CN115093084B

CN115093084B - Multi-point multi-groove synchronous electrochemical dephosphorization system and dephosphorization method thereof

Info

Publication number: CN115093084B
Application number: CN202210939788.7A
Authority: CN
Inventors: 马明; 高东东; 许利; 肖杰; 邹俊良; 田庆华; 王春
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: 2023-05-05
Anticipated expiration: 2042-08-05
Also published as: CN115093084A

Abstract

The invention discloses a multipoint multi-groove synchronous electrochemical phosphorus removal system and a phosphorus removal method thereof, and relates to the technical field of wastewater treatment. The invention not only solves the problems of secondary pollution and unsatisfactory dephosphorization and denitrification effects caused by excessive dosing in the existing wastewater treatment process, but also is applicable to the treatment of different wastewater, so that the wastewater treatment is more systematic.

Description

Multi-point multi-groove synchronous electrochemical dephosphorization system and dephosphorization method thereof

Technical Field

The invention relates to a multipoint multi-groove synchronous electrochemical dephosphorization system and a dephosphorization method thereof.

Background

The phosphorus-rich wastewater includes: domestic sewage, phosphate fertilizer (containing some compound fertilizers) production wastewater, organophosphorus pesticide production wastewater, phosphorite exploitation, cultivation wastewater, slaughter wastewater, meat food processing wastewater and the like. With the continuous improvement of the current living standard, water eutrophication has become a question of interest, and main elements causing the eutrophication are nitrogen and phosphorus. Wherein phosphorus has a special effect on eutrophication of water bodies. Urban domestic sewage and certain industrial wastewater contain phosphorus nutrient substances with higher concentration. Since the beginning of the century, a great deal of research work is carried out on the treatment of the wastewater containing phosphorus at home and abroad, and certain progress is also made on the phosphorus removal and reduction process and related basic theoretical research.

At present, urban wastewater treatment plants in China mostly adopt a chemical dephosphorization method for total phosphorus and derive an enhanced coagulation technology, a super-magnetic separation technology and the like, but the problems of large dosage, large sludge production amount, high sludge disposal cost, easy influence of water environment change on the dephosphorization effect of chemical agents, toxicity of the chemical agents to aquatic organisms, secondary pollution of an ecological system and the like exist; meanwhile, the existing wastewater treatment plant can only treat wastewater of a single type, and cannot treat multiple types of wastewater at the same time, so that the wastewater treatment cannot realize systemization, and the treated wastewater is single in type.

Therefore, there is an urgent need for a multi-point multi-tank synchronous electrochemical phosphorus removal system that is efficient and accurate, has no secondary pollution to the environment, and can simultaneously treat multiple different types of wastewater.

Disclosure of Invention

The invention aims to provide a multipoint multi-groove synchronous electrochemical dephosphorization system and a dephosphorization method thereof, which not only solve the problems of secondary pollution and unsatisfactory dephosphorization and denitrification effects caused by excessive dosing in the existing wastewater treatment process, but also are applicable to the treatment of different wastewater, so that the wastewater treatment is more systematic.

In order to achieve the aim of the invention, the technical scheme adopted is as follows: the multipoint multi-groove synchronous electrochemical phosphorus removal system comprises a pretreatment unit A, a pretreatment unit B, an anaerobic unit, a biochemical treatment unit A, a biochemical treatment unit B, a front phosphorus removal device, a rear phosphorus removal device and a deep treatment unit, wherein the pretreatment unit A, the biochemical treatment unit A and the rear phosphorus removal device are sequentially connected, the pretreatment unit B, the front phosphorus removal device, the anaerobic unit, the biochemical treatment unit B and the rear phosphorus removal device are sequentially connected, a first direct conveying pipeline is also connected between the pretreatment unit B and the anaerobic unit, and the biochemical treatment unit A, the biochemical treatment unit B and the rear phosphorus removal device are all connected with the deep treatment unit;

The pretreatment unit A comprises a first pretreatment tank and a second pretreatment tank which are sequentially connected;

the biochemical treatment unit A comprises an anaerobic tank A, an anoxic tank A, an aerobic tank A and a secondary sedimentation tank which are connected in sequence;

the pretreatment unit B comprises a third pretreatment tank and an adjusting tank which are communicated through overflow;

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 B comprises an anoxic tank B, an aerobic tank B and an MBR tank which are sequentially communicated through overflow;

the biochemical treatment unit B further comprises an anaerobic tank B which is in overflow communication with the anoxic tank B, and a second direct conveying pipeline is further connected between the pretreatment unit B and the anaerobic tank B;

the front phosphorus removal device and the rear phosphorus removal device both comprise phosphorus removal units, each phosphorus removal unit comprises a phosphorus removal groove, and an electrode plate is further arranged in each phosphorus removal groove.

Further, the first pretreatment tank is divided into a plurality of first-stage treatment areas by a partition plate, and a treatment coarse grid A is arranged in the first-stage treatment area at the inlet end of the first pretreatment tank.

Further, a secondary treatment area and an aeration sand setting area which are arranged at intervals are arranged in the second pretreatment tank, a treatment fine grid and two flashboards are arranged in the secondary treatment area, the two flashboards are respectively positioned at the front side and the rear side of the treatment fine grid, water passing holes which are communicated with the secondary treatment area and the aeration sand setting area are also formed in the second pretreatment tank, and a gate for opening or closing the water passing holes is also arranged in the secondary treatment area; the aeration sand settling area is also internally provided with a first aeration component, and the second pretreatment tank is also provided with a first air blower for supplying air to the first aeration component.

Further, an overflow area which is separated from the aeration sand setting area is further arranged in the second pretreatment tank, an overflow port which is communicated with the aeration sand setting area and the overflow area is further arranged on the second pretreatment tank, a baffle is further arranged in the aeration sand setting area, the baffle is close to the inlet end of the overflow port, and the lower end of the baffle is lower than the height of the overflow port.

Further, the outlet end of the overflow area is also provided with a third direct conveying pipeline connected with the anaerobic tank B.

Further, the anaerobic tank A and the anoxic tank A are internally provided with a stirrer A, the anaerobic tank A is also provided with a medicine supplementing pipe A, the aerobic tank A is also internally provided with a second aeration component, a mixed liquid reflux pipeline A is connected between the aerobic tank A and the anoxic tank A, and a sludge reflux pipe A is connected between the secondary sedimentation tank and the anaerobic tank A.

Further, the third pretreatment tank is internally provided with a treatment coarse grid B, 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 drainage pipes, the heights of the outlets of the water drainage pipes are different, and the inlet end of the water inlet pipe and the outlet end of the water drainage 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 discharge pipes.

Further, the pretreatment unit B 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, the front phosphorus removal device also comprises a mixing tank connected with the water outlet pipe, the mixing tank is also provided with a parallel pipeline connected with the upper end of the first direct conveying pipeline in parallel, and the outlet end of the mixing tank is connected with the aerobic tank A or/and the aerobic tank B.

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, a fourth direct conveying pipeline is connected between the outlet end of the anaerobic sedimentation tank and the anoxic tank A.

Further, all be provided with mixer B in anaerobic tank B, the oxygen deficiency pond B, still have on the anaerobic tank B and mend medicine pipe B, good oxygen pond B and MBR pond all are provided with fourth aeration component, and still be equipped with the biological bed that is attached with the microorganism in the good oxygen pond B, still be provided with MBR membrane group in the MBR pond, and be connected with mixed liquor reflux pipeline B between good oxygen pond B and the oxygen deficiency pond B, all be connected with mud back flow B between MBR pond and the anaerobic tank B, between anaerobic precipitation pond and the two-stage UASB.

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 pool and an outlet end of the secondary sedimentation pool are jointly connected with an intermediate pool, and an outlet end of the intermediate pool 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 conveying pipe is connected between the pretreatment unit B, the front phosphorus removal device, the anaerobic unit, the biochemical treatment unit A, the biochemical treatment unit B, 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.

Based on the system, the invention also provides a multipoint multi-tank electrochemical dephosphorization method, which comprises the following steps:

when the urban domestic wastewater is treated, insoluble substances in the urban domestic wastewater are removed through a tap water pipe by a pretreatment unit A; the pretreated wastewater is treated by a biochemical treatment unit A, ammonia nitrogen and degradation organic matters in the wastewater are removed, and the wastewater is temporarily stored in an intermediate water tank; the wastewater in the middle water tank enters a front phosphorus removal device for removing phosphorus, and the wastewater after phosphorus removal enters a biochemical treatment unit A through a water outlet pipe for further removing ammonia nitrogen in the wastewater; the sewage with non-standard phosphorus in the middle water tank is treated by an advanced treatment unit and discharged after reaching the standard.

When the high-concentration industrial wastewater is treated, the wastewater is treated by a pretreatment unit B, insoluble matters in the wastewater are removed, and wastewater H is discharged; the wastewater H is divided into two parts, one part enters an anaerobic unit through a first direct conveying pipeline, the other part enters a front phosphorus removal device through a water inlet pipe for phosphorus removal, and wastewater I is discharged; the wastewater I 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 J is discharged; the wastewater J enters a biochemical treatment unit B, ammonia nitrogen in the wastewater is further nitrified, organic matters in the wastewater are degraded, and wastewater K is discharged; the wastewater K is treated by an advanced treatment unit and discharged after reaching standards;

when the low-concentration industrial wastewater is treated, the wastewater is treated by a pretreatment unit B, insoluble matters in the wastewater are removed, and wastewater H is discharged; the wastewater H enters a biochemical treatment unit B through a second direct conveying pipeline, ammonia nitrogen in the wastewater is nitrified, organic matters in the wastewater are degraded, COD content in the wastewater is reduced, and wastewater J is discharged; after the wastewater J is treated by a biochemical treatment unit, the wastewater is divided into two parts, one part is dephosphorized by a post-dephosphorization device, and the dephosphorized wastewater enters a deep 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.

When the river water is treated, the river water to be treated is divided into two parts, one part of the river water enters a dephosphorization tank through a water inlet pipe, dephosphorization is carried out through an electrode plate, the dephosphorized sewage flows into a drainage tank for sedimentation, and then enters a mixing tank through a water outlet pipe; the first direct conveying pipeline and the parallel pipeline enter the mixing tank, and the two parts of river water are mixed and directly discharged.

In the invention, the current density is 40-60mA/cm during electrochemical dephosphorization ² The electrolysis time is 15-30min.

Further, in the pretreatment unit a, the wastewater is subjected to a first pretreatment tank to remove larger residues, and then is subjected to a second pretreatment tank to remove small particle impurities.

Further, in the pretreatment unit B, insoluble substances are removed from the wastewater by a third pretreatment tank, the PH value of the industrial wastewater is regulated in a regulating tank, and the regulated wastewater is sent into a primary sedimentation tank for sedimentation.

Further, in the anaerobic unit, the wastewater entering the anaerobic water inlet tank is pumped into a secondary UASB tank through an anaerobic lifting pump, and the secondary UASB tank converts macromolecular refractory organics into micromolecular organics which are easy to be degraded by microorganisms by utilizing an organic anaerobic decomposition process, and degrades most insoluble organics into soluble substances, and simultaneously consumes carbon sources, reduces COD and creates conditions for subsequent aerobic treatment; the wastewater after being treated by the secondary UASB tank overflows into an anaerobic sedimentation tank, and the wastewater is sedimentated in the anaerobic sedimentation tank.

Further, in the biochemical treatment unit A, wastewater enters the anaerobic tank A, macromolecular refractory organic matters in the wastewater can be converted into micromolecular organic matters which are easy to be degraded by microorganisms, carbon sources in the wastewater are consumed, COD (chemical oxygen demand) of the wastewater is reduced, the wastewater after the preliminary precipitation enters the anoxic tank A to carry out preliminary precipitation, the micromolecular organic matters which are easy to be degraded by microorganisms are degraded, ammonia nitrogen in the wastewater is nitrified, ammonia nitrogen in the wastewater is removed, COD of the wastewater is further reduced, the wastewater after the ammonia nitrogen is removed continues to enter the secondary precipitation tank to carry out secondary precipitation, and the precipitate secondary precipitation generated in the wastewater is removed.

Further, the anaerobic treatment device is characterized in that a fourth direct conveying pipeline is connected between the outlet end of the anaerobic sedimentation tank and the anoxic tank A, so that wastewater treated by the anaerobic unit can be directly conveyed to the anoxic tank A through the fourth direct conveying pipeline and treated by the biochemical treatment unit A.

Further, in the biochemical treatment unit B, the wastewater sequentially passes through the anaerobic tank B, the anoxic tank B, the aerobic tank B and the MBR tank to remove organic matters and ammonia nitrogen in the wastewater and reduce the COD content in the wastewater.

Further, the wastewater in the second pretreatment tank enters the biochemical treatment unit B through the overflow area and the third direct conveying pipe for biochemical treatment.

Further, the water inlet in the dephosphorization tank and the water outlet in the drainage tank in the front dephosphorization device and the rear dephosphorization device are controlled by electromagnetic valves.

Further, in the advanced treatment unit, wastewater is directly fed 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, and finally treated wastewater enters a fiber turntable filter to remove SS, and is sterilized through an ultraviolet sterilizing channel and then discharged after reaching standards.

Further, the sediment in the anaerobic tank A, the secondary sedimentation tank, the primary sedimentation tank, the front phosphorus removal device and the rear phosphorus removal device, the emptying pipe and the sludge discharge pipe, the two-stage UASB, the anaerobic sedimentation tank and the anaerobic tank B, MBR can be fed into the sludge concentration tank through a reflux pump on the sludge conveying pipe and fed into the sludge modification bin, and simultaneously, the modifier in the 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 the filter press, and is directly discharged after being subjected to filter pressing and dehydration through the filter press.

Further, the modifier is one or two of lime and PAM.

