outlet end of the homogenization and adjustment component (100); A sand filter assembly (300), wherein the water inlet end of the sand filter assembly (300) is connected to the water outlet end of the weight removal coagulation sedimentation assembly (200); An electrocatalytic component (400), the electrocatalytic component (400) comprising an electrocatalytic reactor (410), the electrocatalytic reactor (410) being provided with an electrocatalytic reaction dosing area (411) and an electrocatalytic reaction electrolysis area (412) which are connected to each other, and the water inlet end of the electrocatalytic reaction dosing area (411) being connected to the water outlet end of the sand filter component (300); A phosphorus removal coagulation and sedimentation component (500), wherein the water inlet end of the phosphorus removal coagulation and sedimentation component (500) is connected to the water outlet end of the electrocatalytic reaction electrolysis zone (412); A biochemical reaction component (600), wherein the water inlet end of the biochemical reaction component (600) is connected to the water outlet end of the phosphorus removal coagulation and sedimentation component (500).

2. The treatment device (10) for recycling waste water from NMP slurry of waste lithium batteries according to claim 1, characterized in that: The homogenization adjustment component (100) comprises a homogenization adjustment tank (110), the water outlet of the homogenization adjustment tank (110) is connected to the water inlet of the weight removal coagulation sedimentation component (200), and the water inlet of the homogenization adjustment tank (110) is connected to the water outlet of the NMP recovery wastewater discharge component.

3. The treatment device (10) for recycling waste water from NMP slurry of waste lithium batteries according to claim 2 is characterized in that: The weight removal coagulation and sedimentation component (200) comprises a weight removal coagulation and sedimentation reaction tank (210), wherein the weight removal coagulation and sedimentation reaction tank (210) is provided with a first weight removal coagulation reaction zone (211), a second weight removal coagulation reaction zone (212), a third weight removal coagulation reaction zone (213), a weight removal inclined tube sedimentation zone (214) and a weight removal wastewater outlet zone (215) which are sequentially connected along the water inlet direction, wherein the water inlet end of the first weight removal coagulation reaction zone (211) is connected to the water outlet end of the homogenization adjustment tank (110), and the water outlet end of the weight removal wastewater outlet zone (215) is connected to the water inlet end of the sand filter component (300).

4. The treatment device (10) for recycling waste water from NMP slurry of waste lithium batteries according to claim 3 is characterized in that: The sand filter assembly (300) includes at least one sand filter tank (310) and a sand filter water outlet tank (320), the first water inlet end of each of the sand filter tanks (310) is connected to the water outlet end of the de-weighting wastewater outlet area (215), the first water outlet end of each of the sand filter tanks (310) is connected to the water inlet end of the sand filter water outlet tank (320), the second water outlet end of each of the sand filter tanks (310) is connected to the water inlet end of the first de-weighting coagulation reaction area (211), and the water outlet end of the sand filter water outlet tank (320) is respectively connected to the second water inlet ends of multiple sand filter tanks (310) and the water inlet end of the electrocatalytic reaction dosing area (411).

5. The device (10) for treating waste water from NMP slurry recovery of waste lithium batteries according to claim 4, characterized in that: The electrocatalytic component (400) further includes a pH adjustment tank (420), the water inlet of the pH adjustment tank (420) being connected to the water outlet of the deheavy wastewater outlet area (215), and the water outlet of the pH adjustment tank (420) being connected to the water inlet of each of the plurality of sand filter tanks (310).

6. The device (10) for treating waste water from NMP slurry recovery of waste lithium batteries according to claim 5, characterized in that: The phosphorus removal coagulation and sedimentation component (500) comprises a phosphorus removal coagulation and sedimentation reaction tank (510), wherein the phosphorus removal coagulation and sedimentation reaction tank (510) is provided with a first phosphorus removal coagulation reaction zone (511), a second phosphorus removal coagulation reaction zone (512), a third phosphorus removal coagulation reaction zone (513), a fourth phosphorus removal coagulation reaction zone (514), a phosphorus removal inclined tube sedimentation zone (515) and a phosphorus removal wastewater outlet zone (516) which are sequentially connected along the water inlet direction, wherein the water inlet end of the first phosphorus removal coagulation reaction zone (511) is connected to the water outlet end of the electrocatalytic reaction electrolysis zone (412), and the water outlet end of the phosphorus removal wastewater outlet zone (516) is connected to the water inlet end of the biochemical reaction component (600).

7. The device (10) for treating waste water from NMP slurry recovery of waste lithium batteries according to claim 6, characterized in that: The biochemical reaction assembly (600) comprises a biochemical reactor (610) and a biochemical reaction effluent tank (620). The biochemical reactor (610) is provided with an anaerobic reaction zone (611), an anoxic reaction zone (612), an aerobic reaction zone (613) and a secondary sedimentation tank (614) which are sequentially connected along the water inlet direction. The water inlet end of the anaerobic reaction zone (611) is connected to the water outlet end of the phosphorus removal wastewater effluent zone (516), and the water outlet end of the secondary sedimentation tank (614) is respectively connected to the water inlet end of the anaerobic reaction zone (611), the water inlet end of the anoxic reaction zone (612) and the water inlet end of the biochemical reaction effluent tank (620).

8. The device (10) for treating waste water from NMP slurry recovery of waste lithium batteries according to claim 7, characterized in that: The biochemical reaction assembly (600) further comprises a neutralization reaction tank (630) and a plate heat exchanger (640); the water inlet of the neutralization reaction tank (630) is connected to the water outlet of the dephosphorization wastewater outlet area (516); the water outlet of the neutralization reaction tank (630) is respectively connected to the water inlet of the plate heat exchanger (640) and the water inlet of the anaerobic reaction area (611); the water outlet of the plate heat exchanger (640) is connected to the water inlet of the anaerobic reaction area (611).

9. The device (10) for treating waste water from NMP slurry recovery of waste lithium batteries according to claim 7, characterized in that: The treatment device (10) further comprises a wastewater discharge tank (700), wherein a water inlet end of the wastewater discharge tank (700) is in communication with a water outlet end of the biochemical reaction water outlet tank (620).

10. The device (10) for treating waste water from NMP slurry recovery of waste lithium batteries according to claim 7, characterized in that: A first sludge hopper (220) is provided at the bottom of the degravity inclined tube sedimentation zone (214); A second sludge hopper (520) is provided at the bottom of the phosphorus removal inclined tube sedimentation zone (515); A third sludge hopper (650) is provided at the bottom of the secondary sedimentation tank (614).

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