CN220165992U - Treatment system for waste water in lithium battery anode material production - Google Patents
Treatment system for waste water in lithium battery anode material production Download PDFInfo
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- 239000002351 wastewater Substances 0.000 title claims abstract description 135
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 title claims abstract description 16
- 229910052744 lithium Inorganic materials 0.000 title claims abstract description 16
- 239000010405 anode material Substances 0.000 title claims abstract description 11
- 238000004519 manufacturing process Methods 0.000 title claims description 12
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 61
- 230000003197 catalytic effect Effects 0.000 claims abstract description 58
- 230000003647 oxidation Effects 0.000 claims abstract description 58
- 238000001914 filtration Methods 0.000 claims abstract description 24
- 238000005345 coagulation Methods 0.000 claims abstract description 22
- 230000015271 coagulation Effects 0.000 claims abstract description 22
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims abstract description 13
- 239000011574 phosphorus Substances 0.000 claims abstract description 13
- 229910052698 phosphorus Inorganic materials 0.000 claims abstract description 13
- 229910001385 heavy metal Inorganic materials 0.000 claims abstract description 12
- -1 fluoride ions Chemical class 0.000 claims abstract description 9
- 229910052731 fluorine Inorganic materials 0.000 claims abstract description 5
- 239000011737 fluorine Substances 0.000 claims abstract description 5
- 238000006243 chemical reaction Methods 0.000 claims description 110
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 64
- 239000004576 sand Substances 0.000 claims description 39
- 238000003860 storage Methods 0.000 claims description 37
- 238000004062 sedimentation Methods 0.000 claims description 32
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims description 24
- 238000005406 washing Methods 0.000 claims description 22
- 239000012528 membrane Substances 0.000 claims description 19
- 239000010802 sludge Substances 0.000 claims description 13
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 12
- 238000005273 aeration Methods 0.000 claims description 10
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 10
- 239000000945 filler Substances 0.000 claims description 8
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 claims description 7
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 7
- 229910001424 calcium ion Inorganic materials 0.000 claims description 7
- 239000003054 catalyst Substances 0.000 claims description 7
- 229910052914 metal silicate Inorganic materials 0.000 claims description 7
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 6
- 238000005189 flocculation Methods 0.000 claims description 5
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 claims description 5
- 230000001105 regulatory effect Effects 0.000 claims description 5
- 230000016615 flocculation Effects 0.000 claims description 4
- 239000002245 particle Substances 0.000 claims description 4
- 238000003756 stirring Methods 0.000 claims description 4
- 238000002156 mixing Methods 0.000 claims description 3
- 239000013049 sediment Substances 0.000 claims description 3
- 239000010406 cathode material Substances 0.000 claims description 2
- 238000010438 heat treatment Methods 0.000 claims description 2
- 230000001376 precipitating effect Effects 0.000 claims description 2
- 238000001556 precipitation Methods 0.000 abstract description 14
- 238000000034 method Methods 0.000 abstract description 9
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- 230000008685 targeting Effects 0.000 abstract description 2
- 239000003440 toxic substance Substances 0.000 abstract description 2
- PXGOKWXKJXAPGV-UHFFFAOYSA-N Fluorine Chemical compound FF PXGOKWXKJXAPGV-UHFFFAOYSA-N 0.000 abstract 1
- 229920002401 polyacrylamide Polymers 0.000 description 7
- 239000000243 solution Substances 0.000 description 7
- 239000000126 substance Substances 0.000 description 5
- 230000035484 reaction time Effects 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 238000001223 reverse osmosis Methods 0.000 description 3
- 238000009287 sand filtration Methods 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- KRHYYFGTRYWZRS-UHFFFAOYSA-M Fluoride anion Chemical compound [F-] KRHYYFGTRYWZRS-UHFFFAOYSA-M 0.000 description 2
- YCKRFDGAMUMZLT-UHFFFAOYSA-N Fluorine atom Chemical compound [F] YCKRFDGAMUMZLT-UHFFFAOYSA-N 0.000 description 2
- 239000000920 calcium hydroxide Substances 0.000 description 2
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
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- 150000003839 salts Chemical class 0.000 description 2
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- 241000894006 Bacteria Species 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
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Abstract
The utility model discloses a treatment system for wastewater produced by a lithium battery anode material, which comprises a precipitation coagulation device, a filtering device, a catalytic oxidation device and a biochemical treatment device, wherein the precipitation coagulation device, the filtering device and the catalytic oxidation device reduce the content of biochemical toxic substances such as heavy metals, fluorine, organic phosphorus and the like in the wastewater and increase the biodegradability of the wastewater; the subsequent utilization of the high-efficiency biochemical treatment device further removes the wastewater pollutants, the targeting of the system treatment is strong, the process design is reasonable, the treatment effect is stable and efficient, and the process expandability is good. The system solves the problems that the sewage treatment effect is unstable, the operation cost is high, and pollutants such as fluoride ions, organic phosphorus and the like in the wastewater can not be effectively removed in the prior art.
