CN212293242U - Electrolytic capacitor and electrode foil wastewater treatment system - Google Patents
Electrolytic capacitor and electrode foil wastewater treatment system Download PDFInfo
- Publication number
- CN212293242U CN212293242U CN202021965008.9U CN202021965008U CN212293242U CN 212293242 U CN212293242 U CN 212293242U CN 202021965008 U CN202021965008 U CN 202021965008U CN 212293242 U CN212293242 U CN 212293242U
- Authority
- CN
- China
- Prior art keywords
- tank
- wastewater
- treatment system
- sludge
- treatment
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Water Treatment By Electricity Or Magnetism (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
- Activated Sludge Processes (AREA)
Abstract
The utility model discloses an electrolytic capacitor and electrode foil effluent disposal system belongs to sewage treatment technical field, the system during operation includes the step: 1) classifying and sorting the production wastewater according to the indexes and the concentrations of pollutants, and regulating and storing the production wastewater in respective regulating tanks to stabilize the water quality; 2) pre-reacting the high-phosphorus wastewater in a phosphorus removal reaction sedimentation tank to remove phosphorus; 3) carrying out pre-denitrification treatment on the high-nitrogen wastewater; 4) removing partial impurities and organic matters from the low-concentration wastewater; 5) mixing the pretreated wastewater, continuing the comprehensive treatment of the wastewater, and finally clarifying the effluent to discharge after reaching the standard; 7) and (3) discharging sludge generated in the pretreatment process into a sludge concentration tank, performing filter pressing dehydration, and then transporting the sludge to an outside for disposal. The utility model provides an electrolytic capacitor and electrode foil effluent disposal system combines above-mentioned processing step to successfully solve the difficult problem that the high organic matter of high phosphorus high nitrogen in the electron waste water was handled, has reduced sludge treatment expense, and the working costs is low, the operation is stable, operation maintenance is simple.
Description
Technical Field
The utility model relates to a sewage treatment technical field especially relates to an electrolytic capacitor and electrode foil effluent disposal system.
Background
In recent years, with the multiplied growth of the aluminum electrolytic capacitor industry in China, the aluminum foil industry for capacitors in China also grows rapidly in a leap-type manner. Annual production and consumption of aluminium foil worldwide has progressed from around 1 ten thousand tons in 1995 to the level of about 10 ten thousand tons at present. The industrial market prospect is wide, but simultaneously along with the continuous increase of the discharged wastewater of the industry, the task of treating the wastewater is heavier and heavier.
The industry is mainly provided with three production lines, namely a low-pressure corrosion production line, a formation production line and a water purifying agent production line. Wherein the corrosion production line is divided into primary corrosion and secondary corrosion, and the used main raw materials comprise: 20% hydrochloric acid, 8% sulfuric acid, 3% phosphoric acid, 3% nitric acid and the like, under the action of alternating current, firstly, primary corrosion is carried out to form initial corrosion holes on the surface of the plain foil, and then, secondary corrosion is carried out to further activate and expand the corrosion holes so as to form more spongy holes and enlarge the effective area of the aluminum foil. Finally, through a plurality of cleaning steps, residual corrosive liquid on the surface of the aluminum foil and impurities in the holes are cleaned, and the step can generate a large amount of cleaning wastewater containing high-concentration nitrate radicals and phosphate radicals.
The formation production line mainly adopts 1-5% of ammonium adipate as a raw material, is matched with 5% of phosphoric acid, adopts a direct current power supply, takes an aluminum foil as a positive electrode and an electrode plate as a negative electrode, generates an aluminum oxide oxidation film medium on the surface of the aluminum foil under the action of an electric field, and controls the thickness of an oxidation film through a five-stage formation step to prepare the formation foil with various voltage resistance (VF) specifications. This procedure produces a high phosphate radical, high organic content rinse effluent.
The main wastewater of the water purifying agent production line is produced into ground washing wastewater, equipment washing wastewater and spray tower wastewater of a water purifying agent workshop.
Besides the three production lines, domestic sewage and canteen wastewater are additionally attached to form various wastewater streams with different types of pollutants, different indexes, different concentrations and different water amounts, a targeted treatment process needs to be found, the wastewater streams are distinguished and sorted, and the treated wastewater reaches the standard and is discharged in a corresponding pretreatment and comprehensive treatment mode.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing an electrolytic capacitor and electrode foil effluent disposal system to solve the problem that above-mentioned prior art exists, realize the effective getting rid of organic matter thorough degradation, total nitrogen, total phosphorus in the aluminium foil trade waste water, and the mud yield of whole technology is little, and most can be in the systematic digestion mud, has effectively reduced sludge treatment's investment and working costs, has advantages such as running cost is low, operation management is simple.
