CN113845275A - Method for deeply removing COD (chemical oxygen demand) in wastewater - Google Patents
Method for deeply removing COD (chemical oxygen demand) in wastewater Download PDFInfo
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- CN113845275A CN113845275A CN202111268659.1A CN202111268659A CN113845275A CN 113845275 A CN113845275 A CN 113845275A CN 202111268659 A CN202111268659 A CN 202111268659A CN 113845275 A CN113845275 A CN 113845275A
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- hydrolysis
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- sludge
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Images
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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
-
- 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
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
-
- 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
- C02F2001/007—Processes including a sedimentation step
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/343—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the pharmaceutical industry, e.g. containing antibiotics
-
- 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
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
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- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
Abstract
The invention discloses a method for deeply removing COD (chemical oxygen demand) in wastewater, which comprises the steps of adding sewage into a hydrolysis tank, feeding mixed liquid hydrolyzed by the hydrolysis tank into an aerobic tank, refluxing the mixed liquid at one end of the aerobic tank, which is far away from the hydrolysis tank, into the hydrolysis tank, feeding the mixed liquid in the aerobic tank into a secondary sedimentation tank, and feeding sludge precipitated in the secondary sedimentation tank back into the hydrolysis tank; and (2) the water in the secondary sedimentation tank enters a coagulation tank, ferrous sulfate and hydrogen peroxide are added into the coagulation tank, the water in the coagulation tank flows into a defoaming tank, air is introduced into the defoaming tank, the water in the defoaming tank flows into a flocculation tank, a flocculating agent is added into the flocculation tank, and mud-water separation is carried out in a tertiary sedimentation tank to obtain clean effluent. Compared with the conventional Fenton method, the method has the advantages that the use amount of the medicament (especially the use amount of hydrogen peroxide and acid-base) of the oxidation coupling-precipitation technology is reduced by 50-75%, and the operation cost is greatly reduced.
Description
Technical Field
The application relates to the field of wastewater purification, in particular to a method for deeply removing COD (chemical oxygen demand) in wastewater.
Background
Throughout the technical field of industrial water treatment, the existing and mature industrial water treatment technology in the market still stays at the level of standard treatment and nano-tube discharge. Especially in the treatment of industrial wastewater which is difficult to degrade, most of the environmental protection efforts are focused on advanced wastewater oxidation technologies such as supercritical water oxidation technology, ozone catalytic oxidation, electron beam oxidation, etc., while the deep potential of the conventional microorganism treatment capacity is ignored, and the deep degradation of pollutants or the degradation limit of pollutants is more difficult to talk about.
The source of membrane fouling is mainly two areas: on one hand, the problem of membrane pollution caused by the crystallization process of inorganic particles on the membrane surface is relieved along with the research and development of advanced membrane components such as ceramic membranes and the like; on the other hand, if the biochemical effluent is the inlet water of the double-membrane method, the membrane pollution problem caused by residual organic matters contained in the biochemical effluent is highlighted because the prior researches are few and no mature coping technologies exist in the market.
Generally, the residual organic matters after the secondary biochemical treatment of the sewage are collectively called biochemical treatment effluent organic matters (EfOM). The EfOM mainly comprises soluble organic matters which account for more than 85 percent of the total organic matter content of the effluent, and mainly comprises microbial metabolites (SMP), Natural Organic Matters (NOM) and biochemical non-degradable organic matters. SMP and NOM are mainly used, and the chemical structures and molecular weight distributions of the SMP and the NOM also represent the main characteristics of the EfOM. The SMP mainly composed of the humoid and the proteinoid organic substances is combined with each other due to the difference of surface charge and hydrophilicity and hydrophobicity to change self properties (such as molecular weight and surface charge) to form macromolecular substances, and the macromolecular substances are enriched near the membrane surface during membrane filtration to reduce diffusion speed and increase the pollution degree of the membrane surface, thereby reducing membrane flux and water production efficiency; most NOM and humic-like substances in SMP contain abundant ester bonds, phenolic hydroxyl groups, quinine, carboxyl groups, hydroxyl groups and the like in self structures, the groups are extremely easy to perform coordination reaction with metal oxides and/or hydroxides to form stable macromolecular complex substances, metal ions play a similar bridging role in the whole complexing process, and a large amount of organic matters formed by complexing are enriched on the surface of a membrane to cause membrane pollution; meanwhile, the electronegativity of the humoid substance is reduced after the humoid substance is combined with metal ions, the electrostatic repulsion among organic matters is weakened, the aggregation degree is increased, and the compaction degree of a membrane surface pollution layer is further increased.
