CN216445206U - Urine extraction wastewater advanced treatment and nitrogen resource recovery system - Google Patents
Urine extraction wastewater advanced treatment and nitrogen resource recovery system Download PDFInfo
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- CN216445206U CN216445206U CN202123340551.7U CN202123340551U CN216445206U CN 216445206 U CN216445206 U CN 216445206U CN 202123340551 U CN202123340551 U CN 202123340551U CN 216445206 U CN216445206 U CN 216445206U
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Abstract
A urine extraction wastewater advanced treatment and nitrogen resource recovery system, wherein a grid is communicated with an adjusting tank, the adjusting tank is communicated with an air flotation tank, the air flotation tank is communicated with an ammoniation tank, the ammoniation tank is communicated with an ammonia nitrogen stripping tower, the ammonia nitrogen stripping tower is communicated with an intermediate water tank, the intermediate water tank is communicated with an HA-UASB tank, the HA-UASB tank is respectively communicated with a nitrosation tank and a denitrification tank, outlets of the nitrosation tank and the denitrification tank are communicated with an inlet of an anaerobic ammonia oxidation tank, a backflow port of the anaerobic ammonia oxidation tank is communicated with a backflow inlet of the denitrification tank, an outlet of the anaerobic ammonia oxidation tank is communicated with an inlet of a composite filter tank, an outlet of the composite filter tank is communicated with an inlet of a coagulative precipitation tank, an outlet of the coagulative precipitation tank is communicated with an inlet of an ozone oxidation tank, and an outlet of the ozone oxidation tank is communicated with an inlet of a reuse water tank; the utility model has scientific and reasonable design, good treatment effect and low operation cost, can deeply remove nitrogen in urine, reduce the yield of excess sludge and has remarkable social and economic benefits.
Description
Technical Field
The utility model relates to wastewater treatment, in particular to a system for advanced treatment of urine extraction wastewater and nitrogen resource recovery of high-nitrogen and high-organic matters.
Background
Urine contains a large amount of organic substances, nitrogen and phosphorus elements and abundant trace elements, can be used as a raw material for extracting and producing medicines, such as Human Chorionic Gonadotropin (HCG), urogonadotropin (HMG), tetraenonene and the like, and wastewater (namely urine extraction wastewater) after useful components are extracted from urine must be treated before being discharged. Because the effective components of the medicine extracted from urine belong to the minority and no enterprises for extracting the medicine on a large scale exist, the existing enterprises collect the wastewater and then mix the wastewater with other wastewater for treatment. At present, complete treatment equipment for directly and completely treating urine extraction wastewater does not exist at home and abroad, most of researches are still on local treatment in laboratories, the scale is small, the equipment practicability is poor, and the equipment is difficult to be directly used for production of large-scale industrial enterprises.
Urine extraction waste water belongs to high nitrogen organic waste water, and the carbon-nitrogen ratio is low, and traditional denitrogenation technology not only needs a large amount of outer carbon sources, improves sewage treatment running cost, has caused the waste of urine extraction waste water nitrogen resource simultaneously, and consequently, how to extract the processing and further recycle of waste water to the urine is the technical problem that needs carefully to solve.
SUMMERY OF THE UTILITY MODEL
In view of the above situation, in order to overcome the defects of the prior art, the present invention provides a system for advanced treatment of urine extraction wastewater and nitrogen resource recovery, which can effectively solve the problems that the prior art cannot effectively treat urine extraction wastewater and cannot further recycle the urine extraction wastewater.
