CN114409183B - Universal gelatin wastewater treatment method - Google Patents
Universal gelatin wastewater treatment method Download PDFInfo
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- CN114409183B CN114409183B CN202111627134.2A CN202111627134A CN114409183B CN 114409183 B CN114409183 B CN 114409183B CN 202111627134 A CN202111627134 A CN 202111627134A CN 114409183 B CN114409183 B CN 114409183B
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- 108010010803 Gelatin Proteins 0.000 title claims abstract description 39
- 229920000159 gelatin Polymers 0.000 title claims abstract description 39
- 239000008273 gelatin Substances 0.000 title claims abstract description 39
- 235000019322 gelatine Nutrition 0.000 title claims abstract description 39
- 235000011852 gelatine desserts Nutrition 0.000 title claims abstract description 39
- 238000004065 wastewater treatment Methods 0.000 title claims abstract description 13
- 239000002351 wastewater Substances 0.000 claims abstract description 120
- 239000010802 sludge Substances 0.000 claims abstract description 108
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 93
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 66
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims abstract description 48
- 229910052698 phosphorus Inorganic materials 0.000 claims abstract description 48
- 239000011574 phosphorus Substances 0.000 claims abstract description 48
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 32
- 238000004062 sedimentation Methods 0.000 claims abstract description 31
- 230000000694 effects Effects 0.000 claims abstract description 28
- 238000009280 upflow anaerobic sludge blanket technology Methods 0.000 claims abstract description 24
- 230000001112 coagulating effect Effects 0.000 claims abstract description 17
- 230000001105 regulatory effect Effects 0.000 claims abstract description 14
- 238000004519 manufacturing process Methods 0.000 claims abstract description 13
- 239000002957 persistent organic pollutant Substances 0.000 claims abstract description 11
- 229910019142 PO4 Inorganic materials 0.000 claims abstract description 5
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 claims abstract description 5
- 239000010452 phosphate Substances 0.000 claims abstract description 5
- 238000003860 storage Methods 0.000 claims abstract description 5
- 238000005345 coagulation Methods 0.000 claims abstract description 4
- 230000015271 coagulation Effects 0.000 claims abstract description 4
- 241000894006 Bacteria Species 0.000 claims description 39
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 30
- 238000006243 chemical reaction Methods 0.000 claims description 29
- 229910002651 NO3 Inorganic materials 0.000 claims description 24
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 claims description 24
- 238000005273 aeration Methods 0.000 claims description 22
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 claims description 20
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 19
- 229910052799 carbon Inorganic materials 0.000 claims description 19
- 239000007788 liquid Substances 0.000 claims description 17
- 238000007034 nitrosation reaction Methods 0.000 claims description 17
- 230000009935 nitrosation Effects 0.000 claims description 16
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 14
- 238000000926 separation method Methods 0.000 claims description 14
- 238000005189 flocculation Methods 0.000 claims description 11
- 230000016615 flocculation Effects 0.000 claims description 11
- 230000001546 nitrifying effect Effects 0.000 claims description 10
- 150000001768 cations Chemical class 0.000 claims description 9
- 229910052751 metal Inorganic materials 0.000 claims description 9
- 239000002184 metal Substances 0.000 claims description 9
- 238000007254 oxidation reaction Methods 0.000 claims description 9
- 238000006731 degradation reaction Methods 0.000 claims description 8
- 230000003301 hydrolyzing effect Effects 0.000 claims description 8
- 230000020477 pH reduction Effects 0.000 claims description 8
- 238000001556 precipitation Methods 0.000 claims description 8
- 150000003839 salts Chemical class 0.000 claims description 8
- 229910021529 ammonia Inorganic materials 0.000 claims description 7
- 230000015556 catabolic process Effects 0.000 claims description 7
- 238000003487 electrochemical reaction Methods 0.000 claims description 7
- 230000003647 oxidation Effects 0.000 claims description 7
- 238000005192 partition Methods 0.000 claims description 7
- 238000004064 recycling Methods 0.000 claims description 7
- 238000003756 stirring Methods 0.000 claims description 7
- 239000011259 mixed solution Substances 0.000 claims description 6
- 239000003344 environmental pollutant Substances 0.000 claims description 5
- 231100000719 pollutant Toxicity 0.000 claims description 5
- 239000007787 solid Substances 0.000 claims description 5
- 208000034699 Vitreous floaters Diseases 0.000 claims description 4
- 239000003513 alkali Substances 0.000 claims description 4
- 244000005700 microbiome Species 0.000 claims description 4
- 239000002253 acid Substances 0.000 claims description 3
- 210000005056 cell body Anatomy 0.000 claims description 3
- 230000018044 dehydration Effects 0.000 claims description 3
- 238000006297 dehydration reaction Methods 0.000 claims description 3
- 230000000696 methanogenic effect Effects 0.000 claims description 3
- 239000000243 solution Substances 0.000 claims description 3
- 239000006228 supernatant Substances 0.000 claims description 3
- 239000003814 drug Substances 0.000 claims description 2
- 239000013049 sediment Substances 0.000 claims 1
- 238000000034 method Methods 0.000 abstract description 17
- 239000002994 raw material Substances 0.000 abstract description 10
- 238000010992 reflux Methods 0.000 description 6
- 239000002245 particle Substances 0.000 description 5
- 239000002893 slag Substances 0.000 description 5
- 210000004027 cell Anatomy 0.000 description 4
- 238000010586 diagram Methods 0.000 description 3
- 238000009826 distribution Methods 0.000 description 3
- 239000010865 sewage Substances 0.000 description 3
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 2
- 229910000975 Carbon steel Inorganic materials 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 2
- 241000282894 Sus scrofa domesticus Species 0.000 description 2
- 229910052782 aluminium Inorganic materials 0.000 description 2
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 2
