CN114149154B - Urine extraction wastewater treatment and nitrogen resource recovery method - Google Patents
Urine extraction wastewater treatment and nitrogen resource recovery method Download PDFInfo
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- CN114149154B CN114149154B CN202111625815.5A CN202111625815A CN114149154B CN 114149154 B CN114149154 B CN 114149154B CN 202111625815 A CN202111625815 A CN 202111625815A CN 114149154 B CN114149154 B CN 114149154B
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 72
- 210000002700 urine Anatomy 0.000 title claims abstract description 56
- 238000000605 extraction Methods 0.000 title claims abstract description 48
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 40
- 238000000034 method Methods 0.000 title claims abstract description 34
- 238000011084 recovery Methods 0.000 title claims abstract description 14
- 238000004065 wastewater treatment Methods 0.000 title claims abstract description 10
- 239000010802 sludge Substances 0.000 claims abstract description 121
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 113
- 239000002351 wastewater Substances 0.000 claims abstract description 106
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 63
- 230000003647 oxidation Effects 0.000 claims abstract description 58
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 31
- 238000004064 recycling Methods 0.000 claims abstract description 12
- 230000000694 effects Effects 0.000 claims abstract description 9
- 238000003860 storage Methods 0.000 claims abstract description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 74
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 66
- 241000894006 Bacteria Species 0.000 claims description 49
- 238000007034 nitrosation reaction Methods 0.000 claims description 45
- 230000009935 nitrosation Effects 0.000 claims description 44
- 238000000926 separation method Methods 0.000 claims description 39
- 238000005273 aeration Methods 0.000 claims description 38
- 229910021529 ammonia Inorganic materials 0.000 claims description 37
- 238000006243 chemical reaction Methods 0.000 claims description 36
- 239000007788 liquid Substances 0.000 claims description 26
- 238000009280 upflow anaerobic sludge blanket technology Methods 0.000 claims description 26
- 238000010992 reflux Methods 0.000 claims description 25
- 239000002131 composite material Substances 0.000 claims description 22
- 238000004062 sedimentation Methods 0.000 claims description 16
- 230000001112 coagulating effect Effects 0.000 claims description 15
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 12
- 230000003301 hydrolyzing effect Effects 0.000 claims description 12
- 230000020477 pH reduction Effects 0.000 claims description 12
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 claims description 10
- 238000001914 filtration Methods 0.000 claims description 10
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 9
- 238000004176 ammonification Methods 0.000 claims description 8
- 238000001179 sorption measurement Methods 0.000 claims description 8
- 230000000593 degrading effect Effects 0.000 claims description 7
- 239000000463 material Substances 0.000 claims description 7
- 244000005700 microbiome Species 0.000 claims description 7
- 239000010865 sewage Substances 0.000 claims description 7
- 238000009826 distribution Methods 0.000 claims description 6
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 claims description 6
- 239000007921 spray Substances 0.000 claims description 6
- 229910019142 PO4 Inorganic materials 0.000 claims description 5
- MMDJDBSEMBIJBB-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] MMDJDBSEMBIJBB-UHFFFAOYSA-N 0.000 claims description 5
- 230000018044 dehydration Effects 0.000 claims description 5
- 238000006297 dehydration reaction Methods 0.000 claims description 5
- 230000000696 methanogenic effect Effects 0.000 claims description 5
- 238000002156 mixing Methods 0.000 claims description 5
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 claims description 5
- 239000010452 phosphate Substances 0.000 claims description 5
- 230000001105 regulatory effect Effects 0.000 claims description 4
- 241000108664 Nitrobacteria Species 0.000 claims description 3
- 239000003513 alkali Substances 0.000 claims description 3
- 238000012258 culturing Methods 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims description 3
- 238000011049 filling Methods 0.000 claims description 3
- 230000014759 maintenance of location Effects 0.000 claims description 3
- 230000004060 metabolic process Effects 0.000 claims description 3
- 230000015556 catabolic process Effects 0.000 claims description 2
- 238000006731 degradation reaction Methods 0.000 claims description 2
- 230000000249 desinfective effect Effects 0.000 claims description 2
- 230000001546 nitrifying effect Effects 0.000 claims description 2
- 230000001590 oxidative effect Effects 0.000 claims description 2
- 244000052616 bacterial pathogen Species 0.000 claims 1
- 230000009189 diving Effects 0.000 claims 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 7
- 229910052799 carbon Inorganic materials 0.000 description 7
- 238000010586 diagram Methods 0.000 description 6
- 239000000243 solution Substances 0.000 description 5
- 230000001276 controlling effect Effects 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 239000003814 drug Substances 0.000 description 3
- 229940079593 drug Drugs 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 229910002651 NO3 Inorganic materials 0.000 description 2
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 2
- 241001453382 Nitrosomonadales Species 0.000 description 2
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 2
- 230000002411 adverse Effects 0.000 description 2
- BIGPRXCJEDHCLP-UHFFFAOYSA-N ammonium bisulfate Chemical compound [NH4+].OS([O-])(=O)=O BIGPRXCJEDHCLP-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 230000033228 biological regulation Effects 0.000 description 2
- 238000007664 blowing Methods 0.000 description 2
- 239000004202 carbamide Substances 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 239000012528 membrane Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000010979 pH adjustment Methods 0.000 description 2
- 229920001184 polypeptide Polymers 0.000 description 2
- 102000004196 processed proteins & peptides Human genes 0.000 description 2
- 108090000765 processed proteins & peptides Proteins 0.000 description 2
- 102000004169 proteins and genes Human genes 0.000 description 2
- 108090000623 proteins and genes Proteins 0.000 description 2