The invention has the advantages that,

the pretreatment unit A, the pretreatment unit B, the anaerobic unit, the biochemical treatment unit A, the biochemical treatment unit B, the front phosphorus removal device, the rear phosphorus removal device and the advanced treatment unit are matched together to form a complete wastewater treatment system, and the wastewater treatment system can be used for treating urban domestic wastewater, industrial wastewater with different concentrations and river water at the same time, so that the whole system is more perfect; meanwhile, 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, the thorough dephosphorization can be realized, and the sludge production amount is greatly reduced.

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 a multi-point multi-tank synchronous electrochemical phosphorus removal system provided by the present invention;

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

FIG. 3 is a system diagram of the biochemical treatment unit A;

FIG. 4 is a system diagram of a preprocessing unit B;

FIG. 5 is a system diagram of a front-end dephosphorization apparatus;

FIG. 6 is a block diagram of a front-end dephosphorization apparatus;

FIG. 7 is a top view of the front-end dephosphorization apparatus;

FIG. 8 is a system diagram of an anaerobic unit;

FIG. 9 is a system diagram of the biochemical treatment unit B;

FIG. 10 is a system diagram of a depth processing unit;

fig. 11 is a system diagram of a sludge treatment unit.

The reference numerals and corresponding part names in the drawings:

1. pretreatment units A,2, pretreatment units B,3, anaerobic units, 4, biochemical treatment units A,5, biochemical treatment units B,6, a front phosphorus removal device, 7, a rear phosphorus removal device, 8, a deep treatment unit, 9, a sludge treatment unit, 10, a first direct conveying pipeline, 11, a second direct conveying pipeline, 12, a third direct conveying pipeline, 13 and a fourth direct conveying pipeline;

100. the device comprises a first pretreatment tank, 101, a second pretreatment tank, 102, a primary treatment area, 103, a coarse treatment grid A,104, a control valve group, 105, water holes, 106, a secondary treatment area, 107, an aeration sand setting area, 108, a fine treatment grid, 109, a flashboard, 110, a gate, 111, a first aeration assembly, 112, a first blower, 113, an overflow area, 114, an overflow port, 115, a baffle, 116 and a lifting pump;

200. The device comprises a third pretreatment tank, 201, an adjusting tank, 202, a coarse treatment grid B,203, a stirring tank, 204, a buffer tank, 205, a water inlet pipe, 206, a drain pipe, 207, a discharge pipe, 208, a primary sedimentation tank, 209, a dosing pipe, 210 and a feeding pipe;

300. an anaerobic water inlet tank 301, two-stage UASB (upflow anaerobic sludge blanket) 302, an anaerobic sedimentation tank 303, a baffle plate 304, a left water tank 305, a right water tank 306 and a baffle plate;

400. anaerobic tank A,401, anoxic tank A,402, aerobic tank A,403, secondary sedimentation tank, 404, stirrer A,405, second aeration component, 406, medicine supplementing pipe A,407, mixed liquor return pipeline A,408, return pump, 409, second blower, 410, sludge return pipe A;

500. anaerobic tank B,501, anoxic tank B,502, aerobic tank B,503, MBR tank, 504, stirrer, 505, chemical supplementing pipe B,506, fourth aeration component, 507, biological bed with microorganism attached, 508, MBR membrane group, 509, mixed liquor return pipeline B,510, middle water tank, 511, fourth blower, 512, sludge return pipe B;

600. the device comprises a dephosphorization tank, 601, a drainage tank, 602, a water inlet pipe, 603, a mud discharging pipe, 604, a supporting frame, 605, an electrode plate, 606, a water outlet pipe, 607, a blow-down pipe, 608, a PLC automatic control cabinet, 609, a power distribution cabinet, 610, a mixing tank, 611, a third aeration assembly, 612, a parallel pipeline, 613 and a third blower;

800. A denitrification deep bed filter tank, 801 a fiber turntable filter tank, 802 an ultraviolet disinfection canal;

900. a sludge concentration tank 901, a sludge conveying pipe 902, a material tank 903, a sludge modification bin 904 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 11, the multipoint multi-tank synchronous electrochemical phosphorus removal system provided by the invention comprises a pretreatment unit A1, a pretreatment unit B2, an anaerobic unit 3, a biochemical treatment unit A4, a biochemical treatment unit B5, a front phosphorus removal device 6, a rear phosphorus removal device 7 and a deep treatment unit 8, wherein the pretreatment unit A1 is used for removing dregs in domestic wastewater and creating conditions for subsequent biochemical treatment; the method comprises the steps of carrying out a first treatment on the surface of the The biochemical treatment unit A4 is used for carrying out biochemical treatment on the domestic wastewater, so that sediment (sludge) in the domestic wastewater can be conveniently removed, and the domestic wastewater can be denitrified and deaminized; the pretreatment unit B2 is used for removing insoluble impurities, particles, suspended solids and the like in the industrial wastewater, adjusting the pH value of the industrial wastewater to a proper value and creating conditions for subsequent treatment; the anaerobic unit 3 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 phosphorus removal device 6 mainly aims at high-concentration industrial wastewater, the rear phosphorus removal device 7 mainly aims at low-concentration industrial wastewater, and the front phosphorus removal device 6 and the rear phosphorus removal device 7 are not used at the same time, but are selected for industrial wastewater with different concentrations; the advanced treatment unit 8 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 A1 is sequentially connected with the biochemical treatment unit A4 and the post-phosphorus removal device 7, and when the domestic wastewater needs to be treated, the domestic wastewater sequentially passes through the pretreatment unit A1, the biochemical treatment unit A4 and the post-phosphorus removal device 7; the pretreatment unit B2, the prepositive phosphorus removal device 6, the anaerobic unit 3, the biochemical treatment unit B5 and the postpositive phosphorus removal device 7 are sequentially connected, a first direct conveying pipeline 10 is also connected between the pretreatment unit B2 and the anaerobic unit 3, when the high-concentration industrial wastewater is required to be treated, the wastewater can sequentially pass through the pretreatment unit B2, the prepositive phosphorus removal device 6, the anaerobic unit 3, the biochemical treatment unit B5 and the advanced treatment unit 8, and when the high-concentration industrial wastewater is required to be treated, the wastewater can sequentially pass through the pretreatment unit B2, the prepositive phosphorus removal device 6, the anaerobic unit 3 and the biochemical treatment unit B5; the biochemical treatment unit A4, the biochemical treatment unit B5 and the post-phosphorus removal device 7 are connected with the advanced treatment unit 8, so that domestic wastewater, industrial wastewater and river water can enter the advanced treatment unit 8 to continue advanced treatment after being treated, and the discharge standard is achieved.

The pretreatment unit A1 comprises a first pretreatment tank 100 and a second pretreatment tank 101 which are sequentially connected, wherein a tap water pipe network for discharging urban domestic wastewater is directly connected with the first pretreatment tank 100, so that wastewater to be treated is directly sent into the first pretreatment tank 100 through the tap water pipe network, and is sent into the second pretreatment tank 101 for secondary pretreatment after being pretreated in the first pretreatment tank 100.

The biochemical treatment unit A4 comprises an anaerobic tank A400, an anoxic tank A401, an aerobic tank A402 and a secondary sedimentation tank 403 which are sequentially connected, so that the wastewater after secondary pretreatment is directly fed into the anaerobic tank A400, macromolecular refractory organic matters in the wastewater can be converted into micromolecular organic matters which are easy to be degraded by microorganisms, carbon sources in the wastewater are consumed, COD (chemical oxygen demand) of the wastewater is reduced, the wastewater after the primary sedimentation enters the anoxic tank A401 to perform primary sedimentation, the micromolecular organic matters which are easy to be degraded by microorganisms are degraded, ammonia nitrogen in the wastewater is nitrified, ammonia nitrogen in the wastewater is removed, COD (chemical oxygen demand) of the wastewater is further reduced, and the wastewater after the ammonia nitrogen removal continuously enters the secondary sedimentation tank to perform secondary sedimentation, so that sediment secondary sedimentation generated in the wastewater is removed.

The pretreatment unit B2 comprises a third pretreatment tank 200 and a regulating tank 201 which are communicated through overflow, the third pretreatment tank 200 and the regulating tank 201 can be of an integrated structure or a split structure, a tap water pipe network for discharging industrial wastewater is directly connected with the third pretreatment tank 200, so that wastewater to be treated is directly fed into the third pretreatment tank 200 through the tap water pipe network, and after being pretreated in the third pretreatment tank 200, the wastewater is directly overflowed into the regulating tank 201 through an overflow port 114 or an overflow pipeline, and the PH value of the industrial wastewater is regulated in the regulating tank 201.

The anaerobic unit 3 comprises an anaerobic water inlet tank 300, two-stage UASB301 and an anaerobic sedimentation tank 302 which are sequentially connected, wherein the bottom of the anaerobic water inlet tank 300 is a slope surface, so that sediment of the anaerobic water inlet tank 300 can be completely discharged in the later period; the outlet end of the anaerobic water inlet tank 300 is communicated with the middle part of the two-stage UASB301, the two-stage UASB301 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 10 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 302 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 B5 comprises an anoxic tank B501, an aerobic tank B502 and an MBR tank 503 which are sequentially communicated through overflow, the anoxic tank B501, the aerobic tank B502 and the MBR tank 503 are sequentially communicated through overflow, the anoxic tank B501 is used for removing ammonia nitrogen and degrading organic matters, the aerobic tank B502 is used for degrading the organic matters, the ammonia nitrogen is nitrified, and the MBR tank 503 is further used for removing ammonia nitrogen and COD.

Specifically, one end of the first direct conveying pipeline 10 is connected with the regulating tank 201, the other end of the first direct conveying pipeline 10 is connected with the anaerobic water inlet tank 300, so that part of wastewater treated by the regulating tank 201 can directly enter the anaerobic water inlet tank 300, and the other part of wastewater treated by the regulating tank 201 can enter the front phosphorus removal device 6 to be subjected to phosphorus removal treatment and then enter the anaerobic water inlet tank 300, and the device is suitable for treating high-concentration industrial wastewater; meanwhile, the biochemical treatment unit B5 further comprises an anaerobic tank B500, the anaerobic tank B500 is positioned at the front end of the inlet of the anoxic tank B501, a second direct conveying pipeline 11 is further connected between the pretreatment unit B2 and the anaerobic tank B500, and the inlet end of the second direct conveying pipeline 11 can be directly connected on the first direct conveying pipeline 10 in parallel, so that wastewater can enter the anaerobic tank B500 first and then enter the anoxic tank B501, and the biochemical treatment unit is suitable for treating low-concentration industrial wastewater.

The front phosphorus removal device 6 and the rear phosphorus removal device 7 both comprise a phosphorus removal unitThe dephosphorization unit includes a dephosphorization tank 600, and an electrode plate 605 is installed in the dephosphorization tank 600. When the device is used for treating industrial wastewater with higher concentration, the front-end dephosphorization device 6 can remove part of organic matters through flocculation, 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 7 for rear phosphorus removal. Specifically, the electrochemical dephosphorization unit includes the dephosphorization groove 600, the dephosphorization groove 600 entrance end in the leading dephosphorization device 6 is connected with the exit end of equalizing basin 201, the dephosphorization groove 600 entrance end in the post-positioned dephosphorization device 7 is connected with the MBR pond 503 exit end in the biochemical treatment unit B5, the dephosphorization groove 600 cell wall is 4-6 mm's engineering plastics material, and the thickness of dephosphorization groove 600 cell wall can specifically be adjusted according to actual conditions, and still install electrode plate 605 in the dephosphorization groove 600, when waste water enters into the dephosphorization groove 600, electrode plate 605 all can contact with waste water. On the scale of 10m of the dephosphorization tank 600 ³ For example,/h, the area of the dephosphorization tank 600 for installing the electrode plate 605 is a rectangle with a size of 600-1000mm, in this case, the thickness of the electrode plate 605 is 2-4mm, and the length of the electrode plate 605 is 400-800mm, but the specific thickness and specific size of the electrode plate 605 can be adjusted according to the size, capacity, wastewater property, etc. of the dephosphorization tank 600 when the electrode plate 605 is designed.

Treating urban domestic wastewater:

when the phosphorus content in the wastewater is not out of standard, the precipitated wastewater can directly enter the denitrification deep bed filter 800 to remove nitrate nitrogen. When the phosphorus content in the wastewater exceeds the standard, the precipitated wastewater enters the dephosphorization tank 600, and the electrode plate 605 is electrified, and the electrode plate 605 is taken as an iron material for example, and the electrode plate 605 is used for forming a redox system in the dephosphorization tank 600, so that a large amount of Fe is generated at the anode ²⁺ 、Fe ³⁺ Ion and high molecular hydroxyl polymer Fe with the ion as core _m (H ₂ O)×(OH) _n (3 _m-n ) The high molecular polymer is higher than the common polymeric ferric sulfate and other flocculating agents by several times or even several timesTen times the activity and specific surface area; when the iron-containing ionic liquid is fully mixed with the wastewater, proper oxygenation aeration is given to promote Fe in the wastewater ²⁺ To Fe ³⁺ Converting and changing the pH value of the wastewater; meanwhile, PO in the phosphorus-containing wastewater ₂ ^3- 、PO ₃ ^3- 、P ₂ O ₇ ^4- The plasma will be oxidized in the system to orthophosphate ions PO ₄ ^3- The Fe mentioned above ²⁺ 、Fe ³⁺ With PO in water ₄ ^3- React to form indissolvable Fe ₃ (PO ₄ ) ₂ And FePO ₄ The 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 dephosphorization of wastewater is realized.

Treating industrial wastewater:

the present invention can pretreat low-concentration industrial wastewater or high-concentration industrial wastewater, which is transported through a tap water pipe network, by the third pretreatment tank 200 in the pretreatment unit B2 to remove dregs, suspended matters, etc. in the low-concentration industrial wastewater or the high-concentration industrial wastewater; the pretreated wastewater enters an adjusting tank 201 to adjust the PH value of the industrial wastewater.