In order to achieve the purpose, the utility model solves the technical scheme that the urine extraction wastewater advanced treatment and nitrogen resource recovery system comprises a grid, an adjusting tank and a middle water tank, wherein an outlet of the grid is communicated with an inlet of the adjusting tank through a pipeline, an outlet of the adjusting tank is communicated with an inlet of an air flotation tank through a pipeline, an outlet of the air flotation tank is communicated with an inlet of an ammoniation tank through a pipeline, an outlet of the ammoniation tank is communicated with an inlet of an ammonia nitrogen stripping tower through a pipeline, an outlet of the ammonia nitrogen stripping tower is communicated with an inlet of the middle water tank through a pipeline, an outlet of the middle water tank is communicated with an inlet of an HA-UASB tank through a pipeline, an outlet of the HA-UASB tank is respectively communicated with inlets of a nitrosation tank and a denitrification tank through a tee joint, outlets of the nitrosation tank and the denitrification tank are communicated with an inlet of an anaerobic ammonia oxygen tank through a tee joint, a return port of the anaerobic ammonia oxygen tank is communicated with a return inlet of the denitrification tank through a pipeline, the outlet of the anaerobic ammonia-oxygen tank is communicated with the inlet of the composite filter tank through a pipeline, the outlet of the composite filter tank is communicated with the inlet of the coagulating sedimentation tank through a pipeline, the outlet of the coagulating sedimentation tank is communicated with the inlet of the ozone oxidation tank through a pipeline, and the outlet of the ozone oxidation tank is communicated with the inlet of the reuse water tank through a pipeline;
the sludge outlets of the air floatation tank, the HA-UASB tank, the coagulating sedimentation tank and the ozone oxidation tank are communicated with the inlet of a sludge concentration tank through pipelines, and the outlet of the sludge concentration tank is communicated with the inlet of a dehydrator through a pipeline.
The utility model has scientific and reasonable design, good treatment effect and low operation cost, can deeply remove nitrogen in urine, reduces the yield of excess sludge and has remarkable social and economic benefits.
Drawings
FIG. 1 is a block diagram of the system architecture of the present invention.
FIG. 2 is a structural connection block diagram of the ammonia nitrogen stripping equipment part of the utility model.
FIG. 3 is a block diagram of the nitrosation basin structure of the present invention.
FIG. 4 is a block diagram of the denitrification tank structure of the present invention.
FIG. 5 is a schematic diagram of the HA-UASB pool structure of the present invention.
FIG. 6 is a schematic diagram of the structure of the anaerobic ammonia-oxygen pond of the utility model.
Detailed Description
The following detailed description of the embodiments of the utility model is provided in connection with the accompanying drawings and the detailed description.
The advanced treatment and nitrogen resource recovery system for urine extraction wastewater is provided by combining the attached drawing, and comprises a grid, an adjusting tank and an intermediate water tank, wherein an outlet of the grid 1 is communicated with an inlet of the adjusting tank 2 through a pipeline, an outlet of the adjusting tank 2 is communicated with an inlet of an air flotation tank 3 through a pipeline, an outlet of the air flotation tank 3 is communicated with an inlet of an ammoniation tank 4 through a pipeline, an outlet of the ammoniation tank 4 is communicated with an inlet of an ammonia nitrogen stripping tower 5 through a pipeline, an outlet of the ammonia nitrogen stripping tower 5 is communicated with an inlet of an intermediate water tank 6 through a pipeline, an outlet of the intermediate water tank 6 is communicated with an inlet of an HA-UASB tank 7 through a pipeline, an outlet of the HA-UASB tank 7 is respectively communicated with inlets of a nitrosation tank 8 and a denitrification tank 9 through a tee joint 17, outlets of the nitrosation tank 8 and the denitrification tank 9 are communicated with an inlet of an anaerobic ammonia oxygen tank 10 through a tee joint, a return port of the anaerobic ammonia oxygen tank 10 is communicated with a return inlet of the denitrification tank 9 through a pipeline, the outlet of the anaerobic ammonia-oxygen tank 10 is communicated with the inlet of the composite filter tank 11 through a pipeline, the outlet of the composite filter tank 11 is communicated with the inlet of the coagulating sedimentation tank 12 through a pipeline, the outlet of the coagulating sedimentation tank 12 is communicated with the inlet of the ozone oxidation tank 13 through a pipeline, and the outlet of the ozone oxidation tank 13 is communicated with the inlet of the reuse water tank 14 through a pipeline;
the sludge outlets of the floatation tank 3, the HA-UASB tank 7, the coagulation sedimentation tank 12 and the ozone oxidation tank 13 are communicated with the sludge inlet of a sludge concentration tank 15 through pipelines, and the sludge outlet of the sludge concentration tank 15 is communicated with the inlet of a dehydrator 16 through a pipeline.