In order to achieve the above object, the utility model provides a following scheme:
the utility model provides an electrolytic capacitor and an electrode foil wastewater treatment method, which comprises the following steps:
s1: respectively introducing high-phosphorus wastewater, high-nitrogen wastewater, high-COD wastewater, low-concentration wastewater and domestic sewage into corresponding collecting tanks to homogenize the wastewater quality, and respectively carrying out aeration stirring, wherein the aeration strength is 2-4 m3/(m2·h)；
S2: the high-phosphorus wastewater passes through a phosphorus removal reaction tank, and phosphorus in the wastewater is subjected to flocculation reaction by adding a phosphorus removal agent;
s3: the high-phosphorus wastewater after the flocculation reaction is accessed into a dephosphorization sedimentation tank for sludge-water separation, sludge is discharged into a sludge concentration tank, and supernatant is accessed into an A/O treatment tank of a comprehensive treatment system;
s4: introducing the high-nitrogen wastewater into a denitrification reaction tank and a nitrification tank for denitrification pretreatment, and introducing effluent into an A/O treatment tank of a comprehensive treatment system;
s5: pumping the low-concentration wastewater into an air floatation treatment system, adding a medicament, and scraping suspended particles, oil stains and other fat pollutants in the wastewater in an air floatation tank by a residue scraping system after attaching to microbubbles and floating to the surface of the liquid along with the rising of the microbubbles through the microbubbles released in the water; the effluent is connected into an A/O treatment pool of the comprehensive treatment system;
s6: directly pumping the high COD wastewater and the domestic sewage into an A/O treatment tank of a comprehensive treatment system;
s7: collecting and uniformly mixing the pretreated high-phosphorus wastewater, high-nitrogen wastewater, low-concentration wastewater and high-COD wastewater and low-concentration wastewater in an A/O (anaerobic/oxic) treatment tank;
s8: carrying out blast aeration in the A/O treatment tank to degrade organic pollutants in the wastewater and remove nitrogen and phosphorus;
s9: the effluent of the A/O treatment tank automatically flows into a secondary sedimentation tank, sludge is settled at the bottom, part of the sludge flows back into the A/O treatment tank, part of the sludge is periodically discharged into a sludge concentration tank, and supernatant enters a reaction tank of a physicochemical treatment system;
s10: adding a flocculating agent into the reaction tank to further perform coagulation reaction on organic matters and suspended matters in the wastewater;
s11: after the coagulation reaction, the wastewater enters a physical and chemical sedimentation tank for sludge-water separation, clear water is discharged into a clear water tank to be discharged after reaching the standard, and precipitated sludge is discharged into a sludge concentration tank;
s12: and carrying out filter pressing on the sludge in the sludge concentration tank, and transporting and disposing the sludge cake.
Optionally, in the step S2, adding alkali to adjust the pH value of the wastewater to 9-10, and adding lime and PAM; the addition amount of the lime is 1-3 kg/m3The addition amount of the PAM is 0.005-0.01 kg/m3Waste water
Optionally, in the step S4, part of the high COD wastewater may be introduced into the denitrification reactor to supplement a denitrification carbon source; the denitrification reaction tank is provided with a three-phase separator which can effectively separate gas, liquid and solid phases; the hydraulic retention time of the denitrification reaction tank reactor is 1.5-2.0 d, and the reaction temperature in the reactor is controlled at 35-38 ℃; the nitrification tank is provided with blast aeration with aeration rate of 5-6 m3/(m2·h)。
Optionally, in the step S5, adding an alkali to adjust the pH to 9-10, and then adding a self-produced water purifying agent PAC and a PAM medicament, wherein the addition amount of the self-produced water purifying agent PAC is 0.15-0.3 kg/m3The addition amount of the PAM is 0.005-0.01 kg/m3Waste water; both the scum and the bottom sediment are discharged into a sludge concentration tank.