- DNXHEGUUPJUMQT-UHFFFAOYSA-N (+)-estrone Natural products OC1=CC=C2C3CCC(C)(C(CC4)=O)C4C3CCC2=C1 DNXHEGUUPJUMQT-UHFFFAOYSA-N 0.000 description 1
- DNXHEGUUPJUMQT-CBZIJGRNSA-N Estrone Chemical compound OC1=CC=C2[C@H]3CC[C@](C)(C(CC4)=O)[C@@H]4[C@@H]3CCC2=C1 DNXHEGUUPJUMQT-CBZIJGRNSA-N 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- CKUAXEQHGKSLHN-UHFFFAOYSA-N [C].[N] Chemical compound [C].[N] CKUAXEQHGKSLHN-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229960004407 chorionic gonadotrophin Drugs 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 230000009615 deamination Effects 0.000 description 1
- 238000006481 deamination reaction Methods 0.000 description 1
- 238000005261 decarburization Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 229960003399 estrone Drugs 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000011159 matrix material Substances 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 239000010815 organic waste Substances 0.000 description 1
- 230000036284 oxygen consumption Effects 0.000 description 1
- 238000005191 phase separation Methods 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000006228 supernatant Substances 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 150000005672 tetraenes Chemical class 0.000 description 1
- 235000013619 trace mineral Nutrition 0.000 description 1
- 239000011573 trace mineral Substances 0.000 description 1
- 230000002485 urinary effect Effects 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/24—Treatment of water, waste water, or sewage by flotation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/105—Phosphorus compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/04—Disinfection
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
Abstract
A urine extraction wastewater treatment and nitrogen resource recovery method comprises the following steps: A. pretreatment of urine extraction wastewater; B. treating organic matters in urine extraction wastewater; C. denitrification treatment of urine extraction wastewater; D. advanced treatment of urine extraction wastewater, wherein the wastewater is oxidized and disinfected in an ozone oxidation pond by adopting an ozone oxidation method, so that organic matters in the water are further removed, the water subjected to ozone oxidation enters a recycling pond for temporary storage, most of the water in the recycling pond is recycled to greening water in a factory, and the redundant water can reach the standard and be discharged; E. sludge treatment; the invention has scientific and reasonable design, simple and easy operation method, good treatment effect and low running cost, can deeply remove nitrogen in urine, reduces the output of residual sludge, and has remarkable social and economic benefits.
Description
Technical Field
The invention relates to wastewater treatment, in particular to a urine extraction wastewater treatment and nitrogen resource recovery method for high-nitrogen and high-organic matters.
Background
The urine contains a large amount of organic matters, nitrogen and phosphorus elements and rich trace elements, and can be used as raw materials for extracting and producing medicines, such as human chorionic gonadotrophin HCG, urinary gonadotrophin HMG, tetraene estrone and the like, and the waste water (namely urine extraction waste water) after the useful components of the urine are extracted can be discharged after being treated. As the effective components of the extracted medicines in urine are relatively belonging to the masses, enterprises which do not extract medicines on a large scale are not available, the existing enterprises collect the waste water and then mix the waste water with other waste water for treatment. At present, no complete treatment process technology for directly and completely treating urine extraction wastewater at home and abroad is available, most of researches are still in local treatment in a laboratory, the scale is small, the process is incomplete, the practicability is poor, and the method is difficult to directly use for production of large-scale industrial enterprises.
The urine draws waste water belongs to high nitrogen organic waste water, and the carbon-nitrogen ratio is low, and traditional denitrification process not only needs a large amount of external carbon source, improves sewage treatment running cost, has caused the waste of nitrogen resource in the urine draws waste water simultaneously, consequently, how to the treatment and the further recycle of urine extraction waste water is the technical problem that need carefully solve.
Disclosure of Invention
Aiming at the situation, the invention aims to overcome the defects of the prior art and provide a urine extraction wastewater treatment and nitrogen resource recovery method which can effectively solve the problems that the prior art cannot effectively treat the urine extraction wastewater and cannot further recycle the urine extraction wastewater.
In order to achieve the above purpose, the technical scheme of the invention is that a urine extraction wastewater treatment and nitrogen resource recovery method comprises the following steps:
A. pretreatment of urine extraction wastewater:
a1, filtering urine extraction wastewater by a sewage pump, carrying out external treatment on the grid residues, enabling the filtered wastewater to enter an adjusting tank to obtain uniform water quality and water quantity, enabling the effluent to enter an air floatation tank, adding 50-100mg/L PAC and 2-5mg/L PAM (namely adding 50-100mg PAC and 2-5mg PAM into each L of wastewater), and removing suspended matters in the wastewater;
A2, enabling air floatation effluent of the air floatation tank to enter an ammonification tank for ammoxidation for 1-2h, converting nitrogen-containing organic matters in the wastewater into ammonia nitrogen, and simultaneously primarily degrading the organic matters, wherein the concentration of the degraded sludge is 3000-5000mg/L; after the pH value of the effluent of the ammoniation pond is regulated to be 10-11, the effluent enters an ammonia nitrogen stripping tower;
A3, enabling the effluent to enter the upper part of an ammonia nitrogen stripping tower for spray stripping treatment, stripping for 1.5-2.0h, enabling ammonia nitrogen to be stripped together with air and enter an ammonia nitrogen adsorption tower for treatment, and enabling the wastewater after the treatment of the ammonia nitrogen stripping tower to enter an intermediate water tank;
B. And (3) treating organic matters in urine extraction wastewater:
b1, enabling the effluent of the ammonia nitrogen stripping tower to enter an intermediate water tank, adjusting pH value to be 7-8, and then entering an HA-UASB tank;