In order to ensure better implementation effect, a temporary storage alkali adjusting tank 401 is arranged between the ammoniation tank 4 and the ammonia nitrogen stripping tower 5, a wastewater outlet of the ammonia nitrogen stripping tower 5 is communicated with an inlet of the middle water tank 6 through a pipeline, and a gas outlet of the ammonia nitrogen stripping tower 5 is communicated with a gas inlet of the ammonia nitrogen adsorption tower 501.
The nitritation tank 8 is internally provided with a micro aeration area 801, a first sludge return area 802 and a first sludge-water separation area 803, the micro aeration area 801 is internally provided with an aeration device, the bottoms of the first sludge return area 802 and the first sludge-water separation area 803 are communicated, a first return water baffle 804 is arranged between the first sludge return area 802 and the first sludge-water separation area 803, and the bottom of the first sludge-water separation area 803 is provided with a first submersible water impeller 805.
The denitrification tank 9 is internally provided with a mixing area 901, a second sludge return area 902 and a second sludge-water separation area 903, the bottoms of the second sludge return area 902 and the second sludge-water separation area 903 are communicated, a second return water baffle 904 is arranged between the second sludge return area 902 and the second sludge-water separation area 903, and a second submersible water impeller 905 is arranged at the bottom of the second sludge-water separation area 903.
The HA-UASB tank 7 is composed of 3 reaction areas from bottom to top, the first reaction area is a flowing sludge bed 701 at the lower part, the second reaction area is a suspended sludge tank 702, the third reaction area is a micro-aeration solid-liquid separation tank 703, and a micro-aeration device is arranged at the lower part of a three-phase separator in the micro-aeration solid-liquid separation tank 703.
The anaerobic ammonia-oxygen tank 10 is composed of 3 reaction areas from bottom to top, the first reaction area is a granular sludge area 10-1 at the lower part, the second reaction area is a completely flowing suspended sludge area 10-2, an aeration pipe is arranged at the bottom of the suspended sludge area 10-2, the third reaction area is a micro-aeration solid-liquid separation area 10-3, and a micro-aeration device is arranged at the lower part of a three-phase separator in the micro-aeration solid-liquid separation area 10-3.
When the device is used specifically, urine extraction wastewater enters the grating 1 through a sewage pump to be filtered, grating residues are transported outside for additional treatment, the filtered wastewater enters the regulating tank 2 to be subjected to water quality regulation, the water quality and the water quantity are uniform, effluent enters the air floatation tank 3, 50-100mg/L PAC and 2-5mg/L PAM (namely 50-100mg PAC and 2-5mg PAM are added into each L of wastewater) are added into the air floatation tank 3, and suspended matters in the wastewater are removed.
The air-float effluent of the air-float tank 3 enters an ammonification tank 4 for ammonia oxidation for 1-2h, and is subjected to ammonia oxidation by anaerobic microorganisms, so that nitrogenous organic matters such as urea, polypeptide and protein in the wastewater are converted into ammonia nitrogen, the subsequent blowing-off and recovery of the ammonia nitrogen are facilitated, the organic matters are preliminarily degraded, and the concentration of the degraded sludge is 3000-plus 5000 mg/L; and the effluent of the ammoniation tank 4 is subjected to pH adjustment in a temporary storage alkali adjusting tank 401, and enters an ammonia nitrogen stripping tower 5 after the pH =10-11 is adjusted by NaOH.
