Cooperative treatment device system for lithium battery material production wastewater

Abstract

The utility model provides a co-treatment device system for lithium battery material production wastewater. The co-treatment device system comprises a neutralization reaction tank, a weight removal reaction tank, a coagulative precipitation tank, a precipitation reaction tank, a steam stripping deamination tower and an evaporative crystallization device which are connected in sequence, the neutralization reaction tank is respectively connected with a ternary precursor production wastewater conveying pipeline and an ammonium-process iron phosphate precursor production wastewater conveying pipeline. The cooperative treatment device system disclosed by the utility model realizes efficient removal of heavy metal ions in ternary precursor production wastewater and ammonium-process iron phosphate precursor production wastewater and resource recovery of moisture, salt, nitrogen and phosphorus, and is suitable for large-scale popularization and application.

Description

Technical Field

[0001] The utility model relates to the technical field of wastewater treatment devices, and in particular to a coordinated treatment device system for wastewater produced by lithium battery materials. Background Art

[0002] The rapid development of new energy vehicles has brought unprecedented opportunities to the development of the lithium battery industry. The lithium battery industry chain has begun to evolve from the era of quantity to the era of quality. Among them, wastewater treatment in the lithium battery industry chain is an important link that cannot be ignored, and it will also become one of the key bottlenecks for the industry to continue to develop rapidly and healthily. At present, ternary lithium batteries and lithium iron phosphate batteries are the two main development and application directions of power lithium batteries. Among them, the positive electrode material is an important component of the lithium battery, and the precursor is a key component of the positive electrode material.

[0003] The production method of conventional ternary lithium battery positive electrode materials is to produce them by high-temperature solid-phase sintering of ternary precursors and lithium sources, and the production method of conventional lithium iron phosphate battery positive electrode materials is to evenly mix iron phosphate precursors with lithium sources and carbon sources and perform high-temperature solid-phase sintering. The production process of ternary precursors and iron phosphate precursors will generate a large amount of process wastewater.

[0004] CN115814475A discloses a treatment system for wastewater produced by positive electrode materials of lithium batteries, including a bottom plate, a first sedimentation tank, a second sedimentation tank and a third sedimentation tank are arranged on one side of the top of the bottom plate in sequence, the first sedimentation tank, the second sedimentation tank and the third sedimentation tank are all detachably connected with a baffle cover, a baffle ring is arranged at the bottom of the baffle cover, a water inlet pipe is connected to one side of the first sedimentation tank, a first connecting pipe is connected between the first sedimentation tank and the second sedimentation tank, and a second connecting pipe is connected between the second sedimentation tank and the third sedimentation tank. Through three sedimentations, the sedimentation effect is better, and continuous sedimentation can be used to save time. By providing a baffle ring and a baffle cover, the outflow of flocculants can be reduced and the sedimentation effect can be improved. By providing a sludge pool, the sediment mixture precipitated at the bottom is collected and filtered through a filter bucket, and the filtered filtrate is precipitated again, and the wastewater in the sediment is recycled.

[0005] CN110282786A discloses a wastewater resource treatment device and method for recycling waste lithium battery positive electrode materials. In view of the characteristics that the high-salt wastewater containing heavy metals generated by the recycling of waste lithium battery positive electrode materials mainly contains sodium sulfate, firstly, liquid alkali, flocculant and powdered carbon are added, and calcium, magnesium and heavy metal impurities are filtered out by tubular microfiltration; secondly, sodium sulfate is concentrated by ultra-high pressure reverse osmosis to produce water for reuse; then, bipolar membrane electrodialysis is used to decompose sodium sulfate into dilute sulfuric acid and dilute liquid alkali, and finally, the dilute sulfuric acid and dilute liquid alkali are evaporated and concentrated respectively, and reused for production.

[0006] CN220165992U discloses a treatment system for lithium battery positive electrode material production wastewater, which includes a precipitation coagulation device, a filtering device, a catalytic oxidation device and a biochemical treatment device. The precipitation coagulation device, the filtering device and the catalytic oxidation device reduce the content of heavy metals, fluorine, organic phosphorus and other biochemically toxic substances in the wastewater, and increase the biodegradability of the wastewater; the wastewater pollutants are further removed by a high-efficiency biochemical treatment device. The system has strong targeted treatment targets, reasonable process design, stable and efficient treatment effects, and good process scalability. The system solves the problems of unstable sewage treatment effects, high operating costs, and inability to effectively remove pollutants such as fluoride ions and organic phosphorus in wastewater in the prior art.

