CN114409183A - Universal gelatin wastewater treatment method - Google Patents
Universal gelatin wastewater treatment method Download PDFInfo
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- CN114409183A CN114409183A CN202111627134.2A CN202111627134A CN114409183A CN 114409183 A CN114409183 A CN 114409183A CN 202111627134 A CN202111627134 A CN 202111627134A CN 114409183 A CN114409183 A CN 114409183A
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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 15
- 239000002351 wastewater Substances 0.000 claims abstract description 124
- 239000010802 sludge Substances 0.000 claims abstract description 111
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 83
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 65
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims abstract description 47
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- 238000004062 sedimentation Methods 0.000 claims abstract description 27
- 238000009280 upflow anaerobic sludge blanket technology Methods 0.000 claims abstract description 24
- 230000000694 effects Effects 0.000 claims abstract description 22
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- 238000003860 storage Methods 0.000 claims abstract description 5
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- 238000006243 chemical reaction Methods 0.000 claims description 31
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- 229910002651 NO3 Inorganic materials 0.000 claims description 23
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- 238000005273 aeration Methods 0.000 claims description 22
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 22
- 239000007788 liquid Substances 0.000 claims description 22
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 19
- 229910052799 carbon Inorganic materials 0.000 claims description 19
- 238000000926 separation method Methods 0.000 claims description 14
- 239000000126 substance Substances 0.000 claims description 13
- 150000001768 cations Chemical class 0.000 claims description 12
- 229910052751 metal Inorganic materials 0.000 claims description 12
- 239000002184 metal Substances 0.000 claims description 12
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- 230000016615 flocculation Effects 0.000 claims description 10
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- 239000002245 particle Substances 0.000 claims description 9
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 claims description 8
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- 238000006481 deamination reaction Methods 0.000 claims description 8
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- 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
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- 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
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- 229910001873 dinitrogen Inorganic materials 0.000 description 1
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- 238000011069 regeneration method Methods 0.000 description 1
- 239000008237 rinsing water Substances 0.000 description 1
- 238000005201 scrubbing Methods 0.000 description 1
- -1 skin Chemical class 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 1
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- 229910052719 titanium Inorganic materials 0.000 description 1
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Images
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
- C02F1/24—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. adjusting the 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 tank enters an HA-TNP tank, nitrogen and phosphorus in the wastewater are removed, and the wastewater after the nitrogen and phosphorus are removed enters a coagulating sedimentation tank; E. coagulation treatment: PAC and PAM are added into a coagulative precipitation tank to remove suspended matters and residual phosphate in water, treated effluent enters a reuse water tank for temporary storage, most of water in the reuse water tank is reused for greening water or production water in a plant area, and redundant water can reach the standard and be discharged; F. sludge treatment; the method is simple, easy to operate, high in universality, suitable for treating the gelatin wastewater generated by various glue making processes with various raw materials, 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
Gelatin has a high application value, which makes the gelatin industry rapidly develop, and the preparation methods of gelatin are generally classified into acid gelatin, alkaline gelatin and enzymatic gelatin, wherein alkaline gelatin is the most commonly used process.
The water consumption in the production process of the gelatin is huge, so that the production of a large amount of wastewater is inevitable, and the environmental pollution is caused. In particular, the alkaline waste water containing high calcium and high organic matters discharged from the liming workshop section in the production process of bone gelatin seriously pollutes the surrounding environment. The raw materials for producing the skin gelatin mainly comprise fresh pigskin, cattle salt edge skin, pig (sheep) salt edge skin and cattle double-layer skin. The wastewater in the production process mainly comes from the wastewater of raw material rinsing water, unhairing and degreasing, pickling, neutralizing, glue making, ion exchange regeneration wastewater, equipment pipeline terrace washing and the like. The produced waste water contains a large amount of soluble protein, including a large amount of colloid, grease, organic particles, suspension and emulsion, and the waste water is difficult to naturally settle and clarify in an alkaline medium. The skin gelatin production wastewater has the following characteristics:
1) because the difference of production raw materials of various manufacturers is large, the quality of the wastewater of various gelatin manufacturers is large in change and fluctuation, for example, when fresh pigskin is adopted as the raw material, the wastewater is acidic, and when brine skinning is adopted as the raw material, the wastewater is alkaline, so that the difficulty is increased for adjusting the pH value of the wastewater treatment;
2) when the salt boundary skin is used as a raw material, unhairing treatment is needed, and a certain amount of sulfur-containing and chlorine-containing wastewater is contained;
3) when the bone is used as the 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 organic matters such as soluble protein, fat and the like on the original skin;
6) the suspended solid concentration is high, easy to decay, the sludge production is large, and the suspended solid concentration in the sewage reaches thousands of milligrams per liter.