The effluent enters the upper part of an ammonia nitrogen stripping tower 5 for spray stripping treatment, a porous filter material in the stripping tower is cut into 0-1mm water films to slowly descend, an air stripping fan sends air into the tower and blows the air upwards for stripping for 1.5-2.0h, ammonia nitrogen is separated from the wastewater, the ammonia nitrogen is stripped along with air and enters an ammonia nitrogen adsorption tower 501, 1-9mol/L sulfuric acid solution is used for absorption to realize the recovery of nitrogen, and the wastewater treated by the ammonia nitrogen stripping tower 5 enters an intermediate water tank 6;
ammonia nitrogen in the water film is very volatile under alkaline condition and becomes ammonia and spills over the surface of water, discharges with the wind and blows the knockout tower and realize the deamination, and ammonia nitrogen blows 5 bottoms in the knockout tower and is equipped with pond and circulating pump of keeping in, can realize the circulation and spray and send waste water to the effect of middle pond 6. Ammonia nitrogen in the ammonia nitrogen stripping tower 5 enters the ammonia nitrogen adsorption tower 501 along with air stripping and is blown upwards from the lower part, a sulfuric acid pool and a circulating pump are arranged at the bottom of the ammonia nitrogen adsorption tower 501, dilute sulfuric acid solution can be sprayed from the top by the circulating pump to form a liquid film, ammonia nitrogen recovery is realized by generating ammonium sulfate through ammonia nitrogen absorption reaction, waste gas after ammonia nitrogen recovery is discharged through a chimney, the ammonia nitrogen adsorption tower is provided with a pH meter, and the effect of recovering ammonia nitrogen can be easily ensured by monitoring the pH meter, discharging an ammonium sulfate byproduct and supplementing new dilute sulfuric acid;
the effluent of the ammonia nitrogen stripping tower 5 enters an intermediate water tank 6, the pH is adjusted to be 7-8 by using 1-6mol/L HCl solution, and then the effluent enters an HA-UASB tank 7; adding activated sludge with hydrolytic acidification bacteria, methanogen strains, nitrosobacteria and anaerobic ammonium oxidation bacteria into an HA-UASB (anaerobic ammonium oxidation sludge-anaerobic sludge bed) tank 7, removing most organic matters through hydrolytic acidification and methanogenesis, simultaneously converting refractory macromolecular organic matters into degradable micromolecular organic matters, improving the biodegradability of the organic matters, providing a carbon source for subsequent organisms, simultaneously converting ammonia nitrogen into nitrite by the nitrosobacteria in a micro-aeration solid-liquid separation tank 703, returning the nitrite to a flowing sludge bed 701, and when a second reaction region is a suspended sludge tank 702 (a pure anaerobic region), utilizing the nitrite and the ammonia nitrogen by the anaerobic ammonium oxidation bacteria to generate nitrogen so as to realize partial denitrification, and then feeding the treated wastewater into a nitrosoation tank 8 and a denitrification tank 9;
the HA-UASB tank 7 is composed of 3 reaction areas from bottom to top, the first reaction area is a flowing sludge bed 701 at the lower part, hydrolytic acidification bacteria and part of methanogens are enriched, the hardly degradable macromolecular organic matters in the wastewater are mainly converted into biodegradable micromolecular organic matters, and meanwhile, part of the organic matters are removed; the second reaction area is a suspended sludge tank 702, sludge in the reaction area is lower than a flowing sludge bed area, methanogens and anaerobic ammonium oxidation bacteria are mainly enriched, organic matters in water are further removed, and meanwhile, anaerobic ammonium oxidation denitrification reaction is carried out; the third reaction area is a micro-aeration solid-liquid separation tank 703, the lower part of a three-phase separator in the micro-aeration solid-liquid separation tank 703 is provided with a micro-aeration device, sludge in the reaction area is lower than a flowing sludge bed area, and the sludge is mainly enriched with nitrosobacteria, so that organic matters in water are further removed, and meanwhile, a nitrosation reaction is carried out; the sludge concentration of the flowing sludge bed 701 is 15000-25000mg/L, the sludge concentration of the suspended sludge pool 702 is 10000-15000mg/L, and the sludge concentration of the micro-aeration solid-liquid separation pool 703 is 5000-10000 mg/L. Meanwhile, the micro-aeration device in the micro-aeration solid-liquid separation tank 703 is turned on, on one hand, solid-liquid separation is realized by the three-phase separator, and simultaneously, the separated activated sludge is quickly returned to the first reaction zone under the action of micro-aeration. The reaction tank not only removes most organic matters, but also converts refractory macromolecule organic matters into degradable micromolecule organic matters through the hydrolysis acidification function and the methane production function of microorganisms.