Optionally, before the aerobic treatment in the step S8, adjusting the pH value to 7.5 to 8.5;in the anoxic and aerobic comprehensive treatment process in the A/O treatment tank, the dissolved oxygen of anoxic treatment is less than or equal to 0.2mg/L, and the carbon-nitrogen ratio is 4: 1-5: 1, and the aeration rate of the anoxic treatment is 0.5-1.0 m3/(m2H); the dissolved oxygen of the aerobic treatment is 3-5 mg/L, and the aeration rate of the aerobic treatment is 5-6 m3/(m2H); and refluxing the sludge-water mixed solution subjected to aerobic treatment to an anoxic tank of the A/O treatment tank according to the reflux ratio of 330-450%.
Optionally, the precipitated sludge in the secondary sedimentation tank in the step S9 is refluxed to the anoxic treatment and aerobic treatment processes according to a reflux ratio of 150% to 300%.
Optionally, adding self-produced water purifying agents PAC and PAM in the coagulation reaction process in step S10; the addition amount of the self-produced water purifying agent PAC is 0.15-0.3 kg/m3The addition amount of the PAM is 0.005-0.01 kg/m3Waste water; adjusting the pH value to 7-8 in the coagulation reaction process; and (3) obtaining materialized precipitated sludge after the materialized precipitation treatment, and carrying out filter pressing concentration treatment on the materialized precipitated sludge in a sewage and sludge concentration tank.
Optionally, in step S12, the sludge property is adjusted by adding cationic PAM, wherein the addition amount of the cationic PAM is 0.002-0.0005 kg/m3And (4) sludge.
The utility model also provides an electrolytic capacitor and an electrode foil wastewater treatment system, which comprises a high-phosphorus wastewater collecting tank, a high-nitrogen wastewater collecting tank, a high-COD wastewater collecting tank, a low-concentration wastewater collecting tank and a domestic sewage collecting tank which are sequentially arranged in parallel; the high-phosphorus wastewater collection tank is connected with a comprehensive treatment system through a phosphorus removal reaction tank and a phosphorus removal sedimentation tank which are connected in series, the high-nitrogen wastewater collection tank is connected with the comprehensive treatment system through a denitrification reaction tank and a nitrification tank which are connected in series, the low-concentration wastewater collection tank is connected with the comprehensive treatment system through an air floatation treatment system, the high-COD wastewater collection tank and the domestic sewage collection tank are connected with the comprehensive treatment system through pipelines, and the comprehensive treatment system is connected with a clean water tank; and the dephosphorization sedimentation tank, the air floatation treatment system and the comprehensive treatment system are respectively communicated with the sludge concentration tank.
Optionally, the comprehensive treatment system comprises an a/O treatment tank, a secondary sedimentation tank, a physicochemical reaction tank and a physicochemical sedimentation tank which are sequentially communicated through pipelines; the A/O treatment pool comprises an anoxic pool and an aerobic pool which are communicated; the aerobic tank is communicated with the secondary sedimentation tank; a nitrifying liquid reflux device is arranged between the aerobic tank and the anoxic tank; a sludge reflux device is arranged between the secondary sedimentation tank and the anoxic tank as well as the aerobic tank, and the secondary sedimentation tank is communicated with a sludge concentration tank; and the dephosphorization sedimentation tank, the air floatation treatment system, the secondary sedimentation tank and the materialization sedimentation tank are respectively provided with a sludge discharge pipe and a sludge discharge pump which are communicated with the sludge concentration tank.
The utility model discloses for prior art gain following technological effect:
the utility model aims at the characteristics of electrolytic capacitor and electrode foil wastewater with high phosphorus, high nitrogen and high organic matter, carries out classification and arrangement of wastewater according to pollutant indexes and concentration, and takes physicochemical pretreatment as a front-stage treatment process route; the comprehensive treatment process of the A/O treatment tank, the secondary sedimentation tank and the coagulating sedimentation tank is adopted as a core, wherein the anoxic and aerobic comprehensive treatment can synchronously carry out denitrification and dephosphorization, remove COD and reduce chroma, and the problems of difficult treatment of nitrogen and phosphorus in the wastewater and the like are effectively solved; the utility model discloses can reduce COD in electrolytic capacitor and the electrode foil waste water to below 500mg/L from 5000mg/L, reduce the phosphate in the waste water to below 5mg/L from 1500mg/L, reduce the ammonia nitrogen content in the waste water to below 25mg/L from 200mg/L simultaneously. The effluent can reach the C grade standard (COD is less than or equal to 500mg/L, ammonia nitrogen is less than or equal to 25mg/L, total nitrogen is less than or equal to 70mg/L, and P is less than or equal to 5mg/L) in the water quality standard for sewage discharge into cities and towns (GB/T31962-2015), the sludge yield of the whole process is small, the investment and the operation cost of sludge treatment are effectively reduced, and the method has the advantages of low power consumption, low operation cost, simple operation and management, stable operation and the like.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings required to be used in the embodiments will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without inventive labor.