- 210000000988 bone and bone Anatomy 0.000 description 2
- 239000011575 calcium Substances 0.000 description 2
- 229910052791 calcium Inorganic materials 0.000 description 2
- 159000000007 calcium salts Chemical class 0.000 description 2
- 239000010962 carbon steel Substances 0.000 description 2
- 239000000084 colloidal system Substances 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 229910001873 dinitrogen Inorganic materials 0.000 description 2
- 239000003292 glue Substances 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 239000004519 grease Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000002244 precipitate Substances 0.000 description 2
- 108090000623 proteins and genes Proteins 0.000 description 2
- 102000004169 proteins and genes Human genes 0.000 description 2
- 238000006722 reduction reaction Methods 0.000 description 2
- -1 skin Chemical class 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- 102000004190 Enzymes Human genes 0.000 description 1
- 108090000790 Enzymes Proteins 0.000 description 1
- 241001453382 Nitrosomonadales Species 0.000 description 1
- 241001494479 Pecora Species 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000000701 coagulant Substances 0.000 description 1
- 238000005238 degreasing Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000000839 emulsion Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 230000005764 inhibitory process Effects 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 239000011146 organic particle Substances 0.000 description 1
- 238000010525 oxidative degradation reaction Methods 0.000 description 1
- 238000010979 pH adjustment Methods 0.000 description 1
- 238000005554 pickling Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000012797 qualification Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000005096 rolling process Methods 0.000 description 1
- 238000007790 scraping Methods 0.000 description 1
- 238000005201 scrubbing Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 238000010408 sweeping Methods 0.000 description 1
- 239000010936 titanium Substances 0.000 description 1
- 229910052719 titanium Inorganic materials 0.000 description 1
Classifications
-
- 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
- C02F1/24—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
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/463—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrocoagulation
-
- 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
- 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
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/308—Biological phosphorus removal
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
Abstract
A general gelatin wastewater treatment method comprises the following steps: A. regulating water quality; B. removing suspended matters and organic pollutants; C. removing organic matters; D. removing nitrogen and phosphorus: the wastewater treated by the HA-UASB pool enters an HA-TNP pool, nitrogen and phosphorus in the wastewater are removed, and the wastewater after the nitrogen and the phosphorus are removed enters a coagulating sedimentation pool; E. and (3) coagulation treatment: PAC and PAM are added into the coagulating sedimentation tank, suspended matters and residual phosphate in water are removed, treated water enters a reuse water tank for temporary storage, most of water in the reuse water tank is recycled to greening water or production water in a factory, and the redundant water can reach the standard and be discharged; F. sludge treatment; the method is simple, easy to operate, strong in universality, suitable for treating gelatin wastewater produced by various raw materials and various gelatin making processes, good in impact resistance, good in effect, low in operation cost and remarkable in social and economic benefits.
Description
Technical Field
The invention relates to wastewater treatment, in particular to a general gelatin wastewater treatment method.
Background
The gelatin has higher application value, so that the gelatin industry is rapidly developed, and the preparation methods of the gelatin are generally divided into acid gelatin, alkali gelatin and enzyme gelatin, wherein the alkali gelatin is the most commonly adopted process.
The water consumption is huge in the gelatin production process, so that a large amount of production wastewater is inevitably generated, thereby causing environmental pollution. In particular to alkaline waste water containing high calcium and high organic matters, which is discharged from an ash leaching section in the bone gelatin production process, and seriously pollutes the surrounding environment. The skin gelatin is prepared from fresh Corii Sus Domestica, carnis bovis Seu Bubali salt edge skin, carnis Sus Domestica (sheep) salt edge skin, and Carnis bovis Seu Bubali two-layer skin. The waste water in the production process mainly comes from raw material rinse water, dehairing and degreasing, pickling, neutralization, glue making, ion exchange regeneration waste water, equipment pipeline floor flushing and the like. The generated waste water contains a large amount of soluble proteins, including a large amount of colloid, grease, organic particles, suspension and emulsion, and is difficult to naturally settle and clarify in alkaline medium. The waste water from the production of the skin gelatin has the following characteristics:
1) Because the raw materials produced by each manufacturer have large difference, the water quality of the wastewater of each gelatin manufacturer has large variation and large fluctuation, for example, when fresh pigskin is taken as a raw material, the wastewater is acidic, and when salt-edge skin is taken as a raw material, the wastewater is alkaline, so that the difficulty for regulating the pH value of wastewater treatment is increased;
2) When salt edge skin is used as a raw material, dehairing treatment is needed, and a certain amount of sulfur-containing and chlorine-containing wastewater is contained;
3) When bone is used as a raw material, a certain amount of calcium-containing wastewater is contained;
4) The pH value of the wastewater generated by different production process sections is different;
5) The sewage contains a large amount of soluble protein, fat and other organic matters on the raw skin;
6) High suspended matter concentration, easy decay, large sludge production amount and suspended solid concentration in sewage reaching thousands of milligrams/liter.