Description
Technical Field
The utility model relates to the technical field of wastewater treatment, in particular to a treatment system for wastewater in lithium battery anode material production.
Background
Along with the reproduction of lithium battery anode materials by utilizing waste lithium batteries to refine valuable metals by a plurality of enterprises, a large amount of high-pollution wastewater can be generated in the reproduction process, and the wastewater has the characteristics of high heavy metal content, high fluorine content, high total phosphorus content, high salt content, high organic matter content, difficult degradation and the like, and the wastewater is discharged after being treated up to the standard.
Patent document CN211595372U discloses a waste battery wastewater treatment system, which comprises an adjusting tank, an electric flocculation device, a primary sedimentation tank, a first intermediate tank, an ABR anaerobic tank, an anoxic tank, a three-stage aerobic tank, a second intermediate tank, a coagulation reaction tank, a secondary sedimentation tank and a discharge tank which are sequentially communicated along the wastewater conveying direction. Although the application can remove more COD, salt and a certain amount of heavy metal in water through the electric flocculation process, and has a certain practical feasibility, the system also has the problems of unstable effect, high operation cost and incapability of effectively removing pollutants such as fluoride ions, organic phosphorus and the like in wastewater, and the fluoride ions can influence the operation of a subsequent system.
Disclosure of Invention
The utility model provides a treatment system for waste water in lithium battery anode material production, and aims to solve the problems that in the background technology, the effect is unstable, the operation cost is high, and pollutants such as fluoride ions, organic phosphorus and the like in the waste water cannot be effectively removed.
The technical scheme provided by the utility model is as follows:
the system for treating the lithium battery anode material production wastewater is characterized by comprising the following components:
the sedimentation coagulation device, the filtering device, the catalytic oxidation device and the biochemical treatment device are sequentially arranged along the pipeline;
the sedimentation coagulation device comprises a reaction tank unit and a sedimentation tank;
the reaction tank unit comprises a plurality of reaction tanks which are connected in sequence and is used for removing fluorine ions, heavy metals and calcium ions in the wastewater to be treated and outputting wastewater in a first state to the sedimentation tank;
the sedimentation tank is communicated with the reaction tank unit and is used for physically precipitating the wastewater in the first state, removing sediment and outputting wastewater in the second state to the filtering device;
the filtering device is communicated with the sedimentation tank and is used for filtering the second-state wastewater, removing suspended matters and outputting third-state wastewater to the catalytic oxidation device;
the catalytic oxidation device is communicated with the filtering device and is used for carrying out catalytic oxidation on the wastewater in the third state, converting organic phosphorus into orthophosphate and outputting wastewater in the fourth state to the biochemical treatment device;
the biochemical treatment device is communicated with the catalytic oxidation device and is used for carrying out anaerobic reaction and aerobic reaction on the wastewater in the fourth state, removing orthophosphate and COD and outputting wastewater in the fifth state;
wherein the wastewater to be treated is wastewater from the production of lithium battery anode materials.
Further, the sedimentation coagulation device is also communicated with a homogenizing value adjusting device;
the homogenizing and regulating device is used for uniformly mixing the wastewater to be treated and regulating the pH value to 6-9.
Further, the reaction tank unit comprises a first reaction tank, a second reaction tank, a third reaction tank and a fourth reaction tank which are integrally arranged, wherein a stirrer is arranged in each of the first reaction tank, the second reaction tank, the third reaction tank and the fourth reaction tank;
the first reaction tank is used for removing fluoride ions and heavy metals in the wastewater to be treated;
the second reaction tank is used for removing calcium ions in the wastewater to be treated;
the third reaction tank is used for carrying out coagulation reaction on the wastewater to be treated;
the fourth reaction tank is used for carrying out flocculation reaction on the wastewater to be treated.