Most of the prior art is directed at treating a certain gelatin wastewater, and has the disadvantages of poor universality, narrow application range, relatively complex process, large dosage, high operating cost, poor practical effect and poor impact resistance, and once the quality of the wastewater is changed, the wastewater is easy to exceed the standard, so that how to design a universal treatment method for different gelatin wastewater is a technical problem to be solved urgently.
Disclosure of Invention
In view of the above situation, the present invention aims to 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 methods.
In order to achieve the aim, the invention provides a general gelatin wastewater treatment method, which comprises the following steps:
A. water quality regulation: the comprehensive wastewater passes through a grating to remove larger suspended matters, floating matters, fiber substances and solid particle substances in the wastewater, the treated wastewater enters an adjusting tank to homogenize the water quality and water quantity, and the pH =6-9 of the wastewater is adjusted;
B. removing suspended matters and organic pollutants: the wastewater treated by the regulating tank enters an air flotation tank, 20-100mg/L PAC and 1-3mg/L PAM are added into the air flotation tank to remove suspended matters in the wastewater, the treated wastewater enters an HADC reactor to remove partial organic pollutants and salts in the wastewater and simultaneously remove partial ammonia nitrogen;
C. removing organic matters: the wastewater treated by the HADC reactor enters an HA-UASB pool, activated sludge with hydrolytic acidification bacteria, methanogen strains, nitrosobacteria and anaerobic ammonium oxidation bacteria is added into the HA-UASB pool, most organic matters are removed through hydrolytic acidification and methanogenesis, meanwhile, persistent macromolecular organic matters are converted and degraded into micromolecular organic matters, meanwhile, nitrite in a micro-aeration solid-liquid separation zone converts ammonia nitrogen into nitrite, and the nitrite is utilized by the anaerobic ammonium oxidation bacteria together with the ammonia nitrogen when the nitrite flows back to a flowing sludge bed and a second reaction zone is a suspended sludge zone, 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 tank enters an HA-TNP tank, nitrogen and phosphorus in the wastewater are removed, and the wastewater after the nitrogen and phosphorus are removed enters a coagulating sedimentation tank;
E. coagulation treatment: PAC and PAM are added into a coagulative precipitation tank, the dosage of PAC is 20-50mg/L, the dosage of PAM is 1-3mg/L, suspended matters and residual phosphate in water are removed, treated effluent enters a reuse tank for temporary storage, most of water in the reuse tank is reused as greening water or production water in a plant area, and redundant water can reach the standard and is discharged;
F. sludge treatment: and 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, and is concentrated in the sludge concentration tank, then is sent to a dehydrator for dehydration, and the dry sludge is transported and disposed.
The method is simple, easy to operate, high in universality, suitable for treating the gelatin wastewater generated by various glue making processes with various raw materials, 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 HA-UASB pool structure of the present invention.
Fig. 3 is a schematic diagram of the HADC reactor configuration of the present invention.
FIG. 4 is a schematic diagram of the HA-TNP pool structure of the present invention.
Fig. 5 is a sectional view taken along line a-a of fig. 4 in accordance with the present invention.
FIG. 6 is a schematic view of the structure of the conditioning tank of the present invention.
Detailed Description
The following detailed description of the embodiments of the invention is provided in connection with the accompanying drawings and the detailed description.
The invention, when used in particular, is illustrated by the following examples, which are given in conjunction with the accompanying drawings.