Most of the prior art aims at treating certain gelatin wastewater, has poor universality, narrow application range, relatively complex process, larger dosage, higher operation cost, poor practical effect and poor impact resistance, and is easy to exceed standard once the quality of the wastewater changes, so how to design a general treatment method for different gelatin wastewater is a technical problem to be solved.
Disclosure of Invention
Aiming at the situation, the invention aims to overcome the defects of the prior art and provide a general gelatin wastewater treatment method which can effectively solve the problems of narrow application range, poor effect and poor impact resistance of the existing gelatin wastewater treatment method.
In order to achieve the above purpose, the technical scheme of the invention is that a general gelatin wastewater treatment method comprises the following steps:
A. and (3) water quality adjustment: removing larger suspended matters, floaters, fibrous matters and solid particulate matters in the wastewater by passing the comprehensive wastewater through a grid, enabling the treated wastewater to enter an adjusting tank to uniform water quality and water quantity, and adjusting the pH value of the wastewater to be 6-9;
B. removing suspended matters and organic pollutants: adding the wastewater treated by the regulating tank into an air floatation tank, adding 20-100mg/L PAC and 1-3mg/L PAM into the air floatation tank, removing suspended matters in the wastewater, adding the treated wastewater into a HADC reactor, removing part of organic pollutants and salts in the wastewater, and simultaneously removing part of ammonia nitrogen;
C. removing organic matters: the wastewater treated by the HADC reactor enters an HA-UASB pool, activated sludge with hydrolytic acidification bacteria, methanogenic bacteria, nitrosation bacteria and anaerobic ammonia oxidation bacteria is added into the HA-UASB pool, most of organic matters are removed through hydrolytic acidification and methanogenesis, meanwhile, the nondegradable macromolecular organic matters are converted and degraded into micromolecular organic matters, meanwhile, nitrosation bacteria in a micro-aeration solid-liquid separation area convert ammonia nitrogen into nitrite, the nitrite flows back to a flowing sludge bed and a second reaction area to be a suspended sludge area, and nitrogen is generated by the anaerobic ammonia oxidation bacteria together with the ammonia nitrogen, so that partial denitrification is realized;
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;
D. removing nitrogen and phosphorus: the wastewater treated by the HA-UASB pool enters an HA-TNP pool, nitrogen and phosphorus in the wastewater are removed, and the wastewater after the nitrogen and the phosphorus are removed enters a coagulating sedimentation pool;
E. and (3) coagulation treatment: PAC and PAM are added into the coagulating sedimentation tank, the adding amount of PAC is 20-50mg/L, the adding amount of PAM is 1-3mg/L, suspended matters and residual phosphate in water are removed, treated effluent enters a recycling water tank for temporary storage, most of water in the recycling water tank is recycled to greening water or production water in a factory, and the redundant water can reach the standard for discharge;
F. sludge treatment: the sludge in the air floatation tank, the HADC reactor, the HA-UASB tank, the HA-TNP tank and the coagulating sedimentation tank is discharged into a sludge concentration tank through a sludge outlet, is concentrated in the sludge concentration tank, and is sent to a dehydrator for dehydration, and the dry sludge is transported and disposed.
The method is simple, easy to operate, strong in universality, suitable for treating gelatin wastewater produced by various raw materials and various gelatin making processes, good in impact resistance, good in effect, low in operation cost and remarkable in social and economic benefits.
Drawings
FIG. 1 is a block diagram of the process equipment of the present invention.
FIG. 2 is a schematic diagram of the structure of the HA-UASB cell of the present invention.
FIG. 3 is a schematic diagram of the structure of the HADC reactor of the present invention.
FIG. 4 is a schematic view of the structure of the HA-TNP pool of the present invention.
Fig. 5 is a cross-sectional view taken along line A-A in fig. 4 in accordance with the present invention.
Fig. 6 is a schematic view of the structure of the regulating reservoir of 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 invention, when used in particular, is illustrated by the following examples in conjunction with the accompanying figures.
