CN115093085B

CN115093085B - Industrial wastewater electrochemical dephosphorization system and dephosphorization method thereof

Info

Publication number: CN115093085B
Application number: CN202210939789.1A
Authority: CN
Inventors: 史鸿乐; 肖杰; 龙泉; 周文波; 许利; 邹俊良; 高东东
Original assignee: SICHUAN ACADEMY OF ENVIRONMENTAL SCIENCES
Current assignee: SICHUAN ACADEMY OF ENVIRONMENTAL SCIENCES
Priority date: 2022-08-05
Filing date: 2022-08-05
Publication date: 2024-05-10
Anticipated expiration: 2042-08-05
Also published as: CN115093085A

Abstract

The invention discloses an electrochemical phosphorus removal system for industrial wastewater and a phosphorus removal method thereof, and relates to the technical field of wastewater treatment. The invention solves the problems that the existing industrial wastewater is difficult to treat, the dephosphorization and denitrification effects are not ideal, and the like, and can treat industrial wastewater with different concentrations at the same time.

Description

Industrial wastewater electrochemical dephosphorization system and dephosphorization method thereof

Technical Field

The invention relates to the technical field of wastewater treatment, in particular to an electrochemical dephosphorization system and a dephosphorization method for industrial wastewater.

Background

Industrial wastewater refers to wastewater and waste liquid generated in an industrial production process, and contains industrial production materials, intermediate products and products which are lost with water and pollutants generated in the production process. At present, industrial wastewater discharged from various industrial processes in the world, particularly in developing countries, has caused serious harm to the environment, has brought about a heavy economic burden to governments and enterprises, and environmental problems have attracted great attention from governments.

In wastewater treatment, mainly removing organic matters, and simultaneously removing phosphorus and nitrogen, there are many methods for treating wastewater containing organic matters and phosphorus at present, mainly an anaerobic-aerobic method, an anaerobic-anoxic-aerobic and activated sludge method, and a sequencing batch activated sludge method. At present, the application is widely used is an anaerobic-anoxic-aerobic biochemical dephosphorization and denitrification process, the process is a process of controlling anaerobic-anoxic-aerobic, and is more suitable for wastewater treatment of dephosphorization and denitrification through degradation nitrification/denitrification, but in practice, a set of process flows are difficult to achieve the aims of simultaneously removing organic matters, denitrifying and dephosphorizing, the dephosphorization and the denitrification are often contradictory, complete biological nitrification is a premise of high-efficiency biochemical denitrification, the lower the biomass on unit area is, the longer the stay time is, the higher the denitrification efficiency is, and the biochemical dephosphorization requires the biomass on unit area to be high and the stay time is short, so that the actual wastewater treatment often has unsatisfactory effect and low dephosphorization and denitrification rate.

In addition, the water quality of the industrial wastewater is divided into two types of high concentration and low concentration, at present, when the industrial wastewater treatment plant is used for treating the industrial wastewater, the industrial wastewater with different concentrations is not treated independently, so that the industrial wastewater with different concentrations is treated by adopting the same treatment system when being treated, but only the dosage is regulated and controlled, the cost is higher, the generated chemical sludge is large, the treatment cost is higher, and the risk of secondary pollution exists.

Disclosure of Invention

The invention aims to provide an electrochemical dephosphorization system and a dephosphorization method for industrial wastewater, which solve the problems that the existing industrial wastewater is difficult to treat, the dephosphorization and denitrification effects are not ideal, and the like.

In order to achieve the aim of the invention, the technical scheme adopted is as follows: the industrial wastewater electrochemical dephosphorization system comprises a pretreatment unit, an anaerobic unit, a biochemical treatment unit, a front dephosphorization device, a rear dephosphorization device and a deep treatment unit, wherein the pretreatment unit, the front dephosphorization device, the anaerobic unit, the biochemical treatment unit and the rear dephosphorization device are sequentially connected, a first direct conveying pipeline is also connected between the pretreatment unit and the anaerobic unit, and the biochemical treatment unit and the rear dephosphorization device are connected with the deep treatment unit;

The pretreatment unit comprises a pretreatment tank and an adjusting tank which are communicated through overflow;

The front phosphorus removal device and the rear phosphorus removal device both comprise phosphorus removal units, the phosphorus removal units comprise phosphorus removal grooves and drainage grooves, the phosphorus removal grooves and the drainage grooves are of an integrated structure or a split structure, and electrode plates are further arranged in the phosphorus removal grooves;

The anaerobic unit comprises an anaerobic water inlet tank, two-stage UASB and an anaerobic sedimentation tank which are connected in sequence;

the biochemical treatment unit comprises an anoxic tank, an aerobic tank and an MBR tank which are sequentially communicated through overflow;

The biochemical treatment unit also comprises an anaerobic tank which is communicated with the anoxic tank in an overflow way, and a second direct conveying pipeline is also connected between the pretreatment unit and the anaerobic tank.

Further, the pretreatment tank is internally provided with a treatment coarse grille, the regulating tank is provided with a grading circulation reaction device, the grading circulation reaction device is provided with a water inlet pipe and a plurality of water outlet pipes, the outlet heights of the water outlet pipes are different, and the inlet end of the water inlet pipe and the outlet end of the water outlet pipes extend into the regulating tank.

Further, the grading circulation reaction device comprises a stirring tank and a buffer tank which are sequentially connected, the outlet end of the water inlet pipe is connected with the stirring tank, and the stirring tank is further provided with a dosing pipe and a discharge pipe connected with one of the water outlet pipes.

Further, the pretreatment unit further comprises a primary sedimentation tank connected to the outlet end of the regulating tank, and a feeding pipe is arranged on the primary sedimentation tank.

Further, the electrochemical dephosphorization unit further comprises a drainage tank, the upper end of the dephosphorization tank is communicated with the upper end of the drainage tank, a supporting frame is further arranged in the dephosphorization tank, a plurality of electrode plates in the dephosphorization tank are arranged on the supporting frame at intervals.

Further, a sludge discharge pipe for discharging sludge and a water inlet pipe for water inflow are further arranged on the dephosphorization tank, and a water outlet pipe is further arranged on the water discharge tank.

Further, the water inlet pipe and the sludge discharge pipe are both positioned at the bottom of the dephosphorization tank, and the outlet end of the water inlet pipe is communicated with the inlet end of the sludge discharge pipe through a three-way joint.

Further, the water outlet pipe is positioned in the middle of the water drainage groove, and the bottom of the water drainage groove is also provided with a blow-down pipe.

Furthermore, solenoid valves are arranged on the sludge discharge pipe, the water inlet pipe, the water outlet pipe and the blow-down pipe.

Furthermore, the electrochemical phosphorus removal units are in a plurality, the electrochemical phosphorus removal units are distributed in a rectangular array, and the electrochemical phosphorus removal units are connected in parallel or connected in series in sequence.

Furthermore, the bottoms of the dephosphorization tank and the drainage tank are funnel-shaped, and the electrode plate is positioned in the middle of the dephosphorization tank.

Further, the electrode plates are alternately arranged in positive and negative poles.

Further, the electrode plate is a carbon steel plate or an iron plate or an aluminum plate.

Furthermore, the supporting frame is connected with the wall of the dephosphorization groove, and the electrode plate is connected with the supporting frame through clamping grooves.

Further, the distance between two adjacent electrode plates is 1-12cm.

Further, a baffle plate is arranged in the anaerobic water inlet tank, the baffle plate separates the inside of the anaerobic water inlet tank from a left water tank and a right water tank which are communicated with the bottom, the water inlet of the anaerobic water inlet tank and the water outlet of the anaerobic water inlet tank are respectively communicated with the left water tank and the right water tank, baffle plates are further arranged in the two-stage UASB, and the baffle plates are positioned on the upper parts of the two-stage UASB.

Further, all be provided with the mixer in anaerobic tank, the oxygen deficiency pond, still have the carbon source on the anaerobic tank and supply the pipe, aerobic tank and MBR pond all are provided with aeration components, and still be equipped with the biological bed that is attached with the microorganism in the aerobic tank, still be provided with MBR membrane group in the MBR pond, and be connected with mixed liquid return line between aerobic tank and the anaerobic tank.

Further, the advanced treatment unit comprises a denitrification deep bed filter, a fiber turntable filter and an ultraviolet disinfection canal which are sequentially connected, wherein an outlet end of the MBR pond is also connected with an intermediate pond, and an outlet end of the intermediate pond is respectively connected with an inlet end of the post-phosphorus removal device and an inlet end of the denitrification deep bed filter.

Further, the device also comprises a sludge treatment unit, wherein the sludge treatment unit comprises a sludge concentration tank and a sludge dewatering machine room which are sequentially connected, and a sludge return pipe is connected among the pretreatment unit, the front phosphorus removal device, the anaerobic unit, the biochemical treatment unit, the rear phosphorus removal device and the sludge concentration tank.

Further, a material tank, a sludge modification bin and a filter press which are sequentially connected are further arranged in the sludge dewatering machine room, and the outlet end of the sludge concentration tank is connected with the inlet end of the sludge modification bin.

The invention also provides a dephosphorization method based on the system, which comprises the following steps:

When the wastewater is high-concentration phosphorus-containing industrial wastewater, the wastewater is treated by a pretreatment unit to remove insoluble matters in the wastewater, and the wastewater A is discharged; the wastewater A is divided into two parts, one part enters an anaerobic unit through a first direct conveying pipeline, and the other part enters a front dephosphorization device through a water inlet pipe to remove phosphorus and discharge wastewater B; the wastewater B enters an anaerobic unit, ammonia nitrogen of the wastewater in the anaerobic unit is nitrified, organic matters in the wastewater are degraded, COD content in the wastewater is reduced, and wastewater C is discharged; the wastewater C enters a biochemical treatment unit, ammonia nitrogen in the wastewater is further nitrified, organic matters in the wastewater are degraded, and wastewater D is discharged; the wastewater D is treated by an advanced treatment unit and is discharged after reaching the standard;

When the wastewater is low-concentration phosphorus-containing industrial wastewater, the wastewater is treated by a pretreatment unit to remove insoluble matters in the wastewater, and the wastewater A is discharged; the wastewater A enters a biochemical treatment unit through a second direct conveying pipeline to nitrify ammonia nitrogen in the wastewater, degrade organic matters in the wastewater, reduce COD content in the wastewater and discharge wastewater D; after the wastewater D is treated by the biochemical treatment unit, the wastewater is divided into two parts, one part is dephosphorized by the post-dephosphorization unit, and the dephosphorized wastewater enters the advanced treatment unit; and part of wastewater directly enters the advanced treatment unit, and the wastewater enters the advanced treatment unit for treatment and then is discharged after reaching the standard.