In view of the above-mentioned related technologies, the inventor believes that the contaminated membrane module causes a series of problems such as increased water and electricity consumption, decreased water production rate, frequent membrane module cleaning, membrane module replacement cost, and significantly increased chemical cost, which results in high use cost and low water production rate of the method for treating sewage by using a dual-membrane method.
Disclosure of Invention
In order to reduce the cost of sewage purification and improve the water yield, the application provides a method for deeply removing COD in wastewater.
The method for deeply removing COD in wastewater provided by the application adopts the following technical scheme:
a method for deeply removing COD in wastewater comprises a biochemical treatment system and a dosing coupling precipitation system;
the biochemical treatment system includes: the sludge treatment method comprises the following steps of (1) maintaining the sludge age in an aerobic tank for 60-120 days, wherein MLSS in the aerobic tank is 8-15 g/L, the sludge load in the aerobic tank is 0.05-0.1 gCOD/(gMLSS. d), maintaining the sludge suspension state in the hydrolysis tank in a hydraulic mixing or mechanical mixing mode, and the surface flow rate in the hydrolysis tank is 0.3-0.5 m/s;
the drug-adding coupling precipitation system comprises: the system comprises a coagulation tank, a defoaming tank, a flocculation tank and a three-precipitation tank, wherein the coagulation tank, the defoaming tank, the flocculation tank and the three-precipitation tank are sequentially connected in series, and the two-precipitation tank is communicated with the precipitation tank;
adding sewage into the hydrolysis tank, feeding the mixed liquid hydrolyzed by the hydrolysis tank into an aerobic tank, wherein the mixed liquid at one end of the aerobic tank, which is far away from the hydrolysis tank, flows back into the hydrolysis tank, the mixed liquid in the aerobic tank flows into a secondary sedimentation tank, and the sludge precipitated in the secondary sedimentation tank flows back into the hydrolysis tank;
and (2) the water in the secondary sedimentation tank enters a coagulation tank, ferrous sulfate and hydrogen peroxide are added into the coagulation tank, the water in the coagulation tank flows into a defoaming tank, air is introduced into the defoaming tank, the water in the defoaming tank flows into a flocculation tank, a flocculating agent is added into the flocculation tank, and mud-water separation is carried out in a tertiary sedimentation tank to obtain clean effluent.
By adopting the technical scheme, when the MLSS in the aerobic tank is 8-15 g/L and the sludge load is 0.05-0.1 gCOD/(gMLSS d), the sludge concentration in the aerobic tank is high, the pollutant load of unit sludge is low, the sludge age is long, and the biological phase is rich. For industrial wastewater containing toxic and harmful substances or substances which are difficult to degrade, the degradation bacteria corresponding to the characteristic pollutants can proliferate and enrich in the sludge system, so that the pollutants can be degraded. Meanwhile, Soluble Microbial Products (SMP) and Extracellular Polymeric Substances (EPS) generated by sludge of the sludge age are less, and the SMP and EPS are important components of biochemical effluent organic matters, so that the sludge age is long, the biological phase is rich, and the deep degradation of pollutants is facilitated. Biochemical effluent flows back to the hydrolysis tank, so that SMP, EPS and other substances generated in the biochemical process are hydrolyzed while the concentration of influent pollutants is buffered, and the degradation degree of the system is further improved. Biochemical effluent flows back to the hydrolysis tank, so that on one hand, the concentration of influent pollutants is reduced, and particularly for substances with biotoxicity, the reduction of the concentration can greatly weaken the inhibition effect on the biochemical process, and further, the maintenance of rich biological phases is facilitated; on the other hand, a large amount of macromolecular difficultly-degradable substances such as SMP, EPS and the like contained in the biochemical effluent are subjected to an anoxic hydrolysis process, so that the ring opening and bond breaking of the macromolecular substances are facilitated, the metabolism of the difficultly-degradable substances is promoted, and the deep degradation of pollutants is finally realized.
In Fe2+Under the action of catalyst, H2O2The decomposition generates hydroxyl free radical which has strong oxidation effect on organic matters in the biochemical effluent, thereby carrying out advanced treatment on the biochemical effluent: the molecular weight distribution of soluble organic matters in the biochemical effluent shows obvious bimodal distribution, namely the organic matters with the molecular weight of more than 10W daltons and less than 1K daltons occupy more than 90% of the biochemical effluent, and the oxidation coupling reaction can effectively remove macromoleculesHumoid substances, but have poor removal effects on small-molecular organic matter. Fe2+Under the catalytic action of H2O2Can decompose to generate hydroxyl free radical, oxidize and decompose residual organic matters in the effluent into small molecules through electron transfer and other ways, and finally degrade the small molecules into CO2And H2And O, the advanced treatment of organic matters in the biochemical effluent is realized, and the water yield is high.