In the case of high-concentration industrial wastewater, a part of the pretreated high-concentration industrial wastewater enters the dephosphorization tank 600 in the pre-dephosphorization device 6, and at this time, the electrode plate 605 is energized, and the electrode plate 605 is taken as an iron material for example, and a redox system is formed in the dephosphorization tank 600 by the electrode plate 605, so that a large amount of Fe is generated at the anode ²⁺ 、Fe ³⁺ Ion and high molecular hydroxyl polymer Fe with the ion as core _m (H ₂ O)×(OH) _n (3 _m-n ) The high molecular polymer has activity and specific surface area which are several times or even tens times higher than that of common polymeric ferric sulfate and other flocculating agents; when the iron-containing ionic liquid is fully mixed with the wastewater, proper oxygenation aeration is given to promote Fe in the wastewater ²⁺ To Fe ³⁺ Converting and changing the pH value of the wastewater; meanwhile, PO in the phosphorus-containing wastewater ₂ ^3- 、PO ₃ ^3- 、P ₂ O ₇ ^4- The plasma will be oxidized in the system to orthophosphate ions PO ₄ ^3- The Fe mentioned above ²⁺ 、Fe ³⁺ With PO in water ₄ ^3- React to form indissolvable Fe ₃ (PO ₄ ) ₂ And FePO ₄ The 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 dephosphorization 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 300 for buffering, the high-concentration industrial wastewater after buffering is fed into a two-stage UASB301, the two-stage UASB301 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 after the treatment of the two-stage UASB301 is fed into an anaerobic sedimentation tank 302 for sedimentation, the wastewater after sedimentation is fed into an anoxic tank B501 for removing ammonia nitrogen and degrading organic matters, the wastewater after the treatment in the anoxic tank B501 is fed into an aerobic tank B502 for degrading organic matters, ammonia nitrogen and COD are further removed in an MBR tank 503 after the treatment, and finally the wastewater after the treatment is fed into a deep treatment unit 8.

When the wastewater is low-concentration industrial wastewater, the pretreated high-concentration industrial wastewater directly enters an anaerobic tank B500, overflows from the anaerobic tank B500 to an anoxic tank B501, an aerobic tank B502 and an MBR tank 503 in sequence, converts macromolecular refractory organic matters in the wastewater into micromolecular organic matters which are easy to be degraded by microorganisms, consumes carbon sources in the wastewater, reduces COD (chemical oxygen demand) in the wastewater, removes ammonia nitrogen in the wastewater, and sends the wastewater into the anoxic tank B501 to remove ammonia nitrogen and degrade organic matters, the wastewater treated in the anoxic tank B501 enters an aerobic tank B502 to degrade organic matters, nitrifies the ammonia nitrogen, enters the MBR tank 503 after being treated to further remove ammonia nitrogen and COD, and sends the wastewater into a dephosphorizing tank 600 in a post-phosphorus removing device 7 after being treated, and the electrode plate 605 is electrified at the moment, and the electrode plate 605 is used as an iron materialFor example, the electrode plate 605 is used to form a redox system in the dephosphorization tank 600, and a large amount of Fe is generated at the anode ²⁺ 、Fe ³⁺ Ion and high molecular hydroxyl polymer Fe with the ion as core _m (H ₂ O)×(OH) _n (3 _m-n ) The high molecular polymer has activity and specific surface area which are several times or even tens times higher than that of common polymeric ferric sulfate and other flocculating agents; when the iron-containing ionic liquid is fully mixed with the wastewater, proper oxygenation aeration is given to promote Fe in the wastewater ²⁺ To Fe ³⁺ Converting and changing the pH value of the wastewater; meanwhile, PO in the phosphorus-containing wastewater ₂ ^3- 、PO ₃ ^3- 、P ₂ O ₇ ^4- The plasma will be oxidized in the system to orthophosphate ions PO ₄ ^3- The Fe mentioned above ²⁺ 、Fe ³⁺ With PO in water ₄ ^3- React to form indissolvable Fe ₃ (PO ₄ ) ₂ And FePO ₄ The 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 dephosphorization of wastewater is realized, and finally the wastewater is sent into the advanced treatment unit 8.

Treating river water:

river water is conveyed into the dephosphorization tank 600 in the front dephosphorization device 6 through a tap water pipe network, at the moment, the electrode plate 605 is electrified, and taking the electrode plate 605 as an iron material for example, the electrode plate 605 forms a redox system in the dephosphorization tank 600, and a large amount of Fe is generated at the anode ²⁺ 、Fe ³⁺ Ion and high molecular hydroxyl polymer Fe with the ion as core _m (H ₂ O)×(OH) _n (3 _m-n ) The high molecular polymer has activity and specific surface area which are several times or even tens times higher than that of common polymeric ferric sulfate and other flocculating agents; when the iron-containing ionic liquid is fully mixed with the wastewater, proper oxygenation aeration is given to promote Fe in the wastewater ²⁺ To Fe ³⁺ Converting and changing the pH value of the wastewater; meanwhile, PO in the phosphorus-containing river water ₂ ^3- 、PO ₃ ^3- 、P ₂ O ₇ ^4- The plasma willOxidized to orthophosphate ions PO in the system ₄ ^3- The Fe mentioned above ²⁺ 、Fe ³⁺ With PO in water ₄ ^3- React to form indissolvable Fe ₃ (PO ₄ ) ₂ And FePO ₄ The 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 dephosphorization of river water is realized, and the dephosphorized river water is conveyed into a river channel through a tap water pipe network.

In some embodiments, the first pretreatment tank 100 is divided into a plurality of areas by a partition plate, and the partition plate and the first pretreatment tank 100 are integrally formed; when the first pretreatment tank 100 is a cement tank, the partition plate can be formed by bricking; when the first pretreatment tank 100 is a metal tank, the partition plate may be formed by welding metal plates. The upper ends of the plurality of partition plates are provided with water holes 105, so that a plurality of areas can be communicated together through the water holes 105, the bottoms of the areas can be arranged in a step manner, the bottom structures of the areas can be adjusted according to actual conditions, and the upper parts of the areas can be respectively covered by a plurality of fences or covered together by one fence; meanwhile, a waste water treatment coarse grating A103 is arranged in the area at the inlet end of the first pretreatment tank 100, the waste water treatment coarse grating A103 intercepts waste water entering the area, waste water can flow to the outlet end of the first pretreatment tank 100 through the waste water treatment coarse grating A103 in the interception process, and residues floating greatly in the waste water are intercepted on the waste water treatment coarse grating A103 and are lifted out of the first pretreatment tank 100 along with the operation of the waste water treatment coarse grating A103, so that preliminary pretreatment of the waste water is realized. A lift pump 116 is arranged in the area at the outlet end of the first pretreatment tank 100, the outlet end of the lift pump 116 is connected with the second pretreatment tank 101, so that the lift pump 116 pumps the wastewater pretreated by the wastewater treatment coarse grid A103 in the first pretreatment tank 100 into the second pretreatment tank 101, and the wastewater enters the second pretreatment tank 101 for second pretreatment; in order to control the pumping of the wastewater in the first pretreatment tank 100 conveniently, a control valve bank 104 can be arranged at the outlet end of the lifting pump 116, and in order to install the control valve bank 104 conveniently, a region can be reserved in the first pretreatment tank 100 for installing the control valve bank 104, so that the control valve bank 104 does not occupy the ground space during installation; the control valve block 104 is a check valve, and can effectively prevent the waste water entering the second pretreatment tank 101 from flowing back.

In some embodiments, the second pretreatment tank 101 is provided with a secondary treatment area 106 and an aeration sand setting area 107 which are arranged at intervals, the secondary treatment area 106 and the aeration sand setting area 107 can be separated by a partition plate, the partition plate can be arranged in the same way as the partition plate in the first pretreatment tank 100, the upper end of the partition plate is also provided with an overflow port 114 for communicating the secondary treatment area 106 with the aeration sand setting area 107, and the secondary treatment area 106 is positioned at the water inlet end of the second pretreatment tank 101, so that the wastewater after the first pretreatment in the first pretreatment tank 100 directly enters the secondary treatment area 106 after being lifted by a lifting pump 116; meanwhile, the upper parts of the secondary treatment area 106 and the aeration sand setting area 107 can be covered by two fences respectively or covered by one fence together.

The secondary treatment area 106 is also provided with a treatment fine grid 108 and two flashboards 109, the treatment fine grid 108 intercepts the wastewater entering the secondary treatment area 106, the wastewater can flow into the aeration sand setting area 107 through the wastewater treatment coarse grid A103 in the interception process of the treatment fine grid 108, small particle impurities in the wastewater are intercepted on the wastewater treatment coarse grid A103, and the intercepted small particle impurities are lifted out of the secondary treatment area 106 along with the operation of the treatment fine grid 108, so that the secondary pretreatment of the wastewater is realized; meanwhile, the two flashboards 109 are respectively positioned at the front side and the rear side of the treatment fine grid 108, so that the treatment fine grid 108 is positioned between the two flashboards 109, the water inflow of wastewater entering the treatment fine grid 108 and the water inflow of wastewater entering the aeration sand setting area 107 are effectively controlled, and because small particle impurities flow along with water easily, when the treatment fine grid 108 lifts the intercepted small particle impurities and sends the intercepted small particle impurities out of the secondary treatment area 106, the two flashboards 109 are matched to intercept the area, the treatment fine grid 108 is prevented from driving the small particle impurities to suspend in the wastewater to directly enter the aeration sand setting area 107 during operation, and the influence on the treatment of the aeration sand setting area 107 is avoided.

The secondary treatment area 106 is also provided with a gate 110 for opening or closing a water passing port, and the gate 110 is used for controlling the connection or disconnection of the secondary treatment area 106 and the aeration sand setting area 107 and controlling the water inflow entering the aeration sand setting area 107; a first aeration assembly 111 is further arranged in the aeration sand setting area 107, an outlet end of an aeration pipe in the first aeration assembly 111 is positioned at the bottom of the aeration sand setting area 107, and a first air blower 112 for supplying air to the first aeration assembly 111 is further arranged on the second pretreatment tank 101; specifically, the number of the first aeration components 111 in the aeration sand setting area 107 may be multiple, and the multiple first aeration components 111 are uniformly distributed in the aeration sand setting area 107, where the air inlet ends of the multiple first aeration components 111 may be connected in parallel to the outlet end of the first blower 112; meanwhile, for the installation of the plurality of first aeration assemblies 111, a fixing frame can be installed in the aeration sand setting region 107, so that the upper ends of the plurality of first aeration assemblies 111 can be installed on the fixing frame, and the installation of the plurality of first aeration assemblies 111 is more stable. By arranging the first aeration assembly 111 in the aeration sand setting area 107, the particles entering the aeration sand setting area 107 can generate friction through aeration, so that the particles in the wastewater are reduced, and the damage to the lifting pump 116 and the like in the subsequent conveying process of the wastewater is effectively prevented.

In some embodiments, the second pretreatment tank 101 is further provided with an overflow area 113 separated from the aerated sand setting area 107, the separation mode of the aerated sand setting area 107 and the overflow area 113 is the same as the separation mode of the secondary treatment area 106 and the aerated sand setting area 107, a partition plate for separating the aerated sand setting area 107 and the overflow area 113 is provided with an overflow port 114, and the overflow port 114 is positioned at the upper end of the partition plate; meanwhile, a baffle plate 115 is further arranged in the aeration sand settling area 107, the left end and the right end of the baffle plate 115 are fixed with the inner wall of the second pretreatment tank 101, the upper end of the baffle plate 115 can be flush with the upper surface of the second pretreatment tank 101, a certain interval is reserved between the lower end of the baffle plate 115 and the bottom of the aeration sand settling area 107, the interval can be used for flowing wastewater, and particularly when the baffle plate 115 is designed, the lower end of the baffle plate 115 is lower than an overflow port 114, so that the wastewater between the baffle plate 115 and the overflow port 114 can be relatively static in the aeration process of the first aeration assembly 111, small particles in the wastewater can be precipitated at the bottom of the aeration sand settling area 107, and the precipitated wastewater enters the overflow area 113 through the overflow port 114, so that the small particles in the wastewater entering the overflow area 113 can be reduced or not exist as much as possible, and conditions are created for the subsequent biochemical units. For convenient control, a gate plate 109 can be arranged in the overflow area 113, the gate plate 109 is close to the overflow port 114, when the water level in the overflow area 113 is higher, the gate plate 109 can intercept the overflow area 113 at this time in order to prevent the wastewater in the aeration sand setting area 107 from directly entering the overflow area 113 to ensure that the wastewater entering the biochemical unit can not meet the treatment requirement of the biochemical unit when the wastewater level in the aeration sand setting area 107 is too high.

In some embodiments, the outlet end of the overflow area 113 is further provided with a third direct conveying pipeline 12 connected with the anaerobic tank B500, so that after the domestic wastewater in the overflow area 113 is pretreated by the pretreatment unit A1, the domestic wastewater can enter the biochemical treatment unit A4 for biochemical treatment, and can also directly enter the biochemical treatment unit B5 for biochemical treatment, so that the domestic wastewater can also be treated under the condition that the biochemical treatment unit A4 is stopped, and the domestic wastewater treatment is not affected.