A general gelatin wastewater treatment method comprises the following steps:
A. water quality regulation: the comprehensive wastewater passes through the grating 1 to remove larger suspended matters, floating matters, fiber substances and solid particle substances in the wastewater, the treated wastewater enters the regulating tank 2 to homogenize the water quality and water quantity, and the pH =6-9 of the wastewater is regulated;
B. removing suspended matters and organic pollutants: the wastewater treated by the regulating tank 2 enters an air flotation tank 3, 20-100mg/L PAC and 1-3mg/L PAM are added into the air flotation tank 3 to remove suspended matters in the wastewater, and the treated wastewater enters an HADC reactor 4 to remove organic pollutants and salts in the wastewater and remove part of ammonia nitrogen;
C. removing organic matters: the wastewater treated by the HADC reactor 4 enters an HA-UASB pool 5, activated sludge with hydrolytic acidification bacteria, methanogen strains, nitrosobacteria and anaerobic ammonium oxidation bacteria is added into the HA-UASB pool 5, most organic matters are removed through hydrolytic acidification and methanogenesis, meanwhile, refractory macromolecular organic matters are converted and degraded into micromolecular organic matters, meanwhile, the nitrosobacteria in the micro-aeration solid-liquid separation area 503 convert ammonia nitrogen into nitrite, and when the nitrite flows back to the flowing sludge bed 501 and the second reaction area is the suspended sludge area 502 (pure anaerobic area), the nitrite is utilized by the anaerobic ammonium oxidation bacteria together with the ammonia nitrogen to generate nitrogen, so that partial denitrification is realized;
the HADC reactor 4 comprises an electrochemical reaction zone 401, a flocculation reaction zone 402 and a precipitation zone 403 which are communicated in sequence, and the effluent of the air floatation tank 3 enters the electrochemical reaction zone 401, the flocculation reaction zone 402 and the precipitation zone 403In the reaction zone 401, under the condition of electrifying, organic pollutants are oxidized and degraded, part of ammonia nitrogen is oxidized into nitrogen, nitrite and nitrate, high-valence or low-valence metal cations in the wastewater obtain electrons at the cathode and are directly reduced into low-valence cations or metal precipitates, after the anode is electrified with direct current, the anode loses electrons to form metal cations, and the metal cations are flocculated in the flocculation reaction zone 402 and OH in the solution-The pollutants in the wastewater are adsorbed and co-precipitated in a precipitation zone 403 to be removed by combining and generating high-activity flocculation groups;
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, hydrolytic acidification bacteria and part of methanogens are enriched, the non-degradable macromolecular organic matters in the wastewater are mainly converted into biodegradable micromolecular organic matters, and part of the organic matters are removed; the second reaction area is a suspended sludge area 502, the sludge in the reaction area is lower than that in the flowing sludge bed area, and the suspended sludge area is mainly enriched with methanogens and anaerobic ammonium oxidation bacteria, so that organic matters in water are further removed, and meanwhile, anaerobic ammonium oxidation denitrification reaction is carried out; the third reaction area is a micro-aeration solid-liquid separation area 503, the lower part of a three-phase separator in the micro-aeration solid-liquid separation area 503 is provided with a micro-aeration device which is mainly used for enriching nitrosobacteria, further removing organic matters in water and simultaneously carrying out nitrosation reaction, 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 the difficultly-degradable macromolecular organic matters are converted into biodegradable micromolecular organic matters in the wastewater in the flowing sludge bed 501, and meanwhile, part of the organic matters are removed; organic matters in the water are further removed in the suspended sludge zone 502, the sludge is accelerated to flow back to the flowing sludge bed 501 through air agitation in the micro-aeration solid-liquid separation zone 503, and the treated wastewater enters the HA-TNP tank 6;