FIG. 1 is a schematic view showing the positional connection between an electrolytic capacitor and an electrode foil wastewater treatment system;
wherein, 1 is a high-phosphorus wastewater collection tank, 2 is a high-nitrogen wastewater collection tank, 3 is a high COD wastewater collection tank, 4 is a low-concentration wastewater collection tank, 5 is a domestic sewage collection tank, 6 is a phosphorus removal reaction tank, 7 is a denitrification reaction tank, 8 is a phosphorus removal sedimentation tank, 9 is a nitrification tank, 10 is an air flotation treatment system, 11 is an A/O treatment tank, 12 is a secondary sedimentation tank, 13 is a physicochemical reaction tank, 14 is a physicochemical sedimentation tank, 15 is a clear water tank, and 16 is a sludge concentration tank.
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
The utility model aims at providing an electrolytic capacitor and electrode foil effluent disposal system to solve the problem that above-mentioned prior art exists, realize the effective getting rid of organic matter thorough degradation, total nitrogen, total phosphorus in the aluminium foil trade waste water, and the mud yield of whole technology is little, and most can be in the systematic digestion mud, has effectively reduced sludge treatment's investment and working costs, has advantages such as running cost is low, operation management is simple.
In order to make the above objects, features and advantages of the present invention more comprehensible, the present invention is described in detail with reference to the accompanying drawings and the detailed description.
The utility model aims to overcome the defects of the prior art, the utility model mainly adopts the prior classified arrangement of each strand of wastewater, and the wastewater is divided into high-phosphorus wastewater, high-nitrogen wastewater, high COD wastewater, low-concentration wastewater and domestic sewage, and then various types of wastewater are pretreated. Wherein the high-phosphorus wastewater adopts a physicochemical phosphorus removal process, the high-nitrogen wastewater adopts a denitrification reactor to denitrate in advance, the low-concentration wastewater adopts an air floatation device to remove partial organic matters and impurities, the pretreated high-phosphorus wastewater enters a comprehensive treatment system to be treated continuously, and the high-COD wastewater and the domestic sewage directly enter the comprehensive treatment system. The comprehensive treatment adopts a process route which mainly comprises an A/O treatment tank, a secondary sedimentation tank and a coagulating sedimentation tank.
The utility model discloses the method can be pertinence to nitrogen, phosphorus high concentration pollutant do get rid of in advance, reduce or avoid as far as possible to follow-up comprehensive biochemical treatment system's influence, synthesize good oxygen biochemical treatment again afterwards in the lump. The process can effectively solve the problems of high nitrogen and phosphorus content, high organic matter concentration and difficult treatment in industrial wastewater. The method has the advantages of realizing the thorough degradation of organic matters in the wastewater in the aluminum foil industry and the effective removal of total nitrogen and total phosphorus, along with small sludge production amount of the whole process, capability of digesting most sludge in the system, effective reduction of the investment and the operating cost of sludge treatment, low operating cost, simple operation and management and the like.
