Denitrification and phosphorus removal device and process of short-cut nitrification / anaerobic ammonia oxidation-sulfur autotrophic denitrification coupled struvite method for treating high-concentration wastewater

Abstract

The present application belongs to the field of biological treatment of high ammonia-nitrogen wastewater, and particularly relates to a denitrification and phosphorus removal device and process for treating high-concentration wastewater by coupling short-cut nitrification / anaerobic ammonia oxidation-sulfur autotrophic denitrification with struvite method. The device comprises an IC anaerobic tank connected with an integrated sedimentation tank I, the integrated sedimentation tank I is connected with a medium-temperature ultrafiltration membrane, the medium-temperature ultrafiltration membrane is connected with a contact oxidation system through a phosphorus removal device, the contact oxidation system is connected with an integrated sedimentation tank II through a denitrification system, and the integrated sedimentation tank II is connected with a clean water tank through a sulfur autotrophic denitrification device. The process comprises: high-concentration wastewater is treated by the IC anaerobic tank, then flows into the rotating screen, and then flows into the integrated sedimentation tank I, and then flows into the medium-temperature ultrafiltration membrane, part of the concentrated liquid is returned to the IC anaerobic tank, the clear liquid enters the phosphorus removal device, and then enters the contact oxidation system, and then enters the denitrification system and the integrated sedimentation tank II, and then enters the sulfur autotrophic denitrification device, and then the filtered wastewater enters the clean water tank. The present application can improve the treatment efficiency of the system.

Description

Technical Field

[0001] This invention belongs to the field of biological treatment technology for high ammonia nitrogen wastewater, specifically relating to a nitrogen and phosphorus removal device and process for treating high-concentration wastewater using a short-cut nitrification / anaerobic ammonia oxidation-sulfur autotrophic denitrification coupled with struvite method. Background Technology

[0002] In recent years, with the continuous advancement of urbanization, solid waste has been increasing daily. To improve the resource utilization, reduction, and harmlessness of solid waste, the implementation of garbage classification policies has been gradually promoted. The total amount of kitchen / food waste is increasing daily, and the liquid-phase biogas production after pretreatment of kitchen / food waste has become the main process in the organic solid waste treatment industry. Sanitary landfill of domestic waste has become one of the main treatment methods. To ensure the stable operation of anaerobic digestion of kitchen / food waste wastewater, the effluent SCOD concentration is controlled at 3000~5000mg / L, NH3-N concentration at 2000~3000mg / L, and total phosphorus concentration at 50~100mg / L. Often, the C / N ratio of the biogas slurry is less than 3. More than 90% of biogas slurry treatment in China adopts a two-stage AO biological treatment system. To meet the operating requirements of the wastewater treatment system for total nitrogen removal, an external carbon source is needed to increase the C / N ratio to more than 5. The front-end anaerobic digestion strives to reduce organic matter, while the back-end wastewater treatment strives to add organic carbon sources, creating a contradiction in system operation and increasing the cost per ton of water treatment by more than 20 yuan. The total phosphorus removal capacity of the biological system is 20~40mg / L, and the total phosphorus in the effluent does not meet the discharge standard requirement of 8mg / L. In order to meet the total phosphorus standard, it is necessary to add air flotation and chemical phosphorus removal at the back end.

[0003] Two-stage A / O biological treatment systems utilize phosphorus-releasing bacteria and polyphosphate-accumulating bacteria to first release and then absorb phosphorus into the sludge, achieving phosphorus removal through sludge discharge. When wastewater contains sufficient organic carbon sources, biological methods can remove a portion of the phosphorus. The mainstream process uses air flotation with chemical phosphorus removal, but this method has high operating costs, cannot utilize phosphorus resources, and produces a large amount of sludge. Two-stage A / O biological treatment technology also suffers from high costs and low nitrogen removal efficiency. Summary of the Invention

[0004] The first objective of this invention is to provide a nitrogen and phosphorus removal device for treating high-concentration wastewater using a short-cut nitrification / anaerobic ammonium oxidation-sulfur autotrophic denitrification coupled with struvite process. The second objective of this invention is to provide a nitrogen and phosphorus removal process for treating high-concentration wastewater using a short-cut nitrification / anaerobic ammonium oxidation-sulfur autotrophic denitrification coupled with struvite process. This invention can improve system treatment efficiency and is suitable for nitrogen and phosphorus removal from high-concentration wastewater with low carbon-to-nitrogen ratio and high total phosphorus.

[0005] This invention provides a nitrogen and phosphorus removal device for treating high-concentration wastewater using a short-cut nitrification / anaerobic ammonia oxidation-sulfur autotrophic denitrification coupled struvite process. The device includes an IC anaerobic tank, which is connected to an integrated sedimentation tank I via a vibrating screen. The integrated sedimentation tank I is connected to a mesophilic ultrafiltration membrane, which is then connected to a contact oxidation system via a phosphorus remover. The contact oxidation system is connected to an integrated sedimentation tank II via a denitrification system. The integrated sedimentation tank II is connected to a clear water tank via a sulfur autotrophic denitrifier. The contact oxidation system includes a contact oxidation tank I, which is used for anoxic denitrification, and is connected to a contact oxidation tank II, which is an aerobic biological contact oxidation tank. The denitrification system includes an anaerobic ammonia oxidation tank.

[0006] In one embodiment of the present invention, the IC anaerobic tank is also connected to the mesophilic ultrafiltration membrane, the IC anaerobic tank is also connected to a forced circulation pump, and a central stirrer is provided inside the IC anaerobic tank; the integrated sedimentation tank is also connected to an external sludge desludge system through an anaerobic sludge pump.

[0007] In one embodiment of the present invention, the dephosphorizer includes a dephosphorizing tank and a stirrer. The stirrer is provided with blades at the bottom and the stirrer penetrates into the reaction zone of the dephosphorizing tank from the center of the top of the dephosphorizing tank. The bottom of the dephosphorizing tank is provided with a cone hopper, and the lower part of the cone hopper is connected to a pneumatic knife gate valve, which is connected to a separator.

[0008] In one embodiment of the present invention, a feed trough is provided on one side of the dephosphorization tank, and a discharge port is provided on the other side of the dephosphorization tank. The dephosphorization tank is also provided with a dephosphorization agent port. A discharge plate is provided inside the dephosphorization tank. The discharge plate includes a middle part and movable plates at both ends of the middle part. The middle part is fixed to the dephosphorization tank at a certain angle by a discharge plate movable bolt. The movable plates at both ends hang down naturally and contact the inner wall of the cone hopper to form a closed state. One end of the movable plate is connected to a manual hoist of the discharge plate, and the other end of the manual hoist of the discharge plate is fixed outside the dephosphorization tank.

[0009] In one embodiment of the present invention, the first contact oxidation tank includes an inlet tank, a cyclone aerator, and a contact oxidation tank outlet. The cyclone aerator is used to provide micro-aeration conditions. The first contact oxidation tank also includes a Pall ring packing module, which is used to place packing material. The Pall ring packing module includes multiple sets of Pall ring packing material, which are connected to each other through upper and lower module connectors. The bottom of the first contact oxidation tank is provided with a contact oxidation tank sludge discharge pipe. The second contact oxidation tank includes an elastic three-dimensional packing module, which includes multiple sets of elastic three-dimensional packing material, which are also connected to each other through upper and lower module connectors. A nano-aeration pipe is provided below the elastic three-dimensional packing module. The bottom of the second contact oxidation tank is also provided with a contact oxidation tank sludge discharge pipe, which is also connected to an external sludge desludge system through the anaerobic sludge pump.

[0010] In one embodiment of the present invention, the second contact oxidation tank further includes a contact oxidation tank sludge separation tank, and the contact oxidation tank sludge separation tank is equipped with an online instrument probe, and the online instrument probe, online detection instrument and aeration blower are interlocked and controlled.

[0011] In one embodiment of the present invention, the anaerobic ammonia oxidation tank is provided with multiple sets of packing devices. Each set of packing devices includes an upper anaerobic ammonia oxidation packing module and a lower anaerobic ammonia oxidation packing module. The upper anaerobic ammonia oxidation packing module and the lower anaerobic ammonia oxidation packing module are connected by an upper and lower packing membrane block connector. The bottom of the packing device is also provided with a microporous aeration disc. The denitrification system also includes an anaerobic ammonia oxidation tank outlet and an anaerobic ammonia oxidation tank inlet.

[0012] In one embodiment of the present invention, the IC anaerobic tank is connected to the vibrating screen via an anaerobic discharge pump, the integrated sedimentation tank is connected to the mesophilic ultrafiltration membrane via a sedimentation discharge pump, the mesophilic ultrafiltration membrane is an ultrafiltration membrane system, the denitrification system is connected to the integrated sedimentation tank via an anaerobic ammonia oxidation discharge pump, the integrated sedimentation tank is also connected to an anaerobic ammonia oxidation granular sludge pump, the integrated sedimentation tank is also connected to the sulfur autotrophic denitrifier via a sedimentation discharge pump, the clear water tank is also connected to a clear water pump, the sulfur autotrophic denitrifier is also connected to the contact oxidation system, and the integrated sedimentation tank is also connected to the contact oxidation system.

[0013] This invention also provides a nitrogen and phosphorus removal process for treating high-concentration wastewater using a short-cut nitrification / anaerobic ammonium oxidation-sulfur autotrophic denitrification coupled with struvite. This process utilizes the aforementioned nitrogen and phosphorus removal device for treating high-concentration wastewater using a short-cut nitrification / anaerobic ammonium oxidation-sulfur autotrophic denitrification coupled with struvite. The process includes the following steps: high-concentration wastewater / high-pollution wastewater undergoes fermentation in an IC anaerobic tank and then enters a vibrating screen to remove large particles, obtaining a liquid phase with removed large particles. This liquid phase flows into an integrated sedimentation tank to remove fine suspended solids, resulting in a separated precipitate and separated sludge. The separated sludge then enters an external... The sludge desludge system of the department, the separated precipitate enters the medium-temperature ultrafiltration membrane for solid-liquid separation, obtaining a clear liquid and a partial concentrate. The partial concentrate is returned to the IC anaerobic tank, and the clear liquid enters the dephosphorizer for phosphorus removal, generating struvite crystals, and also obtaining phosphorus-removed wastewater. The phosphorus-removed wastewater enters the contact oxidation system for short-cut nitrification, removing organic matter and suspended solids. Excess sludge enters the external desludge desludge system. The treated wastewater enters the denitrification system and the integrated sedimentation tank for secondary denitrification, and then enters the sulfur autotrophic denitrifier for sulfur autotrophic denitrification to remove residual nitrogen. The filtered wastewater enters the clear water tank.