D. removing nitrogen and phosphorus: the wastewater treated by the HA-UASB tank 5 enters an HA-TNP tank 6, nitrogen and phosphorus in the wastewater are removed, and the wastewater after the nitrogen and the phosphorus are removed enters a coagulative precipitation tank 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 outsides of the phosphorus release area 602, the first denitrification area 604, the second denitrification area 606 and the third denitrification area 601 respectively correspond to the outsides of the first nitrification area 603, the second nitrification area 605, the third nitrification area 607 and the sedimentation area 608 of the outer ring, the wastewater treated by the HA-UASB pool 5 enters the third denitrification area 601, the sludge in the sedimentation area 608 flows back to the third denitrification area 601, the denitrification flora in the return sludge utilizes the carbon source in the inlet water to denitrify the nitrate remaining in the return sludge into nitrogen to be discharged out of the water body, and the 1-level denitrification is realized; the mixed liquid in the third denitrification zone 601 enters a phosphorus release zone 602, phosphorus-accumulating bacteria in sludge fully release phosphorus under anaerobic conditions and sufficient carbon sources and synthesize carbon sources to be stored in cells, the wastewater treated by the phosphorus release zone 602 enters a first nitrification zone 603, nitrite bacteria and nitrifying bacteria convert ammonia nitrogen in the wastewater into nitrate or nitrite under aerobic conditions, and the effect of 1-level deamination and denitrification is realized, meanwhile, the phosphorus-accumulating bacteria excessively absorb phosphorus by using an internal carbon source and store the phosphorus in the cells under aerobic conditions, so that the transfer of phosphorus in the wastewater from a water body to microorganisms is realized, and meanwhile, part of heterotrophic bacteria in the sludge carry out degradation of organic matters; the wastewater treated by the first nitrification zone 603 enters a first denitrification zone 604, and denitrification floras in the sludge utilize carbon sources in the water to denitrify the nitrate generated by the first nitrification zone 603 into nitrogen gas to be discharged out of the water body, so that 2-level denitrification is realized; the wastewater treated by the first denitrification zone 604 enters a second nitrification zone 605, and under aerobic conditions, nitrite bacteria and nitrifying bacteria convert part of ammonia nitrogen in the wastewater into nitrate or nitrite, so that 2-level ammonia nitrogen removal is realized, and meanwhile, part of heterotrophic bacteria in sludge are subjected to organic matter degradation; the wastewater treated by the second nitrification region 605 enters a second denitrification region 606, and denitrification floras in the sludge utilize carbon sources in the water to denitrify part of nitrate generated by the second nitrification region 605 into nitrogen and discharge the nitrogen out of the water body, so that 3-level denitrification is realized; the wastewater treated by the second denitrification zone 606 enters a third nitrification zone 607, under aerobic conditions, part of ammonia nitrogen in the wastewater can be converted into nitrate or nitrite by the nitrifying bacteria group and the nitrifying bacteria group, so that 3-level deamination and denitrification are realized, and meanwhile, part of heterotrophic bacteria group in the sludge is subjected to organic matter degradation; the wastewater treated by the third nitrification zone 607 enters a sedimentation zone 608, sludge in the sedimentation zone 608 sinks into a sludge hopper and flows back to the third denitrification zone 601, the amount of the returned sludge is 3-5 times of the water inlet flow of the third denitrification zone 601, and supernatant enters a coagulating sedimentation tank 7 through a water outlet;
E. coagulation treatment: PAC and PAM are added into the coagulating sedimentation tank 7, the PAC addition amount is 20-50mg/L, the PAM addition amount is 1-3mg/L, suspended matters and residual phosphate in water are removed, treated effluent enters a reuse tank 8 for temporary storage, most of water in the reuse tank 8 is reused as greening water or production water in a plant area, and the excess water can reach the standard and be discharged;
F. sludge treatment: and the sludge in the 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, is concentrated in the sludge concentration tank 9, is sent to a dehydrator 10 for dehydration, and is transported outside for disposal.
Wherein:
(1) and a grid 1: the comprehensive wastewater passes through the grid channel, and under the interception action of the mechanical grid, larger suspended matters, floating matters, fiber substances and solid particle substances in the wastewater are removed, so that the normal operation of a subsequent treatment structure is ensured, and the treatment load of the subsequent treatment structure is reduced.
(2) And (3) adjusting the pool 2: a submersible stirrer, a pH automatic 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 adjusting system mainly comprises an online pH meter and an acid-base dosing device, a first tank body which is used for neutralizing and adjusting advanced waste water of different gelatin procedures by using self acid and base, and then enters a second tank body, and if the pH value of the tank still deviates from 6-9, the pH automatic adjusting system is automatically controlled to dose and adjust the pH value to be within a range; and a lifting pump is arranged in the second tank body, the waste water is lifted to the air floatation tank, and the lifting pump is provided with a liquid level meter to automatically control the start and stop of the water pump.