In some embodiments, the anaerobic tank a400 and the anoxic tank a401 are both provided with a stirrer a404, the stirrer a404 is a submersible stirrer a404, the anaerobic tank a400, the anoxic tank a401 and the aerobic tank a402 can be in an integrated structure, specifically, two partition boards are arranged in one large-scale water tank, the two partition boards divide the large-scale water tank into the anaerobic tank a400, the anoxic tank a401 and the aerobic tank a402, of course, water holes 105 are also formed in the two partition boards so as to ensure the communication between the anaerobic tank a400, the anoxic tank a401 and the aerobic tank a402, the anaerobic tank a400 is communicated with the overflow area 113 in the second pretreatment tank 101, the aerobic tank a402 is communicated with the secondary sedimentation tank 403, and by arranging the stirrer a404 in the anaerobic tank a400 and the anoxic tank a401, the flora in the anaerobic tank a400 and the anoxic tank a401 are uniformly distributed by stirring of the stirrer a404, so that the ammonia nitrogen in the aerobic tank is more efficient; meanwhile, a medicine supplementing pipe A406 is also arranged on the anaerobic tank A400, so that the wastewater is convenient to add a regulator into the anaerobic tank A400 in the treatment process, and specifically, the regulator is a carbon source such as sodium acetate, and the outlet end of the medicine supplementing pipe A406 can extend to the bottom of the anaerobic tank A400 and can be directly positioned above the liquid level in the anaerobic tank A400. A second aeration assembly 405 is further arranged in the aerobic tank, the structure of the second aeration assembly 405 is the same as that of the first aeration assembly 111, the outlet end of an aeration pipe in the second aeration assembly 405 is positioned at the bottom of the aerobic tank A402, and a second blower 409 can be independently arranged for supplying air to the second aeration assembly 405; meanwhile, the number of the second aeration components 405 may be plural, and the plurality of second aeration components 405 are uniformly distributed in the aerobic tank, at this time, the air inlet ends of the plurality of second aeration components 405 may be connected in parallel with the outlet end of the second air blower 409, and of course, the layout of the second air blower 409 may be omitted here, at this time, the air inlet ends of the plurality of second aeration components 405 may be connected in parallel with the outlet end of the first air blower 112, so that the equipment cost may be saved under the condition of meeting the use of the first aeration components 111 and the second aeration components 405.

A mixed liquid reflux pipeline A407 is connected between the aerobic tank A402 and the anaerobic tank A400, a reflux pump 408 is also arranged on the mixed liquid reflux pipeline A407, and a butterfly valve and a check valve can be arranged on the mixed liquid reflux pipeline A407, so that wastewater in the aerobic tank can flow back into the anoxic tank A401 through the mixed liquid mixed flow pipeline, and untreated wastewater thoroughly flows back into the anoxic tank A401 for circulation treatment; a sludge return pipe A410 is connected between the secondary sedimentation tank 403 and the anaerobic tank A400, so that the sludge in the secondary sedimentation tank 403 can be conveyed into the anaerobic tank A400 through the sludge return pipe A410 when needed, and in order to facilitate the conveying of the sludge, a return pump 408 can be arranged on the sludge return pipe A410. In order to facilitate the wastewater in the overflow area 113 to enter the anaerobic tank A400 in an overflow mode, an overflow weir can be arranged at the inlet of the anaerobic tank A400; similarly, an overflow weir may be provided at the outlet of the aerobic tank a402 so that the wastewater treated in the aerobic tank a402 can be discharged in an overflow manner.

In some embodiments, a coarse treatment grid B202 is disposed in the third pretreatment tank 200, the wastewater can flow to the outlet end of the third pretreatment tank 200 through the coarse treatment grid B202, and insoluble impurities, particles, suspended solids and the like in the wastewater are intercepted on the coarse treatment grid B202, and the intercepted insoluble impurities, particles, suspended solids and the like are lifted out of the third pretreatment tank 200 along with the operation of the coarse treatment grid B202, so as to realize the preliminary pretreatment of the wastewater; be equipped with hierarchical circulation reaction unit on equalizing basin 201, hierarchical circulation reaction unit has a water inlet pipe 205 and a plurality of drain pipe 206, and a plurality of drain pipe 206 export height are unequal, and the entrance point of water inlet pipe 205 and the exit end of a plurality of drain pipe 206 all stretch into in equalizing basin 201, make hierarchical circulation reaction unit can directly adopt the waste water in the third preliminary treatment pond 200 when the material is disposed, and the water intaking is convenient, pipe system is simpler, and cooperates through a plurality of drain pipes 206, realizes the multiposition play water, makes the regulation in the equalizing basin more convenient quick.

In some embodiments, the staged circulation reaction device includes a stirring tank 203 and a buffer tank 204 which are sequentially connected, the stirring tank 203 is provided with a pipeline for adding slaked lime or sodium hydroxide, the regulating tank 201 is also provided with two circulation pumps, the two circulation pumps are connected in parallel at the inlet end of the water inlet pipe 205, 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 203 is communicated with the buffer tank 204, so that the liquid entering the buffer tank 204 is the supernatant liquid in the stirring tank 203, and the inlet ends of the plurality of drain pipes 206 are connected in parallel with the upper end of the buffer tank 204, so that the supernatant liquid in the buffer tank 204 flows back to the regulating tank 201 through the drain pipes 206. In the present invention, in order to facilitate the discharge of the precipitate in the agitation tank 203 and the buffer tank 204, an evacuation pipe may be provided at the bottom of the agitation tank 203 and the bottom of the buffer tank 204, and the outlet end of the evacuation pipe may be connected to any one or more drain pipes 206, so that the precipitate may be directly discharged into the regulating tank 201. For ease of control, ball valves are installed at the parallel ends of both the two evacuation tubes and the plurality of drain tubes 206.

In some embodiments, the pretreatment unit B2 further includes a primary sedimentation tank 208 connected to the outlet end of the adjustment tank 201, the bottom of the primary sedimentation tank 208 is funnel-shaped, an overflow weir is provided at the inlet of the primary sedimentation tank 208, and the water in the adjustment tank 201 overflows through the overflow weir before entering the primary sedimentation tank 208, so as to intercept suspended matters on the surface of the wastewater; the primary sedimentation tank 208 is also provided with a feeding pipe 210 for feeding aluminum salt or ferric salt, so that the sedimentation effect in the primary sedimentation tank 208 is better.

In some embodiments, the electrochemical phosphorus removal unit further includes a drain tank 601, and the phosphorus removal tank 600 and the drain tank 601 may be in an integral structure or a separate structure. When the dephosphorization tank 600 and the drainage tank 601 are in an integrated structure, a box body can be directly adopted, a flow baffle 303 is arranged in the box body to divide the interior of the box body into the dephosphorization tank 600 and the drainage tank 601 which are arranged left and right, at the moment, the height of the dephosphorization tank 600 is equal to that of the drainage tank 601, the bottom of the dephosphorization tank 600 is flush with that of the drainage tank 601, the width of the dephosphorization tank 600 is 200-400mm, and the upper end of the flow baffle 303 is lower than the upper end of the shell or the upper end of the flow baffle 303 is provided with a water passing hole 105, so that the upper end of the dephosphorization tank 600 is communicated with the upper end of the drainage tank 601; when the dephosphorization tank 600 and the drainage tank 601 are of a split structure, the upper end of the dephosphorization tank 600 and the upper end of the drainage tank 601 can be communicated with a water passing pipe or a water passing tank, and in this case, the treated water in the dephosphorization tank 600 can overflow into the drainage tank 601. In the present invention, the dephosphorization tank 600 and the drain tank 601 preferably have an integrated structure.

The supporting frame 604 is installed in the dephosphorization tank 600, a plurality of electrode plates 605 are installed in the dephosphorization tank 600, a certain interval is arranged between the plurality of electrode plates 605, and the plurality of electrode plates 605 are jointly installed on the supporting frame 604, so that the plurality of electrode plates 605 are jointly supported in the dephosphorization tank 600 through the supporting frame 604, and when wastewater enters the dephosphorization tank 600, the plurality of electrode plates 605 can be contacted with the wastewater.

In some embodiments, the dephosphorization tank 600 is further provided with a sludge discharge pipe 603 and a water inlet pipe 602, the water inlet pipe 602 in the front dephosphorization device 6 is connected with the outlet end of the primary sedimentation tank 208, the water inlet pipe 602 in the rear dephosphorization device 7 is connected with the outlet end of the MBR tank 503 and the secondary sedimentation tank 403, and the sludge discharge pipe 603 is used for discharging colloidal particles and precipitated sludge generated after dephosphorization in the dephosphorization tank 600 out of the dephosphorization tank 600; meanwhile, a water outlet pipe 606 is further arranged on the water discharge tank 601, the water outlet pipe 606 is used for directly discharging water overflowed into the water discharge tank 601 after the dephosphorization treatment to the outside of the water discharge tank 601, the water outlet pipe 606 in the front dephosphorization device 6 is connected with the anaerobic water inlet tank 300, and the water outlet pipe 606 in the rear dephosphorization device 7 is connected with the advanced treatment unit 8. Through the synergistic effect of the sludge discharge pipe 603, the water inlet pipe 602 and the water outlet pipe 606, 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 606 is equal to the height of the lower end of the electrode plate 605, so as to facilitate the discharge of the wastewater in the water discharge tank 601.

In some embodiments, the water inlet pipe 602 and the sludge discharge pipe 603 are both positioned at the bottom of the dephosphorization tank 600, and the water inlet pipe 602 is connected in parallel to the sludge discharge pipe 603, so that the water inlet pipe 602 and the sludge discharge pipe 603 together form a three-way pipe, and the pipeline system on the dephosphorization tank 600 is simpler; meanwhile, as the water inlet pipe 602 is positioned at the bottom of the dephosphorization tank 600, the wastewater can not directly contact the electrode plate 605 when entering the dephosphorization tank 600, so that the sediment in the wastewater can not be attached to the electrode plate 605 as much as possible, and the electrolysis effect is ensured.

In some embodiments, the bottom of the water draining tank 601 is further provided with a blow-down pipe 607, so that the wastewater overflowed into the water draining tank 601 can be precipitated in the water draining tank 601, after precipitation, the upper wastewater in the water draining tank 601 can be directly discharged through the water outlet pipe 606, and the precipitate generated by precipitation can be directly discharged through the blow-down pipe 607, so that the wastewater after the dephosphorization treatment is precipitated in the water draining tank 601.

In some embodiments, the sludge discharge pipe 603, the water inlet pipe 602, the water outlet pipe 606 and the emptying pipe 607 are all provided with electromagnetic valves, so as to prevent the sludge discharge pipe 603 from depositing during sludge discharge or colloidal particles generated during dephosphorization from entering the water inlet pipe 602, and the electromagnetic valves on the water inlet pipe 602 are preferentially installed at the outlet end of the water inlet pipe 602. Specifically, the invention can be provided with the PLC automatic control cabinet 608 and the power distribution cabinet 609, the power distribution cabinet 609 supplies power to the PLC automatic control cabinet 608, the electrode plate 605 and the electromagnetic valve respectively, the PLC automatic control cabinet 608 not only controls the opening and closing of the electromagnetic valve on the mud discharging pipe 603, the water inlet pipe 602, the water outlet pipe 606 and the blow-down pipe 607, but also controls the electrode plate 605 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, the electromagnetic valve is arranged on the water inlet pipe 602, so that the wastewater amount entering the dephosphorization tank 600 is effectively controlled, and the voltage of the electrode plate 605 can be controlled according to the wastewater amount entering the dephosphorization tank 600 in the dephosphorization process, so that 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 2 x 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 discharging pipes 603 on the electrochemical phosphorus removal units are connected in parallel, the inlet ends of the water inlet pipes 602 on the electrochemical phosphorus removal units are connected in parallel, the outlet ends of the water outlet pipes 606 on the electrochemical phosphorus removal units are connected in parallel, and the outlet ends of the blow-down pipes 607 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 600 and the drainage tank 601 are funnel-shaped, so that the sediment generated in the dephosphorization process and the sediment generated in the drainage tank 601 after dephosphorization can be collected automatically by gravity and then discharged in a concentrated manner, and the sediment in the dephosphorization tank 600 and the drainage tank 601 is more thorough in discharge; meanwhile, the electrode plate 605 is positioned in the middle of the dephosphorization tank 600, and the sediment generated in the dephosphorization process of the wastewater can drop to the bottom of the dephosphorization tank 600 through dead weight, so that the sediment generated in the dephosphorization process is always separated from the electrode plate 605, the influence of the sediment generated in the dephosphorization process on the quantity of ions generated by the electrode plate 605 is avoided, and the dephosphorization effect is effectively ensured.

In some embodiments, the electrode plates 605 are alternately arranged with positive electrodes and negative electrodes, and in order to prevent the electrode plates 605 from hardening and passivating, the electrode plates 605 can also be powered by a pulse power source, and the positive electrodes and the negative electrodes of the electrode plates 605 can be switched according to a set frequency, so that the electrode plates 605 can generate enough electric ions when being electrified, and the amount of the electric ions generated by the electrode plates 605 is ensured.

In some embodiments, the electrode plate 605 is a carbon steel plate or an iron plate or an aluminum plate, and the specific material of the electrode plate 605 can be adjusted according to actual requirements.

In some embodiments, the supporting frame 604 is connected with the slot wall of the dephosphorizing slot 600, and the electrode plate 605 is connected with the supporting frame 604 by a clamping slot, specifically, the dephosphorizing slot 600 and the supporting frame 604 can be prefabricated into a clamping slot structure in the production and processing process, so that the subsequent independent installation of the clamping slot structure on the slot wall of the supporting frame 604 and the slot wall of the dephosphorizing slot 600 is not needed, the clamping connection of the supporting frame 604 can be realized through the clamping slot on the slot wall of the dephosphorizing slot 600 during the installation, and the clamping connection of the electrode plate 605 can be realized through the clamping slot on the supporting frame 604 during the installation, so that the installation and the disassembly of the electrode plate 605 are more convenient.

In some embodiments, the spacing between adjacent electrode plates 605 is 1-12cm, and the specific size of the spacing between adjacent electrode plates 605 may be adjusted by computational adjustment or the like based on the thickness of electrode plates 605, the concentration of wastewater, the flow rate of wastewater, and the like.