Further, the filtering device comprises at least one sand filtering tank and a sand filtering water storage tank communicated with the sand filtering tank, wherein the sand filtering tank is communicated with an air compressor, and air washing is carried out through the air compressor;
the sand filter tank filters the second-state wastewater to obtain the third-state wastewater, and conveys the third-state wastewater to the sand filter water storage tank, and the sand filter tank performs forward washing and reverse washing through the sand filter water storage tank;
the sand filter tank is communicated with the homogenizing value adjusting device, and forward washing water and backward washing water are conveyed to the homogenizing value adjusting device.
Further, the catalytic oxidation device comprises an ozone catalytic oxidation tower and a catalytic oxidation water storage tank which are communicated;
the ozone catalytic oxidation tower is internally filled with catalytic oxidation filler, the bottom of the ozone catalytic oxidation tower is provided with an aeration disc, and the aeration disc is communicated with an ozone generator;
when the device works, the ozone generator is used for introducing ozone into the ozone catalytic oxidation tower through the aeration disc, the third-state wastewater flows from top to bottom in the ozone catalytic oxidation tower, after a period of catalytic oxidation reaction, the fourth-state wastewater is obtained, and the fourth-state wastewater is conveyed to the catalytic oxidation water storage tank.
Further, the biochemical treatment device comprises an anaerobic reactor and an aerobic biochemical device which are communicated;
the anaerobic reactor comprises a water distributor, an anaerobic reaction zone, a three-phase separator and a methane collecting and utilizing component;
the anaerobic reaction zone comprises a high-concentration sludge reaction zone and a low-concentration sludge reaction zone;
the aerobic biochemical device comprises an aerobic tank, wherein an MBR membrane assembly is arranged at the tail end of the aerobic tank, and the MBR membrane assembly is communicated with an MBR water storage tank.
Further, a plate heat exchanger is arranged between the catalytic oxidation water storage tank and the anaerobic reactor and is used for heating the fourth-state wastewater, so that the temperature of the fourth-state wastewater entering the anaerobic reactor is maintained at 20-35 ℃.
Further, the homogenizing and adjusting device comprises a homogenizing and adjusting tank.
Further, the catalytic oxidation filler comprises a metal silicate catalyst, and the particle size of the metal silicate catalyst is 80-100 meshes.
Further, the first reaction tank is added with 5-10% of calcium hydroxide solution by mass percent;
sodium carbonate solution with mass percent of 5-10% is added into the second reaction tank;
PAC is added into the third reaction tank, and the adding amount of the PAC is 100-200 mg/L;
PAM is added into the fourth reaction tank, and the addition amount of the PAM is 2-5 mg/L.
Compared with the prior art, the utility model has the beneficial effects that:
the utility model provides a treatment system of lithium battery anode material production wastewater, which reduces the content of biochemical toxic substances such as heavy metal, fluorine, organic phosphorus and the like in the wastewater and increases the biodegradability of the wastewater through a precipitation coagulation device, a filtering device and a catalytic oxidation device; the subsequent utilization of the high-efficiency biochemical treatment device further removes the wastewater pollutants, the targeting of the system treatment is strong, the process design is reasonable, the treatment effect is stable and efficient, and the process expandability is good.
Drawings
Fig. 1 is a schematic structural diagram of a treatment system for wastewater from lithium battery cathode material production in an embodiment of the utility model.
The reference numerals are as follows:
1-homogenizing a value adjusting tank; the device comprises a 2-precipitation coagulation device, a 21-first reaction tank, a 22-second reaction tank, a 23-third reaction tank, a 24-fourth reaction tank, a 25-precipitation tank, a 26-discharge port, a 27-precipitation water storage tank and a 28-stirrer; 3-sand filter tank, 31-emptying pipe, 32-sand filter water storage tank; 4-catalytic oxidation tower, 41-catalytic oxidation filler; 5-catalytic oxidation water storage tank, 51-water storage return pipe; 6-plate heat exchanger; 7-anaerobic reactor, 71-water sealed tank, 72-methane pipeline; 8-an aerobic biochemical device, 81-an MBR online dosing and cleaning pipeline and 82-an MBR membrane component; 9-MBR water storage tank.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present utility model more clear, the technical solutions of the embodiments of the present utility model will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present utility model. It will be apparent that the embodiments described below are some, but not all, embodiments of the utility model. The components of the embodiments of the present utility model generally described and illustrated in the figures herein may be arranged and designed in a wide variety of different configurations.