[0007] However, the above wastewater treatment methods still have problems such as high treatment cost and low removal rate of various pollutants in the wastewater. Utility Model Content

[0008] In view of the problems existing in the prior art, the utility model provides a coordinated treatment device system for lithium battery material production wastewater, which mixes the ternary precursor production wastewater and the ammonium ferric phosphate precursor production wastewater in a neutralization reaction tank for neutralization and homogenization, and then enters a weight removal reaction tank, a coagulation sedimentation tank, a precipitation reaction tank, a steam stripping deammonification tower and an evaporation crystallization device in sequence, so as to achieve efficient removal of heavy metal ions in the wastewater and resource recovery of water, salt, nitrogen and phosphorus; the coordinated treatment device system is reasonably designed and has a prospect for large-scale promotion and application.

[0009] To achieve this purpose, the utility model adopts the following technical solutions:

[0010] The utility model provides a coordinated treatment device system for lithium battery material production wastewater, the coordinated treatment device system comprises a neutralization reaction tank, a weight removal reaction tank, a coagulation sedimentation tank, a precipitation reaction tank, a steam stripping deammoniation tower and an evaporation crystallization device which are connected in sequence; the neutralization reaction tank is respectively connected to a ternary precursor production wastewater conveying pipeline and an ammonium process iron phosphate precursor production wastewater conveying pipeline.

[0011] The synergistic treatment device system of lithium battery material production wastewater described in the utility model mixes the ternary precursor production wastewater and the ammonium iron phosphate precursor production wastewater in the neutralization reaction tank, and then enters the weight removal reaction tank to remove heavy metals, the coagulation sedimentation tank to remove impurities, the precipitation reaction tank to remove phosphorus, and the stripping deamination tower to perform stripping separation and deamination. The wastewater after the reaction is treated by an evaporation crystallization device to obtain sodium sulfate salt, thereby achieving the removal of heavy metal ions in the wastewater and the resource recovery of water, salt, nitrogen and phosphorus. The utility model first enters the weight removal reaction tank to remove heavy metals after neutralization and homogenization, then enters the coagulation sedimentation tank to remove impurities, and then enters the precipitation reaction tank to remove phosphorus and the stripping deamination tower to perform stripping separation and deamination. Such a treatment setting has the advantages of less dosage of reagents, low treatment cost, good impurity removal and resource recovery effect. When the order of the precipitation reaction tank and the coagulation sedimentation tank is changed, the amount of pH regulator will increase, the removal effect of heavy metal ions will be poor, and struvite will be difficult to recycle and utilize.

[0012] In the neutralization reaction tank of the utility model, the pH of the mixed wastewater is adjusted to 9-9.5. Within this pH range, sulfide precipitation of heavy metal ions, coagulation precipitation to remove heavy metals and impurities, and magnesium ammonium phosphate precipitation to remove phosphorus can all achieve good treatment effects, and the cost of adding reagents is the lowest. In the precipitation reaction tank, the pH of the wastewater is adjusted to 9-10, and the magnesium ammonium phosphate precipitation reaction is carried out to achieve wastewater dephosphorization; before the wastewater enters the stripping deammonification tower, the pH is adjusted to 10-12. Within this pH range, ammonium ions in the wastewater can be converted into free ammonia as much as possible, which is conducive to the subsequent efficient removal of ammonia nitrogen stripping separation.