(3) And (3) floatation tank: the air floatation tank adopts integrated complete carbon steel equipment, and comprises a carbon steel tank body, a dissolved air 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 substances and grease, the air can be compressed and enter the wastewater under the high-pressure condition through the air dissolving system, the compressed air in the wastewater can be released from the wastewater in the form of micro bubbles when the pressure is normal, the compressed air can be combined with SS and oil in the water to be brought to the water surface to form a scum layer in the floating process of the bubbles, the scum layer is scraped to a scum collecting tank by a scum scraping machine and then discharged to a sludge concentration tank, the floating oil scum and partial organic matters are removed, the subsequent treatment load is reduced, the wastewater is more suitable for subsequent biochemical treatment, PAC and PAM are correspondingly added according to the amount of the oil and other suspended substances contained in the wastewater, and the air floatation effect is improved.
(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 voltage power supply, a negative electrode plate (a negative plate titanium plate, and an anode adopts an aluminum plate) and an air scrubbing and mixing system; the flocculation reaction zone mainly comprises a stirrer and a flocculating agent dosing system; the settling zone mainly comprises water inlet and distribution, inclined tube filling and a water outlet weir. The air-float effluent firstly enters an electrochemical reaction zone of the HADC reactor, under the condition of electrification, the anode plate side generates direct oxidation reaction and indirect oxidation reaction, organic pollutants can be oxidized and degraded, part of ammonia nitrogen can also be oxidized into nitrogen, nitrite and nitrate, the cathode plate side generates direct reduction reaction and indirect reduction reaction, and high-valence or low-valence metal cations in the wastewater obtain electrons at the cathode and are directly reduced into low-valence cations or metal precipitates. After the anode aluminum plate is electrified with direct current, the anode loses electrons to form metal cation Al3+The flocculant has strong adsorption capacity and flocculation effect superior to that of common flocculant, and the assistant flocculant PAM has stronger adsorption bridging, net trapping, sweeping and other functions, and can adsorb pollutant in waste water and co-precipitate in the settling area to eliminate pollutant. Therefore, the HADC reactor can not only remove organic pollutants, but also 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 reactor interior was divided into 3 reaction zones: the first reaction area is a flowing sludge bed, is rich in hydrolytic acidification bacteria and part of methanogens, mainly converts the refractory macromolecular organic matters in the wastewater into biodegradable micromolecular organic matters, and simultaneously removes part of the organic matters; the second reaction area is a suspended sludge area, sludge in the reaction area is lower than a flowing sludge bed area, and methanogens are mainly enriched to further remove organic matters in water; the third reaction area is a micro-aeration solid-liquid separation area, a three-phase separator is arranged in the third reaction 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 by air stirring. The micro-aeration setting does not interfere with the anaerobic environment at the bottom of the HA-UASB reactor.
(6) HA-TNP pool 6: the novel integrated nitrogen and phosphorus removal reactor is of a primary-secondary tank partition structure and is divided into a phosphorus release area, a first nitrification area, a first denitrification area, a second nitrification area, a second denitrification area, a third nitrification area, a third denitrification area and a settling area, wherein the phosphorus release area and the 3 denitrification areas are provided with stirring mixers, the 3 nitrification areas are provided with blast aeration systems, and the settling area is provided with a sludge discharge pump, a water inlet pipeline, a water outlet pipeline and a sludge return system. The effluent of the HA-UASB automatically flows into a third denitrification area, simultaneously a large amount of sludge flows back from the bottom of the sedimentation tank to the third denitrification area, and denitrification floras in the sludge utilize a carbon source in the inlet water to denitrify part of nitrate remaining in the returned sludge into nitrogen to be discharged out of a water body, so that the grade-1 denitrification is realized; the mixed liquor in the third denitrification zone automatically flows into the phosphorus release zone from the lower part, and because the nitrate is removed, phosphorus accumulating bacteria in the sludge can fully release phosphorus and synthesize a carbon source to be stored in a cell body under the anaerobic condition and the sufficient condition of the carbon source; the mixed liquid in the phosphorus release zone automatically flows into the first nitrification zone from the upper part, under the aerobic condition, the nitrosation flora and the nitrification flora can convert ammonia nitrogen in the gelatin wastewater into nitrate or nitrite, so that the 1-level deamination and denitrification effect is realized, meanwhile, the phosphorus accumulating bacteria excessively absorb phosphorus by utilizing an internal carbon source and store the phosphorus in cells under the aerobic condition, so that the transfer of the phosphorus in the gelatin wastewater from a water body to a microorganism body is realized, and meanwhile, part of heterotrophic flora in the sludge also performs the degradation effect of organic matters; the mixed