Accordingly, the following detailed description of the embodiments of the utility model, taken in conjunction with the accompanying drawings, is intended to represent only selected embodiments of the utility model, and not to limit the scope of the utility model as claimed. All other embodiments, which can be made by one of ordinary skill in the art without undue burden on the person of ordinary skill in the art based on the embodiments of the present utility model, are within the scope of the present utility model.
It should be understood that in the description of the embodiments of the present utility model, the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", etc. indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings are merely for convenience in describing the embodiments of the present utility model and to simplify the description, and do not indicate or imply that the devices or elements referred to must have a specific orientation, be configured and operated in a specific orientation, and therefore should not be construed as limiting the embodiments of the present utility model. Furthermore, the terms "first," "second," "third," "fourth" and the like are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, features defining "first", "second", "third", "fourth" may include one or more of the described features, either explicitly or implicitly. In the description of the embodiments of the present utility model, the meaning of "plurality" is two or more, unless explicitly defined otherwise.
In describing embodiments of the present utility model, it should be noted that, unless explicitly stated and limited otherwise, the terms "disposed," "mounted," "connected," and "connected" should be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically connected, electrically connected or can be communicated with each other; can be directly connected or indirectly connected through an intermediate medium, and can be communicated with the inside of two elements or the interaction relationship of the two elements. The specific meaning of the above terms in the embodiments of the present utility model can be understood by those of ordinary skill in the art according to specific circumstances.
The utility model relates to a specific embodiment of a treatment system for wastewater in lithium battery anode material production. As shown in fig. 1, the device comprises a homogenizing and adjusting tank 1, a sedimentation and coagulation device 2, a sand filtration tank 3, a catalytic oxidation tower 4, a catalytic oxidation water storage tank 5, a plate heat exchanger 6, an anaerobic reactor 7 and an aerobic biochemical device 8 which are sequentially arranged and communicated along the pipeline water flow direction. The wastewater to be treated in the treatment system is specifically wastewater generated in the production process of the anode of the lithium battery. Wherein, precipitation coagulation device 2 includes a plurality of reaction tanks and sedimentation tank 25 that connect gradually, and the reaction tank includes first reaction tank 21, second reaction tank 22, third reaction tank 23 and fourth reaction tank 24 that the integration set up, and sedimentation tank 25 is connected with fourth reaction tank 24, all is provided with mixer 28 in the reaction tank, and the mixer 28 selects vertical mixer in this embodiment for use for stirring the waste water in the reaction tank. The sedimentation tank 25 is designed as a inclined tube sedimentation tank, the bottom is provided with a discharge port 26, sludge is discharged through the discharge port 26, the right side of the sedimentation tank 25 is provided with a sedimentation water storage tank 27, and the top of the sedimentation water storage tank 27 is also provided with a stirrer 28.
The first reaction tank 21 is charged with a calcium hydroxide solution for removing fluoride ions and heavy metals from the wastewater to be treated during use.
The second reaction tank 22 is charged with sodium carbonate solution for removing calcium ions in the wastewater to be treated during use.
The third reaction tank 23 is charged with PAC for coagulation reaction of the wastewater to be treated during use. Polyaluminium chloride (PAC) is an inorganic substance, an emerging water purification material, an inorganic high polymer coagulant, and polyaluminium for short.
The fourth reaction tank 24 is charged with PAM during use for flocculation reaction of the wastewater to be treated. Polyacrylamide (PAM) is a linear high molecular polymer, which is a hard glassy solid at ordinary temperature, and the products include glue, latex, white powder, translucent beads, flakes, and the like. The thermal stability is good. Can be dissolved in water in any proportion, and the aqueous solution is uniform and transparent liquid.