In the invention, the COD concentration in the high-concentration phosphorus-containing industrial wastewater is more than 3000mg/L, the total phosphorus concentration is more than 40mg/L, the COD concentration in the low-concentration phosphorus-containing industrial wastewater is less than 500mg/L, and the total phosphorus concentration is less than 8mg/L.

When the COD concentration in the water body is 500 mg/L-3000 mg/L and the total phosphorus concentration is 8 mg/L-40 mg/L, both processes can be carried out.

Further, the wastewater treatment by the pretreatment unit means that the industrial wastewater is directly connected with the pretreatment tank by a tap water pipe network, the wastewater to be treated is directly sent into the pretreatment tank by the tap water pipe network, and overflows into the regulating tank directly through an overflow port or an overflow pipeline after pretreatment in the pretreatment tank, the PH value of the industrial wastewater is regulated to 9-11 in the regulating tank, and the regulated wastewater is sent into the primary sedimentation tank for preliminary sedimentation, and the wastewater A is discharged.

Further, the wastewater A enters a dephosphorization tank through a water inlet pipe, dephosphorizes through an electrode plate, and flows into a drainage tank for precipitation, and then is discharged through a water outlet pipe to obtain wastewater B.

In the invention, when electrochemical dephosphorization is carried out, the current density is 40-60mA/cm ², and the electrolysis time is 15-30min.

Further, in the anaerobic unit, waste water enters an anaerobic water inlet tank, is pumped into a secondary UASB tank through an anaerobic lifting pump, organic matters in the waste water are degraded in the secondary UASB tank, COD content in the waste water is reduced, waste water overflows after being treated by the secondary UASB tank and enters an anaerobic sedimentation tank, and waste water is sedimentated in the anaerobic sedimentation tank, and waste water C is discharged.

Further, ammonia nitrogen and degradation organic matters are removed from the wastewater C in the anoxic tank, the wastewater after being treated in the anoxic tank overflows into the aerobic tank, the air blower supplies air to the aeration component in the aerobic tank, the aeration component starts aeration, the biological bed attached with microorganisms in the aerobic tank can degrade the organic matters in the wastewater and nitrify the ammonia nitrogen, the wastewater after being treated in the aerobic tank overflows into the MBR tank, the ammonia nitrogen and COD are further removed from the MBR membrane group in the MBR tank, the wastewater after being treated in the MBR tank is sent into the middle water tank, and the wastewater D is discharged.

Further, the wastewater in the aerobic tank flows back to the anoxic tank through the mixed liquid return pipeline, so that the wastewater which is not completely treated flows back to the anoxic tank for circulation treatment.

Further, the wastewater entering the advanced treatment unit is directly sent into a denitrification deep bed filter, a carbon source or a flocculating agent is added into the denitrification deep bed filter, nitrate nitrogen is further removed through the denitrification deep bed filter and is converted into nitrogen, the finally treated wastewater enters a fiber turntable filter to remove SS, and the wastewater reaches the standard after being disinfected by an ultraviolet disinfection channel and is discharged.

Further, the carbon source is selected from one or more of sodium acetate, methanol and glucose, and the flocculant is selected from one or two of PAC flocculant and ferric salt.

In the technical scheme of the invention, sediment in a primary sedimentation tank, a dephosphorization tank, a drainage tank, a two-stage UASB (anaerobic sludge blanket), an anaerobic sedimentation tank, an anoxic tank and an MBR (membrane bioreactor) tank can be fed into a sludge concentration tank through a reflux pump on a sludge conveying pipe and fed into a sludge modification bin, and simultaneously, a modifier in a material tank is conveyed into the sludge modification bin, so that the sludge entering the sludge modification bin fully reacts with the modifier, and after the sludge reacts in the sludge modification bin, the sludge in the sludge modification bin is fed into a filter press, and is directly discharged after being subjected to filter pressing and dehydration through the filter press.

Further, one or two of lime and PAM are used as modifiers.

The beneficial effects of the invention are as follows:

According to the invention, the electrode plates in the dephosphorization tank are adopted to realize dephosphorization, so that any medicament (physical medicament and chemical medicament) is not required to be added in the dephosphorization treatment process of the wastewater, the environment friendliness is high, thorough dephosphorization can be realized, and the sludge production amount is greatly reduced; meanwhile, the pretreatment unit, the preposed dephosphorization device, the anaerobic unit, the biochemical treatment unit and the postposed dephosphorization device are matched, so that the industrial wastewater with different concentrations can realize the system dephosphorization treatment, the industrial wastewater can not only realize dephosphorization through the system when being required to be treated, but also realize the advanced deslagging in the earlier stage and the advanced treatment of the wastewater after dephosphorization in the later stage, the treatment of the domestic wastewater is more systematic, and the treated wastewater can be directly discharged on the ground surface.

Through set up the solenoid valve on the inlet tube of a plurality of electrochemistry dephosphorization units, make every electrochemistry dephosphorization unit's inflow can obtain accurate control, not only can realize total phosphorus and get rid of multistage regulation and control, and can regulate and control the current density of electrode plate according to the inflow, make the dephosphorization more high-efficient, thoroughly.

Drawings

The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the principles of the invention.

FIG. 1 is a system diagram of an electrochemical dephosphorization system for industrial wastewater provided by the invention;

FIG. 2 is a system diagram of a preprocessing unit;

FIG. 3 is a system diagram of a front-end dephosphorization apparatus;

FIG. 4 is a schematic view of the structure of the front-end dephosphorization apparatus;

FIG. 5 is a top view of the front-end dephosphorization apparatus;

FIG. 6 is a system diagram of an anaerobic unit;

FIG. 7 is a system diagram of a biochemical processing unit;

FIG. 8 is a system diagram of a depth processing unit;

Fig. 9 is a system diagram of a sludge treatment unit.

The reference numerals and corresponding part names in the drawings:

1. The device comprises a pretreatment unit, 2, an anaerobic unit, 3, a biochemical treatment unit, 4, a front phosphorus removal device, 5, a rear phosphorus removal device, 6, a deep treatment unit, 7, a sludge treatment unit, 8, a first direct conveying pipeline, 9 and a second direct conveying pipeline;

100. the device comprises a pretreatment tank, 101, an adjusting tank, 102, a coarse treatment grid, 103, a stirring tank, 104, a buffer tank, 105, a water inlet pipe, 106, a drain pipe, 107, a discharge pipe, 108, a primary sedimentation tank, 109, a dosing pipe, 110 and a feeding pipe;

200. two-stage UASB (upflow anaerobic sludge blanket) 201, an anaerobic water inlet tank 202, an anaerobic sedimentation tank 203, a baffle plate 204, a left water tank 205, a right water tank 206 and a baffle plate;

300. An anaerobic tank 301, an anoxic tank 302, an aerobic tank 303, an MBR tank 304, a stirrer 305, a carbon source supplementing pipe 306, an aeration component 307, a biological bed attached with microorganisms 308, an MBR membrane group 309, a mixed liquor return pipeline 310, an intermediate water tank 311 and a blower;

400. The device comprises a dephosphorization tank 401, a drainage tank 402, a water inlet pipe 403, a sludge discharge pipe 404, a supporting frame 405, an electrode plate 406, a water outlet pipe 407, a blow-down pipe 408, a PLC automatic control cabinet 409 and a power distribution cabinet;

600. a denitrification deep bed filter, 601, a fiber turntable filter, 602 and an ultraviolet disinfection canal;

700. a sludge concentration tank 701, a sludge return pipe 702, a material tank 703, a sludge modification bin 704 and a filter press.

Detailed Description

The present invention will be described in further detail with reference to the drawings and embodiments. It is to be understood that the specific embodiments described herein are merely illustrative of the substances, and not restrictive of the invention. It should be further noted that, for convenience of description, only the portions related to the present invention are shown in the drawings.

In addition, the embodiments of the present invention and the features of the embodiments may be combined with each other without collision. The present invention will be described in detail below with reference to the accompanying drawings in conjunction with embodiments.

As shown in fig. 1 to 7, the electrochemical dephosphorization system for industrial wastewater provided by the invention comprises a pretreatment unit 1, an anaerobic unit 2, a biochemical treatment unit 3, a front dephosphorization device 4, a rear dephosphorization device 5 and a deep treatment unit 6; the pretreatment unit 1 is used for removing insoluble impurities, particles, suspended solids and the like in industrial wastewater, adjusting the pH value of the industrial wastewater to a proper value and creating conditions for subsequent treatment; the anaerobic unit 2 is used for converting macromolecular refractory organic matters into micromolecular organic matters which are easy to be degraded by microorganisms and degrading most insoluble organic matters into soluble matters; the front-end dephosphorization device 4 mainly aims at high-concentration industrial wastewater, the rear-end dephosphorization device 5 mainly aims at low-concentration industrial wastewater, and the front-end dephosphorization device 4 and the rear-end dephosphorization device 5 are not used at the same time, but are selected for industrial wastewater with different concentrations; the advanced treatment unit 6 is used for further removing nitrogen from the dephosphorized, deaminated and denitrified wastewater so as to ensure that the treated wastewater can be directly discharged.