The utility model provides an electrolytic capacitor and an electrode foil wastewater treatment method, as shown in figure 1, comprising the following steps:
s1: respectively feeding high-phosphorus wastewater, high-nitrogen wastewater, high-COD wastewater, low-concentration wastewater and domestic sewage into a high-phosphorus wastewater collecting tank 1, a high-nitrogen wastewater collecting tank 2, a high-COD wastewater collecting tank 3, a low-concentration wastewater collecting tank 4 and a domestic sewage collecting tank 5 which respectively correspond to each other to homogenize the quality of the wastewater;
s2: high-phosphorus wastewater passes through a phosphorus removal reaction tank 6, and phosphorus in the wastewater is subjected to flocculation reaction by adding a phosphorus removal agent;
s3: the high-phosphorus wastewater after the flocculation reaction is accessed into a dephosphorization sedimentation tank 8 for sludge-water separation, sludge is discharged into a sludge concentration tank 16, and supernatant is accessed into an A/O treatment tank 11 of the comprehensive treatment system;
s4: the high-nitrogen wastewater is subjected to denitrification pretreatment, namely a denitrification reaction tank 7(DeTN) and a nitrification tank 9. Under the anoxic condition, the denitrification reaction tank 7 utilizes denitrifying bacteria groups with different gradients, organic matters are taken as electron donors, nitrate radicals returned by the nitrification tank 9 are taken as electron acceptors, and heterotrophic bacteria groups are obtainedIn the process, nitrate radical is finally converted into N2Discharging the water body and realizing the high-efficiency denitrification of the wastewater. The effluent is connected into an A/O treatment pool 11 of the comprehensive treatment system;
s5: the low concentration wastewater is pumped into the air flotation treatment system 10. By adding the medicament, suspended particles, oil stains and other fat pollutants in the wastewater in the air floatation treatment system 10 are scraped by the residue scraping system after attaching to microbubbles and floating to the liquid surface along with the rising of the microbubbles through the microbubbles released in the water. The effluent is connected into an A/O treatment pool 11 of the comprehensive treatment system;
s6: directly pumping the high COD wastewater and the domestic sewage into a comprehensive treatment system;
s7: collecting and uniformly mixing the pretreated high-phosphorus wastewater, high-nitrogen wastewater, low-concentration wastewater and high-COD wastewater and low-concentration wastewater in an A/O treatment tank 11;
s8: blast aeration is carried out in the A/O treatment tank 11, most organic pollutants in the wastewater are degraded, and nitrogen and phosphorus are removed;
s9: the effluent of the A/O treatment tank 11 automatically flows into a secondary sedimentation tank 12, sludge is settled at the bottom, part of the sludge flows back into the aerobic tank, and part of the sludge is periodically discharged into a sludge concentration tank 16. The supernatant enters a physicochemical reaction tank 13 of a physicochemical treatment system;
s10: adding a flocculating agent into the physicochemical reaction tank 13 to further perform coagulation reaction on organic matters and suspended matters in the wastewater;
s11: after the coagulation reaction, the wastewater enters a physical and chemical sedimentation tank 14 for mud-water separation, clear water is discharged into a clear water tank 15 and discharged out after reaching the standard, and precipitated sludge is discharged into a sludge concentration tank 16;
s12: and (4) carrying out filter pressing on the sludge in the sludge concentration tank 16, and transporting and disposing the sludge cakes.
The comprehensive treatment system comprises A/O aerobic biochemical treatment and physicochemical advanced treatment which are connected in series.
In the step S1, the collecting tanks are all matched with aeration stirring systems, and the aeration intensity is 2-4 m3/(m2H). In the step S2, adding alkali to adjust the pH value of the wastewater to 9-10, and adding lime and PAM; the addition amount of lime is 1-3 kg/m3The addition amount of PAM in the wastewater is 0.005-0.01 kg/m3Waste water; step by stepIn the step S3, the phosphorus removal sedimentation tank is preferably a radial flow sedimentation tank, the linear speed of the selected mud scraper is 2-3 m/min, and the rotating speed is 1-3 r/h;
in step S4, part of the high COD wastewater can be connected into the denitrification reactor to supplement the denitrification carbon source; the denitrification reaction tank (DeTN) is provided with a three-phase separator for effectively separating gas, liquid and solid phases; the hydraulic retention time of the reactor is preferably 4d, and the reaction temperature in the reactor is controlled to be 35-38 ℃; the nitrification tank is provided with blast aeration with aeration rate of 5-6 m3/(m2H), the residence time of the nitrification tank is preferably 4 d; and refluxing the nitrified sludge-water mixed liquid into the denitrification tank according to the reflux ratio of 330-450%.
In the step S5, adding alkali to adjust the pH value to 9-10, and then adding a self-produced water purifying agent PAC and a PAM medicament, wherein the addition amount of the self-produced water purifying agent PAC is 0.15-0.3 kg/m3The addition amount of PAM in the wastewater is 0.005-0.01 kg/m3Waste water; discharging the scum and bottom sludge in the sedimentation tank into a sludge concentration tank; most of oil-containing substances and part of suspended matters are separated through air flotation, so that the influence of floating oil on subsequent treatment is reduced; the utility model discloses do not have special restriction to the parameter of air supporting, adopt the air supporting parameter of this area conventionality can.