For ease of understanding, the wastewater flowing out of the fourth reaction tank 24 is defined as a first-state wastewater, the wastewater flowing out of the sedimentation tank 25 is defined as a second-state wastewater, the wastewater flowing out of the sand filtration tank 3 is defined as a third-state wastewater, the wastewater flowing out of the catalytic oxidation tower 4 is defined as a fourth-state wastewater, and the wastewater flowing out of the aerobic biochemical apparatus 8 is defined as a fifth-state wastewater.
At least one of the quantity of sand filter tanks 3, the right side of the sand filter tank 3 is communicated with a sand filter water storage tank 32, the sand filter tank 3 is communicated with an air compressor through an A pipeline, and air washing is carried out through the air compressor. The sand filter tank 3 filters the second-state wastewater to obtain third-state wastewater, and conveys the third-state wastewater to the sand filter water storage tank 32, and the sand filter tank 3 performs forward washing and reverse washing through the sand filter water storage tank 32; the sand filter tank 3 is communicated with the homogenizing valve tank 1, and forward washing water and backward washing water are conveyed to the homogenizing valve tank 1. In this embodiment, 2 sand filter tanks 3 are used, one for standby. An emptying pipe 31 is arranged at the bottom of the sand filter tank 3, and the waste water in the sand filter tank 3 is emptied by the emptying pipe 31 when the sand filter tank 3 is overhauled or stopped for a long time.
The catalytic oxidation tower 4 is filled with catalytic oxidation filler 41, an aeration disc is arranged at the bottom of the ozone catalytic oxidation tower 4 and is communicated with an ozone generator through a C pipeline, when catalytic oxidation is carried out, the ozone generator is used for introducing ozone into the catalytic oxidation tower 4 through the aeration disc, third-state wastewater flows from top to bottom in the ozone catalytic oxidation tower 4, after a period of catalytic oxidation reaction, fourth-state wastewater is obtained, and the fourth-state wastewater is conveyed to the catalytic oxidation water storage tank 5. The catalytic oxidation packing 41 is mainly a metal silicate catalyst, and the particle size of the metal silicate catalyst is about 80 to 100 mesh.
The anaerobic reactor 7 comprises a water distributor, an anaerobic reaction zone, a three-phase separator and a methane collecting and utilizing component. The anaerobic reaction zone comprises a high-concentration sludge reaction zone and a low-concentration sludge reaction zone. The anaerobic reactor 7 is an upflow anaerobic reactor. The methane collection and utilization assembly is in communication with the anaerobic reaction zone of the anaerobic reactor 7 via a water sealed tank 71.
The aerobic biochemical device 8 comprises an aerobic tank, an MBR online dosing and cleaning pipeline 81 and an MBR membrane module 82, wherein the MBR membrane module 82 is arranged at the tail end of the aerobic tank, and the MBR membrane module 82 is communicated with the MBR water outlet tank 9. The aerobic tank is used for aeration, and in the embodiment, compressed air is introduced into the aerobic tank and the MBR membrane module through a pipeline B.
The MBR water storage tank 9 is used for storing the fifth-state wastewater flowing out of the MBR membrane module 82. The MBR water storage tank 9 is provided with three pipelines D, E and F, wherein if the wastewater in the fifth state meets the discharge standard, the wastewater is directly discharged through the pipeline D, and if the wastewater does not meet the standard, the wastewater can be returned to the homogenizing adjustment tank 1 for further treatment through the pipeline E, and can enter a subsequent advanced treatment system, such as NF and RO membrane systems, for advanced treatment through the pipeline F.
The working principle of the system is as follows: firstly, the wastewater to be treated is introduced into a homogenizing adjusting tank 1 for uniform mixing, and the pH value is adjusted to 6-9.
The waste water to be treated with pH value of 6-9 is pumped into the first reaction tank 21 of the precipitation coagulation device 2 from the homogenizing adjustment tank 1 after being uniformly mixed by a pump, calcium hydroxide solution with mass fraction of 5-10% is added at the waste water feeding end of the first reaction tank 21, the adding amount of calcium hydroxide is 1.2-2 times of the theoretical defluorination amount, the pH value of the first reaction tank 21 is controlled to 8.5-10.5, the calcium hydroxide solution is uniformly stirred by a vertical stirrer, the reaction time is 30-60 min, and the adding amount of calcium hydroxide is adjusted by measuring the fluorine ion and heavy metal ion content of the waste water in the precipitation water outlet tank 27, so that the fluorine ion content is less than or equal to 20mg/L and the heavy metal content is less than or equal to 1mg/L in the waste water in the second state, thereby avoiding the influence on a biochemical system.