The pretreatment unit 1, the preposed dephosphorization device 4, the anaerobic unit 2, the biochemical treatment unit 3 and the postposed dephosphorization device 5 are sequentially connected, and a first direct conveying pipeline 8 is also connected between the pretreatment unit 1 and the anaerobic unit 2. When the high-concentration industrial wastewater is required to be treated, the wastewater can sequentially pass through the pretreatment unit 1, the pre-phosphorus removal device 4, the anaerobic unit 2, the biochemical treatment unit 3 and the advanced treatment unit 6.

The pretreatment unit 1 comprises a pretreatment tank 100 and a regulating tank 101, wherein the pretreatment tank 100 and the regulating tank 101 can be of an integrated structure or a split structure, a tap water pipe network for discharging industrial wastewater is directly connected with the pretreatment tank 100, so that the wastewater to be treated is directly fed into the pretreatment tank 100 through the tap water pipe network, and after pretreatment in the pretreatment tank 100, the wastewater is directly overflowed into the regulating tank 101 through an overflow port or an overflow pipeline, and the pH value of the industrial wastewater is regulated in the regulating tank 101.

The front phosphorus removal device 4 and the rear phosphorus removal device 5 both comprise electrochemical phosphorus removal units; when the device is used for treating industrial wastewater with higher concentration, partial organic matters can be removed by flocculation by the front-end dephosphorization device 4, but the follow-up carbon source is not insufficient due to higher concentration of the organic matters; when the device is used for treating industrial wastewater with lower organic matters, due to lower concentration of the organic matters, if the device adopts the front phosphorus removal, part of the organic matters can be removed through flocculation, so that the subsequent carbon source is insufficient, and therefore, the device needs to adopt the rear phosphorus removal device 5 for rear phosphorus removal. Specifically, the electrochemical dephosphorization unit includes the dephosphorization groove 400, and the dephosphorization groove 400 entrance end in the leading dephosphorization device 4 is connected with the exit end of equalizing basin 101, and the dephosphorization groove 400 entrance end in the rearmounted dephosphorization device 5 is connected with the MBR pond 303 exit end in the biochemical treatment unit 3, and the engineering plastics material that dephosphorization groove 400 cell wall is 4-6mm, and the thickness of dephosphorization groove 400 cell wall can specifically be adjusted according to actual conditions, and still installs electrode plate 405 in the dephosphorization groove 400, and when waste water entered into in the dephosphorization groove 400, electrode plate 405 all can contact with waste water. Taking the scale of 10m3/h of the dephosphorization tank 400 as an example, the area of the dephosphorization tank 400 for installing the electrode plate 405 is rectangular with the size of 600-1000mm, at this time, the thickness of the electrode plate 405 is 2-4mm, and the length of the electrode plate 405 is 400-800mm, but the specific thickness and specific size of the electrode plate 405 can be adjusted according to the size, capacity, wastewater property, etc. of the dephosphorization tank 400 when the electrode plate 405 is designed.

The anaerobic unit 2 comprises an anaerobic water inlet tank 201, a two-stage UASB200 and an anaerobic sedimentation tank 202 which are sequentially connected; the bottom of the anaerobic water inlet tank 201 is a slope, so that sediment in the anaerobic water inlet tank 201 can be discharged completely in the later period; the outlet end of the anaerobic water inlet tank 201 is communicated with the middle part of the two-stage UASB200, the two-stage UASB200 is two UASB tanks, the two UASB tanks are of an integrated structure, the two UASB tanks are in overflow communication, the outlet end of the first direct conveying pipeline 8 and the outlet end of the front-value dephosphorization unit are both communicated with the middle part of the first UASB tank, and the second UASB tank is communicated with the anaerobic sedimentation tank 202 after overflow; and the two UASB tanks are respectively provided with an anaerobic circulating pump, and the flow rate of circulating water can be improved through the anaerobic circulating pumps, so that the purpose of full reaction is achieved.

The biochemical treatment unit 3 comprises an anoxic tank 301, an aerobic tank 302 and an MBR tank 303, wherein the anoxic tank 301, the aerobic tank 302 and the MBR tank 303 are sequentially communicated in an overflow mode, the anoxic tank 301 is used for removing ammonia nitrogen and degrading organic matters, the aerobic tank 302 degrades the organic matters, nitrifies the ammonia nitrogen, and the MBR tank 303 further removes the ammonia nitrogen and COD.

Specifically, one end of the first direct conveying pipeline 8 is connected with the regulating tank 101, the other end of the first direct conveying pipeline 8 is connected with the anaerobic water inlet tank 201, so that part of wastewater treated by the regulating tank 101 can directly enter the anaerobic water inlet tank 201, and the other part of wastewater treated by the regulating tank 101 can enter the anaerobic water inlet tank 201 after dephosphorization treatment in the pre-dephosphorization device 4, and is suitable for treating high-concentration wastewater at the moment; meanwhile, the biochemical treatment unit 3 further comprises an anaerobic tank 300, the anaerobic tank 300 is positioned at the front end of the inlet of the anoxic tank 301, a second direct conveying pipeline 9 is further connected between the pretreatment unit 1 and the anaerobic tank 300, and the inlet end of the second direct conveying pipeline 9 can be directly connected to the first direct conveying pipeline 8 in parallel, so that wastewater can enter the anaerobic tank 300 first and then enter the anoxic tank 301, and the biochemical treatment unit is suitable for treating low-concentration industrial wastewater.

The pretreatment tank 100 in the pretreatment unit 1 can be used for pretreating low-concentration industrial wastewater or high-concentration industrial wastewater conveyed by a tap water pipe network to remove dregs, suspended matters and the like in the low-concentration industrial wastewater or the high-concentration industrial wastewater; the pretreated wastewater enters an adjusting tank 101 to adjust the PH value of the industrial wastewater.

When the wastewater is high-concentration industrial wastewater, a part of the pretreated high-concentration industrial wastewater enters the dephosphorization tank 400 in the pre-dephosphorization device 4, at the moment, the electrode plate 405 is electrified, the electrode plate 405 is taken as an iron material for example, an oxidation-reduction system is formed in the dephosphorization tank 400 by utilizing the electrode plate 405, a large amount of Fe ²⁺、Fe³⁺ ions are generated at the anode of the electrode plate 405, and the high-molecular hydroxyl polymer Fe _m(H₂O)×(OH)_n(3_m-n taking the ions as a core is higher than the commonly used flocculating agent such as polymeric ferric sulfate by a plurality of times or tens of times in activity and specific surface area. When the iron-containing ionic liquid is fully mixed with the wastewater, moderate oxygenation aeration is given, so that Fe ²⁺ in the wastewater can be pushed to be converted into Fe ³⁺, and the pH value of the wastewater can be changed. Meanwhile, PO ₂ ^3-、PO₃ ^3-、P₂O₇ ^4- plasma in the phosphorus-containing wastewater is oxidized into orthophosphate ions PO ₄ ^3- in the system, fe ²⁺、Fe³⁺ reacts with PO ₄ ^3- in water to generate indissolvable Fe ₃(PO₄)₂ and FePO ₄, and the high-activity iron core high-molecular hydroxyl polymer in the system has strong adsorption, coagulation, capturing and bridging capabilities, and captures and colloid particles rapidly and thoroughly, so that thorough phosphorus removal of wastewater is realized.

The wastewater after dephosphorization and the other part of wastewater after pretreatment are jointly fed into an anaerobic water inlet tank 201 for buffering, the buffered high-concentration industrial wastewater is fed into a two-stage UASB200, the two-stage UASB200 utilizes the anaerobic decomposition process of organic matters to convert macromolecular refractory organic matters into micro-molecular organic matters which are easy to be degraded by microorganisms, most of insoluble organic matters are degraded into soluble matters, carbon sources are consumed simultaneously, COD (chemical oxygen demand) is reduced, conditions are created for subsequent aerobic treatment, the wastewater enters an anaerobic sedimentation tank 202 for sedimentation after the two-stage UASB200 treatment, ammonia nitrogen and degraded organic matters are removed in an anoxic tank 301, the wastewater after the anoxic tank 301 is fed into an aerobic tank 302 for degrading the organic matters, the ammonia nitrogen is nitrified, the ammonia nitrogen and COD are further removed in an MBR tank 303 after the treatment, and finally the wastewater is fed into a deep treatment unit 6.

When the wastewater is low-concentration industrial wastewater, the pretreated high-concentration industrial wastewater directly enters the anaerobic tank 300, overflows from the anaerobic tank 300 to the anoxic tank 301, the aerobic tank 302 and the MBR tank 303 in sequence, macromolecular refractory organic matters in the wastewater are converted into micromolecular organic matters which are easy to be degraded by microorganisms, a carbon source in the wastewater is consumed, COD (chemical oxygen demand) of the wastewater is reduced, ammonia nitrogen in the wastewater is removed, the wastewater is sent into the anoxic tank 301 to remove the ammonia nitrogen and the degraded organic matters, the wastewater after being treated in the anoxic tank 301 enters the aerobic tank 302 to degrade the organic matters, nitrifies the ammonia nitrogen, enters the MBR tank 303 after being treated to further remove the ammonia nitrogen and COD, and is sent into the dephosphorizing tank 400 in the post-dephosphorizing device 5 after being treated, at this time, the electrode plate 405 is electrified, the electrode plate 405 is used as an iron material for example to form a redox system in the dephosphorizing tank 400, the anode of the electrode plate 405 generates a large amount of Fe ²⁺、Fe³⁺ ions, and the macromolecular hydroxyl polymer Fe _m(H₂O)×(OH)_n(3_m-n taking the ions as a core), and the specific activity of the macromolecular polymer is even ten times higher than that of the flocculant such as the conventional ferric sulfate. When the iron-containing ionic liquid is fully mixed with the wastewater, moderate oxygenation aeration is given, so that Fe ²⁺ in the wastewater can be pushed to be converted into Fe ³⁺, and the pH value of the wastewater can be changed. Meanwhile, PO ₂ ^3-、PO₃ ^3-、P₂O₇ ^4- plasma in the phosphorus-containing wastewater is oxidized into orthophosphate ions PO ₄ ^3- in the system, fe ²⁺、Fe³⁺ reacts with PO ₄ ^3- in water to generate indissolvable Fe ₃(PO₄)₂ and FePO ₄, and the high-activity iron core high-molecular hydroxyl polymer in the system has strong adsorption, coagulation, capturing and bridging capabilities, and captures and colloid particles rapidly and thoroughly, so that thorough phosphorus removal of the wastewater is realized, and finally the wastewater is sent into the deep treatment unit 6.