[0014] The dephosphorizer is filled with a packing material, which includes at least one of a mesh polyurethane packing material and a mesh sponge dephosphorization and denitrification packing material. The raw materials of the mesh sponge dephosphorization and denitrification packing material include the following components in parts by weight: 70-100 parts of polyether polyol, 3-6 parts of water, 1-2 parts of catalyst, 1-2 parts of surfactant, 2-5 parts of filler, 5-20 parts of magnesium salt, and 5-20 parts of pyrite powder. The preparation method of the mesh sponge dephosphorization and denitrification packing material includes the following steps: stirring the raw materials in proportion to obtain a mixed pre-agent; foaming the mixed pre-agent to obtain the mesh sponge dephosphorization and denitrification packing material.

[0015] In one embodiment of the present invention, the catalyst includes an amine catalyst, wherein the amine catalyst includes at least one of triethylamine, ethylenediamine, and alkanolamine; the surfactant includes at least one of a pore-opening agent and silicone oil, wherein the pore-opening agent includes at least one of an alkali metal salt of fatty acid, kerosene, and mineral oil, and the silicone oil includes silicone oil L580; the filler includes at least one of light calcium carbonate, silica lime, and bentonite, and the particle size of the filler is 200-500 mesh; the magnesium salt includes at least one of magnesium hydroxide, magnesium chloride, and magnesium sulfate, and the particle size of the magnesium salt is 200-500 mesh; the pyrite powder has a particle size of 200-500 mesh; and the preparation method of the mesh sponge dephosphorization and denitrification filler includes the following steps: mixing the raw materials in a 10 The mixture is stirred at 00~2000 r / min for 20~40 min to obtain a mixed pre-reagent. The mixed pre-reagent is foamed, and after the high-pressure reactor is heated to 150±5℃, the mixed pre-reagent and 40~60 parts of toluene diisocyanate are stirred at 3000~4000 r / min for 5~8 s. The mixture is then quickly poured into a high-pressure reactor that has been heated to 150±5℃. Carbon dioxide is then introduced into the high-pressure reactor at a pressure of 3~7 MPa. After maintaining the pressure for 30~60 min, the pressure in the high-pressure reactor is instantly reduced and released to obtain the initial mesh sponge phosphorus and nitrogen removal packing. After cooling to room temperature, the initial mesh sponge phosphorus and nitrogen removal packing is cut into square packing with a side length of 20~30 mm to obtain the mesh sponge phosphorus and nitrogen removal packing.

[0016] In one embodiment of the present invention, the operating parameters of the IC anaerobic digester include:

[0017] Feed load OLR: 5~10 kg / m 3 • d, pH: 7.2~8.0, volatile fatty acids (VFA): 500~1000 mg / L, alkalinity: 25000~30000 mg / L, hydraulic retention time (HRT): 30~45 days, NH3-N: 2000~2500 mg / L, total nitrogen (TN): 2500~3000 mg / L, COD: 2500~6000 mg / L, total sulfide (TS): 1.5%~2.0%, total vitamin C (VS): 25%~35%, temperature: 55℃; biogas production per ton of influent: 80~110 m³ / ton 3 / h, CH4: 68%~70%, CO: 29.6%~31.7%, O2: 0, H2S: 0.3%~0.4%;

[0018] The operating parameters of the medium-temperature ultrafiltration membrane include: ultrafiltration water production rate: 50%~70%, water production flux: 60~110 LMH, operating temperature: 50~60℃, pipeline flow rate: 4~6 m / s, effluent SS <500 mg / L, and chemical cleaning when the water production flux decreases by 10%~20%.

[0019] The operating parameters of the contact oxidation system include: an aeration ratio controlled at 3:1 to 10:1, dissolved oxygen controlled at 0.5 to 0.7 mg / L, and a five-day biochemical oxygen demand (BOD5) volumetric loading of 0.2 to 1.5 kg BOD5 / (m³). 3 •d); The suspended packing filling rate of the first contact oxidation tank is 50%~80%; the suspended packing filling rate of the second contact oxidation tank is 50%~80%; the hydraulic retention time is 0.5h~3.0h for the first contact oxidation tank and 12h~48h for the second contact oxidation tank; the clear liquid reflux ratio of the second integrated sedimentation tank is 50%~200%;

[0020] The operating parameters of the anaerobic ammonia oxidation tank include: influent nitrate nitrogen: 400 mg / L; alkalinity: ≥1700 mg / L; pH>7.2, operating temperature controlled at 30℃~37℃; effluent nitrate nitrogen: 70 mg / L; alkalinity: no requirement; pH>6-9; reactor: diameter × height = 0.5 m * 2.5 m, of which the packing height is 2 m; hydraulic retention time: 4-6 h; volumetric loading: 0.8~1.3 kgN / m3·d; influent type: upflow type; backwashing: adopts upflow high-speed water flow backwashing method, backwashing once every 1-2 months, backwashing intensity is 7~10 L / (m2·s), and rinsing time is 3~5 min.

[0021] It should be noted that in this invention, the two-stage A / O biological treatment system utilizes phosphorus-releasing bacteria and polyphosphate-accumulating bacteria to first release and then absorb phosphorus into the sludge, achieving phosphorus removal through sludge discharge. When there is sufficient organic carbon source in the wastewater, biological methods can remove a portion of the phosphorus. The mainstream process uses air flotation with chemical phosphorus removal, but this method has high operating costs, cannot utilize phosphorus resources, and produces a large amount of sludge. In biogas slurry, the concentration of free ammonia nitrogen is high and the concentration of total phosphorus is low. This invention utilizes the principle of struvite crystallization. By adding magnesium salts and controlling the Mg:P mass ratio at 1.1:1~1.5:1, the total phosphorus in the effluent is reduced to below 10 mg / L after overcoming the magnesium salt limitation factor for struvite crystallization. Resource utilization is achieved by separating and recovering the struvite crystals.

[0022] Two-stage A / O biological treatment technology suffers from high costs and low nitrogen removal efficiency. To achieve sustainable development in wastewater treatment, this invention utilizes a low-energy, high-efficiency combined process of a short-cut nitrification biological contact oxidation tank + an anaerobic ammonia oxidation tank + a sulfur autotrophic denitrification process. After solid-liquid separation, the biogas slurry enters the biological contact oxidation tank, where heterotrophic bacteria utilize COD, while simultaneously, under a microaerobic environment, ammonia-oxidizing bacteria reduce NH4+. + -N is converted to NO2 - -N, aeration rate and online NH4 + -N, NO2 - -N and NO3 -The -N detector and analyzer employs intelligent interlock control. When ammonia nitrogen reaches its "low point," the frequency of Roots blower aeration is reduced to keep the system in the short-cut nitrification stage. The short-cut nitrification effluent provides NH4 to the anaerobic ammonia oxidation process. + -N and NO2 - -N, approximately 10% NO3 will be produced during anaerobic ammonium oxidation. - -N, the back end uses sulfur-autotrophic denitrifying bacteria to remove total nitrogen using CO2 carbon source, so that the total nitrogen and total phosphorus in the effluent meet the discharge standards.

[0023] The beneficial effects of this invention are:

[0024] 1) Since kitchen waste / food scrap is rich in phosphorus (P), a phosphorus removal reactor converts the phosphorus into struvite, which contains over 60% phosphorus. Struvite can be used as a raw material for phosphate fertilizer production or as a slow-release fertilizer for crop growth. This process transforms kitchen wastewater into valuable resources and fundamentally solves the problem of struvite scaling in downstream process pipelines.

[0025] 2) Solid-liquid separation of biogas slurry is achieved through an integrated sedimentation tank and ultrafiltration membrane. The solids are recycled to the anaerobic system, further converting organic matter into biogas, increasing the organic matter conversion rate to 5%~10%. Using membrane separation, compared to conventional centrifugation with flocculants, saves at least 20 yuan / ton in operating costs. It also avoids the impact of flocculant addition on subsequent wastewater biological treatment systems. The SS in the membrane-permeable effluent is <500mg / L, fundamentally solving the operational problem of high SS in the influent leading to high sludge production, which prevents the enrichment of microorganisms in the contact oxidation and anaerobic ammonia oxidation tanks.

[0026] 3) The packing materials in the contact oxidation system and denitrification system adopt a modular design, which is simple in structure and easy to install. The pre-cultivated microbial strain modules can be sold externally as strains, and can also serve as a microbial strain cultivation base for new projects.

[0027] 4) This project has low operating costs. Compared to the conventional two-stage A / O process, the sludge discharge of this invention is less than 10% of the former; the air-to-water ratio of the two-stage A / O process is controlled above 20:1, while the air-to-water ratio of this invention is less than half of that; the two-stage A / O process requires an external carbon source reagent cost of 30-50 yuan / ton of water to achieve total nitrogen removal, while this invention does not require an external carbon source. The total operating cost of this invention is 15%-30% of that of the two-stage A / O process.

[0028] 5) The use of sulfur autotrophic denitrification process replaces the conventional A / O system, reducing operating costs by 70%~80% and simplifying operation and maintenance.

[0029] In summary, this invention is suitable for small-scale food waste processing projects, operates stably, and can effectively handle by-products. Attached Figure Description

[0030] The accompanying drawings are provided to further illustrate the invention and form part of the specification. They are used in conjunction with embodiments of the invention to explain the invention and do not constitute a limitation thereof. In the drawings:

[0031] Figure 1 This is a schematic diagram of the process flow of the present invention;

[0032] Figure 2 This is a schematic diagram of the overall structure of the device of the present invention;

[0033] Figure 3 This is the invention Figure 2 Enlarged view of part A in the image; Figure 3 The text on the left side of the image refers to high-concentration wastewater, while the text on the right side refers to the sludge removal system.