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, the pre-phosphorus removal device 6 further includes a mixing tank 610 connected to the water outlet pipe 606, so that the wastewater after phosphorus removal by the phosphorus removal unit can be directly discharged through the water outlet pipe 606 and then conveyed into the mixing tank 610, and a parallel pipeline 612 connected in parallel to the upper end of the first direct conveying pipeline 10 is further disposed on the mixing tank 610, so that the wastewater after phosphorus removal and wastewater without phosphorus removal can be directly conveyed into the mixing tank 610 through the first direct conveying pipeline 10 and the parallel pipeline 612; meanwhile, the outlet end of the mixing tank 610 is connected with the aerobic tank a402 and/or the aerobic tank B502, a third aeration assembly 611 is arranged in the mixing tank 610, the structure of the third aeration assembly 611 is the same as that of the first aeration assembly 111 and the second aeration assembly 405, and in order to facilitate air supply to the third aeration assembly 611, a third blower 613 can be independently arranged, and the air inlet end of the third aeration assembly 611 can also be directly connected in parallel with the outlet of the first blower 112 or the outlet of the second blower 409. The outlet end of the mixing tank 610 is connected with the aerobic tank A402 or/and the aerobic tank A402, so that the mixed wastewater can be sent into the biochemical treatment unit A4 or/and the biochemical treatment unit B5 for biochemical treatment, and the domestic wastewater can be treated under the condition that the biochemical treatment unit A4 is stopped, so that the domestic wastewater treatment is not influenced.

In order to facilitate the river water to be sent into the front-end dephosphorization device 6 and the mixing tank 610 in the river water treatment process, the pipelines for conveying the river water can be respectively connected on the first direct conveying pipeline 10 and the water inlet pipe 602 of the front-end dephosphorization device 6 in parallel, so that the river water is directly sent into the front-end dephosphorization device 6 for treatment, and can also directly enter the mixing tank 610 through the first direct conveying pipeline 10 and the parallel pipeline 612.

In some embodiments, a baffle plate 303 is disposed in the anaerobic water inlet tank 300, a certain gap is formed between the lower end of the baffle plate 303 and the anaerobic water inlet tank 300, so that the baffle plate 303 makes the anaerobic water inlet tank 300 be a left water tank 304 and a right water tank 305 which are communicated through the bottom, a water inlet of the anaerobic water inlet tank 300 is communicated with a water making tank, a water outlet of the anaerobic water inlet tank 300 is communicated with the right water tank 305, and when wastewater enters the anaerobic water inlet tank 300, the baffle plate 303 can reduce the area of disturbance generated when the wastewater enters the anaerobic water inlet tank 300; the waste water in the anaerobic water inlet tank 300 can be lifted and fed into the two-stage UASB301 by the lifting pump 116, and a check valve is arranged at the outlet end of the lifting pump 116 to prevent the waste water from flowing back; the baffle 306 is further arranged in the two-stage UASB301, so that wastewater in the two-stage UASB301 can be intercepted through the baffle 306 when overflows, and insoluble impurities, particles, suspended solids and the like in the two-stage UASB301 can be intercepted and deposited at the bottom of the two-stage UASB301, so that the wastewater can be deposited.

In some embodiments, a fourth direct conveying pipeline 13 is connected between the outlet end of the anaerobic sedimentation tank 302 and the anoxic tank a401, so that the wastewater treated by the anaerobic unit 3 can be directly conveyed to the anoxic tank a401 through the fourth direct conveying pipeline 13 and treated by the biochemical treatment unit A4, and the domestic wastewater can be treated under the condition that the biochemical treatment unit B5 is stopped, so that the domestic wastewater treatment is not affected.

In some embodiments, the anaerobic tank B500 and the anoxic tank B501 are both provided with a stirrer 504B, the stirrer 504B is a submersible stirrer 504B, the anaerobic tank B500, the anoxic tank B501 and the MBR tank 503 can be in an integrated structure, specifically, two partition boards are arranged in one large-scale water tank, the large-scale water tank is partitioned into the anaerobic tank B500, the anoxic tank B501 and the MBR tank 503 by the two partition boards, of course, the two partition boards are also provided with water holes 105 so as to ensure the communication among the anaerobic tank B500, the anoxic tank B501 and the MBR tank 503, the anaerobic tank B500 is communicated with the primary sedimentation tank 208, the anoxic tank B501 is simultaneously connected with the anaerobic sedimentation tank 302, so that the wastewater treated by the primary sedimentation tank 208 can enter the anoxic tank B501 after entering the anaerobic tank B500, or the wastewater treated by the anaerobic sedimentation tank 302 can directly enter the anoxic tank B501 without passing through the anaerobic tank B500, so that the industrial wastewater with different concentrations can be treated by the anaerobic tank B500, and the anaerobic tank B501 can be uniformly distributed in the anoxic tank B501, and the anaerobic tank B has high ammonia nitrogen and nitrogen mixing efficiency; meanwhile, a medicine supplementing pipe B505 is further arranged on the anaerobic tank B500, so that the wastewater is convenient to add a regulator into the anaerobic tank B500 in the treatment process, and specifically, the regulator is a carbon source such as sodium acetate, and the outlet end of the medicine supplementing pipe B505 can extend to the bottom of the anaerobic tank B500 and can be directly positioned above the liquid level in the anaerobic tank B500.

The aerobic tank B502 and the MBR tank 503 are both internally provided with a fourth aeration component 506, the outlet end of an aeration pipe in the fourth aeration component 506 is positioned at the bottom of the aerobic tank B502 or the bottom of the MBR tank 503, a fourth air blower 511 for supplying air to the fourth aeration component 506 can be arranged, and a fixing frame can be arranged in the aerobic tank B502 and the MBR tank 503 for the installation of the fourth aeration component 506, so that the upper end of the fourth aeration component 506 can be arranged on the fixing frame, and the installation of the fourth aeration component 506 is more stable. By arranging the fourth aeration component 506 in the aerobic tank B502 and the MBR tank 503, the particles entering the aerobic tank B502 and the MBR tank 503 can be aerated to improve the efficiency of degrading organic matters and nitrifying ammonia nitrogen in the wastewater of the biological bed 507 attached with microorganisms.

The aerobic tank B502 is internally provided with a biological bed 507 attached with microorganisms, the biological bed 507 attached with microorganisms can degrade organic matters in wastewater and nitrify ammonia nitrogen, the MBR tank 503 is internally provided with an MBR membrane group 508, and the MBR membrane group 508 further removes ammonia nitrogen and COD; a mixed liquid reflux pipeline B509 is connected between the aerobic tank B502 and the anaerobic tank B500, a reflux pump 408 is further arranged on the mixed liquid reflux pipeline B509, and a butterfly valve and a check valve can be further arranged on the mixed liquid reflux pipeline B509, so that wastewater in the aerobic tank B502 can flow back into the anoxic tank B501 through the mixed liquid mixed flow pipeline, and untreated wastewater and wastewater flowing back into the anoxic tank B501 are subjected to circulation treatment. Sludge reflux pipes B512 are respectively connected between the MBR tank 503 and the anaerobic tank B500 and between the secondary sedimentation tank 403 and the two-stage UASB301, so that when needed, sludge in the MBR tank 503 is conveyed into the anaerobic tank B500 through the sludge reflux pipes B512, sludge in the anaerobic sedimentation tank 302 is conveyed into the two-stage UASB301 through the sludge reflux pipes B512, and in order to facilitate the conveying of the sludge, a reflux pump 408 can be arranged on the sludge reflux pipes B512.

In some embodiments, the outlet end of the MBR tank 503 and the outlet end of the secondary sedimentation tank 403 are also connected with an intermediate water tank 510, the outlet end of the intermediate water tank 510 is connected with the inlet end of the post-phosphorus removal device 7, the intermediate water tank 510 can be used for temporary storage of wastewater to be post-phosphorus removed or wastewater to be removed by the denitrification deep bed filter 800 through the intermediate water tank 510; the water inlet pipe 602 of the dephosphorization tank 600 in the rear dephosphorization device 7 is connected in parallel with the outlet end of the middle water tank 510, and the middle water tank 510 is internally provided with the lifting pump 116, so that when the water level of the middle water tank 510 is low, the use of the dephosphorization tank 600 and the denitrification deep bed filter 800 can be met by lifting the wastewater through the lifting pump 116, and the outlet end of the middle water tank 510 is simultaneously connected in parallel with the inlet end of the denitrification deep bed filter 800.

The advanced treatment unit 8 comprises a denitrification deep bed filter 800, a fiber rotary disc filter 801 and an ultraviolet disinfection canal 802 which are sequentially connected, wherein the limiting rotary disc filter and the ultraviolet disinfection canal are sequentially connected to the water outlet end of the denitrification deep bed filter 800, so that wastewater subjected to further denitrification in the denitrification deep bed filter 800 is subjected to SS removal through the fiber rotary disc filter 801, ultraviolet disinfection is performed through the ultraviolet disinfection canal 802, and then the wastewater is discharged after reaching standards, and the wastewater treated by the dephosphorization system provided by the invention can be directly discharged. It is noted that the fiber rotary disc filter 801 can be replaced by an artificial wetland.

In some embodiments, the invention further comprises a sludge concentration tank 900 and a sludge dewatering machine room which are sequentially connected, specifically, the anaerobic tank A400, the secondary sedimentation tank 403, the primary sedimentation tank 208, the front dephosphorization device 6 and the rear dephosphorization device 7, the blow-down pipe 607, the sludge discharge pipe 603, the two-stage UASB301, the anaerobic sedimentation tank 302, the anaerobic tank B500 and the MBR tank 503 are all connected with the sludge concentration tank 900 by adopting the connection of a sludge conveying pipe 901, so that sediment, sludge and the like generated in the system can be sent into the sludge concentration tank 900 for concentrated concentration treatment, and then directly sent into the sludge dewatering machine room for dewatering treatment after concentration treatment, and finally the dewatered sludge is obtained.

In order to ensure the sludge discharge effect of the anaerobic tank A400, the secondary sedimentation tank 403, the primary sedimentation tank 208, the front phosphorus removal device 6 and the rear phosphorus removal device 7, the blow-down pipe 607 and the sludge discharge pipe 603, the two-stage UASB301, the anaerobic sedimentation tank 302, the anaerobic tank B500 and the MBR tank 503, a reflux pump 408 can be installed on the sludge conveying pipe 901, the equipment cost is saved, the blow-down pipe 607 and the sludge discharge pipe 603 used for conveying the anaerobic tank A400, the primary sedimentation tank 208, the front phosphorus removal device 6 and the rear phosphorus removal device 7, the two-stage UASB301, the anaerobic sedimentation tank 302, the anaerobic tank B500 and the sludge conveying pipe 901 in the MBR tank 503 can be connected in parallel and then connected with the sludge concentration tank 900, at this time, an electromagnetic valve can be installed on each sludge conveying pipe 901, and the inlet end of the sludge concentration tank 900 is provided with the reflux pump 408.

In some embodiments, the sludge dewatering machine room is further provided with a material tank 902, a sludge modification bin 903 and a filter press 904 which are sequentially connected, the outlet end of the sludge concentration tank 900 is connected with the inlet end of the sludge modification bin 903, the material tank 902 is used for storing a modifier, the modifier in the material tank 902 can be added into the sludge modification bin 903 according to requirements, the sludge sent into the sludge modification bin 903 through the sludge concentration tank 900 is modified after being reacted with the modifier, and the sludge is sent into the filter press 904 after being modified, so that dewatered sludge is obtained, and the sludge after being filter-pressed and dewatered through the filter press 904 can be loaded and removed through a lifting machine.

In the invention, in order to facilitate the air supply to the first aeration assembly 111, the second aeration assembly 405, the third aeration assembly 611 and the fourth aeration assembly 506, a blower room can be directly arranged, and a large blower can be installed in the blower room, and in this case, the first blower 112, the second blower 409, the third blower 613 and the fourth blower 511 can be omitted, and the air inlet ends of the first aeration assembly 111, the second aeration assembly 405, the third aeration assembly 611 and the fourth aeration assembly 506 can be commonly connected with the large blower outlet in the blower room; similarly, in order to put carbon source and PAC into the anaerobic tank a400, the anaerobic tank B500, and the denitrification deep bed filter 800, a material tank 902 for storing carbon source and PAC respectively may be provided, and then the carbon source replenishing pipe and the chemical adding pipe 209 may be connected to the material tank 902 for storing carbon source and PAC.

When the invention is used for treating urban domestic wastewater, the specific treatment steps are as follows:

pretreatment unit A1: the urban domestic wastewater is firstly sent into the first pretreatment tank 100 through wastewater conveyed by a tap water pipe network, the urban domestic wastewater is intercepted by the wastewater treatment coarse grating A103 after entering the first pretreatment tank 100, the slag floating greatly in the wastewater is intercepted on the wastewater treatment coarse grating A103, the wastewater normally flows, the slag intercepted on the wastewater treatment coarse grating A103 is directly discharged out of the first pretreatment tank 100 through lifting of the wastewater treatment coarse grating A103, the wastewater flows in the first pretreatment tank 100, the wastewater in the first pretreatment tank 100 is finally sent into the secondary treatment area 106 through the lifting pump 116, the wastewater entering the secondary treatment area 106 flows through the fine grating 108, small particle impurities in the wastewater are intercepted on the fine grating 108 in the flowing process, the small particle impurities intercepted on the fine grating 108 are directly discharged out of the treatment area 106 through lifting of the fine grating 108, the gate 110 at the water passing holes 105 is opened, the wastewater enters the sedimentation area 107 along with the normal flow, the first aerator assembly 111 is started, the wastewater is discharged into the overflow area 114 through the overflow area, the wastewater is separated into the overflow area 114 after the wastewater is discharged into the overflow area, and the wastewater is separated into the overflow area, and the overflow area is sent into the overflow area 114 along with the overflow area after the sewage is separated into the overflow area, and the overflow area is separated into the small particles and the overflow area.