In some embodiments, a coarse treatment grid 102 is disposed in the pretreatment tank 100, the wastewater can flow to the outlet end of the pretreatment tank 100 through the coarse treatment grid 102, insoluble impurities, particles, suspended solids and the like in the wastewater are intercepted on the coarse treatment grid 102, and the intercepted insoluble impurities, particles, suspended solids and the like are lifted out of the pretreatment tank 100 along with the operation of the coarse treatment grid 102, so as to realize the preliminary pretreatment of the wastewater; the regulating tank 101 is provided with a grading circulation reaction device, the grading circulation reaction device is provided with a water inlet pipe 105 and a plurality of water outlet pipes 106, the outlet heights of the water outlet pipes 106 are different, the inlet end of the water inlet pipe 105 and the outlet ends of the water outlet pipes 106 extend into the regulating tank 101, so that the grading circulation reaction device can directly adopt waste water in the pretreatment tank 100 when materials are configured, water taking is convenient, a pipeline system is simpler, and multi-point water outlet is realized through the cooperation of the water outlet pipes 106, and the regulation in the regulating water MBR tank 303 is more convenient and rapid.

In some embodiments, the staged circulation reaction device includes a stirring tank 103 and a buffer tank 104 which are sequentially connected, the stirring tank 103 is provided with a pipeline for adding slaked lime or sodium hydroxide, the regulating tank 101 is also provided with two circulation pumps, the two circulation pumps are connected in parallel at the inlet end of the water inlet pipe 105, and the inlet end of the circulation pump and the outlet end of the circulation pump are both provided with ball valves; the upper end of the stirring tank 103 is communicated with the buffer tank 104, so that the liquid entering the buffer tank 104 is the supernatant liquid in the stirring tank 103, and the inlet ends of the plurality of drain pipes 106 are connected in parallel with the upper end of the buffer tank 104 together, so that the supernatant liquid in the buffer tank 104 flows back to the regulating tank 101 through the drain pipes 106. In the present invention, in order to facilitate the discharge of the precipitate in the agitation tank 103 and the buffer tank 104, an evacuation pipe may be provided at the bottom of the agitation tank 103 and the bottom of the buffer tank 104, and the outlet end of the evacuation pipe may be connected to any one or more of the drainage pipes 106, so that the precipitate may be directly discharged into the regulating reservoir 101. For ease of control, ball valves are installed at the parallel ends of both the two evacuation tubes and the plurality of drain pipes 106.

In some embodiments, the pretreatment unit 1 further includes a primary sedimentation tank 108 connected to the outlet end of the adjustment tank 101, the bottom of the primary sedimentation tank 108 is funnel-shaped, an overflow weir is provided at the inlet of the primary sedimentation tank 108, and the water in the adjustment tank 101 overflows through the overflow weir before entering the primary sedimentation tank 108, so as to intercept suspended matters on the surface of the wastewater; the primary sedimentation tank 108 is also provided with a feeding pipe 110 for feeding aluminum salt or ferric salt, so that the sedimentation effect in the primary sedimentation tank 108 is better.

In some embodiments, the electrochemical dephosphorization unit further comprises a drainage tank 401, and the dephosphorization tank 400 and the drainage tank 401 may be in an integral structure or a split structure. When the dephosphorization tank 400 and the drainage tank 401 are in an integrated structure, a tank body can be directly adopted, a partition plate is arranged in the tank body to divide the interior of the tank body into the dephosphorization tank 400 and the drainage tank 401 which are distributed left and right, at the moment, the height of the dephosphorization tank 400 is equal to that of the drainage tank 401, the bottom of the dephosphorization tank 400 is level with the bottom of the drainage tank 401, the width of the dephosphorization tank 400 is 200-400mm, and the upper end of the partition plate is lower than the upper end of the shell or a water passing hole is formed in the upper end of the partition plate, so that the upper end of the dephosphorization tank 400 is communicated with the upper end of the drainage tank 401; when the dephosphorization tank 400 and the drainage tank 401 are in a split structure, the upper end of the dephosphorization tank 400 and the upper end of the drainage tank 401 can be communicated with a water passing pipe or a water passing tank, and in this case, the treated water in the dephosphorization tank 400 can overflow into the drainage tank 401. In the present invention, the dephosphorization tank 400 and the drainage tank 401 are preferably formed integrally.

The support frame 404 is installed in the dephosphorization tank 400, a plurality of electrode plates 405 in the dephosphorization tank 400 are provided, a certain interval is provided between the plurality of electrode plates 405, and the plurality of electrode plates 405 are commonly installed on the support frame 404, so that the plurality of electrode plates 405 are commonly supported in the dephosphorization tank 400 through the support frame 404, and when wastewater enters the dephosphorization tank 400, the plurality of electrode plates 405 can be contacted with the wastewater.

In some embodiments, the dephosphorization tank 400 is further provided with a sludge discharge pipe 403 and a water inlet pipe 402, the water inlet pipe 402 in the front dephosphorization device 4 is connected with the outlet end of the primary sedimentation tank 108, the water inlet pipe 402 in the rear dephosphorization device 5 is connected with the outlet end of the MBR tank 303, and the sludge discharge pipe 403 is used for discharging colloidal particles and precipitated sludge generated after dephosphorization in the dephosphorization tank 400 out of the dephosphorization tank 400; meanwhile, a water outlet pipe 406 is further arranged on the water drainage tank 401, the water outlet pipe 406 is used for directly discharging water overflowed into the water drainage tank 401 after the dephosphorization treatment to the outside of the water drainage tank 401, the water outlet pipe 406 in the front dephosphorization device 4 is connected with the anaerobic water inlet tank 201, and the water outlet pipe 406 in the rear dephosphorization device 5 is connected with the deep treatment unit 6. Through the synergistic effect of the sludge discharge pipe 403, the water inlet pipe 402 and the water outlet pipe 406, the wastewater is discharged after dephosphorization, and the colloidal particles generated by dephosphorization are discharged without manual participation, so that the dephosphorization of the wastewater is more convenient.

In some embodiments, the height of the water outlet pipe 406 is equal to the height of the lower end of the electrode plate 405, so as to facilitate the discharge of the wastewater in the water discharge tank 401.

In some embodiments, the water inlet pipe 402 and the sludge discharge pipe 403 are both positioned at the bottom of the dephosphorization tank 400, and the water inlet pipe 402 is connected in parallel to the sludge discharge pipe 403, so that the water inlet pipe 402 and the sludge discharge pipe 403 together form a three-way pipe, and the pipeline system on the dephosphorization tank 400 is simpler; meanwhile, as the water inlet pipe 402 is positioned at the bottom of the dephosphorization tank 400, the wastewater can not directly contact the electrode plate 405 when entering the dephosphorization tank 400, so that the sediment in the wastewater can not be attached to the electrode plate 405 as much as possible, and the electrolysis effect is ensured.

In some embodiments, the bottom of the drainage tank 401 is further provided with a blow-down pipe 407, so that the wastewater overflowed into the drainage tank 401 can be precipitated in the drainage tank 401, after precipitation, the upper wastewater in the drainage tank 401 can be directly discharged through a water outlet pipe 406, and the precipitate generated by precipitation can be directly discharged through the blow-down pipe 407, so that the wastewater after the dephosphorization treatment is precipitated in the drainage tank 401.

In some embodiments, the sludge discharge pipe 403, the water inlet pipe 402, the water outlet pipe 406 and the emptying pipe 407 are all provided with electromagnetic valves, so as to prevent the sludge discharge pipe 403 from depositing during sludge discharge or colloidal particles generated during dephosphorization from entering the water inlet pipe 402, and the electromagnetic valves on the water inlet pipe 402 are preferentially installed at the outlet end of the water inlet pipe 402. Specifically, the invention can be provided with the PLC automatic control cabinet 408 and the power distribution cabinet 409, the power distribution cabinet 409 supplies power to the PLC automatic control cabinet 408, the electrode plate 405 and the electromagnetic valve respectively, the PLC automatic control cabinet 408 not only controls the opening and closing of the electromagnetic valve on the sludge discharging pipe 403, the water inlet pipe 402, the water outlet pipe 406 and the blow-down pipe 407, but also controls the electrode plate 405 to be electrified or powered off, so that the automatic control is realized in the wastewater dephosphorization process, and the wastewater dephosphorization process is not needed to be manually participated, so that the wastewater dephosphorization is simpler and more convenient. Meanwhile, by arranging the electromagnetic valve on the water inlet pipe 402, the amount of wastewater entering the dephosphorization tank 400 is effectively controlled, so that the voltage of the electrode plate 405 can be controlled according to the amount of wastewater entering the dephosphorization tank 400 in the dephosphorization process, and the efficient dephosphorization is realized.

In some embodiments, the electrochemical phosphorus removal unit is a plurality of electrochemical phosphorus removal units arranged in a rectangular array, e.g., 8 electrochemical phosphorus removal units and 8 electrochemical phosphorus removal units are arranged in a 2x 4 arrangement. In order to reduce the occupied area of the invention, a plurality of electrochemical phosphorus removal units can be arranged without interval between two adjacent electrochemical phosphorus removal units; meanwhile, when the electrochemical phosphorus removal units are multiple, the outlet ends of the sludge discharge pipes 403 on the electrochemical phosphorus removal units are connected in parallel, the inlet ends of the water inlet pipes 402 on the electrochemical phosphorus removal units are connected in parallel, the outlet ends of the water outlet pipes 406 on the electrochemical phosphorus removal units are connected in parallel, and the outlet ends of the blow-down pipes 407 on the electrochemical phosphorus removal units are connected in parallel, so that the electrochemical phosphorus removal units can supplement wastewater which is not phosphorus removed together or discharge sediment together or discharge wastewater after phosphorus removal together.