[0034] Figure 4 This is the invention Figure 2 Enlarged view of part B in the image; Figure 4 The text in the text indicates that bird droppings granules are sold externally.

[0035] Figure 5 This is the invention Figure 2 Enlarged view of part C in the image; Figure 5 The text on the left side indicates that granular sludge is sold externally, while the text on the right side indicates that clean water is discharged in compliance with standards.

[0036] Figure 6 This is a schematic diagram of the phosphorus removal device structure of the present invention;

[0037] Figure 7 This is a schematic diagram of the contact oxidation system and denitrification system of the present invention;

[0038] Figure 8 This is a schematic diagram illustrating the principle of the present invention;

[0039] The diagram is labeled as follows: 1. IC anaerobic tank; 2. Central agitator; 3. Forced circulation pump; 4. Anaerobic discharge pump; 5. Vibrating screen; 6. Integrated sedimentation tank one; 7. Anaerobic sludge pump; 8. Sedimentation discharge pump one; 9. Medium-temperature ultrafiltration membrane; 10. Phosphorus remover; 10-1. Phosphorus removal tank; 10-2. Agitator; 10-3. Manual hoist for unloading plate; 10-4. Phosphorus removal agent inlet; 10-5. Feed trough; 10-6. Discharge port; 10-7. Unloading plate; 10-8. Unloading plate movable bolt; 10-9. Pneumatic knife gate valve; 11. Separator; 12. Contact oxidation system; 12-1. Inlet tank; 12-2. Cyclone aerator; 12-3. Contact oxidation tank outlet; 12-4. Pall ring packing module; 12-5. Contact oxidation tank one; 12-6. Upper and lower module connector; 12 12-7. Nano-aeration pipe; 12-8. Sludge discharge pipe of contact oxidation tank; 12-9. Contact oxidation tank II; 12-10. Elastic three-dimensional packing module; 12-11. Online instrument probe; 12-12. Sludge separation tank of contact oxidation tank; 13. Denitrification system; 13-1. Inlet hole of anaerobic ammonia oxidation tank; 13-2. Microporous aeration disc; 13-3. Lower anaerobic ammonia oxidation packing module; 13-4. Upper anaerobic ammonia oxidation packing module; 13-5. Anaerobic ammonia oxidation tank; 13-6. Connector of upper and lower packing membrane blocks; 13-7. Outlet hole of anaerobic ammonia oxidation tank; 14. Aeration blower; 15. Anaerobic ammonia oxidation discharge pump; 16. Integrated sedimentation tank II; 17. Anaerobic ammonia oxidation granular sludge pump; 18. Sedimentation discharge pump II; 19. Sulfate autotrophic denitrifier; 20. Clear water tank; 21. Clear water pump. Detailed Implementation

[0040] The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0041] Unless otherwise specified, the equipment and materials used in the embodiments can be readily obtained from commercial companies.

[0042] The basic working principles / structures of the following components are well-known and will not be elaborated upon: IC anaerobic tank 1, forced circulation pump 3, vibrating screen 5, integrated sedimentation tank or integrated sedimentation tank, medium temperature ultrafiltration membrane 9, manual hoist / hand chain hoist, movable bolt, pneumatic knife gate valve 10-9, cyclone aerator 12-2, Pall ring packing, anoxic denitrification contact oxidation tank, aerobic biological contact oxidation tank, elastic three-dimensional packing, nano aeration pipe 12-7, anaerobic ammonia oxidation tank 13-5, and sulfur autotrophic denitrifier 19.

[0043] Anaerobic discharge pump 4 is a discharge pump; manual hoist 10-3 is a manual hoist / hand-operated hoist; movable bolt 10-8 is a movable bolt; Pall ring packing module 12-4 is Pall ring packing; contact oxidation tank one 12-5 is an anoxic denitrification contact oxidation tank; contact oxidation tank two 12-9 is an aerobic biological contact oxidation tank. Integrated sedimentation tank one 6 and integrated sedimentation tank two 16 are both integrated sedimentation tanks or combined sedimentation tanks.

[0044] Example 1

[0045] Reference Figure 2 A nitrogen and phosphorus removal device for treating high-concentration wastewater using a short-cut nitrification / anaerobic ammonia oxidation-sulfur autotrophic denitrification coupled struvite process, including IC anaerobic tank 1.

[0046] Reference Figure 2 and Figure 3 The IC anaerobic tank 1 has a central agitator 2 in its center. The top of the IC anaerobic tank 1 has an upper discharge port and a lower discharge port.

[0047] The IC anaerobic digester 1 is connected to the forced circulation pump 3 via a pipeline. The IC anaerobic digester 1 is connected to the vibrating screen 5 via an anaerobic discharge pump 4, specifically: the IC anaerobic digester 1 is connected to the anaerobic discharge pump 4 via a pipeline, and the anaerobic discharge pump 4 is connected to the vibrating screen 5 via a pipeline. The internal structure of the vibrating screen 5, from top to bottom, includes: a screen body, a vibration source, and a screen bottom. The screen body includes a screen frame, a screen surface, and a screen mesh, with screen holes formed on the screen mesh. The vibration source is a motor, with weights mounted above and below the motor bearings. The screen bottom includes a liquid hopper; the vibrating screen 5 also has a slag hopper at its bottom.

[0048] The vibrating screen 5 is connected via a pipe to an integrated sedimentation tank 6. The integrated sedimentation tank 6 is an inclined plate sedimentation tank with a 90° inclination angle. The integrated sedimentation tank 6 includes an inlet zone, a sedimentation zone, an effluent zone, and a sludge collection zone. The inlet zone includes an inlet baffle and connects to the sedimentation zone. A set of parallel plates or a set of square pipes are installed within the sedimentation zone. An overflow plate is installed outside the parallel plates or square pipes, and the overflow plate connects to a storage tank for storing the settled clear sludge. The sedimentation zone connects to the sludge collection zone, which includes a sludge hopper for collecting settled sludge. The sludge hopper connects to an anaerobic sludge pump 7, which is connected via a pipe to an external sludge removal system.

[0049] Reference Figure 2 and Figure 4The storage tank is connected to the effluent area, which is piped to sedimentation discharge pump 8. Sedimentation discharge pump 8 is piped to the mesophilic ultrafiltration membrane 9. The mesophilic ultrafiltration membrane 9 is an ultrafiltration membrane system, which consists of multiple tubular ultrafiltration membranes resistant to 50~70℃, forming an ultrafiltration membrane module. The ultrafiltration membrane can be used for filtration. The ultrafiltration membrane module is equipped with an ultrafiltration circulation pump, which is piped to the ultrafiltration circulation pump. The mesophilic ultrafiltration membrane 9 is also piped to the upper part of the IC anaerobic tank 1. The medium-temperature ultrafiltration membrane 9 is also connected in a pipeline to the dephosphorizer 10. The dephosphorizer 10 includes a dephosphorizer tank 10-1, a feed trough 10-5 on one side of the dephosphorizer tank 10-1, a discharge port 10-6 on the other side of the dephosphorizer tank 10-1, and a dephosphorizing agent port 10-4 at the top of the dephosphorizer tank 10-1. The number of dephosphorizing agent ports 10-4 can be two. A conical hopper is provided at the bottom of the dephosphorizer tank 10-1, and a pneumatic knife gate valve 10-9 is connected to the lower part of the conical hopper. The pneumatic knife gate valve 10-9 is connected in a pipeline to the separator 11. A reaction zone is provided inside the dephosphorizer tank 10-1.

[0050] Reference Figures 2-4 and Figure 6 The dephosphorizer 10 also includes an agitator 10-2. The agitator 10-2 has blades at its bottom and penetrates into the reaction zone of the dephosphorizer 10-1 from the center of its top. The bottom of the dephosphorizer 10-1 is equipped with a discharge plate 10-7. The discharge plate 10-7 includes movable plates at both ends and a central section. The central section is fixed to the dephosphorizer 10-1 at a certain angle by a discharge plate movable bolt 10-8. The movable plates at both ends hang naturally and contact the inner wall of the cone to form a closed state. The discharge plate movable bolt 10-8 is a movable bolt. One end of the movable plate is connected to a manual discharge plate hoist 10-3, and the other end of the manual discharge plate hoist 10-3 is fixed to the top of the dephosphorizer 10-1. The manual discharge plate hoist 10-3 is a manual hoist / hand-operated hoist.

[0051] Reference Figures 2-4 and Figures 6-7 The discharge port 10-6 of the dephosphorizer 10 is connected via a pipeline to the contact oxidation system 12. The contact oxidation system 12 includes a contact oxidation tank 12-5, which is used for anoxic denitrification and is also an anoxic denitrification contact oxidation tank. The contact oxidation tank 12-5 includes an inlet tank 12-1 and a swirl aerator 12-2, which provides micro-aeration conditions. The contact oxidation tank 12-5 also includes a Pall ring packing module 12-4, which is a Pall ring packing module used to hold the packing material. The Pall ring packing module 12-4 is made of PP and includes two sets of Pall ring packing, which are connected by an upper and lower module connector 12-6. A contact oxidation tank sludge discharge pipe 12-8 is provided at the bottom of the contact oxidation tank 12-5.

[0052] The contact oxidation system 12 also includes a second contact oxidation tank 12-9, which is pipe-connected to the contact oxidation tank outlet 12-3 of the first contact oxidation tank 12-5. The second contact oxidation tank 12-9 is an aerobic biological contact oxidation tank, and includes an elastic three-dimensional packing module 12-10. The elastic three-dimensional packing module 12-10 includes two sets of elastic three-dimensional packing materials connected by an upper and lower module connector 12-6. A nano-aeration pipe 12-7 is located at the bottom of the elastic three-dimensional packing module 12-10. A sludge discharge pipe 12-8 is located at the bottom of the second contact oxidation tank 12-9.