Biochemical treatment unit A4: the wastewater sent out through the overflow area 113 enters the anaerobic tank A400, and enters the anaerobic tank A400 in an overflow mode through an overflow weir, the wastewater enters the anaerobic tank A400 and is added with carbon sources such as sodium acetate and the like, the stirrer A404 in the anaerobic tank A400 is simultaneously stirred, the sodium acetate converts the organic matters which are difficult to degrade in the wastewater into small molecular organic matters which are easy to degrade by 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 A401, the stirrer A404 in the anoxic tank A401 is stirred, in the stirring process, bacterial groups in the wastewater are uniformly distributed in the anoxic tank A401, ammonia nitrogen and degrading organic matters in the wastewater are removed, then the upper layer of the anoxic tank A401 automatically flows into the aerobic tank, at the moment, the second blower 409 operates, the second blower 409 provides an air source for the wastewater to degrade the organic matters in the aerobic tank, the organic matters in the aerobic tank are degraded, the wastewater is directly subjected to the secondary phosphorus removal sedimentation tank after the wastewater reaches the standard sedimentation tank, and finally the wastewater is directly enters the secondary sedimentation tank after the secondary sedimentation tank 600, and the secondary sedimentation tank after the wastewater is subjected to the secondary sedimentation tank is subjected to the super-standard sedimentation tank, and the secondary sedimentation tank is directly enters the sedimentation tank after the secondary sedimentation tank after the sedimentation tank is subjected to the secondary sedimentation tank is subjected to the sedimentation tank, and the secondary sedimentation tank is subjected to the sedimentation after the secondary sedimentation, and the secondary sedimentation tank is subjected to the sedimentation, and the secondary sedimentation.

In the treatment unit, when the degradation of organic matters in the wastewater passing through the aeration in the aerobic tank is not thorough, the wastewater in the aerobic tank can be directly fed into the anoxic tank A401 from the new stage through the mixed liquid reflux pipeline A407 for repeated operation, and the wastewater in the aerobic tank can be pumped through the reflux pump 408 on the mixed liquid mixed flow pipeline when being conveyed through the mixed liquid reflux pipeline A407.

Electrochemical dephosphorization unit: when the phosphorus content of the wastewater after secondary precipitation exceeds the standard and the wastewater needs to enter the dephosphorization tank 600 through the water inlet pipe 602, the electromagnetic valves on the water inlet pipe 602 and the water outlet pipe 606 are opened, the wastewater to be dephosphorized enters the inlet end of the sludge discharge pipe 603 through the water inlet pipe 602 and finally enters the dephosphorization tank 600, the electrode plate 605 is electrified, and a large amount of Fe is generated at the anode of the electrode plate 605 ²⁺ 、Fe ³⁺ Ion and high molecular hydroxyl polymer Fe with the ion as core _m (H ₂ O)×(OH) _n (3 _m-n ) The high molecular polymer has activity and specific surface area which are several times or even tens times higher than that of common polymeric ferric sulfate and other flocculating agents. When the iron-containing ionic liquid is fully mixed with the wastewater, proper oxygenation aeration is given to promote Fe in the wastewater ²⁺ To Fe ³⁺ Change over and change the pH value of the wastewater. Meanwhile, PO in the phosphorus-containing wastewater ₂ ^3- 、PO ₃ ^3- 、P ₂ O ₇ ^4- The plasma will be oxidized in the system to orthophosphate ions PO ₄ ^3- The Fe mentioned above ²⁺ 、Fe ³⁺ With PO in water ₄ ^3- React to form indissolvable Fe ₃ (PO ₄ ) ₂ And FePO ₄ Body of a toyThe iron core high molecular hydroxyl polymer with high activity has strong adsorption, coagulation, capturing and bridging capabilities, rapidly and thoroughly captures and colloid particles, and the colloid particles are deposited at the bottom of the dephosphorization tank 6001 by self weight.

In the dephosphorization process in the dephosphorization tank 600, the water inlet pipe 602 continuously supplements the wastewater in the dephosphorization tank 600, so that the water level in the dephosphorization tank 600 is gradually increased, when the water level in the dephosphorization tank 600 reaches the water passing hole 105, the wastewater after dephosphorization in the dephosphorization tank 600 overflows to the water draining tank 601 through the water passing hole 105, the wastewater entering the water draining tank 601 automatically precipitates, the precipitated precipitate is accumulated at the bottom of the water draining tank 601, and the wastewater precipitated in the water draining tank 601 overflows and is discharged through the water outlet pipe 606 and is sent into the aerobic tank, and the steps in the biochemical treatment unit A4 are repeated.

When the sediment in the water drain tank 601 and the dephosphorization tank 600 is deposited more, the electromagnetic valve on the water outlet pipe 606 is closed, the electrode plate 605 is powered off, the electromagnetic valve on the sludge discharging pipe 603 and the emptying pipe 607 is opened, the sediment in the water drain tank 601 is discharged through the emptying pipe 607, and the sediment in the dephosphorization tank 600 is discharged through the sludge discharging pipe 603.

Depth processing unit 8: when the phosphorus is not out of standard, the wastewater in the middle water tank 510 is directly sent into the denitrification deep bed filter 800, and a carbon source (sodium acetate) is added into the denitrification deep bed filter 800, if necessary, a PAC flocculant is also added, nitrate nitrogen is further removed through the denitrification deep bed filter 800 and is converted into nitrogen, the finally treated wastewater enters the fiber turntable filter 801 to remove SS, and the wastewater is sterilized through the ultraviolet sterilizing channel 802 and then discharged after reaching standards.

Sludge treatment unit 9: the sediment in the anaerobic tank A400, the secondary sedimentation tank 403, the dephosphorization tank 600 and the water outlet tank can be fed into the sludge concentration tank 900 through the reflux pump 408 on the sludge conveying pipe 901, specifically, the electromagnetic valves on the sludge discharging pipe 603 and the blow-down pipe 607 are opened, so that the sediment in the dephosphorization tank 600 and the sediment in the water outlet tank can be conveyed into the sludge concentration tank 900 through the sludge conveying pipe 901, the sediment in the anaerobic tank A400, the secondary sedimentation tank 403, the dephosphorization tank 600 and the water outlet tank is fed into the sludge modification tank 903 after entering the sludge concentration tank 900, meanwhile, the modifier in the material tank 902 is conveyed into the sludge modification tank 903, so that the sludge entering the sludge modification tank 903 fully reacts with the modifier, the sludge in the sludge modification tank 903 is fed into the filter press 904 after reacting in the sludge modification tank 903, and the sludge is directly discharged after being dehydrated through the filter press 904.

When the invention is used for treating high-concentration industrial wastewater, the specific treatment steps are as follows:

pretreatment unit B2: the high-concentration industrial wastewater is conveyed by a tap water pipe network and is firstly conveyed into the third pretreatment tank 200, the high-concentration industrial wastewater is intercepted by the treatment coarse grid B202 after entering the third pretreatment tank 200, undissolved impurities, particles, suspended solids and the like which float in the wastewater are intercepted in the treatment coarse grid B202, the wastewater normally flows, the undissolved impurities, particles, suspended solids and the like which are intercepted on the treatment coarse grid B202 are lifted by the treatment coarse grid B202 and directly discharged out of the third pretreatment tank 200, the wastewater overflows into the regulating tank 201 along with the flowing of the wastewater in the third pretreatment tank 200, part of the wastewater in the regulating tank 201 is pumped into the stirring tank 203 through a circulating pump on a water inlet pipe 205, slaked lime or sodium hydroxide is added into the stirring tank 203, after the slaked lime or sodium hydroxide is dissolved, the supernatant in the stirring tank 203 enters the buffer tank 204 and is respectively discharged into the regulating tank 201 through a plurality of water discharging pipes 206, the pH value of the wastewater is regulated, the regulated wastewater is conveyed into the primary sedimentation tank 208 for primary sedimentation, and ferric salt or aluminum salt is added into the primary sedimentation tank 208.

Front-mounted electric dephosphorization device: after the wastewater is precipitated in the primary sedimentation tank 208, the wastewater is divided into two parts, one part of the wastewater is directly sent into the anaerobic water inlet tank 300 through the first direct conveying pipeline 10, the other part of the wastewater is sent into the dephosphorization tank 600 through the water inlet pipe 602, the electrode plate 605 is electrified, and a large amount of Fe is generated at the anode of the electrode plate 605 ²⁺ 、Fe ³⁺ Ion and high molecular hydroxyl polymer Fe with the ion as core _m (H ₂ O)×(OH) _n (3 _m-n ) The method comprisesThe activity and specific surface area of the polymer are several times or tens times higher than those of the common polymeric ferric sulfate and other flocculants. When the iron-containing ionic liquid is fully mixed with the wastewater, proper oxygenation aeration is given to promote Fe in the wastewater ²⁺ To Fe ³⁺ Change over and change the pH value of the wastewater. Meanwhile, PO in the phosphorus-containing wastewater ₂ ^3- 、PO ₃ ^3- 、P ₂ O ₇ ^4- The plasma will be oxidized in the system to orthophosphate ions PO ₄ ^3- The Fe mentioned above ²⁺ 、Fe ³⁺ With PO in water ₄ ^3- React to form indissolvable Fe ₃ (PO ₄ ) ₂ And FePO ₄ The 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 dephosphorization tank 600 by self weight.

In the dephosphorization process of the dephosphorization tank 600, the water inlet pipe 602 continuously supplements the wastewater in the dephosphorization tank 600, so that the water level in the dephosphorization tank 600 is gradually increased, when the water level in the dephosphorization tank 600 reaches the water passing hole 105, the wastewater after dephosphorization in the dephosphorization tank 600 overflows to the water draining tank 601 through the water passing hole 105, the wastewater entering the water draining tank 601 automatically precipitates, the precipitated precipitate is accumulated at the tank bottom of the water draining tank 601, and the wastewater precipitated in the water draining tank 601 is overflowed and discharged through the water outlet pipe 606 to be sent into the anaerobic water inlet tank 300 along with the increase of the water level of the water draining tank 601.

Anaerobic unit 3: the wastewater entering the anaerobic water inlet tank 300 is pumped into a secondary UASB tank through the anaerobic lift pump 116, 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 the organic matters which are difficult to degrade into the micro-molecular organic matters which are easy to degrade by microorganisms, and most of 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 302, the wastewater is sedimentated in the anaerobic sedimentation tank 302, and the sedimentated wastewater overflows into the anoxic tank B501.

Biochemical treatment unit B5: the wastewater is subjected to ammonia nitrogen removal and organic matter degradation in the anoxic tank B501, the wastewater after being treated in the anoxic tank B501 overflows into the aerobic tank B502, an air blower supplies air to a fourth aeration assembly 506 in the aerobic tank B502, the fourth aeration assembly 506 starts aeration, a biological bed 507 attached with microorganisms in the aerobic tank B502 can degrade the organic matter in the wastewater and nitrify ammonia nitrogen, the wastewater after being treated in the aerobic tank B502 overflows into the MBR tank 503, an MBR membrane group 508 in the MBR tank 503 further removes ammonia nitrogen and COD, and the wastewater after being treated in the MBR tank 503 is sent into an intermediate water tank 510.

In the treatment unit, when the degradation of organic matters in the wastewater passing through the aeration in the aerobic tank B502 is not thorough, the wastewater in the aerobic tank B502 can be directly fed into the anoxic tank B501 from the new state through the mixed liquid reflux pipeline B509 for repeated operation, and the wastewater in the aerobic tank B502 can be pumped through the reflux pump 408 on the mixed liquid reflux pipeline when being conveyed through the mixed liquid reflux pipeline B509.

Depth processing unit 8: the wastewater entering the middle water tank 510 is directly sent into the denitrification deep bed filter 800, a carbon source (sodium acetate or methanol or glucose) is added into the denitrification deep bed filter 800, if necessary, PAC flocculant or ferric salt is also added, nitrate nitrogen is further removed through the denitrification deep bed filter 800 and is converted into nitrogen, the finally treated wastewater enters the fiber turntable filter 801 to remove SS, and the wastewater is sterilized through the ultraviolet sterilizing channel 802 and then discharged after reaching standards.

Sludge treatment unit 9: the sediment in the primary sedimentation tank 208, the dephosphorization tank 600, the drainage tank 601, the two-stage UASB301, the anaerobic sedimentation tank 302, the anoxic tank B501 and the MBR tank 503 can be fed into the sludge thickening tank 900 through a reflux pump 408 on a sludge conveying pipe 901, specifically, electromagnetic valves on a sludge discharging pipe 603 and a blow-down pipe 607 are opened, the sediment in the dephosphorization tank 600 is discharged through the sludge discharging pipe 603 and the sediment in the water discharging tank are jointly conveyed into the sludge thickening tank 900 through the sludge conveying pipe 901 after being discharged through the blow-down pipe 607, and the sediment in the primary sedimentation tank 208, the two-stage UASB301, the anaerobic sedimentation tank 302, the anoxic tank B501 and the MBR tank 503 is fed into a sludge modifying bin 903 after being fed into the sludge thickening tank 900, meanwhile, the modifier in the material tank 902 is conveyed into the sludge modifying bin 903, the sludge in the sludge modifying bin 903 is fully reacted with the modifier, the sludge in the modifying bin 903 is fed into a filter press 904 after being reacted in the sludge modifying bin 903, and the sludge in the modifying bin is directly discharged after being dehydrated through the filter press 904.

When the invention is used for treating low-concentration industrial wastewater, the specific treatment steps are as follows:

pretreatment unit B2: the low-concentration industrial wastewater is conveyed by a tap water pipe network and is firstly conveyed into the third pretreatment tank 200, the low-concentration industrial wastewater is intercepted by the treatment coarse grid B202 after entering the third pretreatment tank 200, undissolved impurities, particles, suspended solids and the like which float larger in the wastewater are intercepted in the treatment coarse grid B202, the wastewater normally flows, the undissolved impurities, particles, suspended solids and the like which are intercepted on the treatment coarse grid B202 are lifted by the treatment coarse grid B202 and directly discharged out of the third pretreatment tank 200, the wastewater overflows into the regulating tank 201 along with the flowing of the wastewater in the third pretreatment tank 200, part of the wastewater in the regulating tank 201 is pumped into the stirring tank 203 through a circulating pump on a water inlet pipe 205, slaked lime or sodium hydroxide is added into the stirring tank 203, after the slaked lime or sodium hydroxide is dissolved, the supernatant in the stirring tank 203 enters the buffer tank 204 and is respectively discharged into the regulating tank 201 through a plurality of water discharging pipes 206, the pH value of the wastewater is regulated, the regulated wastewater is conveyed into the primary sedimentation tank 208 for primary sedimentation, and ferric salt or aluminum salt is added into the primary sedimentation tank 208.