liquid in the first nitrification zone automatically flows to the first denitrification zone from the lower part, part of nitrate and nitrite exist due to no aeration, the zone is an anoxic zone, phosphorus-accumulating bacteria can be prevented from releasing phosphorus in the zone, and denitrification floras in the 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-level denitrification is realized; the mixed liquid in the first denitrification zone automatically flows into the second denitrification zone from the upper part, under the aerobic condition, part of ammonia nitrogen in the gelatin wastewater can be converted into nitrate or nitrite by the nitrosobacteria and the nitrifying bacteria, so that the 2-level deamination and denitrification effect is realized, and meanwhile, part of heterotrophic bacteria in the sludge also perform the degradation effect of organic matters; the mixed liquid in the second nitrification region automatically flows to the second denitrification region from the lower part, part of nitrate and nitrite exist due to no aeration, the region is an anoxic region, phosphorus-accumulating bacteria can be prevented from releasing phosphorus in the region, and denitrification floras in the sludge utilize a carbon source in water to denitrify part of nitrate generated in the second nitrification region into nitrogen to be discharged out of a water body, so that 3-level denitrification is realized; the mixed liquor in the second denitrification zone automatically flows into a third nitrification zone from the upper part, under the aerobic condition, part of ammonia nitrogen in the gelatin wastewater can be converted into nitrate or nitrite by the nitrifying bacteria and the nitrifying bacteria, so that the 3-level deamination and denitrification effect is realized, and meanwhile, part of heterotrophic bacteria in the sludge also perform the degradation effect of organic matters; the mixed liquid in the third nitrification region enters the upper side of a sludge hopper at the middle lower part of the sedimentation region, the water distribution pipe is a perforated pipe with holes at the upper side and the lower side, the mud-water mixture enters the sedimentation region from a water distribution hole, the mud with heavier gravity and density sinks into the sludge hopper, the supernatant enters a water outlet weir to be discharged, a sludge return region is arranged at the bottom of the sludge hopper, the liquid level of the return region is improved and automatically flows into a third denitrification region by utilizing the air lifting effect, and the amount of the returned sludge is generally controlled to be 3-5 times of the water inlet flow rate for ensuring the nitrogen and phosphorus removal effect; in order to ensure the dephosphorization effect of the reactor, the excess sludge must be discharged periodically to achieve the purpose of taking out the phosphorus from the reactor.
(7) 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 suspended matters remaining in the effluent of biochemical treatment are biological floccules with the particle size of several millimeters to 10 mu m and colloid particles which are not coagulated, most of the particles are organic, 50-80% of BOD value of the effluent of secondary treatment comes from the particles, the particles are very necessary to remove for improving the clarity and stability of the effluent of secondary treatment, and meanwhile, TP indexes in the sewage can be treated to the locally specified discharge standard by a chemical phosphorus removal method.
(8) A reuse water tank 8: after the waste water is subjected to coagulating sedimentation treatment, the waste water meets the discharge requirement, enters a reuse water pool for storage, part of the waste water can be reused for plant greening, part of the waste water can be reused 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 flotation 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 transported out to be entrusted to a qualification unit for disposal.
The method is simple, the operation is simple, the universality is strong, and compared with the prior art, the method has the following advantages:
(1) the adjusting tank is divided into a large subarea and a small subarea, wastewater generated in different stages in the gelatin production process enters the large subarea firstly, and the pH value of raw water can be fully utilized for pre-neutralization, so that the medicament is saved, and meanwhile, the wastewater can be ensured to be in a neutral area by automatically adjusting the pH value in the small subarea, and the subsequent treatment effect is ensured;
(2) the HADC reactor can not only realize the oxidative degradation of macromolecular organic matters in the gelatin wastewater, but also remove salts such as sulfate, calcium salt, chloride ions, nitrogen and phosphorus, greatly reduce the inhibition effect of harmful substances on microorganisms and increase 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 subsequent biochemical organic load is greatly reduced, and the biochemical sludge yield is reduced by 60-80%;
(4) the HA-TNP reactor fully utilizes the residual carbon source in the wastewater to realize the nitrogen and phosphorus removal effect, saves the occupied area and energy consumption compared with the traditional A2O and other processes, and can effectively avoid the defect that the sludge at the bottom of the traditional sedimentation tank HAs a dead zone and generates denitrification floating sludge by a method of refluxing a large amount of sludge from the sedimentation zone;
(5) the invention is suitable for treating the gelatin wastewater generated by various raw materials and various gelatin-making processes, has good impact resistance, good effect and low operation cost, and has remarkable social and economic benefits.