[0013] Sulfide is added to the heavy metal removal reaction pool of the utility model to perform precipitation reaction to remove heavy metals. Compared with the hydroxide precipitation method, it has a better precipitation and removal effect on heavy metal ions. Because in the alkaline high-ammonia nitrogen wastewater system, heavy metal ions such as nickel, cobalt, and manganese are mostly present in the form of complexes, and hydroxide is used as a precipitant, and the precipitation effect of heavy metals is poor. The sulfide precipitation reaction of heavy metal ions is thorough and efficient, and the generated precipitate has a small particle size and is in a colloidal state. It can be synergistically removed efficiently together with other suspended matter, colloids and other impurities in the wastewater in the subsequent coagulation and precipitation reaction. After treatment by the sulfide precipitation method, the residual content of heavy metal ions in the wastewater has been reduced to below the emission limit requirements, less than 1 mg / L; the content of suspended matter in the impurity-removing wastewater is less than 10 mg / L.

[0014] In the utility model, a coagulant, polyferric sulfate, and a flocculant, polyacrylamide, are added into a coagulation sedimentation tank.

[0015] Preferably, a sludge discharge pipeline is provided at the bottom of the coagulation sedimentation tank, and the sludge generated by the coagulation sedimentation reaction is collected in a sludge thickening tank, and after being thickened and dehydrated by a plate and frame filter press, waste residue is formed for external disposal.

[0016] In the utility model, a magnesium source, magnesium chloride and / or magnesium hydroxide are added into a precipitation reaction tank to carry out a magnesium ammonium phosphate precipitation reaction, and phosphate radicals, ammonium radicals and magnesium sources in wastewater react to generate white precipitates, which are dehydrated by a plate and frame filter press to form struvite.

[0017] Preferably, a struvite discharge pipe is provided at the bottom of the precipitation reaction tank, and the discharged struvite can be used as fertilizer to achieve the purpose of resource utilization.

[0018] Preferably, the stripping and deamination tower comprises a packed tower.

[0019] The utility model preferably comprises a packed tower, which can increase the contact mass transfer and heat transfer reaction rate and degree between water vapor and wastewater, and improve the deamination effect and efficiency, and the ammonia nitrogen content of the wastewater after deamination is less than 10 mg / L.

[0020] Preferably, a gaseous ammonia outlet is provided at the top of the stripping and deammonification tower, and the treatment method of the gaseous ammonia includes preparing ammonia water or preparing ammonium sulfate salt.

[0021] Preferably, a feed wastewater distributor is provided on the upper portion of the stripping deamination tower.

[0022] Preferably, an alkali liquid distributor is provided in the middle of the stripping and deamination tower.

[0023] Preferably, the alkali liquid distributor is arranged at 1 / 3 to 2 / 3 from the top, for example, it can be 1 / 3, 7 / 20, 2 / 5, 1 / 2 or 2 / 3, etc., but is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable.

[0024] Preferably, a steam inlet is provided on the side of the stripping and deamination tower.

[0025] Preferably, a wastewater outlet is provided at the bottom of the stripping and deammonification tower.

[0026] Preferably, an alkali solution regulating spraying device is also provided inside the stripping deamination tower.

[0027] Preferably, the evaporation crystallization device comprises an evaporator and a crystallizer connected in sequence.

[0028] The secondary steam generated in the evaporation crystallization device of the utility model is reused as product water after condensation and heat recovery, and the total recovery rate of waste water reaches more than 95%.

[0029] Preferably, the evaporator comprises a multiple-effect evaporator or an MVR evaporator to reduce the consumption of process steam, electricity and other energy; the crystallizer adopts a forced circulation type, with high evaporation intensity, strong anti-scaling ability and high online rate.

[0030] Preferably, a sodium sulfate discharge pipeline is provided at the bottom of the evaporation crystallization device, and the sodium sulfate can be exported as a printing and dyeing auxiliary agent, etc., to achieve the purpose of resource utilization.

[0031] Preferably, the coordinated treatment device system for lithium battery material production wastewater also includes a mother liquor drying device.

[0032] Preferably, the mother liquor drying device is connected to a drying heat source delivery pipeline.

[0033] Preferably, the mother liquor drying device is connected to the evaporation crystallization device and the impurity salt discharge pipeline respectively.