Adding activated sludge with hydrolytic acidification bacteria, methanogenic bacteria, nitrosation bacteria and anaerobic ammoxidation bacteria into the HA-UASB pool, removing most of organic matters through hydrolytic acidification and methanogenesis, simultaneously converting and degrading small molecular organic matters with nondegradable macromolecular organic matters, converting ammonia nitrogen into nitrite by nitrosation bacteria in the micro-aeration solid-liquid separation area, refluxing the nitrite to a flowing sludge bed and a second reaction area which are suspended sludge areas, and utilizing the nitrite and the ammonia nitrogen by the anaerobic ammoxidation bacteria to generate nitrogen, so that partial denitrification is realized, and the treated wastewater enters the nitrosation pool and the denitrification pool through a tee joint;
The HA-UASB pool is composed of 3 reaction areas from bottom to top, the first reaction area is a flowing sludge bed at the lower part, the second reaction area is a suspended sludge area, the third reaction area is a micro-aeration solid-liquid separation area, and a micro-aeration device is arranged at the lower part of a three-phase separator in the micro-aeration solid-liquid separation area;
C. Denitrification treatment of urine extraction wastewater:
Diverting the wastewater treated by the C1 and HA-UASB tanks according to the proportion of 1:1-2:1, respectively entering a nitrosation tank and a denitrification tank, adding sludge with nitrosation function into the nitrosation tank, controlling the concentration of the sludge to be 3000-6000mg/L, hydraulically staying in the nitrosation tank for 1-2h, converting ammonia nitrogen in the wastewater into NO 2 — N, adding sludge with denitrification function into the denitrification tank, controlling the concentration of the sludge to be 3000-6000mg/L, hydraulically staying in the denitrification tank for 1-2h, and converting nitrate nitrogen in the wastewater into N 2;
C2, the effluent of the nitrosation tank and the denitrification tank enter an anaerobic ammonia oxidation tank together, the water power stays for 5-10h, the anaerobic ammonia oxidation reaction is carried out, the mixed solution in the anaerobic ammonia oxidation tank flows back to the denitrification tank, the reflux ratio is 50-80%, and NO 3 - -N generated by the reaction is removed;
D. Advanced treatment of urine extraction wastewater:
And D1, enabling the effluent of the anaerobic ammonia oxidation tank to enter a composite filter tank, filtering suspended matters in the water, further removing residual total nitrogen, enabling the effluent of the composite filter tank to enter a coagulating sedimentation tank, adding PAC and PAM into the coagulating sedimentation tank, wherein the adding quantity of PAC is 20-50mg/L, the adding quantity of PAM is 1-3mg/L, and removing suspended matters and residual phosphate in the water. The treated effluent enters an ozone oxidation pond;
D2, oxidizing and disinfecting the wastewater in an ozone oxidation pond by adopting an ozone oxidation method, further removing organic matters in the water, temporarily storing the water after ozone oxidation in a reuse pond, recycling most of the water in the reuse pond into greening water in a factory, and discharging the redundant water up to the standard;
E. Sludge treatment:
Concentrating and dehydrating: the sludge in the air floatation tank, the HA-UASB tank, the coagulating sedimentation tank and the ozone oxidation tank enters a sludge concentration tank, is concentrated in the sludge concentration tank, and is sent to a dehydrator for dehydration, and dry sludge is transported and disposed.
The invention has scientific and reasonable design, simple and easy operation method, good treatment effect and low running cost, can deeply remove nitrogen in urine, reduces the output of residual sludge, and has remarkable social and economic benefits.
Drawings
FIG. 1 is a flow diagram of a process plant of the present invention.
FIG. 2 is a block diagram of a process equipment of the ammonia nitrogen stripping part of the present invention.
FIG. 3 is a block diagram of the construction of the nitrosation cell of the present invention.
FIG. 4 is a block diagram of the construction of the denitrification tank according to the invention.
FIG. 5 is a schematic diagram of the structure of the HA-UASB cell of the present invention.
FIG. 6 is a schematic diagram of the structure of an anaerobic ammonia oxidation tank according to the present invention.
Detailed Description
The following detailed description of specific embodiments of the invention refers to the accompanying drawings and the detailed description.
The method for treating urine extraction wastewater and recycling nitrogen resources comprises the following steps of:
A. pretreatment of urine extraction wastewater:
a1, filtering the urine extraction wastewater by a sewage pump, carrying out additional treatment on the wastewater after the wastewater is filtered by a grid 1, carrying out water quality regulation on the filtered wastewater in an adjusting tank 2, homogenizing water quality and water quantity, and feeding the discharged water in an air floatation tank 3, wherein 50-100mg/L PAC and 2-5mg/L PAM are added in the air floatation tank 3 to remove suspended matters in the wastewater;
A2, enabling air floatation effluent of the air floatation tank 3 to enter an ammonification tank 4 for ammoxidation for 1-2h, and performing ammonification by anaerobic microorganisms to convert nitrogen-containing organic matters such as urea, polypeptide and protein in the wastewater into ammonia nitrogen, so that subsequent stripping and recovery of the ammonia nitrogen are facilitated, meanwhile, the organic matters are primarily degraded, and the concentration of the degraded sludge is 3000-5000mg/L; the effluent of the ammoniation pond 4 is subjected to pH adjustment in a temporary alkali adjustment pond 401, and enters an ammonia nitrogen stripping tower 5 after the pH is adjusted to be 10-11 by NaOH;
A3, enabling the effluent to enter the upper part of an ammonia nitrogen stripping tower 5 for spray stripping treatment, cutting the effluent into a water film with the thickness of 0-1mm by a porous filter material in the stripping tower, slowly descending, sending air into the tower by a stripping fan, blowing upwards, stripping for 1.5-2.0h, separating ammonia nitrogen from wastewater, blowing ammonia nitrogen along with air into an ammonia nitrogen adsorption tower 501, absorbing by using a sulfuric acid solution with the thickness of 1-9mol/L, and enabling the wastewater treated by the ammonia nitrogen stripping tower 5 to enter an intermediate water tank 6;