The treated wastewater in the HA-UASB tank 7 is divided according to the proportion of 1:1-2:1, the divided flows can respectively enter a nitrosation tank 8 and a denitrification tank 9 through the diameter control of a pipeline connected with a tee 17, sludge with the nitrosation function is added into the nitrosation tank 8, the concentration of the sludge is controlled to be 3000-plus 6000mg/L, the sludge stays in the nitrosation tank 8 for 1-2h under the action of nitrosobacteria, and ammonia nitrogen in the wastewater is converted into NO under the action of the nitrosobacteria2 —N, adding sludge with denitrification function into the denitrification tank 9, controlling the concentration of the sludge to be 3000-6000mg/L, and staying for 1-2h in the denitrification tank 9 under the hydraulic power, wherein the denitrification bacteria utilize organic matters in the water to convert nitrate nitrogen in the wastewater into N2。
Nitrosation tank 8 containing NO2 -the-N effluent and the denitrification tank 9 contain NH4 +The effluent of the anaerobic ammonia oxidation tank enters an anaerobic ammonia oxidation tank 10 together, the anaerobic ammonia oxidation bacteria stay for 5 to 10 hours by water power, and NO in the water is utilized by the anaerobic ammonia oxidation bacteria2 --N and NH4 +Carrying out anaerobic ammoxidation reaction on the-N, refluxing the mixed solution in the anaerobic ammoxidation tank 10 to the denitrification tank 9 at the reflux ratio of 50-80%, and removing NO generated by the reaction3 --N；
The nitrosation tank 8 is internally provided with a micro-aeration area 801, a first sludge return area 802 and a first sludge-water separation area 803, the micro-aeration area 801 is internally provided with an aeration device, dissolved oxygen DO =0.5-1.0mg/L, and NH is treated by nitrosobacteria4 +Conversion of-N to NO2 --N, providing NO to anammox cell2 -N matrix, the first sludge reflux area 802 is communicated with the bottom of the first sludge-water separation area 803, a first backwater baffle 804 is arranged between the first sludge reflux area 802 and the first sludge-water separation area 803, and the bottom of the first sludge-water separation area 803 is provided with a first backwater baffle 804The first submersible flow impeller 805 is arranged, sewage is pushed into the first sludge return area 802 along with micro-aeration, under the action of airflow and the first return water baffle 804, a sludge-water mixed solution firstly enters the first sludge-water separation area 803 from top to bottom through a return pipe to be subjected to sludge-water separation, supernatant is discharged, and sinking sludge is returned to the micro-aeration area 801 by the first submersible flow impeller 805;
a mixing area 901, a second sludge return area 902 and a second sludge-water separation area 903 are arranged in the denitrification tank 9, and denitrification bacteria utilize a water-feeding carbon source to remove NO in the return liquid in the mixing area 9013 -Conversion of-N to N2The bottom of the second sludge reflux area 902 is communicated with the bottom of the second sludge-water separation area 903, a second water return baffle 904 is arranged between the second sludge reflux area 902 and the second sludge-water separation area 903, a second submersible water impeller 905 is arranged at the bottom of the second sludge-water separation area 903, and under the action of the second water return baffle 904 and the second submersible water impeller 905, sludge-water mixed liquid firstly enters the second sludge-water separation area 903 from top to bottom through a return pipe to carry out sludge-water separation area, and under the action of the second submersible water impeller 905, precipitated sludge is refluxed to the mixing area 901;
the anaerobic ammonia oxidation tank 10 is composed of 3 reaction areas from bottom to top, the first reaction area is a lower granular sludge area 10-1 which mainly comprises anaerobic ammonia oxidizing bacteria and denitrifying bacteria, a small amount of nitrate contained in internal return sludge can perform denitrification by utilizing a carbon source in inlet water, not only can accelerate denitrification but also can avoid adverse effects of the carbon source on the anaerobic ammonia oxidation, the second reaction area is a completely flowing suspended sludge area 10-2, an aerator pipe is arranged at the bottom of the suspended sludge area 10-2, an aeration gas source is an anaerobic ammonia oxidation tank three-phase separation gas source, the main component is nitrogen to avoid adverse effects of oxygen on the anaerobic ammonia oxidation, and the area is used for culturing the abundant anaerobic ammonia oxidizing bacteria to be fully mixed with ammonia nitrogen and nitrite in the inlet water to perform efficient reaction to generate the nitrogen and the small amount of nitrate; the third reaction zone is a micro-aeration solid-liquid separation zone 10-3, the lower part of a three-phase separator in the micro-aeration solid-liquid separation zone 10-3 is provided with a micro-aeration device, the sludge is accelerated to flow back to the bottom by air stirring, a micro-aeration gas source almost contains no oxygen (can be ignored), the micro-aeration gas source mainly plays a role in mixing and accelerating the sludge flow back, and the micro-aeration gas source is provided with a non-interference anaerobic environment at the bottom of the anaerobic ammonia oxidation tank reactor.