The wastewater to be treated automatically flows from the first reaction tank 21 to the second reaction tank 22, a sodium carbonate solution with the mass fraction of 5-10% is added into the second reaction tank 22, the adding amount is 1.2-2 times of the theoretical adding amount, the second reaction tank 22 is provided with a vertical stirrer, the sodium carbonate solution is stirred at a constant speed, the reaction time is 30-60 min, the adding amount of the sodium carbonate in the second reaction tank 22 is adjusted according to the calcium ion concentration of the wastewater in the second state in the precipitation water storage tank 27, and the calcium ion content in the wastewater in the second state is ensured to be less than or equal to 50mg/L.
The wastewater in the second state flows into a third reaction tank 23 and a fourth reaction tank 24 from the second reaction tank 22, PAC is added into the third reaction tank 23, the coagulation reaction time is 5-20 min, the adding amount is 100-200 mg/L, and a vertical stirrer equipped with the third reaction tank 23 is adopted for stirring; the wastewater after the generation treatment flows out of the coagulation reaction tank 23 and enters the fourth reaction tank 24, anionic PAM is added into the fourth reaction tank 24 for 5-20 min, the addition amount of the PAM is 2-5 mg/L, and a vertical stirrer equipped in the fourth reaction tank 24 is adopted for stirring. After the reaction is completed, the wastewater in the first state is obtained.
The wastewater in the first state automatically flows into a sedimentation tank 25 from the fourth reaction tank 24, and physical sedimentation is carried out on sediment generated by chemical reaction and coagulation of the wastewater through the inclined tube sedimentation tank, so that effluent suspended solids are reduced. The second state wastewater is treated by the sedimentation tank 25 and flows into the sedimentation water storage tank 27.
The pH of the precipitation tank 27 is adjusted to 6 to 8 by adding an acid.
The second-state wastewater in the precipitation water storage tank 27 enters the sand filter tank 3 by a pump to carry out deep filtration, suspended matters in the wastewater are further reduced, the sand filter tank 3 comprises a forward washing system, a reverse washing system and an air washing system, the forward washing system and the reverse washing system are provided by the sand filter water storage tank 32, compressed air is provided by an air compressor, forward washing system and the reverse washing system in the sand filter process flow into the homogenizing and regulating tank 1, the suspended matter content in the third-state wastewater after sand filtration is not higher than 20mg/L, and the wastewater in the sand filter tank 3 is emptied by the emptying pipe 31 when the sand filter tank 3 is overhauled or is stopped for a long time.
The third-state wastewater is treated by a catalytic oxidation tower 4, the third-state wastewater flows from top to bottom, catalytic oxidation filler 41 is filled in the catalytic oxidation tower 4, the main component of the catalytic oxidation filler is a metal silicate catalyst, the particle size is about 80-100 meshes, ozone is prepared by an ozone generator as required, ozone enters the tower body from a bottom aeration disc, the reaction time of the wastewater in the catalytic oxidation tower 4 is 60-12 min, the catalytic oxidation tower 4 is provided with a tail gas destruction device, and the fourth-state wastewater treated by the catalytic oxidation tower 4 enters a catalytic oxidation water storage tank 5 for storage.
The fourth-state wastewater subsequently enters a plate heat exchanger 6 for heat exchange, the plate heat exchanger 6 comprises an overrun pipeline, and when the temperature of the fourth-state wastewater reaches the requirement, the fourth-state wastewater can enter an anaerobic reactor 7 from the overrun pipeline, so that the temperature of the wastewater entering the upflow anaerobic reactor is maintained at 20-35 ℃, and the requirement of the water inlet temperature of a biochemical anaerobic system is met; the unqualified wastewater is returned to the precipitation coagulation device 2 through the water storage return pipe 51, on one hand, orthophosphate converted by the catalytic oxidation of organic phosphorus is removed by using the coagulation precipitation reaction, the total phosphorus content of the system is reduced, and on the other hand, the unqualified wastewater is returned to the front-end process reprocessing pipeline.