Ammonia nitrogen in the water film is easy to volatilize into ammonia to overflow the water surface under the alkaline condition, the ammonia is discharged out of the stripping tower along with wind to realize deamination, and a temporary storage tank and a circulating pump are arranged at the bottom of the ammonia nitrogen stripping tower 5, so that the effects of circulating spraying and delivering waste water to the intermediate tank 6 can be realized. The ammonia nitrogen in the ammonia nitrogen stripping tower 5 is stripped along with air and enters the ammonia nitrogen adsorption tower 501, and is blown upwards from the lower part, a sulfuric acid tank and a circulating pump are arranged at the bottom of the ammonia nitrogen adsorption tower 501, the circulating pump can spray a dilute sulfuric acid solution from the top to form a liquid film, ammonia nitrogen recovery is realized by being beneficial to ammonia nitrogen absorption reaction to generate ammonia sulfate, the ammonia nitrogen recovery waste gas is discharged through a chimney, the ammonia nitrogen adsorption tower is provided with a pH meter, and ammonia nitrogen recovery effect can be easily ensured by monitoring a pH meter and discharging an ammonia sulfate byproduct and supplementing new dilute sulfuric acid;
B. And (3) treating organic matters in urine extraction wastewater:
b1, enabling effluent of the ammonia nitrogen stripping tower 5 to enter an intermediate water tank 6, adjusting pH=7-8 by using 1-6mol/L HCl solution, and then entering an HA-UASB tank 7;
2, adding activated sludge with hydrolytic acidification bacteria, methanogenic bacteria, nitrosation bacteria and anaerobic ammoxidation bacteria into the HA-UASB tank 7, removing most of organic matters through hydrolytic acidification and methanogenesis, simultaneously converting and degrading small molecular organic matters with nondegradable macromolecular organic matters, improving biodegradability of the organic matters, providing a carbon source for subsequent organisms, simultaneously converting ammonia nitrogen into nitrite by nitrosation bacteria of the micro-aeration solid-liquid separation area 703, refluxing the nitrite to the flowing sludge bed 701, and enabling the treated wastewater to enter the nitrosation tank 8 and the denitrification tank 9 through the tee joint 17 when the second reaction area is a suspended sludge area 702 (pure anaerobic area), and utilizing the anaerobic ammoxidation bacteria together with the ammonia nitrogen to generate nitrogen, thereby realizing partial denitrification;
The HA-UASB pool 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, enriches hydrolytic acidification bacteria and partial methanogens, mainly converts refractory macromolecular organic matters in wastewater into biodegradable micromolecular organic matters, and simultaneously removes partial organic matters; the second reaction area is a suspended sludge area 702, the sludge in the reaction area is lower than that in a flowing sludge bed area, and mainly enriches methanogens and anaerobic ammonia oxidizing bacteria, so that organic matters in water are further removed, and meanwhile, anaerobic ammonia oxidation denitrification reaction is carried out; the third reaction area is a micro-aeration solid-liquid separation area 703, a micro-aeration device is arranged at the lower part of a three-phase separator in the micro-aeration solid-liquid separation area 703, sludge in the reaction area is lower than that in a flowing sludge bed area, nitrosating bacteria are mainly enriched, organic matters in water are further removed, and nitrosation reaction is carried out simultaneously; the sludge concentration of the flowing sludge bed 701 is 15000-25000mg/L, the sludge concentration of the suspended sludge zone 702 is 10000-15000mg/L, and the sludge concentration of the micro-aeration solid-liquid separation zone 703 is 5000-10000mg/L. Simultaneously, a micro-aeration device in the micro-aeration solid-liquid separation area 703 is started, on one hand, solid-liquid separation is realized through a three-phase separator, and meanwhile, the separated activated sludge is quickly returned to the first reaction area under the action of micro-aeration. The reaction tank not only removes most of organic matters through the hydrolytic acidification and the methanogenesis of microorganisms, but also converts the difficult-to-degrade macromolecular organic matters into degradable micromolecular organic matters;
C. Denitrification treatment of urine extraction wastewater:
Diverting the wastewater treated by the C1 and HA-UASB pool 7 according to the proportion of 1:1-2:1, respectively entering a nitrosation pool 8 and a denitrification pool 9, adding sludge with nitrosation function into the nitrosation pool 8, controlling the concentration of the sludge to be 3000-6000mg/L, staying in the nitrosation pool 8 by water for 1-2h, converting ammonia nitrogen in the wastewater into NO 2 — N under the action of nitrobacteria, adding sludge with the denitrification function into the denitrification pool 9, controlling the concentration of the sludge to be 3000-6000mg/L, staying in the denitrification pool 9 by water for 1-2h, and converting nitrate nitrogen in the wastewater into N 2 by using organic matters in the water;
C2, the effluent water containing NO 2 - -N from the nitrosation tank 8 and the effluent water containing NH 4 + -N from the denitrification tank 9 enter an anaerobic ammonia oxidation tank 10 together, the hydraulic retention time is 5-10h, anaerobic ammonia oxidation bacteria carry out anaerobic ammonia oxidation reaction by using NO 2 - -N and NH 4 + -N in the water, mixed liquid in the anaerobic ammonia oxidation tank 10 flows back to the denitrification tank 9, the reflux ratio is 50% -80%, and NO 3 - -N generated by the reaction is removed;
The nitrosation pool 8 is internally provided with a micro aeration zone 801, a sludge reflux zone 802 and a mud-water separation zone 803, the micro aeration zone 801 is internally provided with an aeration device, dissolved oxygen DO=0.5-1.0 mg/L, NH 4 + -N is converted into NO 2 - -N by using nitrosation bacteria, NO 2 - -N matrix is provided for the anaerobic ammoxidation pool, the sludge reflux zone 802 is communicated with the bottom of the mud-water separation zone 803, a backwater baffle 804 is arranged between the sludge reflux zone 802 and the mud-water separation zone 803, the bottom of the mud-water separation zone 803 is provided with a submerged impeller 805, along with the micro aeration to push sewage into the sludge reflux zone, the mixed liquid enters the mud-water separation zone from top to bottom under the action of the backwater baffle to carry out mud-water separation by a reflux pipe, supernatant fluid is discharged, and the sinking sludge is refluxed to the micro aeration zone by using the submerged impeller;