In some embodiments, the bottoms of the dephosphorization tank 400 and the drainage tank 401 are funnel-shaped, so that the sediment generated in the dephosphorization process and the sediment generated in the drainage tank 401 after dephosphorization can be collected automatically by gravity and then discharged in a concentrated manner, and the sediment in the dephosphorization tank 400 and the drainage tank 401 is more thorough in discharge; meanwhile, the electrode plate 405 is located in the middle of the dephosphorization tank 400, and the sediment generated in the dephosphorization process of the wastewater can fall to the bottom of the dephosphorization tank 400 through dead weight, so that the sediment generated in the dephosphorization process is always separated from the electrode plate 405, the influence of the sediment generated in the dephosphorization process on the quantity of ions generated in the electrode plate 405 is avoided, and the dephosphorization effect is effectively ensured.

In some embodiments, the electrode plates 405 are alternately arranged with positive electrodes and negative electrodes, and in order to prevent the electrode plates 405 from hardening and passivating, the electrode plates 405 may be further powered by a pulse power source, and the positive electrodes and the negative electrodes of the electrode plates 405 may be switched according to a set frequency, so that the electrode plates 405 can generate enough electric ions when electrified, and the amount of electric ions generated by the electrode plates 405 is ensured.

In some embodiments, the electrode plate 405 is a carbon steel plate, or an iron plate, or an aluminum plate, and the specific material of the electrode plate 405 may be adjusted according to actual requirements.

In some embodiments, the supporting frame 404 is connected with the wall of the dephosphorizing tank 400, and the electrode plate 405 is connected with the supporting frame 404 by a clamping groove, in particular, the dephosphorizing tank 400 and the supporting frame 404 can be prefabricated by a clamping groove structure in the production and processing process, so that the clamping groove structure is not required to be separately installed on the supporting frame 404 and the wall of the dephosphorizing tank 400, the clamping groove on the wall of the supporting frame 404 can be clamped when the supporting frame 404 is installed, and the clamping groove on the wall of the supporting frame 400 can be clamped when the electrode plate 405 is installed, so that the electrode plate 405 can be installed and disassembled more conveniently.

In some embodiments, the spacing between two adjacent electrode plates 405 is 1-12cm, and the specific size of the spacing between two adjacent electrode plates 405 may be adjusted by calculation, adjustment, etc. according to the thickness of the electrode plates 405, the concentration of wastewater, the flow rate of wastewater, etc.

In some embodiments, the steel crawling ladder and the steel guardrails can be arranged on the same side of the electrochemical dephosphorization units, so that workers can conveniently inspect and overhaul at any time in the wastewater dephosphorization treatment process.

In some embodiments, a baffle 203 is disposed in the anaerobic water inlet tank 201, a certain gap is formed between the lower end of the baffle 203 and the anaerobic water inlet tank 201, so that the baffle 203 makes the anaerobic water inlet tank 201 be a left water tank 204 and a right water tank 205 which are communicated through the bottom, a water inlet of the anaerobic water inlet tank 201 is communicated with the left water tank 204, a water outlet of the anaerobic water inlet tank 201 is communicated with the right water tank 205, and when wastewater enters the anaerobic water inlet tank 201, the baffle 203 can reduce the area of disturbance generated when the wastewater enters the anaerobic water inlet tank 201; the waste water in the anaerobic water inlet tank 201 can be lifted and fed into the two-stage UASB200 by a lifting pump, and a check valve is arranged at the outlet end of the lifting pump to prevent the waste water from flowing back; the baffle plates 206 are further arranged in the two-stage UASB200, so that wastewater in the two-stage UASB200 can be intercepted by the baffle plates 206 when overflowed, and insoluble impurities, particles, suspended solids and the like in the two-stage UASB200 can be intercepted and deposited at the bottom of the two-stage UASB200, so that the wastewater is deposited.

In some embodiments, the anaerobic tank 300 and the anoxic tank 301 are both provided with a stirrer 304, the stirrer 304 is a submersible stirrer 304, the anaerobic tank 300, the anoxic tank 301 and the MBR tank 303 can be in an integrated structure, specifically, two partition boards are arranged in one large-scale water MBR tank, the two partition boards divide the large-scale water MBR tank into the anaerobic tank 300, the anoxic tank 301 and the MBR tank 303, of course, water holes are formed in the two partition boards to ensure the communication among the anaerobic tank 300, the anoxic tank 301 and the MBR tank 303, the anaerobic tank 300 is communicated with the primary sedimentation tank 108, the anoxic tank 301 is simultaneously connected with the anaerobic sedimentation tank 202, so that the wastewater treated by the primary sedimentation tank 108 can enter the anoxic tank 301 after entering the anaerobic tank 300, and the wastewater treated by the anaerobic sedimentation tank 202 can also enter the anoxic tank 301 directly without passing through the anaerobic tank 300, so that the industrial wastewater with different concentrations can be treated by selecting different procedures, and the anaerobic tank 300 and the anoxic tank 301 are uniformly distributed with high ammonia nitrogen and nitrogen in the anoxic tank 301 by stirring of the stirrer 304; meanwhile, a chemical supplementing pipe is also arranged on the anaerobic tank 300, so that the wastewater is convenient to add a regulator into the anaerobic tank 300 in the treatment process, and specifically, the regulator is a carbon source such as sodium acetate, and the outlet end of the chemical supplementing pipe can extend to the bottom of the anaerobic tank 300 and can be directly positioned above the liquid level in the anaerobic tank 300.

Aeration components 306 can be arranged in the aerobic tank 302 and the MBR tank 303, the outlet ends of aeration pipes in the aeration components 306 are positioned at the bottom of the aerobic tank 302 or the bottom of the MBR tank 303, a blower 311 for supplying air to the aeration components 306 can be arranged, and fixing frames can be arranged in the aerobic tank 302 and the MBR tank 303 for installing the aeration components 306, so that the upper ends of the aeration components 306 can be arranged on the fixing frames, and the installation of the aeration components 306 is more stable. By arranging the aeration component 306 in the aerobic tank 302 and the MBR tank 303, the particulate matters entering the aerobic tank 302 and the MBR tank 303 can be aerated to improve the efficiency of degrading organic matters in the wastewater of the biological bed 307 attached with microorganisms and nitrifying ammonia nitrogen.

The aerobic tank 302 is also internally provided with a biological bed 307 attached with microorganisms, the biological bed 307 attached with microorganisms can degrade organic matters in the wastewater and nitrify ammonia nitrogen, the MBR tank 303 is also internally provided with an MBR membrane group 308, and the MBR membrane group 308 further removes ammonia nitrogen and COD; a mixed liquid backflow pipeline 309 is connected between the aerobic tank 302 and the anaerobic tank 300, a backflow pump is further installed on the mixed liquid backflow pipeline 309, and a butterfly valve and a check valve can be further arranged on the mixed liquid backflow pipeline 309, so that wastewater in the aerobic tank 302 can flow back into the anoxic tank 301 through the mixed liquid mixed flow pipeline, and wastewater which is thoroughly untreated and flows back into the anoxic tank 301 for circulation treatment.

In some embodiments, the outlet end of the MBR tank 303 is further connected to an intermediate water tank 310, the outlet end of the intermediate water tank 310 is connected to the inlet end of the post-phosphorus removal device 5, the intermediate water tank 310 can be used for temporary storage of wastewater to be post-phosphorus removed or wastewater to be removed by the denitrification deep bed filter 600 through the intermediate water tank 310; the water inlet pipe 402 of the dephosphorization tank 400 in the rear dephosphorization device 5 is connected in parallel with the outlet end of the middle water tank 310, and a lifting pump is also arranged in the middle water tank 310, so that when the water level of the middle water tank 310 is low, the use of the dephosphorization tank 400 and the denitrification deep bed filter 600 can be met through the lifting of the lifting pump, and the outlet end of the middle water tank 310 is simultaneously connected in parallel with the inlet end of the denitrification deep bed filter 600.

As shown in fig. 8, the advanced treatment unit 6 includes a denitrification deep bed filter 600, a fiber turntable filter 601 and an ultraviolet disinfection canal 602 which are sequentially connected, wherein the fiber turntable filter 601 and the ultraviolet disinfection canal are sequentially connected at the water outlet end of the denitrification deep bed filter 600, so that the wastewater after further denitrification in the denitrification deep bed filter 600 is discharged after removing SS through the fiber turntable filter 601 and then is subjected to ultraviolet disinfection through the ultraviolet disinfection canal 602, and the wastewater after treatment through the phosphorus removal system provided by the invention can be directly discharged. It should be noted that the fiber rotary disc filter 601 may be replaced by an artificial wetland.

In some embodiments, as shown in fig. 9, the invention further includes a sludge treatment unit 7, where the sludge treatment unit 7 includes a sludge concentration tank 700 and a sludge dewatering machine room which are sequentially connected, specifically, the connection between the blow-down pipe 407 and the sludge discharge pipe 403 in the primary sedimentation tank 108, the front dephosphorization device 4 and the rear dephosphorization device 5, the two-stage UASB200, the anaerobic sedimentation tank 202, the anaerobic tank 300, the anoxic tank 301, the MBR tank 303 and the sludge concentration tank 700 may adopt a connection of a sludge return pipe 701, so that sediment, sludge and the like generated in the system can be sent into the sludge concentration tank 700 for concentrated concentration treatment, and then directly sent into the sludge dewatering machine room for dewatering treatment after concentration treatment, and finally dewatered sludge is obtained.