Biochemical treatment unit B5: the wastewater enters the anaerobic tank B500 through the second direct conveying pipeline 11 after being precipitated in the primary sedimentation tank 208, and enters the anaerobic tank B500 in an overflow mode through the overflow weir when entering the anaerobic tank B500, carbon sources such as sodium acetate and the like are added into the anaerobic tank B500 when entering the anaerobic tank B500, the stirrer 504B in the anaerobic tank B500 is simultaneously stirred, the sodium acetate converts organic matters which are difficult to degrade in molecules in the wastewater into small molecular organic matters which are easy to degrade in microorganisms after being dissolved, the carbon sources in the wastewater are consumed, COD of the wastewater is reduced, the wastewater after uniformly dissolving the sodium acetate automatically flows into the anoxic tank B501, the stirrer 504B in the anoxic tank B501 is stirred, in the stirring process, the flora in the wastewater is uniformly distributed in the anoxic tank B501, ammonia nitrogen and degrading organic matters in the wastewater are removed, then supernatant in the anoxic tank B501 automatically flows into the aerobic tank B502, at the moment, a blower supplies air to a fourth aeration assembly 506 in the aerobic tank B502, the fourth aeration assembly 506 starts aeration, a biological bed 507 attached with microorganisms in the aerobic tank B502 can degrade the organic matters in the wastewater and nitrify the ammonia nitrogen, the wastewater after the treatment in the aerobic tank B502 overflows into the MBR tank 503, the ammonia nitrogen and COD are further removed by an MBR membrane group 508 in the MBR tank 503, and the wastewater after the treatment in the MBR tank 503 is sent into an intermediate water tank 510.

Post dephosphorization device 7: the wastewater in the middle water tank 510 is divided into two parts, one part of wastewater is directly sent into the denitrification deep bed filter 800 through the direct feeding, the other part of wastewater is sent into the dephosphorization tank 600 through the water inlet pipe 602, the electrode plate 605 is electrified, and a large amount of Fe is generated at the anode of the electrode plate 605 ²⁺ 、Fe ³⁺ Ion and high molecular hydroxyl polymer Fe with the ion as core _m (H ₂ O)×(OH) _n (3 _m-n ) The high molecular polymer has activity and specific surface area which are several times or even tens times higher than that of common polymeric ferric sulfate and other flocculating agents. When the iron-containing ionic liquid is fully mixed with the wastewater, proper oxygenation aeration is given to promote Fe in the wastewater ²⁺ To Fe ³⁺ Change over and change the pH value of the wastewater. Meanwhile, PO in the phosphorus-containing wastewater ₂ ^3- 、PO ₃ ^3- 、P ₂ O ₇ ^4- The plasma will be oxidized in the system to orthophosphoric acid Root ion PO ₄ ^3- The Fe mentioned above ²⁺ 、Fe ³⁺ With PO in water ₄ ^3- React to form indissolvable Fe ₃ (PO ₄ ) ₂ And FePO ₄ The 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 dephosphorization tank 600 by self weight.

In the dephosphorization process of the dephosphorization tank 600, the water inlet pipe 602 continuously supplements the wastewater in the dephosphorization tank 600, so that the water level in the dephosphorization tank 600 is gradually increased, when the water level in the dephosphorization tank 600 reaches the water passing hole 105, the wastewater after dephosphorization in the dephosphorization tank 600 overflows to the water draining tank 601 through the water passing hole 105, the wastewater entering the water draining tank 601 automatically precipitates, the precipitated precipitate is accumulated at the tank bottom of the water draining tank 601, and the wastewater precipitated in the water draining tank 601 is overflowed and discharged through the water outlet pipe 606 to be sent into the denitrification deep bed filter 800 along with the increase of the water level of the water draining tank 601.

Depth processing unit 8: adding carbon source (sodium acetate) into the denitrification deep bed filter 800, and if necessary, adding PAC flocculant, further removing nitrate nitrogen through the denitrification deep bed filter 800, converting the nitrate nitrogen into nitrogen, enabling the finally treated wastewater to enter a fiber rotary disc filter 801 to remove SS, sterilizing through an ultraviolet sterilizing channel 802, and discharging after reaching the standard.

Sludge treatment unit 9: the sediment in the primary sedimentation tank 208, the anaerobic tank B500, the anoxic tank B501, the MBR tank 503, the dephosphorization tank 600 and the drainage tank 601 can be fed into the sludge concentration tank 900 through the reflux pump 408 on the sludge conveying pipe 901, specifically, the electromagnetic valves on the sludge discharging pipe 603 and the blow-down pipe 607 are opened, the sediment in the dephosphorization tank 600 is discharged through the sludge discharging pipe 603 and the sediment in the water discharging tank are jointly conveyed into the sludge concentration tank 900 through the sludge conveying pipe 901 after being discharged through the blow-down pipe 607, the sediment in the primary sedimentation tank 208, the anaerobic tank B500, the anoxic tank B501 and the MBR tank 503 is conveyed into the sludge modification bin after entering the sludge concentration tank 900, meanwhile, the modifier in the material tank 902 is conveyed into the sludge modification bin 903, so that the sludge entering the sludge modification bin 903 fully reacts with the modifier, the sludge in the sludge modification bin 903 is conveyed into the filter press 904 after being reacted in the sludge modification bin 903, and is directly discharged after being dehydrated through the filter press filter 904.

When the invention is used for treating river water, the specific treatment steps are as follows:

the river water to be treated is divided into two parts, one part of river water directly enters the water inlet pipe 602 and enters the dephosphorization tank 600 through the water inlet pipe 602, the other part of river water enters the mixing tank 610 through the first direct conveying pipeline 10 and the parallel pipeline 612 and enters the dephosphorization tank 600 in the front dephosphorization device 6, at the moment, the electrode plate 605 is electrified, and the electrode plate 605 is taken as an iron material for example, an oxidation-reduction system is formed in the dephosphorization tank 600 by utilizing the electrode plate 605, and a large amount of Fe is generated at the anode ²⁺ 、Fe ³⁺ Ion and high molecular hydroxyl polymer Fe with the ion as core _m (H ₂ O)×(OH) _n (3 _m-n ) The high molecular polymer has activity and specific surface area which are several times or even tens times higher than that of common polymeric ferric sulfate and other flocculating agents; when the iron-containing ionic liquid is fully mixed with the wastewater, proper oxygenation aeration is given to promote Fe in the wastewater ²⁺ To Fe ³⁺ Converting and changing the pH value of the wastewater; meanwhile, PO in the phosphorus-containing river water ₂ ^3- 、PO ₃ ^3- 、P ₂ O ₇ ^4- The plasma will be oxidized in the system to orthophosphate ions PO ₄ ^3- The Fe mentioned above ²⁺ 、Fe ³⁺ With PO in water ₄ ^3- React to form indissolvable Fe ₃ (PO ₄ ) ₂ And FePO ₄ The 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 dephosphorization of river water is realized, and the dephosphorized river water enters the mixing tank 610 and can be directly discharged into a river channel after being mixed in the mixing tank 610.

Example 1 town sewage treatment

Taking general town domestic sewage as an example, A ₂ The total phosphorus of the effluent of the O process can reach the first grade A standard of pollutant emission standard of urban sewage treatment plant (GB 18918-2002), and after an electrochemical dephosphorization unit and a subsequent advanced treatment unit are added on the basis of a biochemical process, the total phosphorus and other indexes of the whole effluent of the process can stably reach the pollutant emission standard of water in Yi Jiang and Tuo river basin of Sichuan province (DB 51/2311-2016).

Example 2 treatment of high concentration Industrial wastewater

The COD concentration of the high-concentration phosphorus-containing industrial wastewater is more than 3000mg/L, and the total phosphorus concentration is more than 40mg/L.

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 3 treatment of Low concentration Industrial wastewater

COD concentration of low-concentration phosphorus-containing industrial wastewater is less than 500mg/L, and total phosphorus concentration is less than 8mg/L

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.

Example 4 river Water treatment

Taking river water with total phosphorus exceeding standard as an example, the total phosphorus content of the river water is more than 0.3mg/L, and the river water is IV class, V class or inferior V class. 50% -80% of the extracted river water enters an electrochemical dephosphorization unit, the total phosphorus removal rate is 97%, and the electrolysis time is 20min, so that the concentration of the mixed water can reach the class III standard of the quality standard of the surface water environment (GB 3838-2002).

In the description of the present specification, reference to the terms "one embodiment/manner," "some embodiments/manner," "example," "specific example," or "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 present 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" is at least two, such as two, three, etc., unless explicitly 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 multipoint multi-groove synchronous electrochemical phosphorus removal system is characterized by comprising a pretreatment unit A (1), a pretreatment unit B (2), an anaerobic unit (3), a biochemical treatment unit A (4), a biochemical treatment unit B (5), a front phosphorus removal device (6), a rear phosphorus removal device (7) and a deep treatment unit (8), wherein the pretreatment unit A (1), the biochemical treatment unit A (4) and the rear phosphorus removal device (7) are sequentially connected, the pretreatment unit B (2), the front phosphorus removal device (6), the anaerobic unit (3), the biochemical treatment unit B (5) and the rear phosphorus removal device (7) are sequentially connected, a first direct conveying pipeline (10) is further connected between the pretreatment unit B (2) and the anaerobic unit (3), and the biochemical treatment unit A (4), the biochemical treatment unit B (5) and the rear phosphorus removal device (7) are all connected with the deep treatment unit (8);

the pretreatment unit A (1) comprises a first pretreatment tank (100) and a second pretreatment tank (101) which are sequentially connected, a secondary treatment area (106) and an aeration sand setting area (107) which are arranged in a separated mode are arranged in the second pretreatment tank (101), an overflow area (113) which is separated from the aeration sand setting area (107) is further arranged in the second pretreatment tank (101), and a third direct conveying pipeline (12) connected with the anaerobic tank B (500) is further arranged at the outlet end of the overflow area (113); a fine treatment grid (108) and two flashboards (109) are arranged in the secondary treatment area (106), the two flashboards (109) are respectively positioned at the front side and the rear side of the fine treatment grid (108), the second pretreatment tank (101) is also provided with a water passing hole (105) communicated with the secondary treatment area (106) and the aeration sand setting area (107), and the secondary treatment area (106) is also provided with a gate (110) for opening or closing the water passing hole (105); a first aeration assembly (111) is further arranged in the aeration sand setting area (107), and a first air blower (112) for supplying air to the first aeration assembly (111) is further arranged on the second pretreatment tank (101); the second pretreatment tank (101) is also provided with an overflow port (114) which is communicated with the aeration sand setting area (107) and the overflow area (113), a baffle plate (115) is arranged in the aeration sand setting area (107), the baffle plate (115) is close to the inlet end of the overflow port (114), and the lower end of the baffle plate (115) is lower than the height of the overflow port (114);

The pretreatment unit B (2) comprises a third pretreatment tank (200) and a regulating tank (201) which are communicated through overflow;

the anaerobic unit (3) comprises an anaerobic water inlet tank (301), a two-stage UASB (300) and an anaerobic sedimentation tank (302) which are sequentially connected;

the biochemical treatment unit A (4) comprises an anaerobic tank A (400), an anoxic tank A (401), an aerobic tank A (402) and a secondary sedimentation tank (403) which are sequentially connected, a mixed liquid return pipeline A (407) is connected between the aerobic tank A (402) and the anoxic tank A (401), and a sludge return pipe A (410) is connected between the secondary sedimentation tank (403) and the anaerobic tank A (400);

a stirrer A (404) is arranged in each of the anaerobic tank A (400) and the anoxic tank A (401), a medicine supplementing pipe A (406) is arranged on the anaerobic tank A (400), and a second aeration component (405) is arranged in the aerobic tank A (402);

the biochemical treatment unit B (5) comprises an anoxic tank B (501), an aerobic tank B (502) and an MBR tank (503) which are sequentially communicated through overflow;

the biochemical treatment unit B (5) further comprises an anaerobic tank B (500) which is in overflow communication with the anoxic tank B (501), and a second direct conveying pipeline (11) is further connected between the pretreatment unit B (2) and the anaerobic tank B (500);

the front phosphorus removal device (6) and the rear phosphorus removal device (7) both comprise an electrochemical phosphorus removal unit, the electrochemical phosphorus removal unit comprises a phosphorus removal tank (600) and a drainage tank (601), the phosphorus removal tank (600) and the drainage tank (601) are of an integrated structure or a split structure, and an electrode plate (605) is further arranged in the phosphorus removal tank (600).

2. The multipoint multi-tank synchronous electrochemical phosphorus removal system according to claim 1, wherein the first pretreatment tank (100) is divided into a plurality of primary treatment areas (102) by a partition plate, and a coarse treatment grid a (103) is disposed in the primary treatment area (102) at the inlet end of the first pretreatment tank (100).

3. The multipoint multi-tank synchronous electrochemical phosphorus removal system according to claim 1, wherein a coarse treatment grid B (202) is arranged in the third pretreatment tank (200), a graded circulation reaction device is arranged on the regulating tank (201), the graded circulation reaction device is provided with a water inlet pipe (205) and a plurality of water outlet pipes (206), the outlet heights of the water outlet pipes (206) are different, and the inlet ends of the water inlet pipe (205) and the outlet ends of the water outlet pipes (206) extend into the regulating tank (201).

4. The multi-point multi-tank synchronous electrochemical phosphorus removal system according to claim 3, wherein the grading circulation reaction device comprises a stirring tank (203) and a buffer tank (204) which are sequentially connected, the outlet end of a water inlet pipe (205) is connected with the stirring tank (203), and a chemical adding pipe (209) and a discharge pipe (207) connected with one of drain pipes (206) are further arranged on the stirring tank (203).

5. The multipoint multi-tank synchronous electrochemical phosphorus removal system according to claim 1, wherein the pretreatment unit B (2) further comprises a primary sedimentation tank (208) connected to an outlet end of the regulating tank (201), and a feeding pipe (210) is provided on the primary sedimentation tank (208).