The denitrification tank 9 is internally provided with a mixing area 901, a sludge reflux area 902 and a sludge-water separation area 903, NO 3 - -N in reflux liquid is converted into N 2 by denitrifying bacteria in the mixing area 901 by using a water inlet carbon source, the bottoms of the sludge reflux area 902 and the sludge-water separation area 903 are communicated, a backwater baffle 904 is arranged between the sludge reflux area 902 and the sludge-water separation area 903, a submerged impeller 905 is arranged at the bottom of the sludge-water separation area 903, the sludge-water mixture enters the sludge-water separation area 903 from top to bottom through a backwater under the action of the backwater baffle 904 and the submerged impeller 905 to carry out sludge-water separation area, and precipitated sludge is refluxed to the mixing area 901 under the action of the submerged impeller 905;
The anaerobic ammonia oxidation pond 10 is composed of 3 reaction areas from bottom to top, wherein the first reaction area is a granular sludge area 10-1 at the lower part, the area is mainly anaerobic ammonia oxidation bacteria and denitrifying bacteria, a small amount of nitrate contained in internal reflux sludge can utilize a carbon source in water to perform denitrification and denitrification, the denitrification can be accelerated, the adverse effect of the carbon source on the anaerobic ammonia oxidation can be avoided, the second reaction area is a fully-flowing suspended sludge area 10-2, an aeration pipe is arranged at the bottom of the suspended sludge area 10-2, an aeration air source is a three-phase separation air source of the anaerobic ammonia oxidation pond, the main component is nitrogen, so that the adverse effect of oxygen on the anaerobic ammonia oxidation is avoided, and the area cultures the enriched anaerobic ammonia oxidation bacteria, ammonia nitrogen and nitrite in the water to be fully mixed and efficiently react to generate nitrogen and a small amount of nitrate; the third reaction zone is a micro-aeration solid-liquid separation zone 10-3, a micro-aeration device is arranged at the lower part of a three-phase separator in the micro-aeration solid-liquid separation zone 10-3, the return flow of sludge is accelerated to the bottom through air stirring, a micro-aeration air source hardly contains oxygen (negligible), mainly plays a role in mixing and accelerating the return flow of sludge, and is arranged to not interfere with the anaerobic environment at the bottom of an anaerobic ammoxidation tank reactor;
D. Advanced treatment of urine extraction wastewater:
D1, enabling effluent of the anaerobic ammonia oxidation tank 10 to enter a composite filter tank 11, filtering suspended matters in water, further removing residual total nitrogen, filling cobbles and ceramsites at the lower part of the composite filter tank, paving air distribution and water distribution devices, culturing the inner and outer surfaces of filter materials in the composite filter tank to generate composite biological membranes, wherein the inner and outer surfaces of the filter materials in the composite filter tank contain nitrosates, nitrifiers, denitrifiers and anaerobic ammonia oxidation bacteria, further removing the residual total nitrogen, achieving stable standard, enabling the effluent of the composite filter tank 11 to enter a coagulating sedimentation tank 12, adding PAC and PAM into the coagulating sedimentation tank 12, wherein the adding quantity of PAC is 20-50mg/L, the adding quantity of PAM is 1-3mg/L, removing suspended matters and residual phosphate in the water, and enabling treated effluent to enter an ozone oxidation tank 13;
d2, the wastewater is oxidized and disinfected in an ozone oxidation pond 13 by adopting an ozone oxidation method, hydroxyl radicals generated by ozone interfere with microorganism metabolism, so that bacteria are killed, meanwhile, organic matters in the water can be further removed, the water after ozone oxidation enters a reuse pond 14 for temporary storage, most of the water in the reuse pond 14 is reused for greening water in a factory, and the redundant water can reach the standard for discharge;
E. Sludge treatment:
Concentrating and dehydrating: the sludge in the air floatation tank 3, the HA-UASB tank 7, the coagulating sedimentation tank 12 and the ozone oxidation tank 13 enters a sludge concentration tank 15, is concentrated in the sludge concentration tank 15, and is sent to a dehydrator 16 for dehydration, and the dry sludge is transported and disposed.
The invention, when embodied, is illustrated by the following examples.
A urine extraction wastewater treatment and nitrogen resource recovery method comprises the following steps:
A. pretreatment of urine extraction wastewater:
A1, filtering the urine extraction wastewater by a sewage pump, carrying out additional treatment on the wastewater after the wastewater is filtered by a grid 1, carrying out water quality regulation on the filtered wastewater in an adjusting tank 2, homogenizing water quality and water quantity, and feeding the discharged water in an air floatation tank 3, wherein 60mg/L PAC and 3mg/L PAM are added in the air floatation tank 3 to remove suspended matters in the wastewater;
a2, enabling air floatation effluent of the air floatation tank 3 to enter an ammonification tank 4 for ammoxidation for 1.5 hours, and performing ammonification by anaerobic microorganisms to convert nitrogen-containing organic matters such as urea, polypeptide and protein in the wastewater into ammonia nitrogen, and simultaneously performing preliminary degradation on the organic matters, wherein the concentration of the degraded sludge is 3000-5000mg/L; the effluent of the ammoniation pond 4 is subjected to pH adjustment in a temporary alkali adjustment pond 401, and enters an ammonia nitrogen stripping tower 5 after the pH=10 is adjusted by NaOH;
A3, enabling the effluent to enter the upper part of the ammonia nitrogen stripping tower 5 for spray stripping treatment, stripping for 1.5 hours, separating ammonia nitrogen from the wastewater, enabling the ammonia nitrogen to enter the ammonia nitrogen adsorption tower 501 along with air, absorbing by using 2mol/L sulfuric acid solution, recycling nitrogen, and enabling the wastewater treated by the ammonia nitrogen stripping tower 5 to enter an intermediate water tank 6;