In order to ensure the sludge discharge effect of the primary sedimentation tank 108, the vent pipe 407 and the sludge discharge pipe 403 in the front dephosphorization device 4 and the rear dephosphorization device 5, the two-stage UASB200, the anaerobic sedimentation tank 202, the anaerobic tank 300, the anoxic tank 301 and the MBR tank 303, a reflux pump can be installed on the sludge reflux pipe 701, the equipment cost is saved, and the sludge reflux pipes 701 used for conveying the vent pipe 407 and the sludge discharge pipe 403 in the primary sedimentation tank 108, the front dephosphorization device 4 and the rear dephosphorization device 5, the two-stage UASB200, the anaerobic sedimentation tank 202, the anaerobic tank 300, the anoxic tank 301 and the MBR tank 303 can be connected in parallel and then connected with the sludge concentration tank 700, at this time, an electromagnetic valve can be installed on each sludge reflux pipe 701, and a reflux pump can be installed at the inlet end of the sludge concentration tank 700.

In some embodiments, the sludge dewatering machine room is further provided with a material tank 702, a sludge modification bin 703 and a filter press 704 which are sequentially connected, the outlet end of the sludge concentration tank 700 is connected with the inlet end of the sludge modification bin 703, the material tank 702 is internally used for storing a modifier, the modifier in the material tank 702 can be added into the sludge modification bin 703 according to requirements, so that the sludge fed into the sludge modification bin 703 through the sludge concentration tank 700 is modified after being reacted with the modifier, and is fed into the filter press 704 after being modified, and is subjected to filter pressing treatment, so that dewatered sludge is obtained, and the sludge after filter pressing and dewatering through the filter press 704 can be loaded and removed through a lifting machine.

When high-concentration industrial wastewater is required to be treated, the specific treatment steps are as follows:

Pretreatment unit 1: the high-concentration industrial wastewater is conveyed by a tap water pipe network and is firstly conveyed into the pretreatment tank 100, the high-concentration industrial wastewater is intercepted by the treatment coarse grille 102 after entering the pretreatment tank 100, undissolved impurities, particles, suspended solids and the like which float larger in the wastewater are intercepted in the treatment coarse grille 102, the wastewater normally flows, the undissolved impurities, particles, suspended solids and the like which are intercepted on the treatment coarse grille 102 are lifted by the treatment coarse grille 102 and directly discharged out of the pretreatment tank 100, and overflows into the regulating tank 101 along with the flowing of the wastewater in the pretreatment tank 100, a part of the wastewater in the regulating tank 101 is pumped into the stirring tank 103 by a circulating pump on a water inlet pipe 105, slaked lime or sodium hydroxide is added into the stirring tank 103, after the slaked lime or sodium hydroxide is dissolved, the supernatant in the stirring tank 103 enters the buffer tank 104 and is respectively discharged into the regulating tank 101 by a plurality of water discharging pipes 106, so that the pH value of the wastewater is regulated, the regulated wastewater is conveyed into the primary sedimentation tank 108 for preliminary sedimentation, and ferric salt or aluminum salt is added into the primary sedimentation tank 108 in the sedimentation process.

Front-mounted electric dephosphorization device: after the wastewater is precipitated in the primary sedimentation tank 108, the wastewater is divided into two parts, one part of wastewater is directly sent into the anaerobic water inlet tank 201 through the first direct conveying pipeline 8, the other part of wastewater is sent into the dephosphorization tank 400 through the water inlet pipe 402, the electrode plate 405 is electrified, a large amount of Fe ²⁺、Fe³⁺ ions are generated at the anode of the electrode plate 405, and the high molecular hydroxyl polymer Fe _m(H₂O)×(OH)_n(3_m-n taking the ions as the core) has activity and specific surface area which are several times or even tens of times higher than those of the common flocculating agents such as polymeric ferric sulfate. When the iron-containing ionic liquid is fully mixed with the wastewater, moderate oxygenation aeration is given, so that Fe ²⁺ in the wastewater can be pushed to be converted into Fe ³⁺, and the pH value of the wastewater can be changed. Meanwhile, PO ₂ ^3-、PO₃ ^3-、P₂O₇ ^4- plasma in the phosphorus-containing wastewater is oxidized into orthophosphate ions PO ₄ ^3- in the system, fe ²⁺、Fe³⁺ reacts with PO ₄ ^3- in water to generate indissolvable Fe ₃(PO₄)₂ and FePO ₄, and the high-activity iron core high-molecular hydroxyl polymer in the system has strong adsorption, coagulation, capturing and bridging capabilities, and rapidly and thoroughly captures and colloid particles, and the colloid particles are deposited at the bottom of the phosphorus removal tank 400 by self weight.

In the dephosphorization process of the dephosphorization tank 400, the water inlet pipe 402 continuously supplements the wastewater in the dephosphorization tank 400, so that the water level in the dephosphorization tank 400 is gradually increased, when the water level in the dephosphorization tank 400 reaches the water passing hole, the wastewater after dephosphorization in the dephosphorization tank 400 overflows to the water draining tank 401 through the water passing hole, the wastewater entering the water draining tank 401 automatically precipitates, the precipitated precipitate is accumulated at the bottom of the water draining tank 401, and the wastewater precipitated in the water draining tank 401 overflows and is discharged through the water outlet pipe 406 to be sent into the anaerobic water inlet tank 201 along with the increase of the water level of the water draining tank 401.

Anaerobic unit 2: the wastewater entering the anaerobic water inlet tank 201 is pumped into a secondary UASB tank through an anaerobic lift pump, the wastewater in the secondary UASB tank is circularly flowed through the pumping of a circulating pump on the secondary UASB tank, the secondary UASB tank utilizes the anaerobic decomposition process of organic matters to convert macromolecular refractory organic matters into micromolecular organic matters which are easy to be degraded by microorganisms, and most insoluble organic matters are degraded into soluble matters, and meanwhile, a carbon source is consumed, COD is reduced, so that conditions are created for the subsequent aerobic treatment; the wastewater after being treated by the secondary UASB tank overflows into the anaerobic sedimentation tank 202, the wastewater is sedimentated in the anaerobic sedimentation tank 202, and the sedimentated wastewater overflows into the anoxic tank 301.

Biochemical treatment unit 3: the wastewater is subjected to ammonia nitrogen removal and organic matter degradation in the anoxic tank 301, the wastewater after being treated in the anoxic tank 301 overflows into the aerobic tank 302, an air blower 311 supplies air to an aeration component 306 in the aerobic tank 302, the aeration component 306 starts aeration, a biological bed 307 attached with microorganisms in the aerobic tank 302 can degrade the organic matter in the wastewater and nitrify ammonia nitrogen, the wastewater after being treated in the aerobic tank 302 overflows into an MBR tank 303, an MBR membrane group 308 in the MBR tank 303 further removes ammonia nitrogen and COD, and the wastewater after being treated in the MBR tank 303 is sent into an intermediate water tank 310.

In the treatment unit, when the degradation of organic matters in the wastewater passing through the aeration in the aerobic tank 302 is not thorough, the wastewater in the aerobic tank 302 can be directly fed into the anoxic tank 301 from the new stage through the mixed liquor reflux pipeline 309 for repeated operation, and the wastewater in the aerobic tank 302 can be pumped through the reflux pump on the mixed liquor reflux pipeline when being conveyed through the mixed liquor reflux pipeline 309.

Depth processing unit 6: the wastewater entering the middle water tank 310 is directly fed into the denitrification deep bed filter 600, a carbon source (sodium acetate) is added into the denitrification deep bed filter 600, if necessary, a PAC flocculant is also added, nitrate nitrogen is further removed through the denitrification deep bed filter 600 and is converted into nitrogen, the finally treated wastewater enters the fiber turntable filter 601 to remove SS, and the wastewater is sterilized through the ultraviolet sterilizing channel 602 and then discharged after reaching standards.

Sludge treatment unit 7: the sediment in the primary sedimentation tank 108, the dephosphorization tank 400, the drainage tank 401, the two-stage UASB200, the anaerobic sedimentation tank 202, the anoxic tank 301 and the MBR tank 303 can be fed into the sludge concentration tank 700 through a reflux pump on a sludge reflux pipe 701, specifically, the electromagnetic valves on the sludge discharge pipe 403 and the blow-down pipe 407 are opened, the sediment in the dephosphorization tank 400 is discharged through the sludge discharge pipe 403 and the sediment in the water outlet tank are jointly fed into the sludge concentration tank 700 through the sludge reflux pipe 701 after being discharged through the blow-down pipe 407, the sediment in the primary sedimentation tank 108, the two-stage UASB200, the anaerobic sedimentation tank 202, the anoxic tank 301 and the MBR tank 303 is fed into the sludge modification bin 703 after being fed into the sludge concentration tank 703, meanwhile, the modifier in the material tank 702 is fed into the sludge modification bin 703, the sludge in the sludge modification bin 703 is fully reacted with the modifier, the sludge in the sludge modification bin 703 is fed into the filter press filter 704 after being dehydrated through the filter press 704, and is directly discharged.

When the low-concentration industrial wastewater is required to be treated, the specific treatment steps are as follows:

Pretreatment unit 1: the low-concentration industrial wastewater is conveyed by a tap water pipe network and is firstly conveyed into the pretreatment tank 100, the low-concentration industrial wastewater is intercepted by the treatment coarse grille 102 after entering the pretreatment tank 100, undissolved impurities, particles, suspended solids and the like which float larger in the wastewater are intercepted in the treatment coarse grille 102, the wastewater normally flows, the undissolved impurities, particles, suspended solids and the like which are intercepted on the treatment coarse grille 102 are lifted by the treatment coarse grille 102 and directly discharged out of the pretreatment tank 100, and overflows into the regulating tank 101 along with the flowing of the wastewater in the pretreatment tank 100, a part of the wastewater in the regulating tank 101 is pumped into the stirring tank 103 by a circulating pump on a water inlet pipe 105, slaked lime or sodium hydroxide is added into the stirring tank 103, after the slaked lime or sodium hydroxide is dissolved, the supernatant in the stirring tank 103 enters the buffer tank 104 and is respectively discharged into the regulating tank 101 by a plurality of water discharging pipes 106, so that the pH value of the wastewater is regulated, the regulated wastewater is conveyed into the primary sedimentation tank 108 for preliminary sedimentation, and ferric salt or aluminum salt is added into the primary sedimentation tank 108 in the sedimentation process.