A general gelatin wastewater treatment method comprises the following steps:
A. and (3) water quality adjustment: the comprehensive wastewater passes through a grid 1, larger suspended matters, floaters, fibrous matters and solid particulate matters in the wastewater are removed, the treated wastewater enters an adjusting tank 2 to uniform water quality and water quantity, and the pH value of the wastewater is adjusted to be 6-9;
B. removing suspended matters and organic pollutants: the wastewater treated by the regulating tank 2 enters an air floatation tank 3, 20-100mg/L PAC and 1-3mg/L PAM are added into the air floatation tank 3 to remove suspended matters in the wastewater, the treated wastewater enters a HADC reactor 4 to remove organic pollutants and salts in the wastewater, and meanwhile, part of ammonia nitrogen is removed;
C. removing organic matters: the wastewater treated by the HADC reactor 4 enters an HA-UASB pool 5, activated sludge with hydrolytic acidification bacteria, methanogenic bacteria strains, nitrosation bacteria and anaerobic ammonia oxidation bacteria is added into the HA-UASB pool 5, most of organic matters are removed through hydrolytic acidification and methanogenesis, meanwhile, the nondegradable macromolecular organic matters are converted and degraded into micromolecular organic matters, meanwhile, the nitrosation bacteria in a micro-aeration solid-liquid separation area 503 convert ammonia nitrogen into nitrite, and when the nitrite flows back to a flowing sludge bed 501 and a second reaction area to be a suspended sludge area 502 (pure anaerobic area), nitrogen is generated by the anaerobic ammonia oxidation bacteria together with the ammonia nitrogen, so that partial denitrification is realized;
the HADC reactor 4 comprises an electrochemical reaction zone 401, a flocculation reaction zone 402 and a sedimentation zone 403 which are sequentially communicated, wherein the effluent of the air floatation tank 3 enters the electrochemical reaction zone 401, and under the condition of electrifying, organic pollutants are separatedOxidative degradation, partial ammonia nitrogen is oxidized into nitrogen, nitrite and nitrate, high-valence or low-valence metal cations in the wastewater are directly reduced into low-valence cations or metal precipitates at the cathode by electrons, the anode loses electrons to form metal cations after direct current is applied to the anode, and OH in the flocculation reaction zone 402 and the solution - Combining to generate a flocculation group with high activity, adsorbing pollutants in the wastewater, and co-precipitating in a precipitation area 403 to remove the pollutants;
the HA-UASB pool 5 is composed of 3 reaction areas from bottom to top, the first reaction area is a flowing sludge bed 501 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 502, 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, further removes organic matters in water, and simultaneously carries out anaerobic ammonia oxidation denitrification reaction; the third reaction area is a micro-aeration solid-liquid separation area 503, a micro-aeration device is arranged at the lower part of a three-phase separator in the micro-aeration solid-liquid separation area 503, nitrosations are mainly enriched, organic matters in water are further removed, nitrosation reaction is performed simultaneously, the sludge concentration of a flowing sludge bed 501 is 15000-25000mg/L, the sludge concentration of a suspended sludge area 502 is 10000-15000mg/L, the sludge concentration of the micro-aeration solid-liquid separation area 503 is 5000-10000mg/L, and waste water converts difficult-degradation macromolecular organic matters into biodegradable micromolecular organic matters in the flowing sludge bed 501 and simultaneously removes part of organic matters; further removing organic matters in water in a suspended sludge area 502, accelerating sludge backflow to a flowing sludge bed 501 in a micro-aeration solid-liquid separation area 503 through air stirring, and enabling the treated wastewater to enter an HA-TNP pool 6;
D. removing nitrogen and phosphorus: the wastewater treated by the HA-UASB pool 5 enters an HA-TNP pool 6, nitrogen and phosphorus in the wastewater are removed, and the wastewater after the nitrogen and the phosphorus are removed enters a coagulating sedimentation pool 7;
the HA-TNP pool 6 is of a primary-secondary tank partition structure, the inner ring is sequentially provided with a phosphorus release area 602, a first denitrification area 604, a second denitrification area 606 and a third denitrification area 601, the outside of the phosphorus release area 602, the outside of the first denitrification area 604, the outside of the second denitrification area 606 and the outside of the third denitrification area 601 are respectively corresponding to the outside of the first nitrification area 603, the outside of the second nitrification area 605, the outside of the third nitrification area 607 and the outside of the precipitation area 608 of the outer ring, the wastewater treated by the HA-UASB pool 5 enters the third denitrification area 601, sludge in the precipitation area 608 flows back to the third denitrification area 601, and denitrifying bacteria in the returned sludge utilize carbon sources in the inlet water to denitrify nitrate remained in the returned sludge into nitrogen to be discharged out of the water body, so that 1-level denitrification is realized; the mixed solution in the third denitrification region 601 enters a phosphorus release region 602, phosphorus accumulating bacteria in sludge fully release phosphorus under anaerobic conditions and carbon source sufficiency conditions and synthesize carbon sources to be stored in cells, wastewater treated in the phosphorus release region 602 enters a first nitrification region 603 from the beginning, under aerobic conditions, nitrosation flora and nitrifying flora convert ammonia nitrogen in the wastewater into nitrate or nitrite to realize a 1-level ammonia nitrogen removal effect, and meanwhile, phosphorus accumulating bacteria utilize an excessive amount of internal carbon sources to absorb phosphorus and store in cells under aerobic conditions to realize transfer of phosphorus in the wastewater from water to microorganisms, and meanwhile, partial heterotrophic flora in the sludge carries out degradation of organic matters; the wastewater treated in the first nitrification region 603 enters a first denitrification region 604, and denitrifying bacteria in the sludge denitrifies nitrate generated in the first nitrification region 603 into nitrogen by using a carbon source in the water and discharges the nitrogen out of the water body to realize 2-stage denitrification; the wastewater treated in the first denitrification region 604 enters a second nitrification region 605, and under the aerobic condition, nitrosations and nitrifying bacteria groups convert part of ammonia nitrogen in the wastewater into nitrate or nitrite to realize the 2-level ammonia nitrogen removal effect, and meanwhile, part of heterotrophic bacteria in sludge carry out the degradation effect of organic matters; the wastewater treated in the second nitrification zone 605 enters a second denitrification zone 606, and denitrifying bacteria in the sludge denitrifies partial nitrate generated in the second nitrification zone 605 into nitrogen by using a carbon source in the water and discharges the nitrogen out of the water body to realize 3-stage denitrification; the wastewater treated in the second denitrification region 606 enters a third nitrification region 607, and under the aerobic condition, nitrosation flora and nitrifying flora can convert part of ammonia nitrogen in the wastewater into nitrate or nitrite to realize the 3-level ammonia nitrogen removal effect, and meanwhile, part of heterotrophic flora in sludge can degrade organic matters; the wastewater treated in the third nitrification region 607 enters a sedimentation region 608, sludge in the sedimentation region 608 sinks into a mud bucket and flows back to the third denitrification region 601, the amount of the returned sludge is 3-5 times of the water inflow of the third denitrification region 601, and the supernatant enters a coagulating sedimentation tank 7 through a water outlet;
E. and (3) coagulation treatment: PAC and PAM are added into the coagulating sedimentation tank 7, the adding amount of PAC is 20-50mg/L, the adding amount of PAM is 1-3mg/L, suspended matters and residual phosphate in water are removed, treated water enters the recycling water tank 8 for temporary storage, most of water in the recycling water tank 8 is recycled to greening water or production water in a factory, and the redundant water can reach the standard and be discharged;
F. sludge treatment: the sludge in the air floatation tank 3, the HADC reactor 4, the HA-UASB tank 5, the HA-TNP tank 6 and the coagulating sedimentation tank 7 is discharged into a sludge concentration tank 9 through a sludge outlet, concentrated in the sludge concentration tank 9, and then sent to a dehydrator 10 for dehydration, and the dry sludge is transported to be disposed.