Air blowing-off is needed before flocculation, and the action of blowing-off by introducing air into the defoaming tank is mainly three: firstly, the hydrogen peroxide and the ferrous sulfate can be more fully mixed with the wastewater under the action of mixing and stirring; secondly, blowing off excessive and incompletely reacted hydrogen peroxide to avoid floating sludge caused by bubbles generated in the sedimentation process and blowing off carbon dioxide generated by the reaction to raise the pH of the wastewater and improve the flocculation sedimentation effect; and thirdly, oxidizing ferrous ions of the wastewater into ferric ions to generate better ferric hydroxide flocs and reduce the chromaticity of the wastewater.
The method really realizes the degradation of pollutants by deeply excavating the treatment potential of the activated sludge, can realize automatic dosing by dosing coupled precipitation, has simple operation and saves labor cost. Compared with the conventional Fenton method, the method has the advantages that the use amount of the medicament (especially the use amount of hydrogen peroxide and acid-base) of the oxidation coupling-precipitation technology is reduced by 50-75%, and the operation cost is greatly reduced.
Optionally, the aeration intensity in the aerobic tank (12) is 0.7-1.0 m3/h/m3。
By adopting the technical scheme, the oxygen demand of the sludge in the aeration intensity range and the mixed energy consumption of the sludge suspended state can be met.
Optionally, the reflux ratio of the nitrifying liquid at the tail end of the aerobic tank is (4-10): 1; the sludge reflux ratio of the secondary sedimentation tank (13) is (1-2): 1.
By adopting the technical scheme, the backflow ratio of the large flow enables the biochemical system to be more resistant to the coincidence impact.
Optionally, the hydrogen peroxide (H)2O2) The molar ratio of the water to the COD is (0).5～1):1。
By adopting the technical scheme, the medicine adding amount is obviously smaller than the conventional Fenton oxidation medicine adding amount, and the pH value of the wastewater is not required to be adjusted, so the operation cost is greatly reduced.
Optionally, the hydrogen peroxide (H)2O2) With ferrous iron (Fe)2+) The molar ratio of (2-4) to (1).
By adopting the technical scheme, the medicine adding amount is obviously smaller than the conventional Fenton oxidation medicine adding amount, and the pH value of the wastewater is not required to be adjusted, so the operation cost is greatly reduced.
Optionally, the retention time of the coagulation tank is 0.5-1 h, and the retention time of the flocculation tank is 1.5-3 h.
By adopting the technical scheme, the coagulation reaction and the flocculation reaction are separately carried out, so that the method is suitable for different coagulation and flocculation time and stirring strength, and the removal efficiency is improved.
Optionally, the surface load of the three-sedimentation tank is 0.8-1.0 m3/(m2·h)。
By adopting the technical scheme, the removal of COD in the wastewater is higher within the surface load range.
Optionally, the ratio of gas to water in the defoaming tank is (2-5): 1.
The ferrous ions in the wastewater are oxidized into ferric ions, better ferric hydroxide floc is generated, and the chromaticity of the wastewater is reduced.