Before the aerobic treatment in the step S8, adjusting the pH value to 7.5-8.5; in the process of anoxic and aerobic (A/O) comprehensive treatment, the dissolved oxygen of the anoxic treatment is less than or equal to 0.2mg/L, the carbon-nitrogen ratio is (4-5): 1, and the aeration rate of the anoxic treatment is 0.5-1.0 m3/(m2H); the dissolved oxygen of the aerobic treatment is 3-5 mg/L, and the aeration rate of the aerobic treatment is 5-6 m3/(m2H). In the utility model, the total hydraulic retention time of the anoxic and aerobic treatment is preferably 2 days, and the hydraulic retention time of each treatment stage is preferably equal. In the utility model, the sludge sedimentation ratio (SV30) of the anoxic and aerobic comprehensive treatment is preferably 70-80%; in the utility model, the preferable nitrifying liquid generated in the aerobic treatment flows back to the anoxic treatment process. The utility model discloses it is 330 ~ 450%, more preferably 350 ~ 400% to prefer nitrify liquid according to the reflux ratio. The utility model preferably returns the nitrifying liquid to the anoxic zone under the condition of the reflux ratioIn the process, the requirement of the denitrification of the heterotrophic bacteria on NO under the anoxic condition is favorably met3-And is beneficial to reducing energy consumption. Refluxing the precipitated sludge in the secondary sedimentation tank in the step S9 to the anoxic treatment and the aerobic treatment according to the reflux ratio of 150-300%; the surface load of the secondary sedimentation tank is preferably 0.7m3/(m2·h)。
The utility model discloses after biochemical treatment, waste water after with biochemical treatment flocculates, mud-water separation obtains effluent up to standard. In the utility model, a flocculating agent and a coagulant are preferably added into the wastewater in the flocculation treatment process; the utility model discloses do not have special restriction to the kind of flocculating agent and coagulant, adopt the reagent that technical personnel in the field are familiar with can, in the embodiment of the utility model, the preferred polyaluminium chloride (from the production water purifying agent PAC) flocculating agent and anionic Polyacrylamide (PAM) coagulant of adopting, Al in the production water purifying agent PAC flocculating agent2O3The content is preferably 24%, and the molecular weight of the PAM coagulant is preferably 1200 ten thousand. In the utility model, the addition amount of the self-produced water purifying agent PAC is 0.15-0.3 kg/m3The addition amount of PAM in the wastewater is 0.005-0.01 kg/m3Waste water; adding alkali to adjust the pH value to 7-8 in the coagulation reaction process; the utility model discloses a flocculation treatment gets rid of Suspended Solid (SS), further reduces COD and reduces colourity in the waste water.
The utility model discloses in, the purpose of materialization sedimentation treatment is to realize mud-water separation, makes the play water more limpid, avoids mud to run off. The utility model discloses do not have special restriction to mud-water separation's specific operating condition, adopt the operating condition that technical personnel in the field are familiar with can. The utility model discloses after the materialization is deposited and is handled, the gained effluent reaches emission standard promptly, can directly discharge. And (3) obtaining the materialized precipitated sludge after the materialized precipitation treatment, and carrying out filter pressing concentration treatment on the materialized precipitated sludge in a sewage and sludge concentration tank.
In the step S12, the sludge filter press is preferably plate-and-frame filter pressing, the sludge property is adjusted by adding cationic PAM, and the adding amount of the cationic PAM is 0.002-0.0005 kg/m3And (4) sludge.
The utility model also provides an electrolytic capacitor and electrode foil wastewater treatment system, the structures of each collecting tank, sedimentation tank and treatment tank related in the system are known at present, the utility model mainly protects the arrangement and connection mode, and concretely, the connection relation is shown in figure 1, comprising a high-phosphorus wastewater collecting tank 1, a high-nitrogen wastewater collecting tank 2, a high COD wastewater collecting tank 3, a low-concentration wastewater collecting tank 4 and a domestic wastewater collecting tank 5 which are arranged in parallel in sequence; the high-phosphorus wastewater collection tank 1 is connected with a dephosphorization reaction tank 6 and a dephosphorization sedimentation tank 8 through serial pipelines and is finally connected with a comprehensive treatment system through pipelines, the high-nitrogen wastewater collection tank 2 is connected with a denitrification reaction tank 7 and a nitrification tank 9 through serial pipelines and is finally connected with the comprehensive treatment system through pipelines, after the low-concentration wastewater collection tank 4 is communicated with an air floatation treatment system 10 through a pipeline, the air floatation treatment system 10 is connected with the comprehensive treatment system through a pipeline, the high-COD wastewater collection tank 3 and the domestic sewage collection tank 5 are connected with the comprehensive treatment system through pipelines, and the comprehensive treatment system is connected with a clean water tank 15 through a pipeline; the dephosphorization sedimentation tank 8, the air floatation treatment system 10 and the comprehensive treatment system are respectively communicated with a sludge concentration tank 16. In fig. 1, arrows above the phosphorus removal reaction tank 6, the air flotation treatment system 10 and the physicochemical reaction tank 13 indicate positions where the corresponding agents are respectively added.