Claims (5)
1. A general gelatin wastewater treatment method is characterized by comprising the following steps:
A. water quality regulation: the comprehensive wastewater passes through the grating (1) to remove larger suspended matters, floating matters, fiber substances and solid particle substances in the wastewater, the treated wastewater enters the regulating tank (2) to homogenize the water quality and the water quantity, and the pH =6-9 of the wastewater is regulated;
B. removing suspended matters and organic pollutants: the wastewater treated by the regulating tank (2) enters an air flotation tank (3), 20-100mg/L PAC and 1-3mg/L PAM are added into the air flotation tank (3) to remove suspended matters in the wastewater, and the treated wastewater enters an HADC reactor (4) to remove part of organic pollutants and salts in the wastewater and simultaneously remove part of ammonia nitrogen;
C. removing organic matters: the wastewater treated by the HADC reactor (4) enters an HA-UASB pool (5), activated sludge with hydrolytic acidification bacteria, methanogen strains, nitrosobacteria and anaerobic ammonium oxidation bacteria is added into the HA-UASB pool (5), most organic matters are removed through hydrolytic acidification and methanogenesis, meanwhile, difficultly-degradable macromolecular organic matters are converted and degraded into micromolecular organic matters, meanwhile, the nitrite in a micro-aeration solid-liquid separation zone (503) converts ammonia nitrogen into nitrite, and the nitrite is utilized by the anaerobic ammonium oxidation bacteria to generate nitrogen together with the ammonia nitrogen when flowing sludge bed (501) and a second reaction zone is a suspended sludge zone (502) so as to realize partial denitrification;
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 tank (5) enters an HA-TNP tank (6), nitrogen and phosphorus in the wastewater are removed, and the wastewater after the nitrogen and the phosphorus are removed enters a coagulating sedimentation tank (7);
E. coagulation treatment: PAC and PAM are added into a coagulating sedimentation tank (7), the dosage of PAC is 20-50mg/L, the dosage of PAM is 1-3mg/L, suspended matters and residual phosphate in water are removed, treated effluent enters a reuse tank (8) for temporary storage, most of water in the reuse tank (8) is reused as greening water or production water in a plant area, and the surplus water can reach the standard for discharge;
F. sludge treatment: and 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, and is concentrated in the sludge concentration tank (9), and then is sent to a dehydrator (10) for dehydration, and the dry sludge is transported and disposed.
2. The general gelatin wastewater treatment method according to claim 1, wherein the HA-TNP tank (6) is of a 'primary-secondary' tank partition structure, the inner rings are a phosphorus release zone (602), a first denitrification zone (604), a second denitrification zone (606) and a third denitrification zone (601) in sequence, the outsides of the phosphorus release zone (602), the first denitrification zone (604), the second denitrification zone (606) and the third denitrification zone (601) correspond to the outer rings of the first nitrification zone (603), the second nitrification zone (605), the third nitrification zone (607) and the sedimentation zone (608) respectively, wastewater treated by the HA-UASB tank (5) enters the third denitrification zone (601), sludge in the sedimentation zone (608) flows back to the third denitrification zone (601), denitrification flora in the sludge flow back utilizes carbon sources in the water to nitrify residual denitrification nitrogen in the sludge into water and discharge water, realizing the grade-1 denitrification; the mixed liquor in the third denitrification zone (601) enters a phosphorus release zone (602), phosphorus-accumulating bacteria in the sludge fully release phosphorus under anaerobic conditions and sufficient carbon sources and synthesize carbon sources to be stored in cells, the wastewater treated by the phosphorus release zone (602) enters a first nitrification zone (603), nitrite bacteria and nitrifying bacteria convert ammonia nitrogen in the wastewater into nitrate or nitrite under aerobic conditions, and the grade-1 deamination and nitrogen removal effects are realized, meanwhile, the phosphorus-accumulating bacteria excessively absorb phosphorus by using internal carbon sources and store the phosphorus in the cells under aerobic conditions, so that the transfer of phosphorus in the wastewater from a water body to microorganisms is realized, and meanwhile, part of heterotrophic bacteria in the sludge carry out the degradation of organic matters; the wastewater