[0053] The sludge discharge pipe 12-8 of the contact oxidation tank is connected to an external sludge desludge system. The second contact oxidation tank 12-9 also includes a sludge separation tank 12-12. NH4+ is installed above the sludge separation tank 12-12. + -N and NO2 - -N online instrument probe 12-11. Online instrument probe 12-11 is interlocked with online detection instruments and aeration fan 14, which is a Roots blower.

[0054] The sludge separation tank 12-12 of the contact oxidation tank is connected to the inlet 13-1 of the anaerobic ammonia oxidation tank of the denitrification system 13. The denitrification system 13 also includes an anaerobic ammonia oxidation tank 13-5, which is equipped with two sets of packing devices. Each set of packing devices includes an upper anaerobic ammonia oxidation packing module 13-4 and a lower anaerobic ammonia oxidation packing module 13-3, which are connected by an upper and lower packing membrane block connector 13-6. The upper and lower packing membrane block connector 13-6 can be a bolt connector. A microporous aeration disc 13-2 is also provided at the bottom of the packing device. The denitrification system 13 also includes an anaerobic ammonia oxidation tank outlet 13-7.

[0055] The anaerobic ammonia oxidation tank effluent outlet 13-7 is pipe-connected to the anaerobic ammonia oxidation discharge pump 15. The anaerobic ammonia oxidation discharge pump 15 is pipe-connected to the integrated sedimentation tank 16. The structure of the integrated sedimentation tank 16 is the same as that of the integrated sedimentation tank 6. The integrated sedimentation tank 16 is also pipe-connected to the anaerobic ammonia oxidation granular sludge pump 17. The integrated sedimentation tank 16 is also pipe-connected to the sedimentation discharge pump 18. The sedimentation discharge pump 18 is pipe-connected to the contact oxidation tank 12-5. The sedimentation discharge pump 18 is also pipe-connected to the sulfur autotrophic denitrifier 19. The sulfur autotrophic denitrifier 19 includes activated biological packing material for nitrogen removal. The bottom of the sulfur autotrophic denitrifier 19 has a water distribution pipe with activated biological packing material on it. A stainless steel sieve plate is added on top of the activated biological packing material, and a filter bed is set on the stainless steel sieve plate. An effluent trough is set on the filter bed. The sulfur autotrophic denitrifier 19 is also connected to an external backwashing device for backwashing the sulfur autotrophic denitrifier 19. The sulfur autotrophic denitrifier 19 is also connected to the contact oxidation system 12.

[0056] The outlet tank of the sulfur autotrophic denitrifier 19 is connected to the clear water tank 20 via a pipeline, and the clear water tank 20 is connected to the clear water pump 21 via a pipeline. The aeration blower 14 is connected to the contact oxidation system 12, the denitrification system 13, and the sulfur autotrophic denitrifier 19 to control the overall aeration rate.

[0057] The specific processes and parameters of the above-mentioned equipment are described in detail in the following operating steps.

[0058] Reference Figure 1 The nitrogen and phosphorus removal process for treating high-concentration wastewater using short-cut nitrification / anaerobic ammonium oxidation-sulfur autotrophic denitrification coupled with struvite, combined with the aforementioned equipment, includes the following process / operation steps:

[0059] S1: High-concentration wastewater / high-volume sewage undergoes fermentation in IC anaerobic tank 1. High-concentration wastewater is fed from the top of IC anaerobic tank 1 and mixed by the central agitator 2 inside the tank, maintaining a completely mixed state. To increase the processing load, a forced circulation pump 3 is installed externally to maintain an upward flow velocity of 2~10 m / s within the cross-section of IC anaerobic tank 1. The high-concentration wastewater (mainly containing carbohydrates, proteins, and fats) enters IC anaerobic tank 1 and, after decomposition and metabolism by various microorganisms, produces methane, carbon dioxide, hydrogen sulfide, and water.

[0060] Top discharge port: Allows for periodic discharge from the top, preventing top scum from forming a crust and reducing adverse effects on anaerobic digestion.

[0061] Bottom discharge port: Under the combined stirring action of the central agitator 2 and the forced circulation pump 3, the sand and gravel in the IC anaerobic tank 1 are suspended and discharged from the system through the bottom discharge port.

[0062] By alternating between upper and lower discharge operations, the problems of scum crusting at the top and sand accumulation at the bottom of IC anaerobic tank 1 are solved.

[0063] After being concentrated and separated by the medium-temperature ultrafiltration membrane 9, the concentrated liquid is returned to the upper part of the IC anaerobic tank 1 to further increase the biogas production from further fermentation of organic matter.

[0064] S2: The IC anaerobic tank 1 discharges to the rotary vibrating screen 5 to remove large particles. The anaerobic discharge pump 4 pumps the material from the upper or lower discharge port of the IC tank to the rotary screen 5. Under the high speed of rotation, the liquid phase with a particle size of less than 0.6mm passes through the screen holes and drips into the liquid collection hopper. The solid phase is squeezed and dewatered by the power of the rotating vibrating screen 5 and thrown into the slag hopper. The residue in the slag hopper is transported off-site for disposal. The residue can be transported off-site using a sludge / residue transport vehicle.

[0065] Specifically, the vibrating screen 5 utilizes counterweights (unbalanced hammers) mounted above and below the motor bearings to convert the motor's rotational motion into a three-dimensional motion encompassing horizontal, vertical, and inclined directions. This motion is then transmitted to the screen surface via a plug cylinder, causing the material to undergo an outward involute motion on the screen surface. Simultaneously, this provides rotational kinetic energy to the particles on the screen surface, causing fibrous materials to roll into spherical shapes. The inner and outer layers of these spherical materials are compressed, achieving dewatering. Additionally, large gravel is directly thrown to the slag outlet. The spherical materials on the screen surface undergo tangential motion under centrifugal force, thus being thrown to the slag outlet. Meanwhile, the liquid phase drips through the screen holes into the liquid collection hopper and flows by gravity to the integrated sedimentation tank 6 for natural sedimentation and separation.

[0066] To prevent suspended matter from clogging the screen holes, an automatic flush should be performed every 8 to 12 hours. The flushing water pressure should be 0.2 to 0.35 MPa. Rotate the automatic nozzle, keeping the nozzle 0.1 to 0.15 m away from the screen surface, and use tap water for 1 to 5 minutes.

[0067] S3: The liquid phase material removed from the vibrating screen 5 flows into the integrated sedimentation tank 6 by gravity to remove fine suspended solids.

[0068] Specifically: Wastewater separated by the vibrating screen 5 enters the integrated sedimentation tank 6. Under the deceleration and buffering effect of the inlet baffle in the integrated sedimentation tank 6, the wastewater slowly and evenly enters the sedimentation zone from the bottom of the inlet baffle. A set of parallel plates (or a set of square pipes) is installed in the sedimentation zone to allow the treated water and settled sludge to move and separate in the shallow sedimentation layer. The liquid phase after shallow separation flows horizontally to the circular (or triangular) overflow plate at the outlet end for further separation. The separated precipitate flows to the storage tank of the sedimentation tank and is pumped to the medium-temperature ultrafiltration membrane 9 by the sedimentation discharge pump 8. Wastewater and the separated sludge are collected in the sludge hopper. The sludge in the sludge hopper is transported to the external sludge desludge system by the anaerobic sludge pump 7. The desludge clear liquid is returned to the storage tank of the integrated sedimentation tank 6, and the dry sludge is transported for disposal.

[0069] S4: Medium-temperature ultrafiltration for solid-liquid separation.

[0070] Specifically, the liquid phase in the storage tank of the integrated sedimentation tank 6 is transported to the medium-temperature ultrafiltration membrane 9 by the sedimentation discharge pump 8. Then, the liquid phase is pressurized by the ultrafiltration circulation pump in the medium-temperature ultrafiltration membrane 9 and transported to the water distribution port of the ultrafiltration membrane element, and evenly enters the 8mm (or 12.5mm) membrane tube. Under a pressure of 0.3~0.45 bar, the suspended solids are intercepted by the 0.02-micron membrane pores, and the liquid phase with a diameter of less than 0.02 microns permeates through the membrane pores. The clear liquid is transported to the phosphorus remover 10, part of the concentrated liquid is returned to the IC anaerobic tank 1, and the remaining concentrated liquid is returned to the ultrafiltration circulation pump.

[0071] S5: Phosphorus removal is performed by the dephosphorizer.

[0072] The dephosphorizer 10 is filled with packing material. Medium-temperature ultrafiltration permeate enters the feed trough 10-1 within the dephosphorizer 10. Buffered by the baffles in the feed trough 10-1, the material enters the reaction zone of the dephosphorizer 10-1 from the bottom of the feed trough 10-1. Simultaneously, magnesium salt is added from the dephosphorizing agent inlet 10-4 at a Mg:P ratio of 1.1~1.5 to the influent. Under the stirring and mixing action of the agitator 10-2 in the reaction zone, free NH4+ is released. + PO4 3- Mg 2+ A chemical reaction occurs to generate struvite crystals. The crystals adhere to the surface of the packing material. Under the downward pushing action of the bottom impeller of the agitator 10-2, the packing material first moves downward, then bounces back and moves upward. When the packing material reaches the action area of ​​the upper impeller, the upper agitator of the agitator 10-2 keeps the packing material in a suspended state, ensuring that the packing material is in full contact with the struvite crystals produced in the liquid phase, so that the crystals attached to the surface of the packing material grow slowly.

[0073] The packing material inside the phosphorus remover 10 consists of: a porous suspended ball containing a plastic hollow float, a mesh polyurethane packing, and a mesh sponge phosphorus and nitrogen removal packing.

[0074] Production steps of mesh sponge dephosphorization and denitrification filler: (1) Use a stirrer to stir 70-100 parts of polyether polyol, 3-6 parts of water, 1-2 parts of catalyst, 1-2 parts of surfactant, 2-5 parts of filler, 5-20 parts of magnesium salt, and 5-20 parts of pyrite powder for 30 minutes at 1000-2000 r / min to obtain a mixed pre-reagent. Among them, the catalyst is an amine catalyst, such as triethylamine, ethylenediamine, and alkanolamine; the surfactant is a special pore-opening agent and silicone oil, including silicone oil L580, and the pore-opening agent includes fatty acid alkali metal salts, kerosene, and mineral oil; the filler is light calcium carbonate, silica lime, and bentonite with a particle size of 400 mesh; the magnesium salt is magnesium hydroxide, magnesium chloride, and magnesium sulfate with a particle size of 400 mesh; and the pyrite powder has a particle size of 400 mesh.