Wherein:
(1) Grid 1: the comprehensive wastewater passes through the grid canal, and larger suspended matters, floaters, fiber matters and solid particulate matters in the wastewater are removed under the interception effect of the mechanical grid, so that the normal operation of the subsequent treatment structure is ensured, and the treatment load of the subsequent treatment structure is reduced.
(2) And (2) an adjusting tank: a submersible stirrer, an automatic pH adjusting system and a lifting system are arranged in the adjusting tank; the submersible stirrer is used for stirring and mixing the wastewater, adjusting the water quantity and the water quality of the wastewater, and ensuring the stable operation of the subsequent treatment process; the pH automatic regulating system mainly comprises an online pH meter and an acid-base dosing device, wherein the first tank body with the advanced waste water of different gelatin procedures is neutralized and regulated by utilizing acid and alkali of the first tank body, and then the first tank body is fed into the second tank body, and if the pH value of the first tank body still deviates from 6-9, dosing is automatically controlled to be carried out to regulate the pH value to be within a range; and a lifting pump is arranged in the second tank body and used for lifting wastewater to the air floatation tank, and the lifting pump is provided with a liquid level meter to automatically control the water pump to start and stop.
(3) And (3) an air floatation tank: the air floatation tank adopts integrated complete carbon steel equipment, and comprises a carbon steel tank body, a gas dissolving system, a slag scraping system, a circulating system, a dosing system, a stirring system, a control system and the like; the gelatin wastewater contains a large amount of suspended matters and grease, air can be compressed into the wastewater under a high pressure condition through an air dissolving system, the compressed air in the wastewater can be released from the wastewater in the form of tiny bubbles under normal pressure, the bubbles can be combined with SS and oil in the water to form a floating slag layer on the water surface in the floating process, the floating slag layer is scraped to a slag collecting tank by a slag scraper and discharged to a sludge concentration tank, the effects of removing floating oil scum and part of organic matters are realized, the subsequent treatment load is reduced, the wastewater is more suitable for subsequent biochemical treatment, and PAC and PAM are correspondingly added according to the oil and other suspended matters contained in the wastewater so as to improve the air floatation effect.
(4) HADC reactor 4: the device mainly comprises an electrochemical reaction area, a flocculation reaction area and a precipitation area, wherein the electrochemical reaction area mainly comprises a direct-current stabilized power supply, a cathode plate and an anode plate (cathode plate titanium plate, anode adopts an aluminum plate) and an air scrubbing and mixing system; the flocculation reaction zone mainly comprises a stirrer and a flocculant dosing system; the sedimentation zone mainly comprises water inlet distribution, inclined pipe filling and water outlet weirs. The air-floating effluent firstly enters an electrochemical reaction zone of the HADC reactor, under the condition of electrifying, direct oxidation reaction and indirect oxidation reaction are carried out on the anode plate side, organic pollutants can be oxidized and degraded, partial ammonia nitrogen can be oxidized into nitrogen, nitrite and nitrate, direct reduction reaction and indirect reduction reaction are carried out on the cathode plate side, and high-valence or low-valence metal cations in the wastewater are directly reduced into low-valence cations or metal precipitates at the cathode. After the anode aluminum plate is electrified with direct current, the anode loses electrons to form metal cation Al 3+ The flocculation reaction zone combines with OH-in the solution to generate high-activity flocculation groups, the adsorption capacity is extremely strong, the flocculation effect is superior to that of a common flocculant, and the flocculation effect is stronger in adsorption bridging, net capturing and rolling sweeping and the like by assisting with a coagulant aid PAM, so that pollutants in the wastewater can be adsorbed and co-precipitated in a precipitation zone to be removed. Therefore, the HADC reactor not only can remove organic pollutants, but also can remove salts such as sulfate, calcium salt, chloride ions, nitrogen and phosphorus, and the like, so that the biodegradability of the gelatin wastewater is greatly enhanced.