The effluent of the anaerobic ammonia oxidation tank 10 enters a composite filter tank 11, suspended matters in the water are filtered, and residual total nitrogen is further removed, cobblestones and ceramsite are filled at the lower part of the composite filter tank, an air distribution device and a water distribution device are laid, the inner surface and the outer surface of a filter material in the composite filter tank can be cultured to generate a composite biological membrane, wherein the composite biological membrane contains nitrosobacteria, nitrobacteria, denitrifying bacteria and anaerobic ammonia oxidizing bacteria, the residual total nitrogen can be further removed, the stable standard reaching is realized, the effluent of the composite filter tank 11 enters a coagulative precipitation tank 12, PAC and PAM are added into the coagulative precipitation tank 12, the PAC adding amount is generally 20-50mg/L, the PAM adding amount is 1-3mg/L, suspended matters and residual phosphate in the water are removed, and the treated effluent enters an ozone oxidation tank 13; waste water adopts the ozone oxidation method to oxidize and disinfect in ozone oxidation pond 13, and the hydroxyl free radical that utilizes ozone to produce disturbs microorganism metabolism, and then kills the germ, can further get rid of the organic matter of aquatic simultaneously, and the water after the ozone oxidation enters into reuse water tank 14 and keeps in, and most water in reuse water tank 14 is recycled to the inside afforestation water in factory, and unnecessary water can discharge up to standard.
The sludge in the floatation tank 3, the HA-UASB tank 7, the coagulation sedimentation tank 12 and the ozone oxidation tank 13 enters a sludge concentration tank 15, is concentrated in the sludge concentration tank 15, and then is sent to a dehydrator 16 for dehydration, and the dry sludge is transported to the outside for disposal.
From the above, the utility model has scientific and reasonable design, and compared with the prior art, the utility model has the following beneficial effects:
(1) the ammonia nitrogen is subjected to stripping recovery treatment, so that the recycling of the ammonia nitrogen is realized, and the total nitrogen load of 70-80% of the subsequent biological treatment is reduced;
(2) the method is characterized in that HA-UASB is improved on the basis of the traditional UASB reactor, a micro-aeration device is arranged at the upper part of the reactor to accelerate the sludge backflow and improve the decarburization efficiency by 10-20%, and meanwhile, the traditional reactor without denitrification HAs the denitrification efficiency of 20-30%;
(3) respectively setting wastewater to respectively enter a nitrosation pool and denitrificationThe pond is changed to realize quantitative and qualitative water inlet, and the carbon source can be effectively utilized to carry out NO2 -Accumulation of-N and NO3 --N removal, providing reaction conditions for the subsequent anammox reaction;
(4) the setting of a sedimentation tank is not needed, the unit processing load is high, and the occupied area is reduced by 30-50% and the capital construction cost is reduced by 20-40%;
(5) the sludge age of the whole system is longer, the output of the excess sludge can be reduced, the output of biochemical sludge can be reduced by 80-90% compared with the traditional process, the oxygen consumption is low, the power consumption can be reduced by 50-60% compared with the traditional process, the treatment effect is good, the operation cost is low, the nitrogen in urine can be deeply removed, and the method has remarkable social and economic benefits.