[0075] (2) The mixed pre-reagent is foamed by supercritical CO2 pressure foaming. The method is as follows: after heating the high-pressure reactor to 150±5℃, the mixed pre-reagent and 40~60 parts of toluene diisocyanate are stirred at 3000~4000r / min for 5~8s, and then quickly poured into the high-pressure reactor that has been heated to 150±5℃. Carbon dioxide is pressurized to 3~7MPa and then introduced into the high-pressure reactor. After maintaining the pressure for 30~60min, the pressure in the high-pressure reactor is instantly reduced and released to obtain the initial mesh sponge dephosphorization and denitrification packing. After cooling to room temperature, the initial mesh sponge dephosphorization and denitrification packing is cut into square packing with a side length of 20~30mm.

[0076] (3) Magnesium and iron salts are added to the pores of the mesh sponge phosphorus and nitrogen removal packing, dissolving them in the mixed solution. The free iron salts react with phosphate ions to form ferric phosphate precipitate, which is suspended around the packing. Simultaneously, free magnesium ions react with phosphate and ammonium ions to form magnesium ammonium phosphate hexahydrate. The magnesium ammonium phosphate hexahydrate uses the precipitated ferric phosphate as crystal nuclei, and the crystal nuclei collide with the porous suspended ball skeleton in the phosphorus removal combined packing. The crystals on the porous suspended ball skeleton gradually grow until they are discharged from the system, thus achieving the removal of ammonia nitrogen and total phosphorus.

[0077] When the filler crystals grow large enough, their weight exceeds the thrust of the agitator 10-2, causing the filler crystals to settle above the discharge plate 10-7 at the lowest point. The discharge plate 10-7 is then lifted by the manual hoist 10-3. Supported by the movable bolt 10-8, the discharge plate 10-7 opens an outlet upwards, meaning its movable plate is pulled upwards. After being pulled up, the movable plate remains slightly tilted downwards. Large filler crystals, under the thrust of the agitator 10-2, are discharged into the conical hopper through the outlets on both sides. This outlet is the opening of the discharge plate 10-7.

[0078] After the bottom-set packing crystals are discharged, lower the manual hoist 10-3 of the discharge plate and close the outlet of the discharge plate 10-7. Install staggered pneumatic gate valves 10-9 below the cone hopper. First, open the upper pneumatic gate valve 10-9, close it after 1-2 minutes, and then open the lower pneumatic gate valve 10-9 to discharge the packing crystals to the separator 11. The separator 11 removes the packing crystals from the liquid phase. Larger, qualified packing crystals are sold, while smaller particles are returned to the dephosphorizer 10. The packing crystals are discharged every 1-2 weeks, while packing material equal to half the total volume of the discharged crystals is added to the inside and outside of the dephosphorizer 10-1. The separated packing crystals are dried at 105℃ and vibrated repeatedly until the phosphorus-containing crystal powder falls off the packing surface. The separated dephosphorized packing can then be reused in the dephosphorizer 10. The phosphorus content in the phosphorus-containing crystalline powder exceeds 80%, thus realizing the recovery of phosphorus resources.

[0079] Chemical reaction formula for struvite crystallization:

[0080] .

[0081] Influent total phosphorus: 50~100mg / L, effluent total phosphorus: 6~8mg / L, total phosphorus removal rate: 88%~92%.

[0082] S6: Biological contact oxidation tank for short-cut nitrification, removing organic matter and suspended solids.

[0083] Wastewater after total phosphorus removal by dephosphorizer 10 and return liquid from sedimentation discharge pump 2 18 are mixed and flow into inlet tank 12-1. The mixture then enters the bottom of the reaction tank from the bottom of the inlet tank. Under the micro-aeration conditions of cyclone aerator 12-2, with a dissolved oxygen concentration between 0.5 and 0.7 mg / L, denitrifying bacteria utilize the organic carbon source in the system influent to react with NO3- in the return liquid from sedimentation discharge pump 2 18. - -N undergoes denitrification to produce N2, which degrades some organic pollutants and also generates alkalinity. In an anaerobic environment, ammonia-oxidizing bacteria oxidize ammonia nitrogen into nitrite, forming short-cut nitrification. Microorganisms attached to the surface of the packing material in the anoxic biological contact oxidation tank utilize the organic matter in the influent to grow and form sludge flocs.

[0084] The anoxic denitrification contact oxidation tank, also known as contact oxidation tank 12-5, uses a combined suspended packing material in Pall ring packing module 12-4. Small pieces of polyurethane biological packing material are placed inside the hollow PP spheres of module 12-4. Each spherical packing material is strung together with a rope, and both ends of each string of spherical combined packing materials are fixed to the module frame of module 12-4. Heterotrophic bacteria attached to the spherical packing materials adsorb and capture pollutants using oxygen molecules and then metabolize them. Due to the microaerobic environment in the mixed liquor, the dissolved oxygen on the surface of the heterotrophic bacteria on the spherical packing materials is limited, resulting in a gradual decrease in dissolved oxygen concentration from the outside to the inside of the spherical combined packing materials. The microorganisms on the surface of the spherical packing materials can only adsorb and degrade a portion of the organic pollutants; the majority of organic pollutants seep into the vicinity of the polyurethane packing materials through the gaps on the spherical surface. In the anoxic environment, denitrifying bacteria utilize organic matter to oxidize anaerobic ammonia, releasing residual NO3 from the water. - -N is converted into N2. Polyurethane biofiller provides an environment for the enrichment of denitrifying bacteria, extending the residence time to 15-20 days.

[0085] The aerobic biological contact oxidation tank, also known as contact oxidation tank 2 (12-9), has nano-aeration pipes (12-7) installed at the bottom of the membrane module (12-10) of the elastic three-dimensional packing material. Due to the buoyancy of the rising nano-bubbles, the bubbles supply oxygen to the sludge clumps attached to the elastic three-dimensional packing material, maintaining a micro-aerobic environment with dissolved oxygen between 0.7 and 1.0 mg / L. Heterotrophic bacteria utilize the organic matter in the wastewater for metabolism, while ammonia-oxidizing bacteria autotrophically convert NH4+ into nitrogen. +-N is converted into NO2 - -N, and utilizes the oxidation of ammonia nitrogen to meet the energy requirements for growth. Microorganisms gradually accumulate on the surface of the packing material, but the internal microorganisms gradually enter the aging stage, and their adsorption capacity decreases accordingly. Under the scouring of aeration, the microorganisms attached to the surface of the packing material can be blown off, forming granular sludge. When the sludge in the contact oxidation system 12 accumulates to a certain amount, the sludge is discharged to the desludge system through the sludge discharge pipe 12-8 of the contact oxidation tank. The dry sludge is transported off-site for disposal, and the desludge clear liquid is returned to the contact oxidation system 12.

[0086] When the effluent from the contact oxidation tank passes through the sludge separation tank 12-12, the sludge particles carried in the wastewater are decelerated and separated by the baffles in the sludge separation tank 12-12. The sludge flows back to the second contact oxidation tank 12-9 in an inverted "U" shape, and the separated water overflows into the first contact oxidation tank 12-5.

[0087] NH4 is arranged above the sludge separation tank 12-12 of the contact oxidation tank. + -N and NO2 - -N online instrument probe 12-11 and online detection instruments, as well as aeration fan 14, are interlocked for control of NH4. + -N and NO2 - The -N mass ratio is between 0.8 and 1.0. When NH4... + -N and NO2 - When the N-N mass ratio is higher than this range, increase the aeration rate of the aerobic contact oxidation tank to increase dissolved oxygen; conversely, decrease the dissolved oxygen aeration rate when the N-N mass ratio is lower.

[0088] S7: Anaerobic ammonia oxidation tank for nitrogen removal

[0089] The packing device inside anaerobic ammonia oxidation tank 13-5 uses a combined suspended packing material. Small pieces of polyurethane biological packing material are placed inside hollow PP spheres. Each spherical packing material is strung together with a rope, and both ends of each string of spherical combined packing material are fixed to the module frame. Each membrane frame has upper and lower layers, connected by bolt connectors. Wastewater enters anaerobic ammonia oxidation tank 13-5 from the bottom of the sludge separation tank 12-12 of the contact oxidation tank through the inlet 13-1. Suspended sludge particles in the wastewater adhere to the surface of the packing material inoculated with anaerobic ammonia oxidizing bacteria. The dissolved oxygen gradually decreases from the outside to the inside of the microbial flocs, and the dissolved oxygen is controlled at 0.5~0.8 mg / L. Within anaerobic ammonia oxidation tank 13-5, NH4+... + -N and NO2 - The nitrogen-to-ammonia (N) mass ratio is between 0.8 and 1.0. By adjusting the aeration rate, the short-cut nitrification stage of the system is maintained, achieving symbiosis between ammonia-oxidizing bacteria and anaerobic ammonia-oxidizing bacteria. Aeration is performed using bottom-perforated aeration discs 13-2.

[0090] The anaerobic ammonia oxidation bacteria sludge detached from the packing material flows with the effluent to the integrated sedimentation tank 2-16. The anaerobic ammonia oxidation bacteria sludge enriched within the inclined plates of the integrated sedimentation tank 2-16 is collected and can be sold. The clarified liquid from the sedimentation tank is returned to the contact oxidation tank 12-5, where denitrifying bacteria utilize the organic matter in the incoming water as a carbon source for denitrification and nitrogen removal, generating alkalinity. In the effluent from the anaerobic ammonia oxidation tank 13-5, 92%–95% of total nitrogen (TN) is converted to nitrogen (N2), with 5%–8% of TN remaining, mainly as NO3. - -N exists.