[0034] Exemplarily, the operation process of the coordinated treatment device system for lithium battery material production wastewater provided by the utility model is as follows:

[0035] (1) Mixing the wastewater produced by the ternary precursor and the wastewater produced by the ammonium ferric phosphate precursor, performing a neutralization reaction, and adjusting the pH of the mixed wastewater to 9 to 9.5;

[0036] The salt content of the ternary precursor production wastewater is 8-10%; the pH of the ternary precursor production wastewater is 10-13; the ammonia nitrogen content of the ternary precursor production wastewater is 5000-8000 mg / L; the heavy metal ion Mn 2+ The content is 5-10 mg / L, Ni 2+ The content is 50~150mg / L, Co 2+ The content is 5-15 mg / L;

[0037] The salt content of the wastewater produced by the ammonium ferric phosphate precursor production is 5-8%; the pH of the wastewater produced by the ammonium ferric phosphate precursor production is 1-2; the ammonia nitrogen content of the wastewater produced by the ammonium ferric phosphate precursor production is 4000-6000 mg / L; the phosphate content of the wastewater produced by the ammonium ferric phosphate precursor production is 15000-20000 mg / L;

[0038] (2) adding sulfide to the mixed wastewater to perform precipitation reaction to obtain heavy metal-removed wastewater; the sulfide includes sodium sulfide and / or hydrogen sulfide;

[0039] (3) The heavy metal removal wastewater is subjected to a coagulation and precipitation reaction to obtain impurity-removed wastewater; a coagulant and a flocculant are added during the coagulation and precipitation reaction; the coagulant includes polyferric sulfate, and the dosage is 20 to 100 mg / L; the flocculant includes polyacrylamide, and the dosage is 1 to 10 mg / L;

[0040] (4) The impurity removal wastewater is subjected to a magnesium ammonium phosphate precipitation reaction to obtain dephosphorization wastewater; a magnesium source is added to the magnesium ammonium phosphate precipitation reaction; the magnesium source includes magnesium chloride and / or magnesium hydroxide; the amount of the magnesium source added is controlled so that the molar ratio of Mg:P in the impurity removal wastewater is (1.05-1.1):(0.8-1); the pH of the magnesium ammonium phosphate precipitation reaction is 9-10;

[0041] (5) After the dephosphorization wastewater is adjusted to a pH of 10 to 12, a steam stripping separation reaction is performed to obtain deammoniation wastewater;

[0042] The method for treating ammonia vapor in the stripping separation reaction includes preparing ammonia water or preparing ammonium sulfate salt; the method for preparing ammonia water includes condensing ammonia vapor to obtain ammonia water with a concentration of 15-25%, which is used as a raw material in the ternary precursor co-precipitation production process; the method for preparing ammonium sulfate salt includes absorbing ammonia vapor with sulfuric acid to obtain an ammonium sulfate solution with a concentration of 25-30%, and then sequentially performing second evaporation crystallization and centrifugal drying to obtain ammonium sulfate salt, which is exported as fertilizer;

[0043] (6) The deammoniation wastewater is subjected to a first evaporation crystallization to obtain sodium sulfate salt; the secondary steam generated in the first evaporation crystallization process is reused as product water after condensation and heat recovery.

[0044] Compared with the prior art, the utility model has at least the following beneficial effects:

[0045] The utility model provides a coordinated treatment device system for lithium battery material production wastewater, in which the arrangement order of various reaction pools is reasonable, the operation is simple, the treatment cost is low, the removal efficiency of various pollutants in the wastewater is high, and the sodium sulfate salt is effectively recovered, with a recovery rate of more than 90% and high purity, reaching Class I first-class products, which can be recycled and reused in printing and dyeing, daily chemicals and other industries; the nitrogen element is effectively recovered in the form of ammonia water, which can be recycled and reused in the ternary precursor production process or to obtain ammonium sulfate salt, which can be exported as fertilizer; the phosphorus element is effectively recovered in the form of struvite, which can be exported as a slow-release fertilizer. BRIEF DESCRIPTION OF THE DRAWINGS

[0046] Figure 1 It is a schematic diagram of a coordinated treatment device system for lithium battery material production wastewater in Example 1 of the utility model.

[0047] Figure 2 It is a structural schematic diagram of the stripping and deammoniation tower in the coordinated treatment device system of lithium battery material production wastewater in Example 1 of the utility model.