The wastewater in the fourth state enters an up-flow anaerobic reactor from the bottom for treatment, wherein the up-flow anaerobic reactor comprises a water distributor, an anaerobic reaction zone, a three-phase separator, a methane collection and matched purification and utilization system and the like, the anaerobic reaction zone is divided into a high-concentration sludge reaction zone and a low-concentration sludge reaction zone, the design volume load of the anaerobic reactor is 5-8 kg COD/m < 3 >. D, and the effective water depth is 5-8 m; the rising flow rate is less than 0.8m/h; the surface load of the sedimentation area is not more than 0.8m3/(m2.h); the load of the water outlet weir is not more than 1.7L/(s.m), namely 6.12m 3/(h.m), the COD removal rate in the water outlet of the anaerobic reactor is about 80%, and phosphorus in the wastewater is released in an anaerobic state through phosphorus releasing bacteria so as to be removed by phosphorus accumulation in an aerobic tank.
The wastewater after the anaerobic reaction automatically flows into an aerobic biochemical device 8, and the aerobic biochemical device 8 mainly comprises an aerobic tank, an MBR membrane component 82, an MBR online dosing and cleaning pipeline 81 (a membrane cleaning agent is online dosing, and nutrient solution and alkalinity can be manually added according to the need) and the like; an activated sludge method is adopted, a plate type MBR component 82 is arranged in the activated sludge method, a biochemical effluent sedimentation tank is not arranged, the aerobic biochemical treatment effect is enhanced, and the effluent quality is improved; the sludge concentration of the aerobic tank can be correspondingly adjusted according to the organic load of the inflow water, and the MLSS (mixed solution suspended solid concentration) in the tank is controlled to be in the range of 3000-20000 mg/L by controlling the conditions of the organic load of the inflow water, the growth environment, the periodic sludge discharge and the like of the aerobic tank; the main parameters in the pool are controlled as follows: the pH is 6-9, the dissolved oxygen is 2-4 mg/L, the water temperature is 20-35 ℃, the design flow of MBR membrane effluent is 10-15L/m2.h (8 min is started and 2min is stopped, and the time is adjustable); the main indexes of the MBR membrane effluent are as follows: COD is less than or equal to 500mg/L, heavy metal content is less than or equal to 1mg/L, TP is less than or equal to 10mg/L, TN is less than or equal to 30mg/L, and SS is less than or equal to 1mg/L.
And the wastewater in the fifth state enters the MBR water storage tank 9 and reaches the standard and is discharged, and the rear end of the MBR water storage tank 9 can be expanded and connected into an advanced treatment system, such as an NF (NF) membrane system, an RO (reverse osmosis) membrane system and the like, according to the requirement, so that the effect of recycling the wastewater of the lithium battery is achieved.
The COD (chemical oxygen demand) is the amount of oxidant consumed when a water sample is treated with a certain strong oxidant under a certain condition. It reflects the degree of pollution of substances in water, and the larger the chemical oxygen demand is, the more serious the pollution of organic substances in water is.
MBR is a short name of a Membrane-bioreactor (Membrane Bio-Reactor), and MBR is a novel sewage treatment device formed by combining ultrafiltration and microfiltration Membrane separation technologies with a bioreactor in sewage treatment.
The foregoing is merely illustrative of specific embodiments of the present utility model, and the scope of the present utility model is not limited thereto, but any changes or substitutions within the technical scope of the present utility model should be covered by the scope of the present utility model. Therefore, the protection scope of the present utility model shall be subject to the protection scope of the claims.
Claims (10)
1. A treatment system for wastewater from lithium battery cathode material production, the treatment system comprising:
the sedimentation coagulation device, the filtering device, the catalytic oxidation device and the biochemical treatment device are sequentially arranged along the pipeline;
the sedimentation coagulation device comprises a reaction tank unit and a sedimentation tank;
the reaction tank unit comprises a plurality of reaction tanks which are connected in sequence and is used for removing fluorine ions, heavy metals and calcium ions in the wastewater to be treated and outputting wastewater in a first state to the sedimentation tank;
the sedimentation tank is communicated with the reaction tank unit and is used for physically precipitating the wastewater in the first state, removing sediment and outputting wastewater in the second state to the filtering device;
the filtering device is communicated with the sedimentation tank and is used for filtering the second-state wastewater, removing suspended matters and outputting third-state wastewater to the catalytic oxidation device;
the catalytic oxidation device is communicated with the filtering device and is used for carrying out catalytic oxidation on the wastewater in the third state, converting organic phosphorus into orthophosphate and outputting wastewater in the fourth state to the biochemical treatment device;
the biochemical treatment device is communicated with the catalytic oxidation device and is used for carrying out anaerobic reaction and aerobic reaction on the fourth-state wastewater, removing orthophosphate and COD and outputting fifth-state wastewater;
wherein the wastewater to be treated is wastewater from the production of lithium battery anode materials.