[0091] S8: Sulfur autotrophic denitrification for residual nitrogen removal

[0092] Sulfur-oxidizing bacteria can utilize elemental sulfur as an electron donor under anaerobic or hypoxic conditions, obtaining energy through reduced sulfur, while using nitrate as an electron acceptor and utilizing inorganic carbon (CO2, HCO3). - CO3 2- Using sulfur as a carbon source and supplemented with a certain amount of alkalinity, it is reduced to nitrogen gas, completing the autotrophic denitrification process. Wastewater enters from the bottom of the sulfur autotrophic denitrifier 19 in an upflow manner. The packing material uses activated biological packing material, and based on the optimized design of sulfur, limestone, fly ash and other components, it can adjust the pH value of wastewater, promote the enrichment of functional microorganisms, and construct a new pathway for autotrophic biological nitrogen removal electron transfer. An external heat exchange system is installed to maintain the temperature inside the reactor between 35 and 38°C.

[0093] Bottom water distribution: Perforated pipe water distribution, with openings at a vertical 45-degree angle, two rows, made of corrosion-resistant stainless steel. A stainless steel sieve plate with a 50 mm aperture is added on top of the packing to prevent movement of the filter bed in the sulfur autotrophic denitrifier 19. An outlet trough is installed above the filter bed. Backwashing is performed when the outlet height exceeds the expansion height of the filter media during backwashing. The backwash wastewater is returned to the contact oxidation tank -12-5.

[0094] S9: Clean water meets discharge standards

[0095] Wastewater filtered by the sulfur autotrophic denitrifier 19 enters the clear water tank 20. If the test results meet the standards, the clear water in the clear water tank 20 is pumped out and discharged by the clear water pump 21.

[0096] Example 2

[0097] In this embodiment, the operating parameters of IC anaerobic tank 1 in S1 are as follows. The English abbreviations in the following parameters are general abbreviations in wastewater treatment, and their specific meanings will not be elaborated here.

[0098] Feed load OLR: 5~10 kg / (m²) 3·d), pH: 7.2~8.0, volatile fatty acids (VFA): 500~1000 mg / L, alkalinity: 25000~30000 mg / L (as CaCO3), hydraulic retention time (HRT): 30~45 d, NH3-N: 2000~2500 mg / L, TN: 2500~3000 mg / L, COD: 2500~6000 mg / L, TS: 1.5%~2.0%, VS: 25%~35%, temperature: 55℃.

[0099] Biogas production per ton of water intake: 80~110m³ 3 / h, CH4: 68%~70%, CO: 29.6%~31.7%, O2: 0, H2S: 0.3%~0.4%.

[0100] Example 3

[0101] In this embodiment, the operating parameters of the vibrating screen 5 in S2 are as follows: feed SS = 10.8 g / L, liquid phase SS = 9.8 g / L, SS removal rate of the vibrating screen 9.3%, and residue moisture content 85%. Furthermore, the mesh size of the vibrating screen 5 can be selected according to the material characteristics.

[0102] Example 4

[0103] In this embodiment, the operating parameters of the integrated sedimentation tank 6 in step S3 are as follows:

[0104] The SS (suspended solids) in the clear liquid of the integrated sedimentation tank-6 is 6 g / L, with an SS removal rate of 38.7%. The sludge discharge rate of the integrated sedimentation tank-6 is 20% of the influent volume, and the SS of the clear liquid after sludge removal is 5 g / L.

[0105] Example 5

[0106] In this embodiment, the operating parameters of the medium-temperature ultrafiltration membrane 9 in S4 are as follows: ultrafiltration permeate rate: 50%~70%; permeate flux: 60~110 LMH (LMH is the water flux per square meter per hour); operating temperature: 50~60℃; pipeline flow rate: 4~6 m / s; effluent SS < 500 mg / L. Chemical cleaning is performed when the permeate flux decreases by 10%~20%. The ultrafiltration membrane element can be made of PDEF polymer material.

[0107] The cleaning methods are as follows: Water rinsing cycle: 30-120 minutes / 8 hours. Chemical cleaning cycle: 2 weeks to 1 month / time. Chemical cleaning methods: Acid washing for 4-12 hours, adjusting pH to 2.0 with citric acid or hydrochloric acid; Alkali washing for 4-12 hours, adjusting pH to 13.0 with alkali solution or caustic soda flakes and 0.03%-0.1% sodium hypochlorite; Acid washing for 4-12 hours, adjusting pH to 2.0 with citric acid or hydrochloric acid; Permeate water is returned to the clarified water tank and circulated by the ultrafiltration pump. The chemical cleaning time can be determined based on the actual permeate flow rate.

[0108] Example 6

[0109] In this embodiment, in S5, the operating parameters of the phosphorus remover 10 are as follows: total phosphorus in the influent: 50~125mg / L, total phosphorus in the effluent: 6~8mg / L, and total phosphorus removal rate: 88%~92%.

[0110] Comparative Example 1:

[0111] Currently, anaerobic digestate is treated by adding PAC (800~1300ppm) and PAM (100~300ppm) for coagulation and flocculation, then pumping it into a two-phase centrifuge for separation. The total phosphorus in the effluent is 16.0~26mg / L, with a total phosphorus removal rate of 76%~85%. Specific parameters are shown in Table 1 below:

[0112] Table 1

[0113]

[0114] Results analysis: Comparing Comparative Example 1 with the embodiments of the present invention, it was found that the medium-temperature ultrafiltration membrane 9 combined with the phosphorus remover 10 of the present invention has a significant effect on the removal of total phosphorus.

[0115] Example 7

[0116] In this embodiment, in step S6, the aerobic contact oxidation tank is controlled to perform short-cut nitrification and simultaneous nitrification and denitrification. The packing material for contact oxidation tank 12-5 and contact oxidation tank 22-9 is modular, with the upper and lower parts connected by bolts. The aeration ratio is controlled at 3:1 to 10:1, and the dissolved oxygen is controlled at 0.5 to 0.7 mg / L. The five-day biochemical oxygen demand (BOD5) volumetric loading is 0.2 to 1.5 kg BOD5 / (m³). 3 •d); The filling rate of the suspended packing material in the anoxic tank is 50%~80%; the filling rate of the suspended packing material in the aerobic tank is 50%~80%; the hydraulic retention time is 0.5h~3.0h for the anoxic tank and 12h~48h for the aerobic tank; the clear liquid reflux ratio of the integrated sedimentation tank is 50%~200%.

[0117] Example 8

[0118] In this embodiment, the specific operating parameters in S7 are as follows: 3g of autotrophic denitrification packing material and 4.57g of alkalinity are required to remove 1g of nitrate nitrogen; influent nitrate nitrogen: 400 mg / L; alkalinity: ≥1700 mg / L; pH>7.2; operating temperature controlled at 30℃~37℃. Effluent nitrate nitrogen: 70 mg / L; alkalinity: no requirement; pH>6-9. Reactor: diameter × height = 0.5 m * 2.5 m (of which the packing material height is 2 m); hydraulic retention time: 4-6 h.

[0119] Volumetric loading rate: 0.8~1.3 kg N / m³·d; Inlet type: Upflow type; Backwashing: Upflow high-speed water flow backwashing is adopted, backwashing once every 1-2 months, backwashing intensity is 7~10 L / (m²·s), and backwashing time is 3~5 min. Achieve effluent quality of COD <400mg / L, TN <45mg / L, TP <1.5mg / L, pH 5.5~8.5mg / L, and SS <200mg / L.

[0120] Comparative Example 2

[0121] The existing biogas slurry treatment method uses an aeration tank + anaerobic ammonia oxidation + primary A / O + sedimentation tank. The anaerobic ammonia oxidation effluent has a total nitrogen residue of 10%~30%. Nitrogen removal is achieved through denitrification at the primary A / O stage by adding a large amount of external carbon source, resulting in effluent quality of COD: 500~700 mg / L, TN: 50~70 mg / L, TP: 8~12 mg / L, pH: 6.5~8.5 mg / L, and SS: 500~1000 mg / L. However, this method is costly due to the high cost of external carbon source per ton of water, requires large aeration volumes, produces a large amount of sludge, and results in unstable effluent quality and substandard total phosphorus levels.

[0122] Results analysis: Compared with Comparative Example 2, the effluent quality of the present invention is more stable and the total phosphorus meets the standard.

[0123] Example 9

[0124] In this embodiment, step S5 involves the production of the mesh sponge phosphorus and nitrogen removal packing:

[0125] (1) Using a stirrer, 70 parts of polyether polyol (Changhua Chemical Technology Co., Ltd., CHE-303), 3 parts of water, 1 part of catalyst, 1 part of surfactant, 5 parts of filler, 10 parts of magnesium salt, and 10 parts of pyrite powder are stirred for 30 minutes at 1000~2000 r / min to prepare a mixed pre-reagent. Among them, the catalyst is triethylamine; the surfactant is a mixture of mineral oil and silicone oil L580 with a mixing ratio of 1:2; the filler is light calcium carbonate and silica lime with a mixing ratio of 1:1 and a particle size of 400 mesh; the magnesium salt is magnesium hydroxide with a particle size of 400 mesh; and the pyrite powder has a particle size of 400 mesh.

[0126] (2) When foaming the mixed pre-reagent using supercritical CO2 pressure foaming, 50 parts of toluene diisocyanate are selected. The remaining steps are the same as in Example 1.

[0127] In summary, the present invention will be further described in comparison with existing technologies:

[0128] (1) Problem of low organic matter conversion rate. Conventional kitchen waste slurry is separated by anaerobic digestion + biogas digester + centrifuge or plate and frame separator. The total sulfide (TS) in the anaerobic effluent is 2%~3%, and 1%~1.5% of the TS in the biogas effluent is mainly converted into biogas residue by centrifuge or plate and frame separator after the addition of chemicals. The biogas residue after the addition of chemicals is mainly sent to waste incineration or landfill. At the same time, the suspended solids (SS) in the effluent are 2000~8000 mg / L, and the biogas effluent still contains a large amount of SS. This invention uses a vibrating screen + integrated sedimentation tank + medium temperature ultrafiltration membrane for solid-liquid separation of anaerobic biogas effluent. The vibrating screen removes 3%~5% of SS, and the gravel is discharged through the sedimentation tank. The ultrafiltration concentrate is returned to the anaerobic digester for digestion and gas production. The SS in the ultrafiltration effluent is controlled at 500 mg / L, and the COD in the anaerobic effluent can be controlled at 2000~4000 mg / L, which is conducive to the stable operation of the anaerobic system and improves the utilization rate of organic matter in the system.