(5) HA-UASB pool 5: the interior of the reactor is divided into 3 reaction areas: the first reaction area is a flowing sludge bed, is enriched with hydrolytic acidification bacteria and partial methanogens, mainly converts the refractory macromolecular organic matters in the wastewater into biodegradable micromolecular organic matters, and simultaneously removes partial organic matters; the second reaction area is a suspended sludge area, the sludge in the reaction area is lower than that in the flowing sludge bed area, and mainly enriches methanogens and further removes organic matters in water; the third reaction area is a micro-aeration solid-liquid separation area, a three-phase separator is arranged in the area, a micro-aeration device is arranged at the lower part of the three-phase separator, and the sludge is accelerated to flow back to the bottom through air stirring. The micro-aeration arrangement does not interfere with the anaerobic environment at the bottom of the HA-UASB reactor.
(6) HA-TNP pool 6: the integrated denitrification and dephosphorization reactor is of a primary-secondary tank partition structure and is divided into a phosphorus release region, a first nitrification region, a first denitrification region, a second nitrification region, a second denitrification region, a third nitrification region, a third denitrification region and a precipitation region, wherein the phosphorus release region and 3 denitrification regions are provided with stirring mixers, the 3 denitrification regions are provided with a blast aeration system, and the precipitation region is provided with a sludge discharge pump, a water inlet pipeline, a water outlet pipeline and a sludge reflux system. The HA-UASB effluent automatically flows into a third nitrification zone, and simultaneously a large amount of sludge is refluxed from the bottom of a sedimentation tank to the third nitrification zone, and denitrification bacteria in the sludge denitrifies partial nitrate remained in the reflux sludge into nitrogen gas by utilizing a carbon source in the influent water to discharge the nitrogen gas into a water body, so that 1-stage denitrification is realized; the mixed solution in the third denitrification zone automatically flows into the phosphorus release zone from the lower part, and as nitrate is removed, phosphorus accumulating bacteria in the sludge can fully release phosphorus and synthesize a carbon source to store in a cell body under anaerobic conditions and carbon source sufficient conditions; the mixed solution in the phosphorus release zone automatically flows into a first nitrifying zone from the upper part, under the aerobic condition, nitrosation flora and nitrifying flora can convert ammonia nitrogen in gelatin wastewater into nitrate or nitrite to realize the 1-level ammonia nitrogen removal effect, meanwhile, phosphorus accumulating bacteria utilizes an internal carbon source to excessively absorb phosphorus and store the phosphorus in cells under the aerobic condition to realize the transfer of phosphorus in the gelatin wastewater from water to microorganisms, and meanwhile, partial heterotrophic flora in sludge also performs the degradation effect of organic matters; the mixed liquor of the first nitrification zone automatically flows to a first denitrification zone from the lower part, and part of nitrate and nitrite exist due to no aeration, the zone is an anoxic zone, phosphorus release of phosphorus accumulating bacteria in the zone can be avoided, and denitrification bacteria in sludge utilize a carbon source in water to denitrify part of nitrate generated in the first nitrification zone into nitrogen to be discharged out of a water body, so that 2-stage denitrification is realized; the mixed solution of the first denitrification zone automatically flows into the second nitrification zone from the upper part, and under the aerobic condition, the nitrosation flora and the nitrifying flora can convert part of ammonia nitrogen in the gelatin wastewater into nitrate or nitrite to realize the 2-level ammonia nitrogen removal effect, and meanwhile, part of heterotrophic flora in the sludge also carries out the degradation effect of organic matters; the mixed liquor of the second nitrification zone automatically flows to a second denitrification zone from the lower part, and part of nitrate and nitrite exist due to no aeration, the zone is an anoxic zone, phosphorus release of phosphorus accumulating bacteria in the zone can be avoided, and denitrification bacteria in sludge utilize a carbon source in water to denitrify part of nitrate generated in the second nitrification zone into nitrogen to be discharged out of a water body, so that 3-stage denitrification is realized; the mixed solution of the second denitrification zone automatically flows into a third nitrification zone from the upper part, and under the aerobic condition, the nitrosation flora and the nitrifying flora can convert part of ammonia nitrogen in the gelatin wastewater into nitrate or nitrite to realize the 3-level ammonia nitrogen removal effect, and meanwhile, part of heterotrophic flora in the sludge also carries out the degradation effect of organic matters; the mixed liquid of the third nitrification region enters the upper side of a sludge hopper at the middle and lower part of the sedimentation region, a water distribution pipe is a perforated pipe with holes at the upper and lower sides, a mud-water mixture enters the sedimentation region from the water distribution hole, heavy-density sludge sinks into the sludge hopper under the action of gravity, supernatant enters a water outlet weir for discharging, a sludge reflux region is arranged at the bottom of the sludge hopper, the liquid level of the reflux region is increased by utilizing the action of air lifting and automatically flows into the third denitrification region, and the reflux sludge amount is generally controlled to be 3-5 times of the water inlet flow in order to ensure the denitrification and dephosphorization effects; to ensure the dephosphorization effect of the reactor, excess sludge must be discharged periodically to achieve the purpose of removing phosphorus from the reactor.
(7) And (3) a coagulating sedimentation tank 7: PAC and PAM are added into a coagulating sedimentation tank to remove suspended matters and residual phosphate in water, the residual suspended matters in biochemical treatment effluent are biological floccules with particle diameters ranging from a few millimeters to 10 mu m and non-coagulated colloid particles, most of the particles are organic, 50% -80% of BOD value of secondary treatment effluent is derived from the particles, the particles are very necessary to improve the clarity and stability of the secondary treatment effluent, and TP indexes in sewage can be treated to locally specified emission standards by a chemical dephosphorization method.