B. And (3) treating organic matters in urine extraction wastewater:
B1, enabling effluent of the ammonia nitrogen stripping tower 5 to enter an intermediate water tank 6, adjusting pH=7 by using 1mol/L HCl solution, and then entering an HA-UASB tank 7;
B2, adding activated sludge with hydrolytic acidification bacteria, methanogenic bacteria, nitrosation bacteria and anaerobic ammoxidation bacteria into the HA-UASB tank 7, removing most of organic matters through hydrolytic acidification and methanogenesis, simultaneously converting and degrading small molecular organic matters with refractory macromolecular organic matters, improving the biodegradability of the organic matters, providing a carbon source for subsequent organisms, and enabling the treated wastewater to enter the nitrosation tank 8 and the denitrification tank 9 through the tee joint 17; wherein the sludge concentration of the flowing sludge bed 701 is 20000mg/L, the sludge concentration of the suspended sludge zone 702 is 12500mg/L, and the sludge concentration of the micro-aeration solid-liquid separation zone 703 is 7000mg/L;
C. Denitrification treatment of urine extraction wastewater:
The wastewater treated by the C1 and the HA-UASB tank 7 is split according to the proportion of 1:1, the split can be controlled by the diameter of a pipeline connected with a tee joint 17, the split can respectively enter a nitrosation tank 8 and a denitrification tank 9, sludge with nitrosation function is added into the nitrosation tank 8, the concentration of the sludge is controlled to be 4500mg/L, the water force in the nitrosation tank 8 stays for 1.5h, ammonia nitrogen in the wastewater is converted into NO 2 — N under the action of nitrobacteria, sludge with denitrification function is added into the denitrification tank 9, the concentration of the sludge is controlled to be 4500mg/L, the water force in the denitrification tank 9 stays for 1.5h, and the denitrifying bacteria utilizes organic matters in the water to convert nitrate nitrogen in the wastewater into N 2;
The effluent of the C2 and the nitrosation pool 8 containing NO 2 - -N and the effluent of the denitrification pool 9 containing NH 4 + -N enter an anaerobic ammonia oxidation pool 10 together, the water stays for 8 hours, anaerobic ammonia oxidation bacteria carry out anaerobic ammonia oxidation reaction by using NO 2 - -N and NH 4 + -N in the water, mixed liquid in the anaerobic ammonia oxidation pool 10 flows back to the denitrification pool 9 with a reflux ratio of 60%, and NO 3 - -N generated by the reaction is removed;
D. Advanced treatment of urine extraction wastewater:
D1, enabling effluent of the anaerobic ammonia oxidation tank 10 to enter a composite filter tank 11, filtering suspended matters in water, further removing residual total nitrogen, filling cobbles and ceramsites at the lower part of the composite filter tank, paving air distribution and water distribution devices, culturing the inner and outer surfaces of filter materials in the composite filter tank to generate composite biological membranes, wherein the inner and outer surfaces of the filter materials in the composite filter tank contain nitrosates, nitrifiers, denitrifiers and anaerobic ammonia oxidation bacteria, further removing the residual total nitrogen, achieving stable standard, enabling the effluent of the composite filter tank 11 to enter a coagulating sedimentation tank 12, adding PAC and PAM into the coagulating sedimentation tank 12, wherein the adding quantity of PAC is 30mg/L, the adding quantity of PAM is 1mg/L, removing suspended matters and residual phosphate in water, and enabling treated effluent to enter an ozone oxidation tank 13;
d2, the wastewater is oxidized and disinfected in an ozone oxidation pond 13 by adopting an ozone oxidation method, hydroxyl radicals generated by ozone interfere with microorganism metabolism, so that bacteria are killed, meanwhile, organic matters in the water can be further removed, the water after ozone oxidation enters a reuse pond 14 for temporary storage, most of the water in the reuse pond 14 is reused for greening water in a factory, and the redundant water can reach the standard for discharge;
E. Sludge treatment:
Concentrating and dehydrating: the sludge in the air floatation tank 3, the HA-UASB tank 7, the coagulating sedimentation tank 12 and the ozone oxidation tank 13 enters a sludge concentration tank 15, is concentrated in the sludge concentration tank 15, and is sent to a dehydrator 16 for dehydration, and the dry sludge is transported and disposed.
The design of the invention is scientific and reasonable, the method is simple and easy to operate, and compared with the prior art, the invention 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 subsequent biological treatment is reduced;
(2) The method is characterized in that the method is improved into HA-UASB based on the traditional UASB reactor, a micro-aeration device is arranged at the upper part of the reactor to accelerate the sludge reflux and improve the decarburization efficiency by 10-20%, and meanwhile, the traditional reactor without denitrification effect HAs the denitrification efficiency of 20-30%;
(3) Nitrifying bacteria, nitrosate bacteria and anaerobic ammonia oxidizing bacteria with great difference in growth environment requirements are respectively located in different sludge systems, so that efficient operation of the systems is facilitated;
(4) Respectively setting wastewater to enter a nitrosation tank and a denitrification tank to realize quantitative and qualitative water inflow, and effectively utilizing a carbon source to accumulate NO 2 - -N and remove NO 3 - -N so as to provide reaction conditions for the subsequent anaerobic ammoxidation reaction;
(5) No sedimentation tank is needed, the unit treatment load is high, and the occupied area is reduced by 30-50% and the capital cost is reduced by 20-40%;
(6) The sludge age of the whole system is longer, anaerobic treatment is mainly carried out, the sludge yield is small, the yield of biochemical sludge can be reduced by 80-90% compared with the traditional process, the oxygen consumption is small, the power consumption can be reduced by 50-60% compared with the traditional process, the treatment effect is good, the running cost is low, the nitrogen in urine can be deeply removed, and the method has remarkable social and economic benefits.