Compared with the prior art, the invention has the beneficial effects that:
in the invention, when the MLSS in the aerobic tank is 8-15 g/L and the sludge load is 0.05-0.1 gCOD/(gMLSS d), the sludge concentration in the aerobic tank is high, the pollutant load of unit sludge is low, the sludge age is long and the biological phase is rich. For industrial wastewater containing toxic and harmful substances or refractory substances, degradation bacteria corresponding to characteristic pollutants are proliferated and enriched in a sludge system, so that the pollutants are degraded, meanwhile, Soluble Microbial Products (SMP) and Extracellular Polymeric Substances (EPS) generated by sludge of the sludge age are fewer, and the SMP and EPS are important components of biochemical effluent organic matters, which proves that the sludge age is long, and the biological phase is rich, so that the deep degradation of the pollutants is facilitated. The biochemical effluent flows back to the hydrolysis tank, SMP, EPS and other substances generated in the biochemical process are hydrolyzed while buffering the concentration of the influent pollutants, so that the degradation degree of the system is further improved, the biochemical effluent flows back to the hydrolysis tank, on one hand, the concentration of the influent pollutants is reduced, especially for substances with biotoxicity, the concentration reduction can greatly weaken the inhibition effect on the biochemical process, and further, the maintenance of abundant biological phases is facilitated, on the other hand, a large amount of macromolecular SMP, EPS and other refractory substances contained in the biochemical effluent are subjected to the anoxic hydrolysis process, so that the ring opening and bond breaking of the macromolecular substances are facilitated, the metabolism of the refractory substances is promoted, and the deep degradation of the pollutants is finally realized;
in the present invention, Fe is present2+Under the action of catalyst, H2O2The decomposition generates hydroxyl free radical which has strong oxidation effect on organic matters in the biochemical effluent, thereby carrying out advanced treatment on the biochemical effluent: the molecular weight distribution of soluble organic matters in the biochemical effluent shows obvious bimodal distribution, namely, the organic matters with the molecular weights of more than 10W daltons and less than 1K daltons account for more than 90% of the biochemical effluent, and the oxidation coupling reaction can effectively remove macromolecular humic substances, but the removal effect on small molecular organic matters is not good. Fe2+Under the catalytic action of H2O2Can decompose to generate hydroxyl free radical, oxidize and decompose residual organic matters in the effluent into small molecules through electron transfer and other ways, and finally degrade the small molecules into CO2And H2O, realizing the advanced treatment of organic matters in the biochemical effluent;
the invention needs air stripping before flocculation, and the air introduced into the defoaming tank for stripping has three main functions: firstly, the hydrogen peroxide and the ferrous sulfate can be more fully mixed with the wastewater under the action of mixing and stirring; secondly, blowing off excessive and incompletely reacted hydrogen peroxide to avoid floating sludge caused by bubbles generated in the sedimentation process and blowing off carbon dioxide generated by the reaction to raise the pH of the wastewater and improve the flocculation sedimentation effect; thirdly, oxidizing ferrous ions in the wastewater into ferric ions to generate better ferric hydroxide flocs and reduce the chromaticity of the wastewater;
the method has high pollutant removal efficiency, the effluent quality reaches the first grade A standard of pollutant discharge Standard of urban wastewater treatment plant (GB18918-2002), and simultaneously the water inlet condition of a recycling system is met;
the method has stable operation, high sludge concentration and large flow reflux, so that the biochemical system is more resistant to load impact;
the method really realizes the degradation of pollutants by deeply excavating the treatment potential of the activated sludge, and the dosing coupling precipitation can realize automatic dosing, so the operation is simple and the labor cost is saved;
compared with the conventional Fenton method, the method has the advantages that the operation cost is low, the use amount of the medicament (especially the use amount of hydrogen peroxide and acid-base) of the oxidation coupling-precipitation technology is reduced by 50-75%, and the operation cost is greatly reduced;
the invention has wide application range, is easy to popularize and apply, and is suitable for the treatment of industrial wastewater which is difficult to degrade and toxic and the treatment of industrial park sewage with complex water quality.
Drawings
FIG. 1 is a flow chart of a method for deeply removing COD in wastewater according to the present invention.
In the figure: 1. a biochemical treatment system; 11. a hydrolysis tank; 12. an aerobic tank; 13. a secondary sedimentation tank; 2. a dosing coupling precipitation system; 21. a coagulation tank; 22. a defoaming pool; 23. a flocculation tank; 24. and (4) a three-sedimentation tank.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
With reference to FIG. 1
Example 1, AA centralized sewage treatment plant in a pharmaceutical park mainly collects and treats wastewater of biopharmaceuticals, wherein upstream biopharmaceuticals comprise aureomycin, aureomycin hydrochloride, terramycin, coenzyme Q10, penicillin, pesticide, veterinary drug, enzyme preparation and the like. Design water quantity 12000m3/d。
The method for deeply removing COD in wastewater comprises a biochemical treatment system 1 and a dosing coupling precipitation system 2. The sludge concentration of the biochemical treatment system 1 is controlled to be 10-13 g/L, the biochemical treatment system 1 comprises a hydrolysis tank 11, an aerobic tank 12 and a secondary sedimentation tank 13, and the hydrolysis tank 11 and the aerobic tank 12 are circulating water tanks. The sludge age in the aerobic tank 12 is maintained for 60 days, the sludge age in the aerobic tank 12 is maintained for 120 days, and the sludge load in the aerobic tank 12 is 0.1 gCOD/(gMLSS. d). Adding sewage into the hydrolysis tank 11, feeding the mixed liquid hydrolyzed by the hydrolysis tank 11 into the aerobic tank 12, wherein the mixed liquid at one end of the aerobic tank 12, which is far away from the hydrolysis tank 11, flows back into the hydrolysis tank 11, the mixed liquid in the aerobic tank 12 flows into the secondary sedimentation tank 13, and the sludge precipitated in the secondary sedimentation tank 13 flows back into the hydrolysis tank 11.