[0048] In the figure: 1-neutralization reaction tank; 2-weight removal reaction tank; 3-coagulation sedimentation tank; 4-precipitation reaction tank; 5-stripping deammonification tower; 6-evaporation crystallization device; 7-ternary precursor production wastewater transportation pipeline; 8-ammonium process iron phosphate precursor production wastewater transportation pipeline; 9-sludge discharge pipeline; 10-struvite discharge pipeline; 11-gas ammonia outlet; 12-feed wastewater distributor; 13-alkali liquid distributor; 14-steam inlet; 15-wastewater outlet; 16-sodium sulfate discharge pipeline; 17-mother liquor drying device; 18-drying heat source transportation pipeline; 19-miscellaneous salt discharge pipeline; 20-packing layer. DETAILED DESCRIPTION

[0049] The technical solution of the utility model is further explained below with reference to the accompanying drawings and through specific implementation methods.

[0050] The utility model is further described in detail below. However, the following examples are only simple examples of the utility model and do not represent or limit the scope of protection of the utility model. The scope of protection of the utility model shall be subject to the claims.

[0051] It should be understood that, in the description of the present utility model, the terms "center", "longitudinal", "lateral", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inside", "outside" and the like indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings, which is only for the convenience of describing the present utility model and simplifying the description, and does not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be understood as a limitation on the present utility model. In addition, the terms "first", "second", etc. are only used for descriptive purposes, and cannot be understood as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Therefore, the features defined as "first", "second", etc. may explicitly or implicitly include one or more of the features. In the description of the present utility model, unless otherwise specified, "multiple" means two or more.

[0052] It should be noted that in the description of the present invention, unless otherwise clearly specified and limited, the terms "disposed", "connected", and "connected" should be understood in a broad sense, for example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection, or it can be indirectly connected through an intermediate medium, or it can be the internal communication of two components. For ordinary technicians in this field, the specific meanings of the above terms in the present invention can be understood by specific circumstances.

[0053] Those skilled in the art should understand that the utility model must include necessary pipelines, conventional valves and general pump equipment for realizing a complete process, but the above content does not belong to the main utility model points of the utility model. Those skilled in the art can add layouts on their own based on the process flow and equipment structure selection, and the utility model does not make special requirements and specific limitations on this.

[0054] Example 1

[0055] This embodiment provides a coordinated treatment device system for lithium battery material production wastewater, and its schematic diagram is as follows: Figure 1 shown.

[0056] The collaborative treatment device system comprises a neutralization reaction tank 1, a weight removal reaction tank 2, a coagulation sedimentation tank 3, a sedimentation reaction tank 4, a stripping deammonification tower 5 and an evaporation crystallization device 6 which are connected in sequence.

[0057] The neutralization reaction tank 1 is connected to the ternary precursor production wastewater delivery pipeline 7 and the ammonium ferric phosphate precursor production wastewater delivery pipeline 8 respectively;

[0058] A sludge discharge pipeline 9 is provided at the bottom of the coagulation sedimentation tank 3 .

[0059] A struvite discharge pipe 10 is provided at the bottom of the precipitation reaction tank 4 .

[0060] The stripping deamination tower 5 comprises a packed tower, in which a packing layer 20 is provided. The structural schematic diagram of the stripping deamination tower 5 is as follows: Figure 2 shown.

[0061] The top of the stripping and deamination tower 5 is provided with a gaseous ammonia outlet 11;

[0062] A feed wastewater distributor 12 is provided at the upper portion of the stripping deamination tower 5;

[0063] An alkali liquid distributor 13 is provided in the middle of the stripping deamination tower 5;

[0064] The alkali liquid distributor 13 is arranged at 1 / 3 of the distance from the top;

[0065] The side of the stripping and deamination tower 5 is provided with a steam inlet 14;

[0066] A wastewater outlet 15 is provided at the bottom of the stripping and deammonification tower 5 .

[0067] The stripping and deamination tower 5 is also provided with an alkali solution regulating spraying device.

[0068] The evaporation crystallization device 6 includes an evaporator and a crystallizer connected in sequence.

[0069] The evaporator is an MVR evaporator.

[0070] A sodium sulfate discharge pipeline 16 is provided at the bottom of the evaporation crystallization device 6.