(8) And (3) a reuse water pool 8: after the wastewater is subjected to coagulating sedimentation treatment, the wastewater meets the discharge requirement, enters a recycling water tank for storage, can be partially recycled for greening the factory, and can be partially recycled for primary cleaning of raw materials in a production workshop, and the redundant water is discharged after reaching the standard.
(9) Sludge concentration tank 9: sludge generated in the treatment processes of the air floatation tank, the HADC reactor, the HA-UASB tank, the HA-TNP tank and the coagulating sedimentation tank is periodically discharged into a sludge concentration tank to be concentrated by gravity, and the concentrated sludge is periodically dehydrated by a sludge dehydrator 10 and then is timely and externally transported to be entrusted with qualification unit treatment.
The method of the invention is simple, the operation is simple, the universality is strong, compared with the prior art, the invention has the following advantages:
(1) The regulating tank is divided into a large partition area and a small partition area, waste water generated at different stages in the gelatin production process firstly enters the large partition area, and the pH value of raw water can be fully utilized for preneutralization, so that the medicament is saved, and meanwhile, the automatic pH adjustment is carried out in the small partition area, so that the waste water is ensured to be in a neutral area, and the subsequent treatment effect is ensured;
(2) The HADC reactor not only can realize the oxidative degradation of macromolecular organic matters in the gelatin wastewater, but also can remove salts such as sulfate, calcium salt, chloride ions, nitrogen and phosphorus, and the like, thereby greatly reducing the inhibition of harmful substances on microorganisms and increasing the biodegradability of the wastewater;
(3) The HA-UASB reactor degrades most of macromolecular organic matters into micromolecular organic matters, and simultaneously converts most of organic matters into biogas to be discharged, so that the organic load of subsequent biochemistry is greatly reduced, and the yield of biochemical sludge is reduced by 60-80%;
(4) The HA-TNP reactor fully utilizes the residual carbon source in the wastewater to realize denitrification and dephosphorization, saves the occupied area and energy consumption compared with the traditional A2O and other processes, and effectively avoids the defect that denitrification floating mud occurs in dead areas of sludge at the bottom of the traditional sedimentation tank by adopting a method for refluxing a large amount of sludge from the sedimentation area;
(5) The invention is suitable for treating gelatin wastewater produced by various raw materials and various glue making processes, has good impact resistance, good effect and low operation cost, and has remarkable social and economic benefits.
Claims (3)
1. The universal gelatin wastewater treatment method is characterized by comprising the following steps of:
A. and (3) water quality adjustment: the comprehensive wastewater passes through a grid (1) to remove larger suspended matters, floaters, fibrous matters and solid particulate matters in the wastewater, the treated wastewater enters an adjusting tank (2) to uniform water quality and water quantity, and the pH value of the wastewater is adjusted to be 6-9;
B. removing suspended matters and organic pollutants: the wastewater treated by the regulating tank (2) enters an air floatation tank (3), 20-100mg/L PAC and 1-3mg/L PAM are added into the air floatation tank (3), suspended matters in the wastewater are removed, the treated wastewater enters a HADC reactor (4), part of organic pollutants and salts in the wastewater are removed, and part of ammonia nitrogen is removed;
C. removing organic matters: the wastewater treated by the HADC reactor (4) enters an HA-UASB pool (5), activated sludge with hydrolytic acidification bacteria, methanogenic bacteria strains, nitrosation bacteria and anaerobic ammonia oxidation bacteria is added into the HA-UASB pool (5), most of organic matters are removed through hydrolytic acidification and methanogenesis, meanwhile, the nondegradable macromolecular organic matters are converted and degraded into micromolecular organic matters, meanwhile, the nitrosation bacteria in a micro-aeration solid-liquid separation area (503) convert ammonia nitrogen into nitrite, and the nitrite flows back to a flowing sludge bed (501) and a second reaction area (502) to be utilized by the anaerobic ammonia oxidation bacteria together with the ammonia nitrogen to generate nitrogen, so that partial denitrification is realized;
the HA-UASB pool (5) is composed of 3 reaction areas from bottom to top, the first reaction area is a flowing sludge bed (501) at the lower part, the second reaction area is a suspended sludge area (502), the third reaction area is a micro-aeration solid-liquid separation area (503), and a micro-aeration device is arranged at the lower part of a three-phase separator in the micro-aeration solid-liquid separation area (503);
D. removing nitrogen and phosphorus: the wastewater treated by the HA-UASB pool (5) enters an HA-TNP pool (6) to remove nitrogen and phosphorus in the wastewater, and the wastewater after removing the nitrogen and the phosphorus enters a coagulating sedimentation pool (7);
E. and (3) coagulation treatment: PAC and PAM are added into a coagulating sedimentation tank (7), the adding amount of PAC is 20-50mg/L, the adding amount of PAM is 1-3mg/L, suspended matters and residual phosphate in water are removed, treated water enters a recycling water tank (8) for temporary storage, most of water in the recycling water tank (8) is recycled into greening water or production water in a factory, and the redundant water is discharged after reaching standards;
F. sludge treatment: sludge in the air floatation tank (3), the HADC reactor (4), the HA-UASB tank (5), the HA-TNP tank (6) and the coagulating sedimentation tank (7) is discharged into a sludge concentration tank (9) through a sludge outlet, concentrated in the sludge concentration tank (9), and then sent to a dehydrator (10) for dehydration, and dry sludge is transported and treated outwards;