Biochemical treatment unit 3: the wastewater enters the anaerobic tank 300 through the second direct conveying pipeline 9 after being precipitated in the primary sedimentation tank 108, and enters the anaerobic tank 300 in an overflow mode through an overflow weir when entering the anaerobic tank 300, carbon sources such as sodium acetate and the like are added into the anaerobic tank 300 while the wastewater enters the anaerobic tank 300, and a stirrer 304 in the anaerobic tank 300 is simultaneously stirred, the sodium acetate converts the organic matters which are difficult to degrade in molecules in the wastewater into the organic matters which are easy to degrade in microorganisms after being dissolved, the carbon sources in the wastewater are consumed, COD (chemical oxygen demand) of the wastewater is reduced, the wastewater after the sodium acetate is uniformly dissolved automatically flows into the anoxic tank 301, the stirrer 304 in the anoxic tank 301 is stirred, in the stirring process, bacterial groups in the wastewater are uniformly distributed in the anoxic tank 301, ammonia nitrogen and the organic matters in the wastewater are removed, then, the supernatant fluid in the anoxic tank 301 automatically flows into the aerobic tank 302, at the moment, the stirrer 304 supplies air to the aerator 306, the biological bed 307 attached with microorganisms in the aerobic tank 302 can degrade the organic matters in the aerobic tank 302, the organic matters in the MBR and the MBR (membrane) are further processed in the MBR (membrane reactor) and the MBR (membrane) is further processed in the aerobic tank 303, and the MBR (membrane reactor) is further processed in the MBR) is removed 303).

Post dephosphorization device 5: the waste water in the middle water tank 310 is divided into two parts, one part of the waste water is directly sent into the denitrification deep bed filter 600, the other part of the waste water is sent into the dephosphorization tank 400 through the water inlet pipe 402, the electrode plate 405 is electrified, the anode of the electrode plate 405 generates a large amount of Fe ²⁺、Fe³⁺ ions and a high molecular hydroxyl polymer Fe _m(H₂O)×(OH)_n(3_m-n taking the ions as a core), and the activity and the specific surface area of the high molecular polymer are several times or even tens of times higher than those of the common flocculating agents such as polymeric ferric sulfate. When the iron-containing ionic liquid is fully mixed with the wastewater, moderate oxygenation aeration is given, so that Fe ²⁺ in the wastewater can be pushed to be converted into Fe ³⁺, and the pH value of the wastewater can be changed. Meanwhile, PO ₂ ^3-、PO₃ ^3-、P₂O₇ ^4- plasma in the phosphorus-containing wastewater is oxidized into orthophosphate ions PO ₄ ^3- in the system, fe ²⁺、Fe³⁺ reacts with PO ₄ ^3- in water to generate indissolvable Fe ₃(PO₄)₂ and FePO ₄, and the high-activity iron core high-molecular hydroxyl polymer in the system has strong adsorption, coagulation, capturing and bridging capabilities, and rapidly and thoroughly captures and colloid particles, and the colloid particles are deposited at the bottom of the phosphorus removal tank 400 by self weight.

In the dephosphorization process of the dephosphorization tank 400, the water inlet pipe 402 continuously supplements the wastewater in the dephosphorization tank 400, so that the water level in the dephosphorization tank 400 is gradually increased, when the water level in the dephosphorization tank 400 reaches the water passing hole, the wastewater after dephosphorization in the dephosphorization tank 400 overflows to the water draining tank 401 through the water passing hole, the wastewater entering the water draining tank 401 automatically precipitates, the precipitated precipitate is accumulated at the bottom of the water draining tank 401, and the wastewater precipitated in the water draining tank 401 overflows and is discharged through the water outlet pipe 406 and is fed into the denitrification deep bed filter 600 along with the increase of the water level of the water draining tank 401.

Depth processing unit 6: carbon source (sodium acetate) and PAC flocculant are added into the denitrification deep bed filter 600, if necessary, nitrate nitrogen is further removed through the denitrification deep bed filter 600 and converted into nitrogen, and finally treated wastewater enters the fiber rotary disc filter 601 to remove SS, is sterilized through the ultraviolet sterilizing channel 602 and is discharged after reaching standards.

Sludge treatment unit 7: the sediment in the primary sedimentation tank 108, the anaerobic tank 300, the anoxic tank 301, the MBR tank 303, the dephosphorization tank 400 and the drainage tank 401 can be fed into the sludge concentration tank 700 through a reflux pump on a sludge reflux pipe 701, specifically, electromagnetic valves on a sludge discharge pipe 403 and a blow-down pipe 407 are opened, the sediment in the dephosphorization tank 400 is discharged through the sludge discharge pipe 403 and the sediment in the water outlet tank are jointly fed into the sludge concentration tank 700 through the sludge reflux pipe 701 after being discharged through the blow-down pipe 407, the sediment in the primary sedimentation tank 108, the anaerobic tank 300, the anoxic tank 301 and the MBR tank 303 is fed into the sludge modification tank 703 after entering the sludge concentration tank 700, meanwhile, the modifier in a material tank 702 is fed into the sludge modification tank 703, so that the sludge entering the sludge modification tank 703 fully reacts with the modifier, the sludge in the sludge modification tank 703 is fed into a filter press 704 after reacting in the sludge modification tank 703, and is directly discharged after being dehydrated through the filter press 704.

Example 1 treatment of high concentration phosphorus containing Industrial wastewater

Taking high-concentration brewing wastewater as an example, the total phosphorus content is more than 45mg/L, 25% -30% of the extracted wastewater enters an electrochemical dephosphorization unit, the electrolysis time is 30min, the effluent concentration can reach the standard of integrated wastewater discharge Standard (GB 8978-1996) after the whole process treatment, and the wastewater further needs to enter a sewage treatment plant in a park for treatment.

Example 2 treatment of Low concentration phosphorus containing Industrial wastewater

Taking the sewage treatment plant of the low concentration industrial park as an example, the total phosphorus content is more than 4.5mg/L, 15% -20% of the extracted wastewater enters an electrochemical dephosphorization unit, the electrolysis time is 15min, and the effluent concentration can reach the discharge standard of water pollutants in the river basin of Yinjiang and Tuojiang (DB 51/2311-2016) of Sichuan province after the whole process treatment.

In the description of the present specification, reference to the terms "one embodiment/manner," "some embodiments/manner," "example," "a particular example," "some examples," etc., means that a particular feature, structure, material, or characteristic described in connection with the embodiment/manner or example is included in at least one embodiment/manner or example of the application. In this specification, the schematic representations of the above terms are not necessarily for the same embodiment/manner or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments/modes or examples. Furthermore, the various embodiments/modes or examples described in this specification and the features of the various embodiments/modes or examples can be combined and combined by persons skilled in the art without contradiction.

Furthermore, the terms "first," "second," 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, a feature defining "a first" or "a second" may explicitly or implicitly include at least one such feature. In the description of the present application, the meaning of "plurality" means at least two, for example, two, three, etc., unless specifically defined otherwise.

It will be appreciated by persons skilled in the art that the above embodiments are provided for clarity of illustration only and are not intended to limit the scope of the invention. Other variations or modifications will be apparent to persons skilled in the art from the foregoing disclosure, and such variations or modifications are intended to be within the scope of the present invention.

Claims

1. The electrochemical phosphorus removal system for the industrial wastewater is characterized by comprising a pretreatment unit (1), an anaerobic unit (2), a biochemical treatment unit (3), a front phosphorus removal device (4), a rear phosphorus removal device (5) and a deep treatment unit (6), wherein the pretreatment unit (1), the front phosphorus removal device (4), the anaerobic unit (2), the biochemical treatment unit (3) and the rear phosphorus removal device (5) are sequentially connected, a first direct conveying pipeline (8) is further connected between the pretreatment unit (1) and the anaerobic unit (2), and the biochemical treatment unit (3) and the rear phosphorus removal device (5) are connected with the deep treatment unit (6);

The pretreatment unit (1) comprises a pretreatment tank (100) and a regulating tank (101) which are communicated through overflow; a coarse treatment grid (102) is arranged in the pretreatment tank (100), a grading circulation reaction device is arranged on the regulating tank (101), the grading circulation reaction device is provided with a water inlet pipe (105) and a plurality of drainage pipes (106), the heights of the outlets of the drainage pipes (106) are different, and the inlet end of the water inlet pipe (105) and the outlet end of the drainage pipes (106) extend into the regulating tank (101); the grading circulation reaction device comprises a stirring tank (103) and a buffer tank (104) which are connected in sequence, wherein the outlet end of a water inlet pipe (105) is connected with the stirring tank (103), and the stirring tank (103) is also provided with a dosing pipe (109) and a discharge pipe (107) connected with one of water outlet pipes (406); the pretreatment unit (1) further comprises a primary sedimentation tank (108) connected to the outlet end of the regulating tank (101), and a feeding pipe (110) is arranged on the primary sedimentation tank (108);