The comprehensive treatment system comprises an A/O treatment tank 11, a secondary sedimentation tank 12, a physicochemical reaction tank 13 and a physicochemical sedimentation tank 14 which are sequentially communicated through pipelines; the A/O treatment tank 11 comprises an anoxic tank and an aerobic tank which are communicated through a pipeline, and the aerobic tank is communicated with the secondary sedimentation tank 12; a nitrifying liquid reflux device is arranged between the aerobic tank and the anoxic tank; a sludge reflux device is arranged between the secondary sedimentation tank 12 and the anoxic tank and the aerobic tank, and the secondary sedimentation tank 12 is communicated with a sludge concentration tank 16. The dephosphorization sedimentation tank 8, the air floatation treatment system 10, the secondary sedimentation tank 12 and the materialization sedimentation tank 14 are all provided with sludge discharge pipes and sludge discharge pumps which are communicated with a sludge concentration tank 16.
The utility model aims at the characteristics of electrolytic capacitor and electrode foil wastewater with high phosphorus, high nitrogen and high organic matter, carries out classification and arrangement of wastewater according to pollutant indexes and concentration, and takes physicochemical pretreatment as a front-stage treatment process route; the comprehensive treatment process of the A/O treatment tank, the secondary sedimentation tank and the coagulating sedimentation tank is adopted as a core, wherein the anoxic and aerobic comprehensive treatment can synchronously carry out denitrification and dephosphorization, remove COD and reduce chroma, and the problems of difficult treatment of nitrogen and phosphorus in the wastewater and the like are effectively solved; the utility model discloses can reduce COD in electrolytic capacitor and the electrode foil waste water to below 500mg/L from 5000mg/L, reduce the phosphate in the waste water to below 5mg/L from 1500mg/L, reduce the ammonia nitrogen content in the waste water to below 25mg/L from 200mg/L simultaneously. The effluent can reach the C grade standard (COD is less than or equal to 500mg/L, ammonia nitrogen is less than or equal to 25mg/L, total nitrogen is less than or equal to 70mg/L, and P is less than or equal to 5mg/L) in the water quality standard for sewage discharge into cities and towns (GB/T31962-2015), the sludge yield of the whole process is small, the investment and the operation cost of sludge treatment are effectively reduced, and the method has the advantages of low power consumption, low operation cost, simple operation and management, stable operation and the like.
The utility model discloses a concrete example is applied to explain the principle and the implementation mode of the utility model, and the explanation of the above example is only used to help understand the method and the core idea of the utility model; meanwhile, for the general technical personnel in the field, according to the idea of the present invention, there are changes in the concrete implementation and the application scope. In summary, the content of the present description should not be construed as a limitation of the present invention.
Claims (2)
1. An electrolytic capacitor and electrode foil wastewater treatment system is characterized in that: the system comprises a high-phosphorus wastewater collecting tank, a high-nitrogen wastewater collecting tank, a high-COD wastewater collecting tank, a low-concentration wastewater collecting tank and a domestic sewage collecting tank which are sequentially arranged in parallel; the high-phosphorus wastewater collection tank is connected with a comprehensive treatment system through a phosphorus removal reaction tank and a phosphorus removal sedimentation tank which are connected in series, the high-nitrogen wastewater collection tank is connected with the comprehensive treatment system through a denitrification reaction tank and a nitrification tank which are connected in series, the low-concentration wastewater collection tank is connected with the comprehensive treatment system through an air floatation treatment system, the high-COD wastewater collection tank and the domestic sewage collection tank are connected with the comprehensive treatment system through pipelines, and the comprehensive treatment system is connected with a clean water tank; and the dephosphorization sedimentation tank, the air floatation treatment system and the comprehensive treatment system are respectively communicated with the sludge concentration tank.