The dosing coupling precipitation system 2 comprises: the coagulation tank 21, the defoaming tank 22, the flocculation tank 23 and the three-precipitation tank 24 are sequentially connected in series, and the two-precipitation tank 13 is communicated with the precipitation tank.
2 underwater propellers are arranged in the hydrolysis tank 11 for stirring, and the stirring power of the underwater propellers is 1.0W/m3The surface flow velocity in the hydrolysis tank 11 was 0.4 m/s. A magnetic suspension fan and an HS forced-cutting aerator are arranged to aerate the aerobic tank 12, the aeration intensity is 0.8m3/h/m3, the reflux ratio of nitrifying liquid at the tail end of the aerobic tank 12 is 10:1, and the reflux ratio of sludge in the secondary sedimentation tank 13 is 2: 1. The surface load of the secondary sedimentation tank 13 is 0.5m 3/(m)2H). The effluent of the secondary sedimentation tank 13 enters a coagulation tank 21 for advanced treatment, and ferrous sulfate and hydrogen peroxide (H) are added into the coagulation tank 212O2) The molar ratio of the compound to COD is 0.5:1, and hydrogen peroxide (H)2O2) With ferrous iron (Fe)2+) The molar ratio of (2: 1), the gas-water ratio of the defoaming tank 22 is controlled to be 2:1, and the surface load of the three-precipitation tank 24 is 1.0m3/(m2H). Biochemical system influent COD10000mg/L secondary sedimentation tankThe COD of the 13 effluent is 400-600 mg/L, and the COD of the 24 effluent of the three-sedimentation tank is 50 mg/L.
The enterprise carries out zero discharge recycling on all wastewater, the reuse water process adopts a combined treatment process of a self-cleaning filter, an ultrafiltration membrane system, a sub-osmosis membrane system, a nanofiltration system, a medium-high pressure reverse osmosis membrane and an MVR, and the stable operation of the recycling system is ensured because the COD of the wastewater is fully removed. Through measurement and calculation, the treatment cost of the reuse water is 16.25 yuan/ton of water, and the requirement of design indexes is met.
Example 2
The product of the waste water produced in pharmaceutical factory includes amoxicillin, cephalosporins, tylosin, acetylspiramycin, abamectin, 7ACA and veterinary antibiotics (tilmicosin, tilmicosin phosphate, etc.). Designed water quantity of 20000m3/d。
The sewage treatment device of the embodiment comprises an A/O treatment system and an oxidation coupling advanced treatment system. The sludge concentration of the biochemical treatment system 1 is controlled to be 8-10 g/L, the biochemical treatment system 1 comprises a hydrolysis tank 11, an aerobic tank 12 and a secondary sedimentation tank 13, and the hydrolysis tank 11 and the aerobic tank 12 are circulating water tanks. The sludge age in the aerobic tank 12 was maintained at 120 days, and the sludge load in the aerobic tank 12 was 0.05 gCOD/(gMLSS. d). Adding sewage into the hydrolysis tank 11, feeding the mixed liquid hydrolyzed by the hydrolysis tank 11 into the aerobic tank 12, wherein the mixed liquid at one end of the aerobic tank 12 far away from the hydrolysis tank 11 flows back into the hydrolysis tank 11, the mixed liquid in the aerobic tank 12 flows into the secondary sedimentation tank 13, and the sludge precipitated in the secondary sedimentation tank 13 flows back into the hydrolysis tank 11.
The dosing coupling precipitation system 2 comprises: the coagulation tank 21, the defoaming tank 22, the flocculation tank 23 and the three-precipitation tank 24 are sequentially connected in series, and the two-precipitation tank 13 is communicated with the precipitation tank.