2. The processing system of claim 1, wherein:
the sedimentation coagulation device is also communicated with a homogenizing value adjusting device;
the homogenizing and regulating device is used for uniformly mixing the wastewater to be treated and regulating the pH value to 6-9.
3. The processing system of claim 1, wherein:
the reaction tank unit comprises a first reaction tank, a second reaction tank, a third reaction tank and a fourth reaction tank which are integrally arranged, and stirring machines are arranged in the first reaction tank, the second reaction tank, the third reaction tank and the fourth reaction tank;
the first reaction tank is used for removing fluoride ions and heavy metals in the wastewater to be treated;
the second reaction tank is used for removing calcium ions in the wastewater to be treated;
the third reaction tank is used for carrying out coagulation reaction on the wastewater to be treated;
the fourth reaction tank is used for carrying out flocculation reaction on the wastewater to be treated.
4. The processing system of claim 2, wherein:
the filtering device comprises at least one sand filtering tank and a sand filtering water storage tank communicated with the sand filtering tank, wherein the sand filtering tank is communicated with an air compressor, and air washing is performed through the air compressor;
the sand filter tank filters the second-state wastewater to obtain the third-state wastewater, and conveys the third-state wastewater to the sand filter water storage tank, and the sand filter tank performs forward washing and reverse washing through the sand filter water storage tank;
the sand filter tank is communicated with the homogenizing value adjusting device, and forward washing water and backward washing water are conveyed to the homogenizing value adjusting device.
5. The processing system of claim 1, wherein:
the catalytic oxidation device comprises an ozone catalytic oxidation tower and a catalytic oxidation water storage tank which are communicated;
the ozone catalytic oxidation tower is internally filled with catalytic oxidation filler, the bottom of the ozone catalytic oxidation tower is provided with an aeration disc, and the aeration disc is communicated with an ozone generator;
when the device works, the ozone generator is used for introducing ozone into the ozone catalytic oxidation tower through the aeration disc, the third-state wastewater flows from top to bottom in the ozone catalytic oxidation tower, after a period of catalytic oxidation reaction, the fourth-state wastewater is obtained, and the fourth-state wastewater is conveyed to the catalytic oxidation water storage tank.
6. The processing system of claim 5, wherein:
the biochemical treatment device comprises an anaerobic reactor and an aerobic biochemical device which are communicated;
the anaerobic reactor comprises a water distributor, an anaerobic reaction zone, a three-phase separator and a methane collecting and utilizing component;
the anaerobic reaction zone comprises a high-concentration sludge reaction zone and a low-concentration sludge reaction zone;
the aerobic biochemical device comprises an aerobic tank, wherein an MBR membrane assembly is arranged at the tail end of the aerobic tank, and the MBR membrane assembly is communicated with an MBR water storage tank.
7. The processing system of claim 6, wherein:
a plate heat exchanger is arranged between the catalytic oxidation water storage tank and the anaerobic reactor and is used for heating the fourth-state wastewater, so that the temperature of the fourth-state wastewater entering the anaerobic reactor is maintained at 20-35 ℃.
8. The processing system of claim 2, wherein:
the homogenizing and adjusting device comprises a homogenizing and adjusting tank.
9. A processing system according to any of claims 5-7, wherein:
the catalytic oxidation filler comprises a metal silicate catalyst, and the particle size of the metal silicate catalyst is 80-100 meshes.
10. A processing system according to claim 3, wherein:
the first reaction tank is added with 5-10% of calcium hydroxide solution by mass percent;
sodium carbonate solution with mass percent of 5-10% is added into the second reaction tank;
PAC is added into the third reaction tank, and the adding amount of the PAC is 100-200 mg/L;
PAM is added into the fourth reaction tank, and the addition amount of the PAM is 2-5 mg/L.
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