2. The electrolytic capacitor and electrode foil wastewater treatment system as set forth in claim 1, wherein: the comprehensive treatment system comprises an A/O treatment tank, a secondary sedimentation tank, a physicochemical reaction tank and a physicochemical sedimentation tank which are sequentially communicated through pipelines; the A/O treatment pool comprises an anoxic pool and an aerobic pool which are communicated; the aerobic tank is communicated with the secondary sedimentation tank; a nitrifying liquid reflux device is arranged between the aerobic tank and the anoxic tank; a sludge reflux device is arranged between the secondary sedimentation tank and the anoxic tank as well as the aerobic tank, and the secondary sedimentation tank is communicated with a sludge concentration tank; and the dephosphorization sedimentation tank, the air floatation treatment system, the secondary sedimentation tank and the materialization sedimentation tank are respectively provided with a sludge discharge pipe and a sludge discharge pump which are communicated with the sludge concentration tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021965008.9U CN212293242U (en) | 2020-09-10 | 2020-09-10 | Electrolytic capacitor and electrode foil wastewater treatment system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021965008.9U CN212293242U (en) | 2020-09-10 | 2020-09-10 | Electrolytic capacitor and electrode foil wastewater treatment system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN212293242U true CN212293242U (en) | 2021-01-05 |
Family
ID=73934784
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202021965008.9U Active CN212293242U (en) | 2020-09-10 | 2020-09-10 | Electrolytic capacitor and electrode foil wastewater treatment system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN212293242U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111943461A (en) * | 2020-09-10 | 2020-11-17 | 苏州苏沃特环境科技有限公司 | Electrolytic capacitor and electrode foil wastewater treatment method and treatment system |
-
2020
- 2020-09-10 CN CN202021965008.9U patent/CN212293242U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111943461A (en) * | 2020-09-10 | 2020-11-17 | 苏州苏沃特环境科技有限公司 | Electrolytic capacitor and electrode foil wastewater treatment method and treatment system |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103524001B (en) | Treatment method for high fat food processing wastewater | |
| CN111943461A (en) | Electrolytic capacitor and electrode foil wastewater treatment method and treatment system | |
| CN101774724B (en) | Method for treating production wastewater of glucide | |
| CN102603128A (en) | Method for advanced treatment and recycling of landfill leachate | |
| CN210711182U (en) | Pharmaceutical intermediate waste water treatment system and pretreatment system | |
| CN103408201B (en) | The treatment process of trade effluent during silicon wafer mortar reclaims | |
| CN111453920A (en) | Anodic oxidation wastewater treatment method and system | |
| CN201746432U (en) | Apparatus for strengthening treatment of coking waste water | |
| CN109942150B (en) | Treatment method of waste water produced by utilizing waste vegetable oil | |
| CN212293242U (en) | Electrolytic capacitor and electrode foil wastewater treatment system | |
| CN207512019U (en) | A kind of sanitary sewage, technique waste water, stripper Wastewater Concentrated device | |
| CN211712893U (en) | Difficult degradation industrial waste water treatment system | |
| CN112209577A (en) | Kitchen wastewater treatment method | |
| CN210012702U (en) | Deep sewage purification device | |
| CN111153558A (en) | Garbage transfer station leachate treatment device and treatment method thereof | |
| CN216236438U (en) | Pretreatment system for garbage extrusion leachate | |
| CN212246663U (en) | Anodic oxidation effluent disposal system | |
| CN115367952A (en) | High-salinity sewage accident sewage and low-salinity high-concentration sewage comprehensive treatment system and method | |
| CN210457829U (en) | Landfill leachate's treatment facility | |
| CN211595362U (en) | High-salt-content high-organic-matter chemical wastewater treatment device | |
| CN105776684A (en) | Urban sewage treatment and resource recycling method | |
| CN214571360U (en) | Wastewater treatment system | |
| Powar et al. | A case study on common effluent treatment plant at five star MIDC, Kagal | |
| CN211896530U (en) | Steel comprehensive sewage advanced treatment system | |
| CN220335004U (en) | Lithium iron phosphate production wastewater treatment system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CP01 | Change in the name or title of a patent holder |
Address after: Room 323, building 28, No. 369, Lushan Road, high tech Zone, Suzhou City, Jiangsu Province Patentee after: Suzhou Suwote Environmental Technology Co.,Ltd. Address before: Room 323, building 28, No. 369, Lushan Road, high tech Zone, Suzhou City, Jiangsu Province Patentee before: SUZHOU SUWATER ENVIRONMENTAL SCIENCE AND TECHNOLOGY Co.,Ltd. |
|
| CP01 | Change in the name or title of a patent holder |