[0071] The coordinated treatment device system for lithium battery material production wastewater also includes a mother liquor drying device 17;

[0072] The mother liquid drying device 17 is connected to the drying heat source delivery pipeline 18;

[0073] The mother liquor drying device 17 is connected to the evaporation crystallization device 6 and the impurity salt discharge pipeline 19 respectively.

[0074] The coordinated treatment device system for lithium battery material production wastewater described in this embodiment performs the following treatment steps:

[0075] (1) Mixing the wastewater produced by the ternary precursor and the wastewater produced by the ammonium ferric phosphate precursor, performing a neutralization reaction, and adjusting the pH of the mixed wastewater to 9.2;

[0076] The salt content of the ternary precursor production wastewater is 9%; the pH of the ternary precursor production wastewater is 11; the ammonia nitrogen content of the ternary precursor production wastewater is 6000 mg / L; the heavy metal ion Mn in the ternary precursor production wastewater 2+ The content is 8mg / L, Ni 2+ The content is 110mg / L, Co 2+ The content is 9mg / L;

[0077] The salt content of the wastewater produced by the ammonium ferric phosphate precursor production is 6%; the pH of the wastewater produced by the ammonium ferric phosphate precursor production is 1.2; the ammonia nitrogen content of the wastewater produced by the ammonium ferric phosphate precursor production is 5000 mg / L; the phosphate content of the wastewater produced by the ammonium ferric phosphate precursor production is 15600 mg / L;

[0078] (2) adding 200 mg / L sodium sulfide to the mixed wastewater to perform a precipitation reaction to obtain heavy metal-removing wastewater;

[0079] (3) The heavy metal removal wastewater is subjected to a coagulation and precipitation reaction to obtain impurity-removed wastewater; a coagulant and a flocculant are added during the coagulation and precipitation reaction; the coagulant is polyferric sulfate, and the dosage is 50 mg / L; the flocculant is polyacrylamide, and the dosage is 8 mg / L;

[0080] (4) the impurity removal wastewater is subjected to a magnesium ammonium phosphate precipitation reaction to obtain dephosphorization wastewater; magnesium chloride is added to the magnesium ammonium phosphate precipitation reaction; the dosage of magnesium chloride is controlled so that the molar ratio of Mg:P in the impurity removal wastewater is 1.08:0.86; the pH of the magnesium ammonium phosphate precipitation reaction is 9.3;

[0081] (5) After the dephosphorization wastewater is adjusted to pH 10.8, a stripping separation reaction is performed to obtain deammoniation wastewater; the stripping deammoniation tower is operated at normal pressure, with a tower top temperature of 95° C. and a tower bottom temperature of 105° C.;

[0082] The method for treating ammonia vapor in the stripping separation reaction is as follows: the ammonia vapor is condensed to obtain ammonia water with a concentration of 18%, which is used as a raw material in the ternary precursor co-precipitation production process;

[0083] (6) The deammoniation wastewater is subjected to a first evaporation crystallization at a temperature of 103° C. to obtain sodium sulfate salt; the secondary steam generated during the first evaporation crystallization process is reused as product water after condensation and heat recovery.

[0084] After the treatment in this embodiment, the removal rate of heavy metal ions in the wastewater is 97.8%, the removal rate of phosphate ions is 97.1%, and the removal rate of ammonia nitrogen is 99.8%.

[0085] Comparative Example 1

[0086] This comparative example provides a coordinated treatment device system for lithium battery material production wastewater. The coordinated treatment device system is the same as Example 1 except that the order of the coagulation sedimentation tank and the precipitation reaction tank is adjusted, that is, the neutralization reaction tank, the gravity removal reaction tank, the precipitation reaction tank, the coagulation sedimentation tank, the steam stripping deammonification tower and the evaporation crystallization device are connected in sequence.

[0087] The treatment steps and reaction conditions of the coordinated treatment device system for lithium battery material production wastewater described in this comparative example are the same as those of Example 1, except for adjusting the order of step (3) and step (4).