treated by the first nitrification region (603) enters a first denitrification region (604), and denitrification floras in the sludge utilize a carbon source in the water to denitrify nitrate generated by the first nitrification region (603) into nitrogen to be discharged out of a water body, so that 2-level denitrification is realized; the wastewater treated by the first denitrification zone (604) enters a second nitrification zone (605), nitrite bacteria and nitrifying bacteria convert part of ammonia nitrogen in the wastewater into nitrate or nitrite under aerobic conditions, so that 2-level deamination and denitrification are realized, and meanwhile, part of heterotrophic bacteria in sludge are subjected to organic matter degradation; the wastewater treated by the second nitrification region (605) enters a second denitrification region (606), and denitrification floras in the sludge utilize a carbon source in the water to denitrify part of nitrate generated by the second nitrification region (605) into nitrogen to be discharged out of the water body, so that 3-level denitrification is realized; the wastewater treated by the second denitrification zone (606) enters a third nitrification zone (607), under aerobic conditions, nitrite bacteria and nitrifying bacteria can convert part of ammonia nitrogen in the wastewater into nitrate or nitrite, so that 3-level deamination and denitrification are realized, and meanwhile, part of heterotrophic bacteria in sludge are subjected to organic matter degradation; the wastewater treated by the third nitrification zone (607) enters a sedimentation zone (608), sludge in the sedimentation zone (608) sinks into a sludge hopper and flows back to the third denitrification zone (601), the amount of the returned sludge is 3-5 times of the water inlet flow of the third denitrification zone (601), and supernatant enters a coagulating sedimentation tank (7) through a water outlet.
3. The general gelatin wastewater treatment method according to claim 1, wherein the adjusting 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 an automatic pH adjusting system are arranged in the second tank body (202), wastewater filtered by the grating (1) is neutralized and adjusted by self acid and alkali in the first tank body (201) and then enters the second tank body (202), the pH of the wastewater is detected to be not 6-9 by the automatic pH adjusting system, the wastewater pH =6-9 is adjusted by adding chemicals, and then the wastewater enters the air flotation tank (3) through the lifting pump (204).
4. The general gelatin wastewater treatment method as claimed in claim 1, wherein the HADC reactor (4) comprises an electrochemical reaction zone (401), a flocculation reaction zone (402) and a precipitation zone (403) which are sequentially communicated, the effluent of the flotation tank (3) enters the electrochemical reaction zone (401), under the condition of power-on, organic pollutants are oxidized and degraded, part of ammonia nitrogen is oxidized into nitrogen, nitrite and nitrate, high-valence or low-valence metal cations in the wastewater obtain electrons at a cathode and are directly reduced into low-valence cations or metal precipitates, after the anode is electrified with direct current, the anode loses electrons to form metal cations, and OH in the solution and the flocculation reaction zone (402) is connected with the anode, and the metal cations are oxidized into low-valence cations or metal precipitates-The pollutants in the wastewater are adsorbed and co-precipitated in a precipitation zone (403) to be removed in combination with the generation of highly active flocculation groups.
5. The general gelatin wastewater treatment method as claimed in 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 macromolecule organic matters into biodegradable micromolecule organic matters in the flowing sludge bed (501) and simultaneously removes part of the organic matters; organic matters in water are further removed in the suspended sludge zone (502), the sludge is accelerated to flow back to the flowing sludge bed (501) through air agitation in the micro-aeration solid-liquid separation zone (503), and the treated wastewater enters the HA-TNP tank (6).
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| WO2016187878A1 (en) * | 2015-05-28 | 2016-12-01 | 鹤山市新科达企业有限公司 | Treatment technology for synthetic leather production wastewater |
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| KR20050015277A (en) * | 2003-08-05 | 2005-02-21 | (주)이엔바이오21 | Wastewater Purification Method |
| CN1724418A (en) * | 2005-07-15 | 2006-01-25 | 清华大学 | Chemistry strengthened biological fluidizing recombination reactor |
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