6. The multi-point multi-tank synchronous electrochemical phosphorus removal system of claim 1, wherein the electrochemical phosphorus removal unit further comprises a drainage tank (601), the upper end of the phosphorus removal tank (600) is communicated with the upper end of the drainage tank (601), a supporting frame (604) is further installed in the phosphorus removal tank (600), a plurality of electrode plates (605) in the phosphorus removal tank (600) are arranged, and the plurality of electrode plates (605) are arranged on the supporting frame (604) at intervals.

7. The multipoint multi-tank synchronous electrochemical phosphorus removal system according to claim 6, wherein a sludge discharge pipe (603) for discharging sludge and a water inlet pipe (602) for water inflow are further arranged on the phosphorus removal tank (600), and a water outlet pipe (606) is further arranged on the water discharge tank (601).

8. The multi-point multi-tank synchronous electrochemical phosphorus removal system of claim 7, wherein the water inlet pipe (602) and the sludge discharge pipe (603) are both positioned at the bottom of the phosphorus removal tank (600), and the outlet end of the water inlet pipe (602) is communicated with the inlet end of the sludge discharge pipe (603) through a three-way joint.

9. The multipoint multi-tank synchronous electrochemical phosphorus removal system according to claim 8, wherein the water outlet pipe (606) is positioned in the middle of the water discharge tank (601), and a blow-down pipe (607) is further arranged at the bottom of the water discharge tank (601).

10. The multi-point multi-tank synchronous electrochemical phosphorus removal system of claim 9, wherein solenoid valves are provided on the sludge discharge pipe (603), the water inlet pipe (602), the water outlet pipe (606) and the blow-down pipe (607).

11. The multi-point multi-slot synchronous electrochemical phosphorus removal system of claim 1, wherein the electrochemical phosphorus removal units are a plurality of, the electrochemical phosphorus removal units are arranged in a rectangular array, and the electrochemical phosphorus removal units are connected in parallel or in series in sequence.

12. The multipoint multi-tank synchronous electrochemical phosphorus removal system according to claim 6, wherein the bottoms of the phosphorus removal tank (600) and the drain tank (601) are funnel-shaped, and the electrode plate (605) is positioned in the middle of the phosphorus removal tank (600).

13. The multipoint, multi-tank, synchronous electrochemical phosphorus removal system of claim 1, wherein a plurality of the electrode plates (605) are alternately arranged in positive and negative polarity.

14. The multi-point, multi-tank synchronous electrochemical phosphorus removal system of claim 1, wherein the electrode plate (605) is a carbon steel plate or an iron plate or an aluminum plate.

15. The multi-point, multi-slot synchronous electrochemical phosphorus removal system of claim 6 wherein the support frame (604) is in clamping connection with the walls of the phosphorus removal slot (600), and the electrode plates (605) are in clamping connection with the support frame (604).

16. The multi-point, multi-slot synchronous electrochemical phosphorus removal system of claim 1, wherein a spacing between adjacent two of the electrode plates (605) is 1-12cm.

17. The multipoint multi-tank synchronous electrochemical phosphorus removal system according to claim 7, wherein the front phosphorus removal device (6) further comprises a mixing tank (610) connected with the water outlet pipe (606), the mixing tank (610) is further provided with a parallel pipeline (612) connected with the upper end of the first direct conveying pipeline (10) in parallel, and the outlet end of the mixing tank (610) is connected with the aerobic tank A (402) or/and the aerobic tank B (502).

18. The multipoint multi-tank synchronous electrochemical phosphorus removal system according to claim 1, wherein a flow baffle (303) is arranged in the anaerobic water inlet tank (301), the flow baffle (303) separates a left water tank (304) and a right water tank (305) which are communicated with the bottom of the anaerobic water inlet tank (301), a water inlet of the anaerobic water inlet tank (301) and a water outlet of the anaerobic water inlet tank (301) are respectively communicated with the left water tank (304) and the right water tank (305), a baffle plate (306) is further arranged in the two-stage UASB (300), and the baffle plate (306) is positioned at the upper part of the two-stage UASB (300).

19. The multipoint multi-tank synchronous electrochemical phosphorus removal system according to claim 1, wherein a fourth direct conveying pipeline (13) is connected between the outlet end of the anaerobic sedimentation tank (302) and the anoxic tank a (401).

20. The multipoint multi-tank synchronous electrochemical phosphorus removal system according to claim 1, wherein a stirrer B (504) is arranged in each of the anaerobic tank B (500) and the anoxic tank B (501), a chemical supplementing pipe B (505) is arranged on each of the anaerobic tank B (500), a fourth aeration component (506) is arranged in each of the aerobic tank B (502) and the MBR tank (503), a biological bed (507) attached with microorganisms is arranged in each of the aerobic tank B (502), an MBR membrane group (508) is arranged in each of the MBR tank (503), a mixed liquid backflow pipeline B (509) is connected between each of the aerobic tank B (502) and the anoxic tank B (501), and a sludge backflow pipe B (512) is connected between each of the MBR tank B (503) and the anaerobic tank B (500), and between each of the anaerobic sedimentation tanks (302) and the two-stage UASB (300).

21. The multipoint multi-tank synchronous electrochemical phosphorus removal system according to claim 17, wherein the advanced treatment unit (8) comprises a denitrification deep bed filter (800), a fiber turntable filter (801) and an ultraviolet disinfection channel (802) which are sequentially connected, an outlet end of the MBR tank (503) and an outlet end of the secondary sedimentation tank (403) are commonly connected with an intermediate water tank (510), and an outlet end of the intermediate water tank (510) is respectively connected with an inlet end of the rear phosphorus removal device (7) and an inlet end of the denitrification deep bed filter (800).

22. The multipoint multi-tank synchronous electrochemical phosphorus removal system according to claim 1, further comprising a sludge treatment unit (9), wherein the sludge treatment unit (9) comprises a sludge concentration tank (900) and a sludge dewatering machine room which are sequentially connected, and a sludge conveying pipe (901) is connected between the pretreatment unit B (2), the pre-phosphorus removal device (6), the anaerobic unit (3), the biochemical treatment unit A (4), the biochemical treatment unit B (5), the post-phosphorus removal device (7) and the sludge concentration tank (900).

23. The multipoint multi-tank synchronous electrochemical phosphorus removal system according to claim 1, wherein a material tank (902), a sludge modification bin (903) and a filter press (904) which are sequentially connected are further installed in the sludge dewatering machine room, and an outlet end of the sludge concentration tank (900) is connected with an inlet end of the sludge modification bin (903).

24. A multi-point multi-cell electrochemical phosphorus removal method based on the system of any one of claims 1-23, comprising the following:

when the urban domestic wastewater is treated, insoluble substances in the urban domestic wastewater are removed through a tap water pipe by a pretreatment unit A (1); the pretreated wastewater is treated by a biochemical treatment unit A (4), ammonia nitrogen in the wastewater and degradation organic matters are removed, and the wastewater is temporarily stored in an intermediate water tank (510); the wastewater in the middle water tank (510) enters a front dephosphorization device (7) for dephosphorization, and the wastewater after dephosphorization enters a biochemical treatment unit A (4) through a water outlet pipe (606) for further removing ammonia nitrogen in the wastewater; the sewage with non-standard phosphorus in the middle water tank (510) is treated by a deep treatment unit (8) and discharged after reaching the standard;

when treating high-concentration industrial wastewater, the wastewater is treated by a pretreatment unit B (2) to remove insoluble matters in the wastewater, and wastewater H is discharged; the wastewater H is divided into two parts, one part enters the anaerobic unit (3) through the first direct conveying pipeline (10), and the other part enters the front-mounted dephosphorization device (6) through the water inlet pipe (602) to remove phosphorus, so as to discharge wastewater I; the wastewater I enters an anaerobic unit (3), ammonia nitrogen of the wastewater in the anaerobic unit (3) is nitrified, organic matters in the wastewater are degraded, COD content in the wastewater is reduced, and wastewater J is discharged; the wastewater J enters a biochemical treatment unit B (5), ammonia nitrogen in the wastewater is further nitrified, organic matters in the wastewater are degraded, and wastewater K is discharged; the wastewater K is treated by an advanced treatment unit (8) and discharged after reaching standards;

When the low-concentration industrial wastewater is treated, the wastewater is treated by a pretreatment unit B (2) to remove insoluble matters in the wastewater, and the wastewater H is discharged; the wastewater H enters a biochemical treatment unit B (5) through a second direct conveying pipeline (11), ammonia nitrogen in the wastewater is nitrified, organic matters in the wastewater are degraded, COD content in the wastewater is reduced, and wastewater J is discharged; after the wastewater J is treated by the biochemical treatment unit (5), the wastewater is divided into two parts, one part is dephosphorized by a post-dephosphorization device (7), and the dephosphorized wastewater enters the advanced treatment unit (8); part of wastewater directly enters the advanced treatment unit (8), and the wastewater enters the advanced treatment unit (8) 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;

when the river water is treated, the river water to be treated is divided into two parts, one part of the river water enters a dephosphorization tank (600) through a water inlet pipe (602), dephosphorization is carried out through an electrode plate (605), the dephosphorized sewage flows into a drainage tank (602) for sedimentation, and then enters a mixing tank (601) through a water outlet pipe (606); the first direct conveying pipeline (10) and the parallel pipeline (612) enter the mixing tank (610), and two parts of river water are mixed and directly discharged.

25. The method of claim 24, wherein the current density is 40-60 mA/cm during electrochemical dephosphorization ² The electrolysis time is 15-30 minutes.

26. A method according to claim 24, characterized in that in the pretreatment unit a (1) the waste water is subjected to a first pretreatment tank (100) to remove larger residues and then to a second pretreatment tank (101) to remove small particle impurities.

27. The method according to claim 24, characterized in that the wastewater in the pretreatment unit B (2) is subjected to a third pretreatment tank (200) to remove insoluble substances, and then the PH of the industrial wastewater is adjusted in an adjustment tank (201), and the adjusted wastewater is fed into a primary sedimentation tank (208) for sedimentation.

28. The method according to claim 24, wherein in the anaerobic unit (3), the wastewater entering the anaerobic water inlet tank (301) is pumped into the secondary UASB tank (301) by the anaerobic lift pump (116), and the secondary UASB tank (301) converts large-molecular refractory organic matters into small-molecular organic matters which are easy to be degraded by microorganisms by utilizing an organic matter anaerobic decomposition process, and degrades most insoluble organic matters into soluble matters, and simultaneously consumes carbon sources, reduces COD and creates conditions for the subsequent aerobic treatment; the wastewater treated by the secondary UASB tank (301) overflows into an anaerobic sedimentation tank (302), and the wastewater is sedimented in the anaerobic sedimentation tank (302).

29. The method according to claim 28, wherein in the biochemical treatment unit a (4), the wastewater enters the anaerobic tank a (400), macromolecular refractory organics in the wastewater can be converted into micromolecular organics which are easy to be degraded by microorganisms, carbon sources in the wastewater are consumed, the COD of the wastewater is reduced, the wastewater which is treated enters the anoxic tank a (401) for preliminary precipitation, the wastewater after preliminary precipitation enters the aerobic tank (402), the micromolecular organics which are easy to be degraded by microorganisms are degraded, ammonia nitrogen in the wastewater is nitrified, ammonia nitrogen in the wastewater is removed, the COD of the wastewater is further reduced, the wastewater after ammonia nitrogen removal continues to enter the secondary precipitation tank (403) for secondary precipitation, and the precipitate secondary precipitation generated in the wastewater is removed.

30. The method according to claim 29, characterized in that a fourth direct transfer line (13) is connected between the outlet end of the anaerobic precipitation tank (302) and the anoxic tank a (401), so that the wastewater treated by the anaerobic unit (3) can also be fed directly into the anoxic tank a (401) via the fourth direct transfer line (13) and treated by the biochemical treatment unit a (4).

31. The method according to claim 24, wherein in the biochemical treatment unit B (5), the wastewater sequentially passes through the anaerobic tank B (500), the anoxic tank B (501), the aerobic tank B (502) and the MBR tank (503), thereby removing organic matters, ammonia nitrogen and reducing the COD content in the wastewater.

32. The method according to claim 24, characterized in that the wastewater in the second pretreatment tank (101) is fed via an overflow area (113) to the biochemical treatment unit B (5) via a third direct transfer pipe (12) for biochemical treatment.

33. The multi-point multi-tank synchronous electrochemical phosphorus removal system of claim 24 wherein the water inlet in the phosphorus removal tank (600) and the water outlet in the water outlet tank (601) in the front phosphorus removal device (6) and the rear phosphorus removal device (7) are controlled by solenoid valves.

34. The method according to claim 24, wherein the wastewater is directly fed into the denitrification deep bed filter (800), a carbon source or a flocculating agent is added into the denitrification deep bed filter (800), nitrate nitrogen is further removed through the denitrification deep bed filter (800), the nitrate nitrogen is converted into nitrogen, the finally treated wastewater enters the fiber rotary disc filter (801) to remove SS, and the wastewater is discharged after being sterilized through the ultraviolet sterilizing channel (802) to reach the standard.

35. The method according to claim 29, wherein the sludge in the anaerobic tank a (400), the secondary sedimentation tank (403), the primary sedimentation tank (208), the front dephosphorization device (6) and the rear dephosphorization device (7) can be pumped into the sludge concentration tank (900) by a reflux pump on the sludge conveying pipe (901) through the sludge in each of the two-stage UASB (300), the anaerobic sedimentation tank (302), the anaerobic tank B (500) and the MBR tank (503), and is conveyed into the sludge modification bin (903), and simultaneously, the modifier in the material tank (902) is conveyed into the sludge modification bin (903) so that the sludge entering the sludge modification bin (903) fully reacts with the modifier, and after the sludge reacts in the sludge modification bin (903), the sludge in the sludge modification bin (903) is pressure-filtered into the filter press (904), and is directly discharged after being dehydrated by the filter press (904).

36. The method of claim 35, wherein the modifier is one or both of lime and PAM.