[0088] In this comparative example, since the wastewater after heavy metal removal is first precipitated and dephosphorized before coagulation and precipitation, the reaction of adding magnesium source and combining with phosphate ions in the wastewater to form magnesium ammonium phosphate struvite is limited under high suspended matter content, the dephosphorization efficiency is reduced, and the heavy metal precipitate and struvite precipitate are simultaneously settled in the coagulation sedimentation tank, which is difficult to separate, and the resource utilization of struvite cannot be realized. At the same time, the removal rate of suspended impurities in the coagulation sedimentation tank is also reduced.

[0089] To sum up, the arrangement order of various reaction pools in the coordinated treatment device system of lithium battery material production wastewater described in the utility model is reasonable, the operation is simple, the treatment cost is low, the removal efficiency of various pollutants in the wastewater is high, and the resource recovery of nitrogen and phosphorus elements and the effective recovery of sodium sulfate salt are realized.

[0090] The applicant declares that the utility model illustrates the detailed structural features of the utility model through the above-mentioned embodiments, but the utility model is not limited to the above-mentioned detailed structural features, that is, it does not mean that the utility model must rely on the above-mentioned detailed structural features to be implemented. Those skilled in the art should understand that any improvement to the utility model, equivalent replacement of the components selected by the utility model, addition of auxiliary components, selection of specific methods, etc., all fall within the protection scope and disclosure scope of the utility model.

[0091] The preferred embodiments of the present invention are described in detail above. However, the present invention is not limited to the specific details in the above embodiments. Within the technical concept of the present invention, the technical solution of the present invention can be subjected to a variety of simple modifications, and these simple modifications all belong to the protection scope of the present invention.

Claims

1. A coordinated treatment device system for lithium battery material production wastewater, characterized in that: The collaborative treatment device system includes a neutralization reaction tank, a weight removal reaction tank, a coagulation sedimentation tank, a sedimentation reaction tank, a steam stripping deammoniation tower and an evaporation crystallization device which are connected in sequence; the neutralization reaction tank is respectively connected to a ternary precursor production wastewater delivery pipeline and an ammonium ferric phosphate precursor production wastewater delivery pipeline.

2. The coordinated treatment device system for lithium battery material production wastewater according to claim 1 is characterized in that: A sludge discharge pipeline is arranged at the bottom of the coagulation sedimentation tank.

3. The coordinated treatment device system for lithium battery material production wastewater according to claim 1 is characterized in that: A struvite discharge pipeline is arranged at the bottom of the precipitation reaction tank.

4. The coordinated treatment device system for lithium battery material production wastewater according to claim 1 is characterized in that: The stripping and deamination tower comprises a packed tower.

5. The coordinated treatment device system for lithium battery material production wastewater according to claim 1 is characterized in that: A gaseous ammonia outlet is provided at the top of the stripping deamination tower; A feed wastewater distributor is provided on the upper part of the stripping deamination tower; An alkali liquid distributor is arranged in the middle of the stripping and deamination tower; The alkali liquid distributor is arranged at 1 / 3 to 2 / 3 of the distance from the top; A steam inlet is provided on the side of the stripping and deamination tower; A wastewater outlet is provided at the bottom of the stripping and deamination tower.

6. The coordinated treatment device system for lithium battery material production wastewater according to claim 1 is characterized in that: The stripping and deamination tower is also provided with an alkali solution regulating spraying device.

7. The coordinated treatment device system for lithium battery material production wastewater according to claim 1 is characterized in that: The evaporation crystallization device comprises an evaporator and a crystallizer which are connected in sequence.

8. The coordinated treatment device system for lithium battery material production wastewater according to claim 7 is characterized in that: The evaporator comprises a multiple effect evaporator or an MVR evaporator.

9. The coordinated treatment device system for lithium battery material production wastewater according to claim 1, characterized in that: A sodium sulfate discharge pipeline is arranged at the bottom of the evaporation crystallization device.

10. The coordinated treatment device system for lithium battery material production wastewater according to claim 1, characterized in that: The coordinated treatment device system for lithium battery material production wastewater also includes a mother liquor drying device; The mother liquor drying device is connected to a drying heat source delivery pipeline; The mother liquor drying device is connected to the evaporation crystallization device and the impurity salt discharge pipeline respectively.

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