Claims (6)
1. The urine extraction wastewater treatment and nitrogen resource recovery method is characterized by comprising the following steps of:
A. pretreatment of urine extraction wastewater:
A1, filtering urine extraction wastewater by a sewage pump, carrying out additional treatment on the wastewater after the wastewater enters a grid (1), enabling the filtered wastewater to enter an adjusting tank (2) to be uniform in water quality and water quantity, enabling effluent to enter an air floatation tank (3), adding 50-100mg/L PAC and 2-5mg/L PAM into the air floatation tank (3), and removing suspended matters in the wastewater;
A2, enabling air floatation effluent of the air floatation tank (3) to enter an ammonification tank (4) for ammoxidation for 1-2h, converting nitrogen-containing organic matters in the wastewater into ammonia nitrogen, and simultaneously carrying out preliminary degradation on the organic matters, wherein the concentration of the degraded sludge is 3000-5000mg/L; after the pH value of the effluent of the ammoniation pond (4) is regulated to be 10-11, the effluent enters an ammonia nitrogen stripping tower (5);
A3, enabling the effluent to enter the upper part of an ammonia nitrogen stripping tower (5) for spray stripping treatment, stripping for 1.5-2.0h, enabling ammonia nitrogen to enter an ammonia nitrogen adsorption tower (501) for treatment along with air, and enabling the wastewater treated by the ammonia nitrogen stripping tower (5) to enter an intermediate water tank (6);
B. And (3) treating organic matters in urine extraction wastewater:
B1, enabling effluent of the ammonia nitrogen stripping tower (5) to enter an intermediate water tank (6), adjusting pH=7-8, and then entering an HA-UASB tank (7);
b2, adding activated sludge with hydrolytic acidification bacteria, methanogenic bacteria, nitrosation bacteria and anaerobic ammoxidation bacteria into the HA-UASB tank (7), removing most of organic matters through hydrolytic acidification and methanogenesis, simultaneously converting and degrading small molecular organic matters with nondegradable macromolecular organic matters, simultaneously converting ammonia nitrogen into nitrite by nitrosation bacteria of the first micro-aeration solid-liquid separation area (703), and when the nitrite flows back to the flowing sludge bed (701) and the second reaction area is the first suspended sludge area (702), generating nitrogen by the anaerobic ammoxidation bacteria together with the ammonia nitrogen, realizing partial denitrification, and enabling the treated wastewater to enter the nitrosation tank (8) and the denitrification tank (9) through the tee joint (17);
The HA-UASB pool (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 first suspended sludge area (702), the third reaction area is a first micro-aeration solid-liquid separation area (703), and a micro-aeration device is arranged at the lower part of a three-phase separator in the first micro-aeration solid-liquid separation area (703);
C. Denitrification treatment of urine extraction wastewater:
the wastewater treated by the C1 and HA-UASB tanks (7) is split according to the proportion of 1:1-2:1, and enters a nitrosation tank (8) and a denitrification tank (9) respectively, sludge with nitrosation function is added into the nitrosation tank (8), the concentration of the sludge is controlled to be 3000-6000mg/L, hydraulic retention is carried out for 1-2h in the nitrosation tank (8), ammonia nitrogen in the wastewater is converted into NO 2 — N, sludge with denitrification function is added into the denitrification tank (9), the concentration of the sludge is controlled to be 3000-6000mg/L, hydraulic retention is carried out for 1-2h in the denitrification tank (9), and nitrate nitrogen in the wastewater is converted into N 2;
The effluent of the C2, the nitrosation tank (8) and the denitrification tank (9) enter an anaerobic ammonia oxidation tank (10) together, the hydraulic power stays for 5-10h, the anaerobic ammonia oxidation reaction is carried out, the mixed liquid in the anaerobic ammonia oxidation tank (10) flows back to the denitrification tank (9), the reflux ratio is 50-80%, and NO 3 - -N generated by the reaction is removed;
D. Advanced treatment of urine extraction wastewater:
D1, enabling effluent of the anaerobic ammonia oxidation tank (10) to enter a composite filter tank (11), filtering suspended matters in water, further removing residual total nitrogen, enabling effluent of the composite filter tank (11) to enter a coagulating sedimentation tank (12), adding PAC and PAM into the coagulating sedimentation tank (12), wherein the adding quantity of PAC is 20-50mg/L, the adding quantity of PAM is 1-3mg/L, removing suspended matters in water and residual phosphate, and enabling treated effluent to enter an ozone oxidation tank (13);
D2, oxidizing and disinfecting the wastewater in an ozone oxidation pond (13) by adopting an ozone oxidation method, further removing organic matters in the water, temporarily storing the water after ozone oxidation in a reuse pond (14), recycling most of the water in the reuse pond (14) into greening water in a factory, and discharging the redundant water up to the standard;
E. Sludge treatment:
Concentrating and dehydrating: the sludge in the air floatation tank (3), the HA-UASB tank (7), the coagulating sedimentation tank (12) and the ozone oxidation tank (13) enters a sludge concentration tank (15), is concentrated in the sludge concentration tank (15), and is sent to a dehydrator (16) for dehydration, and the dry sludge is transported to the outside for disposal.