the HA-TNP pool (6) is of a primary-secondary tank partition structure, the inner ring is sequentially provided with a phosphorus release region (602), a first denitrification region (604), a second denitrification region (606) and a third denitrification region (601), the outsides of the phosphorus release region (602), the first denitrification region (604), the second denitrification region (606) and the third denitrification region (601) are respectively corresponding to the first nitrification region (603), the second nitrification region (605), the third nitrification region (607) and a sedimentation region (608) of the outer ring, waste water treated by the HA-UASB pool (5) enters the third denitrification region (601), sludge in the sedimentation region (608) flows back to the third denitrification region (601), and denitrifying bacteria in the returned sludge utilizes a carbon source in the inlet water to denitrify nitrate remained in the returned sludge into nitrogen to be discharged out of the water body, so that primary denitrification is realized; the mixed solution in the third denitrification zone (601) enters a phosphorus release zone (602), phosphorus accumulating bacteria in sludge fully release phosphorus and synthesize a carbon source to be stored in a cell body under anaerobic conditions and carbon source sufficient conditions, wastewater treated by the phosphorus release zone (602) enters a first nitrification zone (603), nitrosation flora and nitrifying flora convert ammonia nitrogen in the wastewater into nitrate or nitrite under aerobic conditions, primary ammonia nitrogen removal is realized, meanwhile, phosphorus accumulating bacteria absorb phosphorus excessively by utilizing an internal carbon source and store the phosphorus in the cell body under aerobic conditions, transfer of phosphorus in the wastewater from a water body to the microorganism body is realized, and partial heterotrophic flora in the sludge is subjected to degradation of organic matters; wastewater treated in the first nitrification region (603) enters a first denitrification region (604), and denitrifying bacteria in sludge denitrifies nitrate generated in the first nitrification region (603) into nitrogen by using a carbon source in the water and discharges the nitrogen out of a water body to realize secondary denitrification; the wastewater treated by the first denitrification region (604) enters a second nitrification region (605), and under the aerobic condition, nitrosation flora and nitrifying flora convert part of ammonia nitrogen in the wastewater into nitrate or nitrite to realize secondary ammonia nitrogen removal effect, and meanwhile, part of heterotrophic flora in sludge is degraded by organic matters; wastewater treated in the second nitrification region (605) enters a second denitrification region (606), and denitrifying bacteria in the sludge denitrifies partial nitrate generated in the second nitrification region (605) into nitrogen by using a carbon source in the water and discharges the nitrogen out of the water body, so that three-stage denitrification is realized; the wastewater treated by the second denitrification region (606) enters a third nitrification region (607), and under the aerobic condition, nitrosation flora and nitrifying flora convert part of ammonia nitrogen in the wastewater into nitrate or nitrite, so that the three-stage ammonia nitrogen removal effect is realized, and meanwhile, part of heterotrophic flora in sludge is degraded by organic matters; the wastewater treated by the third nitrification region (607) enters a sedimentation region (608), sludge in the sedimentation region (608) sinks into a mud bucket and flows back to the third denitrification region (601), the amount of the returned sludge is 3-5 times of the water inflow of the third denitrification region (601), and the supernatant enters a coagulating sedimentation tank (7) through a water outlet;
the HADC reactor (4) comprises an electrochemical reaction area (401), a flocculation reaction area (402) and a sedimentation area (403) which are sequentially communicated, wherein the effluent of the air floatation pond (3) enters the electrochemical reaction area (401), under the condition of electrifying, organic pollutants are oxidized and degraded, partial ammonia nitrogen is oxidized into nitrogen, nitrite and nitrate, high-valence or low-valence metal cations in the wastewater are directly reduced into low-valence cations or metal sediments at a cathode by electrons, the anode loses electrons after direct current is applied to the anode, metal cations are formed, and the wastewater is flocculatedCoagulation reaction zone (402) and OH in solution - The high-activity flocculation groups are combined to adsorb pollutants in the wastewater and coprecipitate in a precipitation zone (403) to remove the pollutants.
2. The general gelatin wastewater treatment method according to claim 1, wherein the regulating tank (2) comprises a first tank body (201) and a second tank body (202), the first tank body (201) is larger than the second tank body (202), a stirring device (203) is arranged in the first tank body (201), a lifting pump (204) and a pH automatic regulating system are arranged in the second tank body (202), wastewater filtered by the grid (1) enters the second tank body (202) after being neutralized and regulated by acid and alkali of the first tank body (201), the pH of the wastewater is detected to be not 6-9 by the pH automatic regulating system, the pH=6-9 of the wastewater is regulated by adding medicine, and then the wastewater enters the air floatation tank (3) by the lifting pump (204).
3. The general gelatin wastewater treatment method according to claim 1, wherein the sludge concentration of the flowing sludge bed (501) is 15000-25000mg/L, the sludge concentration of the suspended sludge zone (502) is 10000-15000mg/L, the sludge concentration of the micro-aeration solid-liquid separation zone (503) is 5000-10000mg/L, and the wastewater converts the refractory macromolecular organic matters into the biodegradable micromolecular organic matters in the flowing sludge bed (501) and simultaneously removes part of the organic matters; organic matters in water are further removed in a suspended sludge area (502), sludge is accelerated to flow back to a flowing sludge bed (501) through air stirring in a micro-aeration solid-liquid separation area (503), and treated wastewater enters an HA-TNP pool (6).
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