The front phosphorus removal device (4) and the rear phosphorus removal device (5) both comprise phosphorus removal units, each phosphorus removal unit comprises a phosphorus removal groove (400) and a drainage groove (401), the phosphorus removal groove (400) and the drainage groove (401) are of an integrated structure or a split structure, and an electrode plate (405) is further arranged in the phosphorus removal groove (400); the dephosphorization unit further comprises a drainage groove (401), the upper end of the dephosphorization groove (400) is communicated with the upper end of the drainage groove (401), a supporting frame (404) is further arranged in the dephosphorization groove (400), a plurality of electrode plates (405) in the dephosphorization groove (400) are arranged, and the plurality of electrode plates (405) are arranged on the supporting frame (404) at intervals; a sludge discharge pipe (403) for discharging sludge and a water inlet pipe (402) for water inflow are also arranged on the dephosphorization tank (400), and a water outlet pipe (406) is also arranged on the water discharge tank (401); the water inlet pipe (402) and the sludge discharge pipe (403) are both positioned at the bottom of the dephosphorization tank (400), and the outlet end of the water inlet pipe (402) is communicated with the inlet end of the sludge discharge pipe (403) through a three-way joint; the water outlet pipe (406) is positioned in the middle of the water drainage groove (401), and a blow-down pipe (407) is further arranged at the bottom of the water drainage groove (401); the mud discharging pipe (403), the water inlet pipe (402), the water outlet pipe (406) and the blow-down pipe (407) are all provided with electromagnetic valves;

the anaerobic unit (2) comprises an anaerobic water inlet tank (201), a two-stage UASB (200) and an anaerobic sedimentation tank (202) which are connected in sequence;

The biochemical treatment unit (3) comprises an anoxic tank (301), an aerobic tank (302) and an MBR tank (303) which are sequentially communicated through overflow;

the biochemical treatment unit (3) further comprises an anaerobic tank (300) which is in overflow communication with the anoxic tank (301), and a second direct conveying pipeline (9) is further connected between the pretreatment unit (1) and the anaerobic tank (300).

2. The electrochemical dephosphorization system for industrial wastewater according to claim 1, wherein the plurality of dephosphorization units are arranged in a rectangular array, and the plurality of dephosphorization units are connected in parallel or in series in sequence; the bottoms of the dephosphorization tank (400) and the drainage tank (401) are funnel-shaped, and the electrode plate (405) is positioned in the middle of the dephosphorization tank (400); the electrode plates (405) are alternately arranged in positive and negative poles; the electrode plate (405) is a carbon steel plate or an iron plate or an aluminum plate; the supporting frame (404) is connected with the groove wall of the dephosphorization groove (400) and the electrode plate (405) is connected with the supporting frame (404) through clamping grooves; the distance between two adjacent electrode plates (405) is 1-12cm.

3. The electrochemical dephosphorization system for industrial wastewater according to claim 1, wherein a baffle plate (203) is arranged in the anaerobic water inlet tank (201), the baffle plate (203) divides the inside of the anaerobic water inlet tank (201) into a left water tank (204) and a right water tank (205) which are communicated with the bottom, the water inlet of the anaerobic water inlet tank (201) and the water outlet of the anaerobic water inlet tank (201) are respectively communicated with the left water tank (204) and the right water tank (205), baffle plates (206) are further arranged in the two-stage UASB (200), and the baffle plates (206) are positioned at the upper parts of the two-stage UASB (200); the anaerobic treatment device is characterized in that a stirrer (304) is arranged in each of the anaerobic tank (300) and the anoxic tank (301), a carbon source supplementing pipe (305) is further arranged on each of the anaerobic tank (300), an aeration assembly (306) is arranged in each of the aerobic tank (302) and the MBR tank (303), a biological bed (307) attached with microorganisms is further arranged in each of the aerobic tank (302), an MBR membrane group (308) is further arranged in each of the MBR tanks (303), and a mixed liquid backflow pipeline (309) is connected between each of the aerobic tank (302) and the anaerobic tank (300).

4. The electrochemical dephosphorization system of industrial wastewater according to claim 1, characterized in that the advanced treatment unit (6) comprises a denitrification deep bed filter (600), a fiber turntable filter (601) and an ultraviolet disinfection canal (602) which are sequentially connected, the outlet end of the MBR tank (303) is further connected with an intermediate water tank (310), and the outlet end of the intermediate water tank (310) is respectively connected with the inlet end of the post-phosphorus removal device (5) and the inlet end of the denitrification deep bed filter (600).

5. The electrochemical dephosphorization system of industrial wastewater according to claim 1, further comprising a sludge treatment unit (7), wherein the sludge treatment unit (7) comprises a sludge concentration tank (700) and a sludge dewatering machine room which are sequentially connected, and a sludge return pipe (701) is connected between the pretreatment unit (1), the front dephosphorization device (4), the anaerobic unit (2), the biochemical treatment unit (3), the rear dephosphorization device (5) and the sludge concentration tank (700); and a material tank (702), a sludge modification bin (703) and a filter press (704) which are sequentially connected are further arranged in the sludge dewatering machine room, and the outlet end of the sludge concentration tank (700) is connected with the inlet end of the sludge modification bin (703).

6. An electrochemical dephosphorization method based on the system of any one of claims 1 to 5, characterized by comprising the following:

When the wastewater is high-concentration phosphorus-containing industrial wastewater, the wastewater is treated by a pretreatment unit (1) to remove insoluble matters in the wastewater, and the wastewater A is discharged; the wastewater A is divided into two parts, one part enters the anaerobic unit (2) through the first direct conveying pipeline (8), the other part enters the front-mounted dephosphorization device (4) through the water inlet pipe (402) to remove phosphorus, and the wastewater B is discharged; the wastewater B enters an anaerobic unit (2), ammonia nitrogen of the wastewater in the anaerobic unit (2) is nitrified, organic matters in the wastewater are degraded, COD content in the wastewater is reduced, and wastewater C is discharged; the wastewater C enters a biochemical treatment unit (3) to further nitrify ammonia nitrogen in the wastewater and degrade organic matters in the wastewater, and the wastewater D is discharged; the wastewater D is treated by an advanced treatment unit (6) and discharged after reaching standards;

When the wastewater is low-concentration phosphorus-containing industrial wastewater, the wastewater is treated by a pretreatment unit (1) to remove insoluble matters in the wastewater, and the wastewater A is discharged; the wastewater A enters a biochemical treatment unit (3) through a second direct conveying pipeline (9), ammonia nitrogen in the wastewater is nitrified, organic matters in the wastewater are degraded, COD content in the wastewater is reduced, and wastewater D is discharged; after the wastewater D is treated by the biochemical treatment unit (3), the wastewater is divided into two parts, one part is dephosphorized by a post-dephosphorization device (5), and the dephosphorized wastewater enters the advanced treatment unit (6); part of wastewater directly enters the advanced treatment unit (6), and the wastewater enters the advanced treatment unit (6) for treatment and then is discharged after reaching the standard;

The COD concentration in the high-concentration phosphorus-containing industrial wastewater is more than 3000mg/L, the total phosphorus concentration is more than 40mg/L, the COD concentration in the low-concentration phosphorus-containing industrial wastewater is less than 500mg/L, and the total phosphorus concentration is less than 8mg/L.

7. The method according to claim 6, wherein the wastewater is treated by the pretreatment unit (1) and is directly connected with the pretreatment tank (100) by a tap water pipe network, the wastewater to be treated is directly sent into the pretreatment tank (100) by the tap water pipe network, and after pretreatment in the pretreatment tank (100), the wastewater is directly overflowed into the regulating tank (101) through an overflow port or an overflow pipeline, the PH value of the industrial wastewater is regulated to 9-11 in the regulating tank (101), and the regulated wastewater is sent into the primary sedimentation tank (108) for preliminary sedimentation, and the wastewater A is discharged;

the wastewater A enters a dephosphorization tank (400) through a water inlet pipe (402), dephosphorization is carried out through an electrode plate (405), the wastewater after dephosphorization flows into a drainage tank (401) for sedimentation, and then the wastewater B is discharged through a water outlet pipe (406);

when electrochemical dephosphorization is carried out, the current density is 40-60mA/cm ², and the electrolysis time is 15-30min.

8. The method according to claim 6, wherein in the anaerobic unit (2), wastewater enters an anaerobic water inlet tank (201), is pumped into two stages of UASB (200) through an anaerobic lifting pump, organic matters in the wastewater are degraded in the two stages of UASB (200), COD content in the wastewater is reduced, the wastewater after being treated by the two stages of UASB (200) overflows into an anaerobic sedimentation tank (202), and the wastewater is sedimented in the anaerobic sedimentation tank (202) to discharge wastewater C; the method comprises the steps that ammonia nitrogen and degradation organic matters are removed from wastewater C in an anoxic tank (301), overflow of the wastewater treated by the anoxic tank (301) enters an aerobic tank (302), an air blower (311) supplies air to an aeration component (306) in the aerobic tank (302), the aeration component (306) starts aeration, a biological bed (307) attached with microorganisms in the aerobic tank (302) can degrade the organic matters in the wastewater and nitrify the ammonia nitrogen, the wastewater treated by the aerobic tank (302) overflows into an MBR tank (303), an MBR membrane group (308) in the MBR tank (303) further removes the ammonia nitrogen and COD, and the wastewater treated by the MBR tank (303) is sent into an intermediate water tank (310) to discharge wastewater D; the wastewater in the aerobic tank (302) flows back to the anoxic tank (301) through a mixed liquid return pipeline (309), so that the wastewater which is not completely treated flows back to the anoxic tank (301) for circulation treatment; the wastewater entering the advanced treatment unit (6) is directly sent into a denitrification deep bed filter (600), a carbon source or a flocculating agent is added into the denitrification deep bed filter (600), nitrate nitrogen is further removed through the denitrification deep bed filter (600) and is converted into nitrogen, and finally the treated wastewater enters a fiber rotary disc filter (601) to remove SS, is sterilized through an ultraviolet sterilizing channel (602) and is discharged after reaching standards; the carbon source is sodium acetate, and the flocculant is PAC flocculant; the sludge in the sludge modification bin (703) is fed into a filter press (704) through a return pump on a sludge return pipe (701), and is directly discharged after being subjected to filter pressing and dehydration by the filter press (704); the modifier is one or two of lime and PAM.