[0129] (2) The cost of total phosphorus removal agents is high, and there is also the problem of pipe scaling. The total phosphorus in the biogas slurry of the IC anaerobic tank is 100~200mg / L, and the total phosphorus requirement for the effluent of the sewage system is 8mg / L or 1.5mg / L. The total phosphorus removal of conventional sewage biological treatment systems is between 20~30mg / L. In order to achieve the goal of effluent total phosphorus exceeding the standard, PAC+PAM needs to be prepared and added at the end for flocculation and sedimentation to remove phosphorus, which is costly. In the pipelines and equipment between the effluent of the IC anaerobic tank and the sewage biological treatment system, the conditions for struvite scaling (NH4+) are met. + -N, TP, Mg2 + High content (pH between 7 and 8) forms bird droppings, leading to scaling problems in equipment and pipes.

[0130] This invention utilizes a phosphorus removal reactor downstream of a medium-temperature ultrafiltration membrane. By adding magnesium salts and controlling the magnesium-to-phosphorus ratio at 1.1:1 to 1.5:1, the total phosphorus in the reactor effluent is controlled within 8-12 mg / L, meeting the total phosphorus requirements for downstream biochemical microorganisms. The invention also removes total phosphorus from the biogas slurry using the principle of struvite scaling, separating the struvite. Struvite has extremely low solubility in water and can be used as a raw material for phosphate fertilizer production or as a slow-release fertilizer for crop growth. This not only facilitates the recycling of phosphorus resources in wastewater but also helps reduce water pollution and the phosphorus removal load. Based on this precipitation method, over 95% of phosphorus in wastewater can be recovered, requiring only the addition of a certain amount of alkali and magnesium source, offering advantages of high efficiency and low cost.

[0131] (3) Conventional biogas slurry solid-liquid separation uses a two-phase centrifuge, which requires the addition of conditioners or flocculants, resulting in high operating costs and unstable effluent quality, leading to the collapse of the downstream anaerobic ammonia oxidation process. The effluent from conventional two-phase centrifuge separation contains a large amount of suspended solids (SS), and the SS content in the effluent is unstable, resulting in a high sludge discharge. At the same time, a large number of anaerobic ammonia oxidation bacteria are discharged from the system with the sludge. Since anaerobic ammonia oxidation bacteria have a long generation time, the system cannot enrich the bacterial species, leading to the collapse of the anaerobic ammonia oxidation process.

[0132] This invention achieves a stable suspended solids (SS) concentration (SS) in the effluent after ultrafiltration membrane separation below 500 mg / L, thus eliminating the drawbacks of using an A / O + sedimentation tank system, such as high aeration volume, high sludge production, high power consumption, and large footprint. It utilizes a contact oxidation tank + anaerobic ammonia oxidation process, which features lower sludge discharge, lower aeration volume, smaller footprint, and lower operating costs.

[0133] (4) Conventional A / O or two-stage A / O processes are used, resulting in large sludge production, large aeration volume, and high operating costs. Anaerobic ammonia oxidation is the most advanced biological nitrogen removal process internationally. Under anaerobic conditions, ammonia is used as an electron donor and nitrite as an electron acceptor to generate nitrogen gas. Anaerobic ammonia oxidation nitrogen removal process has high nitrogen removal efficiency, high load, and no need for external carbon source for total nitrogen removal, which greatly reduces the energy and material consumption input in the nitrogen removal process and reduces greenhouse gas emissions by more than 90%. It is currently the most economical and efficient wastewater nitrogen removal technology. It solves the drawbacks of traditional nitrification and denitrification processes, such as high aeration energy consumption, reliance on external carbon source for total nitrogen removal, and large sludge production.

[0134] Reference Figure 8 As can be seen, anaerobic ammonium oxidation (ANAO) requires neither organic carbon source (COD) nor oxygen (O2) during the reaction process. This offers significant advantages over traditional nitrification-denitrification nitrogen removal methods. It completely changes the traditional approach (denitrification) that requires the addition of electron donors (carbon sources) for nitrogen removal, saving over 60% of aeration energy consumption. Simultaneously, ANAO minimizes the production of excess sludge, thus saving substantial sludge disposal costs. ANAO has a high loading capacity, saves on land area and investment. Furthermore, reduced energy consumption translates to lower CO2 emissions, making it a sustainable, green, and low-carbon biological nitrogen removal technology for wastewater.

[0135] Anaerobic ammonia oxidation (AAO) completely breaks through the basic concept of traditional biological nitrogen removal, providing an optimal pathway for biological treatment of wastewater with low C / N ratios. Compared to traditional nitrification / denitrification processes, AAO has the following advantages: high ammonia nitrogen removal load, 2 to 5 times that of ordinary nitrogen removal processes; according to stoichiometry, AAO can save 62.5% of oxygen supply power consumption; the AAO reaction requires no organic carbon source, and the coupled system saves 90% of organic carbon source consumption; sludge production is extremely low, saving sludge treatment costs; it not only reduces emissions of greenhouse gases such as CO2 but also consumes CO2.

[0136] (5) NO3 in effluent from anaerobic ammonia oxidation process - Nitrogen (N) accounts for 10% of the total nitrogen in the influent. Traditional biological nitrogen removal processes require external carbon sources for denitrification, resulting in high operating costs and large land area requirements. This invention recirculates the clarified liquid from the anaerobic ammonia oxidation tank to the anoxic tank for denitrification, utilizing organic matter in the influent for denitrification. The total nitrogen removal rate in the anaerobic ammonia oxidation effluent is 30%–50%, and the overall system effluent total nitrogen removal rate is increased to 92%–95%. To address the problems of traditional biological nitrogen removal processes, this invention employs sulfur autotrophic denitrification, obtaining energy through reduced sulfur and using nitrate as an electron acceptor, while utilizing inorganic carbon (CO2, HCO3-, CO32-) as a carbon source for denitrification. This reduces the total nitrogen removal cost of downstream wastewater by more than half, requires a smaller land area, and is simple to operate.

[0137] The above description is merely a preferred embodiment of the present invention and is not intended to limit the present invention. Although the present invention has been described in detail with reference to the foregoing embodiments, those skilled in the art can still modify the technical solutions described in the foregoing embodiments or make equivalent substitutions for some of the technical features. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the present invention should be included within the protection scope of the present invention.

Claims

1. A device for denitrification and dephosphorization of high concentration wastewater by short-cut nitrification / anaerobic ammonia oxidation-sulfur autotrophic denitrification coupled struvite process, characterized in that, The application relates to an integrated IC anaerobic tank (1) which is connected with an integrated sedimentation tank (6) through a rotating vibration screen (5), the integrated sedimentation tank (6) is connected with a medium-temperature ultrafiltration membrane (9), the medium-temperature ultrafiltration membrane (9) is connected with a contact oxidation system (12) through a phosphorus removal device (10), the contact oxidation system (12) is connected with an integrated sedimentation tank (16) through a denitrification system (13), and the integrated sedimentation tank (16) is connected with a clean water tank (20) through a sulfur autotrophic denitrification device (19). The contact oxidation system (12) comprises a contact oxidation tank (12-5) which is used for anoxic denitrification, and the contact oxidation tank (12-5) is connected with a contact oxidation tank (12-9) which is an aerobic biological contact oxidation tank. The denitrification system (13) comprises an anaerobic ammonia oxidation tank (13-5). The IC anaerobic tank (1) is further connected with a forced circulation pump (3), and a central agitator (2) is arranged in the IC anaerobic tank (1); the phosphorus removal device (10) comprises a phosphorus removal tank (10-1), the bottom of the phosphorus removal tank (10-1) is provided with a hopper, the lower part of the hopper is connected with a pneumatic knife gate valve (10-9), the phosphorus removal tank (10-1) is provided with a discharge plate (10-7), the discharge plate (10-7) comprises a middle part and movable plates at the two ends of the middle part, the middle part is fixed on the phosphorus removal tank (10-1) at an angle through discharge plate movable bolts (10-8), the movable plates at the two ends are in contact with the inner wall of the hopper to form a closed state, one end of a discharge plate manual hoist (10-3) is connected with the movable plates, and the other end of the discharge plate manual hoist (10-3) is fixed outside the phosphorus removal tank (10-1). The operation indexes of the IC anaerobic tank (1) include a hydraulic retention time HRT: 30-45d, and the mass ratio of Mg:P is controlled to be 1.1:1-1.5:1 by adding magnesium salt.

2. The device for denitrification and dephosphorization of high-concentration sewage by coupling of short-cut nitrification / anaerobic ammonia oxidation-sulfur autotrophic denitrification and struvite process according to claim 1, characterized in that, The IC anaerobic tank (1) is further connected with the medium-temperature ultrafiltration membrane (9), and the integrated sedimentation tank (6) is further connected with an external desludging system through an anaerobic sludge pump (7).

3. The device for denitrification and dephosphorization of high concentration wastewater by coupling short-cut nitrification / anaerobic ammonia oxidation-sulfur autotrophic denitrification with struvite process according to claim 1, characterized in that, The phosphorus removal device (10) comprises an agitator (10-2), the bottom of the agitator (10-2) is provided with a paddle, and the agitator (10-2) penetrates into a reaction area of the phosphorus removal tank (10-1) from the central position of the top of the phosphorus removal tank (10-1). The pneumatic knife gate valve (10-9) is connected with a separator (11).

4. The device for denitrification and dephosphorization of high concentration sewage by short-cut nitrification / ANAMMOX-sulfur autotrophic denitrification coupled struvite process according to claim 3, characterized in that, One side of the phosphorus removal tank (10-1) is provided with a feeding groove (10-5), the other side of the phosphorus removal tank (10-1) is provided with a discharging port (10-6), and the phosphorus removal tank (10-1) is further provided with a phosphorus removal medicament port (10-4).