Claims (6)
1. The utility model provides an urine extraction waste water advanced treatment and nitrogen resources recovery system, including grid, equalizing basin and middle pond, a serial communication port, the export of grid (1) be linked together through the import of pipeline with equalizing basin (2), the export of equalizing basin (2) is linked together through the import of pipeline and air supporting pond (3), the export of air supporting pond (3) is linked together through the import of pipeline with ammoniation pond (4), the export of ammoniation pond (4) is linked together through the import of pipeline with ammonia nitrogen stripping tower (5), the export of ammonia nitrogen stripping tower (5) is linked together through the import of pipeline with middle pond (6), the export of middle pond (6) is linked together through the import of pipeline with HA-UASB pond (7), the export of UASB pond (7) is linked together through tee bend (17) respectively with the import of nitrosation pond (8) and denitrification pond (9), the export of nitrosation pond (8) and denitrification pond (9) is linked together through the import of tee bend and anaerobism ammonia oxygen pond (10), a serial communication port of nitrosation pond (8) is linked together A return port of the anaerobic ammonia-oxygen tank (10) is communicated with a return inlet of the denitrification tank (9) through a pipeline, an outlet of the anaerobic ammonia-oxygen tank (10) is communicated with an inlet of the composite filter tank (11) through a pipeline, an outlet of the composite filter tank (11) is communicated with an inlet of the coagulation sedimentation tank (12) through a pipeline, an outlet of the coagulation sedimentation tank (12) is communicated with an inlet of the ozone oxidation tank (13) through a pipeline, and an outlet of the ozone oxidation tank (13) is communicated with an inlet of the reuse water tank (14) through a pipeline;
sludge outlets of the air floatation tank (3), the HA-UASB tank (7), the coagulating sedimentation tank (12) and the ozone oxidation tank (13) are communicated with a sludge inlet of a sludge concentration tank (15) through pipelines, and a sludge outlet of the sludge concentration tank (15) is communicated with an inlet of a dehydrator (16) through a pipeline.
2. The system for the advanced treatment of urine extraction wastewater and the recovery of nitrogen resources as claimed in claim 1, wherein a temporary storage alkali adjusting tank (401) is arranged between the ammoniation tank (4) and the ammonia nitrogen stripping tower (5), a wastewater outlet of the ammonia nitrogen stripping tower (5) is communicated with an inlet of the intermediate water tank (6) through a pipeline, and a gas outlet of the ammonia nitrogen stripping tower (5) is communicated with a gas inlet of the ammonia nitrogen adsorption tower (501).
3. The advanced treatment of urine extraction wastewater and nitrogen resource recovery system of claim 1, wherein, a micro aeration zone (801), a first sludge recirculation zone (802) and a first sludge-water separation zone (803) are arranged in the nitrosation tank (8), an aeration device is arranged in the micro aeration zone (801), the first sludge recirculation zone (802) is communicated with the bottom of the first sludge-water separation zone (803), a first backwater baffle (804) is arranged between the first sludge recirculation zone (802) and the first sludge-water separation zone (803), and a first submersible water impeller (805) is arranged at the bottom of the first sludge-water separation zone (803).
4. The advanced treatment of urine extraction wastewater and nitrogen resource recovery system of claim 1, characterized in that, a mixing zone (901), a second sludge recirculation zone (902) and a second sludge-water separation zone (903) are arranged in said denitrification tank (9), the bottoms of the second sludge recirculation zone (902) and the second sludge-water separation zone (903) are communicated, a second return water baffle (904) is arranged between the second sludge recirculation zone (902) and the second sludge-water separation zone (903), and a second submersible water impeller (905) is arranged at the bottom of the second sludge-water separation zone (903).
5. The advanced urine extraction wastewater treatment and nitrogen resource recovery system according to claim 1, wherein the HA-UASB tank (7) is composed of 3 reaction zones from bottom to top, the first reaction zone is a lower flowing sludge bed (701), the second reaction zone is a suspended sludge tank (702), the third reaction zone is a micro-aeration solid-liquid separation tank (703), and a micro-aeration device is arranged at the lower part of a three-phase separator in the micro-aeration solid-liquid separation tank (703).
6. The advanced urine extraction wastewater treatment and nitrogen resource recovery system according to claim 1, wherein the anaerobic ammonium-oxygen tank (10) is composed of 3 reaction zones from bottom to top, the first reaction zone is a lower granular sludge zone (10-1), the second reaction zone is a completely flowing suspended sludge zone (10-2), the bottom of the suspended sludge zone (10-2) is provided with an aerator pipe, the third reaction zone is a micro-aeration solid-liquid separation zone (10-3), and the lower part of a three-phase separator in the micro-aeration solid-liquid separation zone (10-3) is provided with a micro-aeration device.
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