2. The urine extraction wastewater treatment and nitrogen resource recovery method according to claim 1, comprising the steps of:
A. pretreatment of urine extraction wastewater:
A1, filtering urine extraction wastewater by a sewage pump, carrying out additional treatment on the wastewater after the wastewater enters a grid (1), enabling the filtered wastewater to enter an adjusting tank (2) to be uniform in water quality and water quantity, enabling effluent to enter an air floatation tank (3), adding 50-100mg/L PAC and 2-5mg/L PAM into the air floatation tank (3), and removing suspended matters in the wastewater;
A2, enabling air floatation effluent of the air floatation tank (3) to enter an ammonification tank (4) for ammoxidation for 1-2h, and converting nitrogen-containing organic matters in the wastewater into ammonia nitrogen through the ammonification effect of anaerobic microorganisms, and simultaneously primarily degrading the organic matters, wherein the concentration of the degraded sludge is 3000-5000mg/L; the effluent of the ammoniation tank (4) is regulated to pH value of 10-11 by NaOH in a temporary alkali regulating tank (401) and enters an ammonia nitrogen stripping tower (5);
A3, enabling the effluent to enter the upper part of an ammonia nitrogen stripping tower (5) for spray stripping treatment, stripping for 1.5-2.0h, enabling ammonia nitrogen to enter an ammonia nitrogen adsorption tower (501) along with air, absorbing by using 1-9mol/L sulfuric acid solution, and enabling the wastewater treated by the ammonia nitrogen stripping tower (5) to enter an intermediate water tank (6);
B. And (3) treating organic matters in urine extraction wastewater:
b1, enabling effluent of the ammonia nitrogen stripping tower (5) to enter an intermediate water tank (6), adjusting pH value to be 7-8 by using 1-6mol/L HCl solution, and then entering an HA-UASB tank (7);
B2, adding activated sludge with hydrolytic acidification bacteria, methanogenic bacteria, nitrosation bacteria and anaerobic ammoxidation bacteria into the HA-UASB tank (7), removing most of organic matters through hydrolytic acidification and methanogenesis, simultaneously converting and degrading small molecular organic matters with nondegradable macromolecular organic matters, simultaneously converting ammonia nitrogen into nitrite by nitrosation bacteria of the first micro-aeration solid-liquid separation area (703), refluxing the nitrite to the flowing sludge bed (701), and when the second reaction area is the first suspended sludge area (702), generating nitrogen by the anaerobic ammoxidation bacteria together with the ammonia nitrogen to realize partial denitrification, and enabling the treated wastewater to enter the nitrosation tank (8) and the denitrification tank (9) through the tee joint (17);
C. Denitrification treatment of urine extraction wastewater:
The wastewater treated by the C1 and HA-UASB tanks (7) is split according to the proportion of 1:1-2:1, and enters a nitrosation tank (8) and a denitrification tank (9) respectively, sludge with nitrosation function is added into the nitrosation tank (8), the concentration of the sludge is controlled to be 3000-6000mg/L, the wastewater is hydraulically stopped for 1-2h in the nitrosation tank (8), ammonia nitrogen in the wastewater is converted into NO 2 — N under the action of nitrobacteria, sludge with denitrification function is added into the denitrification tank (9), the concentration of the sludge is controlled to be 3000-6000mg/L, the water is hydraulically stopped for 1-2h in the denitrification tank (9), and the denitrifying bacteria utilizes organic matters in the water to convert nitrate nitrogen in the wastewater into N 2;
C2, enabling NO 2 - -N-containing effluent from a nitrosation tank (8) and NH 4 + -N-containing effluent from a denitrification tank (9) to enter an anaerobic ammonia oxidation tank (10) together, enabling anaerobic ammonia oxidation bacteria to stay for 5-10h by hydraulic power, performing anaerobic ammonia oxidation reaction by utilizing NO 2 - -N and NH 4 + -N in the water, and enabling mixed liquid in the anaerobic ammonia oxidation tank (10) to flow back to the denitrification tank (9) with a reflux ratio of 50% -80%, and removing NO 3 - -N generated by the reaction;
D. Advanced treatment of urine extraction wastewater:
D1, enabling effluent of an anaerobic ammonia oxidation pond (10) to enter a composite filter pond (11), filtering suspended matters in water, further removing residual total nitrogen, filling cobbles and ceramsites at the lower part of the composite filter pond, paving air distribution devices and water distribution devices, culturing the inner and outer surfaces of filter materials in the composite filter pond to generate a composite biological film, wherein the inner and outer surfaces of the filter materials in the composite filter pond contain nitrosates, nitrifying bacteria, denitrifying bacteria and anaerobic ammonia oxidation bacteria, further removing the residual total nitrogen to achieve stable standard, enabling the effluent of the composite filter pond (11) to enter a coagulating sedimentation pond (12), adding PAC and PAM into the coagulating sedimentation pond (12), wherein the adding quantity of the PAC is 20-50mg/L, the adding quantity of the PAM is 1-3mg/L, removing suspended matters and residual phosphate in water, and enabling treated effluent to enter an ozone oxidation pond (13);
d2, the wastewater is oxidized and disinfected in an ozone oxidation pond (13) by adopting an ozone oxidation method, hydroxyl radicals generated by ozone interfere with microorganism metabolism, so that germs can be killed, meanwhile, organic matters in the water can be further removed, the water after ozone oxidation enters a recycling pond (14) for temporary storage, most of the water in the recycling pond (14) is recycled to greening water in a factory, and the redundant water can reach the standard and be discharged;
E. Sludge treatment:
Concentrating and dehydrating: the sludge in the air floatation tank (3), the HA-UASB tank (7), the coagulating sedimentation tank (12) and the ozone oxidation tank (13) enters a sludge concentration tank (15), is concentrated in the sludge concentration tank (15), and is sent to a dehydrator (16) for dehydration, and the dry sludge is transported to the outside for disposal.
3. The method for treating urine extraction wastewater and recycling nitrogen resources according to claim 1 or 2, wherein a micro aeration zone (801), a first sludge reflux 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 bottoms of the first sludge reflux zone (802) and the first sludge-water separation zone (803) are communicated, a first backwater baffle (804) is arranged between the first sludge reflux zone (802) and the first sludge-water separation zone (803), and a first diving impeller (805) is arranged at the bottom of the first sludge-water separation zone (803).
4. The method for treating the urine extraction wastewater and recycling the nitrogen resources according to claim 1 or 2, wherein a mixing zone (901), a second sludge reflux zone (902) and a second sludge-water separation zone (903) are arranged in the denitrification tank (9), the bottoms of the second sludge reflux zone (902) and the second sludge-water separation zone (903) are communicated, a second backwater baffle (904) is arranged between the second sludge reflux zone (902) and the second sludge-water separation zone (903), and a second submerged impeller (905) is arranged at the bottom of the second sludge-water separation zone (903).
5. The method for treating urine extraction wastewater and recovering nitrogen resources according to claim 1 or 2, wherein the sludge concentration of the flowing sludge bed (701) is 15000-25000mg/L, the sludge concentration of the first suspended sludge zone (702) is 10000-15000mg/L, and the sludge concentration of the first micro-aeration solid-liquid separation zone (703) is 5000-10000mg/L.
6. The method for treating urine extraction wastewater and recycling nitrogen resources according to claim 1 or 2, wherein the anaerobic ammonia oxidation 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 fully flowing second suspended sludge area (10-2), an aeration pipe is arranged at the bottom of the second suspended sludge area (10-2), the third reaction area is a second 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 second micro-aeration solid-liquid separation area (10-3).
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