5. The device for denitrification and dephosphorization of high concentration sewage by coupling short-cut nitrification / anaerobic ammonia oxidation-sulfur autotrophic denitrification with struvite process according to claim 2, characterized in that, The contact oxidation tank one (12-5) comprises an inlet water tank (12-1) and a cyclone aerator (12-2) for providing micro-aeration conditions, and a contact oxidation tank outlet (12-3), and further comprises a Pall ring filler module (12-4) for placing fillers, which comprises a plurality of Pall ring filler modules connected by upper and lower module connectors (12-6), and is provided at the bottom with a contact oxidation tank sludge discharge pipe (12-8); The contact oxidation tank two (12-9) comprises an elastic three-dimensional filler module (12-10) comprising a plurality of elastic three-dimensional filler modules connected by upper and lower module connectors (12-6), and is provided below with a nano-aeration pipe (12-7), and is also provided at the bottom with the contact oxidation tank sludge discharge pipe (12-8) connected to the external sludge removal system by the anaerobic sludge pump (7).

6. The device for denitrification and dephosphorization of high concentration sewage by short-cut nitrification / anaerobic ammonia oxidation-sulfur autotrophic denitrification coupled struvite process according to claim 1, characterized in that, The contact oxidation tank two (12-9) further comprises a contact oxidation tank sludge separation tank (12-12) provided with an online instrument probe (12-11), and the online instrument probe (12-11) and the online detection instrument and the aeration fan (14) are interlocked controlled.

7. The device for denitrification and dephosphorization of high concentration sewage by short-cut nitrification / anaerobic ammonia oxidation-sulfur autotrophic denitrification coupled struvite process according to claim 1, characterized in that, The anaerobic ammonia oxidation tank (13-5) is provided with a plurality of filler devices, each comprising an upper anaerobic ammonia oxidation filler module (13-4) and a lower anaerobic ammonia oxidation filler module (13-3) connected by an upper and lower filler film block connector (13-6), and is further provided at the bottom with a microporous aeration disc (13-2), and further comprises an anaerobic ammonia oxidation tank outlet (13-7) and an anaerobic ammonia oxidation tank inlet (13-1).

8. The device for denitrification and dephosphorization of high concentration sewage by short-cut nitrification / anaerobic ammonia oxidation-sulfur autotrophic denitrification coupled struvite process according to claim 1, characterized in that, The IC anaerobic tank (1) is connected to the rotary vibrating screen (5) through an anaerobic discharge pump (4), the integrated sedimentation tank one (6) is connected to the medium-temperature ultrafiltration membrane (9) through a sediment discharge pump one (8), the medium-temperature ultrafiltration membrane (9) is an ultrafiltration membrane system, the denitrification system (13) is connected to the integrated sedimentation tank two (16) through an anaerobic ammonia oxidation discharge pump (15), the integrated sedimentation tank two (16) is further connected to an anaerobic ammonia oxidation granular sludge pump (17), and the integrated sedimentation tank two (16) is further connected to the sulfur autotrophic denitrification device (19) through a sediment discharge pump two (18), and the clear water tank (20) is further connected to a clear water pump (21), The sulfur autotrophic denitrification device (19) is further connected to the contact oxidation system (12), and the integrated sedimentation tank two (16) is further connected to the contact oxidation system (12).

9. A process for denitrification and dephosphorization of high concentration wastewater by short-cut nitrification / anaerobic ammonia oxidation-sulfur autotrophic denitrification coupled struvite process, characterized in that, The denitrification and phosphorus removal device of the short-cut nitrification / anaerobic ammonia oxidation-sulfur autotrophic denitrification coupled struvite process for treating high-concentration sewage according to any one of claims 1-8 is used in the process, and the process comprises the following steps, The high-concentration sewage is fermented in the IC anaerobic tank (1) and then enters the rotary vibrating screen (5) to remove large-particle materials, so as to obtain a large-particle-removed liquid phase; the large-particle-removed liquid phase flows into the integrated sedimentation tank I (6) to remove fine suspended solids, so as to obtain a separated sedimentation clear liquid and a separated sludge; the separated sludge enters an external sludge removal system; the separated sedimentation clear liquid enters the medium-temperature ultrafiltration membrane (9) to perform solid-liquid separation, so as to obtain a clear liquid and a part of concentrated liquid; the part of concentrated liquid is returned to the IC anaerobic tank (1); the clear liquid enters the phosphorus remover (10) to perform phosphorus removal, so as to generate struvite crystals and a phosphorus-removed sewage; the phosphorus-removed sewage enters the contact oxidation system (12) to perform short-cut nitrification and remove organic matters and suspended solids; excess sludge enters an external sludge removal system; the treated sewage enters the denitrification system (13) and the integrated sedimentation tank II (16) to perform denitrification, and then enters the sulfur autotrophic denitrification device (19) to perform sulfur autotrophic denitrification; the filtered sewage enters the clear water tank (20); The phosphorus remover (10) is internally provided with filler I, and the filler I comprises at least one of a reticular polyurethane filler and a reticular sponge phosphorus and denitrification filler; the raw material of the reticular sponge phosphorus and denitrification filler comprises the following components in parts by weight: 70-100 parts of polyether polyol, 3-6 parts of water, 1-2 parts of a catalyst, 1-2 parts of a surfactant, 2-5 parts of a filler, 5-20 parts of a magnesium salt, and 5-20 parts of pyrite powder; The preparation method of the reticular sponge phosphorus and denitrification filler comprises the following steps: The raw materials are stirred in proportion to prepare a mixed pre-reagent; The mixed pre-reagent is foamed to obtain the reticular sponge phosphorus and denitrification filler.

10. The denitrification and phosphorus removal process of the short-cut nitrification / anaerobic ammonia oxidation-sulfur autotrophic denitrification coupled struvite process for treating high-concentration sewage according to claim 9, characterized in that The catalyst comprises an amine catalyst, and the amine catalyst comprises at least one of triethylamine, ethylene diamine and alcohol amine; the surfactant comprises at least one of a pore opener and silicon oil, the pore opener comprises at least one of an alkali metal salt of a fatty acid, kerosene and mineral oil, the silicon oil comprises silicon oil L580; the filler comprises at least one of light calcium carbonate, silica lime and bentonite, and the particle size of the filler is 200-500 mesh; the magnesium salt comprises at least one of magnesium hydroxide, magnesium chloride and magnesium sulfate, and the particle size of the magnesium salt is 200-500 mesh; the particle size of the pyrite powder is 200-500 mesh, The preparation method of the reticular sponge phosphorus and denitrification filler comprises the following steps: The raw materials are stirred in proportion at 1000-2000 r / min for 20-40 min to prepare a mixed pre-reagent. The mixed pre-reagent is foamed, the high-pressure reaction kettle is warmed to 150±5℃, then the mixed pre-reagent is stirred with 40-60 parts of toluene diisocyanate at 3000-4000 r / min for 5-8 s, quickly poured into the high-pressure reaction kettle which has been warmed to 150±5℃, and then carbon dioxide is pressurized to 3-7 MPa and introduced into the high-pressure reaction kettle, the pressure in the high-pressure reaction kettle is maintained for 30-60 min, then the pressure in the high-pressure reaction kettle is instantaneously released to obtain the initial reticular sponge phosphorus and nitrogen removal filler, and the initial reticular sponge phosphorus and nitrogen removal filler is sheared into square fillers with a side length of 20-30 mm to obtain the reticular sponge phosphorus and nitrogen removal filler; The operation indexes of the IC anaerobic tank (1) include, Feed load OL: 5 ~ 10 kg / m 3 · d, pH: 7.2 ~ 8.0, volatile fatty acids VFA: 500 ~ 1000 mg / L, alkalinity: 25000 ~ 30000 mg / L, hydraulic retention time HRT: 30 ~ 45 d, NH3-N: 2000 ~ 2500 mg / L, TN: 2500 ~ 3000 mg / L, COD: 2500 ~ 6000 mg / L, TS: 1.5% ~ 2.0%, VS: 25% ~ 35%, temperature: 55℃; tons of water biogas: 80 ~ 110 m 3 / h, CH4: 68% ~ 70%, CO: 29.6% ~ 31.7%, O2: 0, H2S: 0.3% ~ 0.4%; The operation indexes of the medium-temperature ultrafiltration membrane (9) include: ultrafiltration water production rate: 50%-70%, water production flux: 60-110 LMH, operation temperature: 50-60℃, pipeline flow: 4-6 m / s, effluent SS: <500 mg / L, and chemical cleaning is performed when the water production flux is reduced by 10%-20%; The operation indexes of the contact oxidation system (12) include: aeration ratio control at 3:1~10:1, dissolved oxygen control at 0.5~0.7mg / L; five-day biochemical oxygen demand filling volume load 0.2~1.5kgBOD5 / (m 3 ·d); the contact oxidation pool one (12-5) suspension filler filling rate 50%~80%; the contact oxidation pool two (12-9) suspension filler filling rate 50%~80%; hydraulic retention time: the contact oxidation pool one (12-5) 0.5h~3.0h, the contact oxidation pool two (12-9) 12h~48h; the integrated sedimentation pool two (16) clear liquid reflux ratio 50%~200%; The operation index of the anaerobic ammonia oxidation tank (13-5) includes: influent nitrate nitrogen: 400 mg / L; alkalinity: ≥1700 mg / L; pH>7.2, the operation temperature is controlled at 30℃-37℃; effluent nitrate nitrogen: 70 mg / L; alkalinity: no requirement; pH>6-9; reactor: diameter x height = 0.5 m x 2.5 m, wherein the filler height is 2 m; hydraulic retention time: 4-6 h; volumetric loading: 0.8-1.3 kg N / m3·d; influent form: upflow type; backwashing: the upflow high-speed water flow backwashing mode is adopted, backwashing once in January-February, and the backwashing intensity is 7-10 L / m 2 ·s, the flushing time is 3-5 min.

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