2 underwater propellers are arranged in the hydrolysis tank 11 for stirring, and the stirring power of the underwater propellers of the hydrolysis tank 11 is 1.0W/m3The surface flow velocity in the hydrolysis tank 11 was 0.3 m/s. A magnetic suspension fan and an HS forced-cutting aerator are arranged to aerate the aerobic tank 12, and the aeration intensity is 0.7m3/h/m3Wherein the reflux ratio of nitrifying liquid at the tail end of the aerobic tank 12 is 8:1, and the reflux ratio of nitrifying liquid in the secondary sedimentation tank 13 isThe sludge reflux ratio is 2: 1. The surface load of the secondary sedimentation tank 13 is 0.5m3/(m 2. h). The effluent of the secondary sedimentation tank 13 enters a coagulation tank 21 for advanced treatment, and ferrous sulfate and hydrogen peroxide (H) are added into the coagulation tank 212O2) The molar ratio of the compound to COD is 0.6:1, and hydrogen peroxide (H)2O2) With ferrous iron (Fe)2+) The molar ratio of (2.5: 1), the gas-water ratio of the deaeration tank 22 is controlled to be 2:1, and the surface load of the tertiary sedimentation tank 24 is 1.0m3/(m2H). The COD of the inlet water of the biochemical system is 5000mg/L, the COD of the outlet water of the secondary sedimentation tank 13 is 350-450 mg/L, and the COD of the outlet water of the tertiary sedimentation tank 24<50mg/L。
The enterprise wastewater is recycled, and the reuse water process unit comprises a hardness removal unit, a nanofiltration salt separation unit, a gradient reverse osmosis membrane concentration unit, an evaporation unit, a public supporting project and the like, so that the problem that the total salt content of the enterprise reaches the standard is effectively solved, and the recycled water is recycled.
In the invention, when the MLSS in the aerobic tank is 8-15 g/L and the sludge load is 0.05-0.1 gCOD/(gMLSS d), the sludge concentration in the aerobic tank is high, the pollutant load of unit sludge is low, the sludge age is long and the biological phase is rich. For industrial wastewater containing toxic and harmful substances or refractory substances, degradation bacteria corresponding to characteristic pollutants are proliferated and enriched in a sludge system, so that the pollutants are degraded, meanwhile, Soluble Microbial Products (SMP) and Extracellular Polymeric Substances (EPS) generated by sludge of the sludge age are fewer, and the SMP and EPS are important components of biochemical effluent organic matters, which proves that the sludge age is long, and the biological phase is rich, so that the deep degradation of the pollutants is facilitated. The biochemical effluent flows back to the hydrolysis tank, SMP, EPS and other substances generated in the biochemical process are hydrolyzed while the concentration of the influent pollutants is buffered, so that the degradation degree of the system is further improved, the biochemical effluent flows back to the hydrolysis tank, on one hand, the concentration of the influent pollutants is reduced, especially for substances with biotoxicity, the concentration reduction can greatly weaken the inhibition effect on the biochemical process, and further, the maintenance of abundant biological phases is facilitated, on the other hand, a large amount of macromolecular SMP, EPS and other refractory substances contained in the biochemical effluent are subjected to the anoxic hydrolysis process, so that the ring opening and bond breaking of the macromolecular substances are facilitated, the metabolism of the refractory substances is promoted, and the deep degradation of the pollutants is finally realized.
In the present invention, Fe is present2+Under the action of catalyst, H2O2The decomposition generates hydroxyl free radical which has strong oxidation effect on organic matters in the biochemical effluent, thereby carrying out advanced treatment on the biochemical effluent: the molecular weight distribution of soluble organic matters in the biochemical effluent shows obvious bimodal distribution, namely, the organic matters with the molecular weights of more than 10W daltons and less than 1K daltons account for more than 90% of the biochemical effluent, and the oxidation coupling reaction can effectively remove macromolecular humic substances, but the removal effect on small molecular organic matters is not good. Under the catalytic action of Fe2+, H2O2 can be decomposed to generate hydroxyl radicals, and residual organic matters in the effluent are oxidized and decomposed into small molecules through electron transfer and other ways, and finally degraded into CO2And H2And O, realizing the advanced treatment of the organic matters in the biochemical effluent.
The invention needs air stripping before flocculation, and the air introduced into the defoaming tank for stripping has three main functions: firstly, the hydrogen peroxide and the ferrous sulfate can be more fully mixed with the wastewater under the action of mixing and stirring; secondly, blowing off excessive and incompletely reacted hydrogen peroxide to avoid floating sludge caused by bubbles generated in the sedimentation process and blowing off carbon dioxide generated by the reaction to raise the pH of the wastewater and improve the flocculation sedimentation effect; thirdly, oxidizing ferrous ions in the wastewater into ferric ions to generate better ferric hydroxide flocs and reduce the chromaticity of the wastewater;
the method has high pollutant removal efficiency, the effluent quality reaches the first grade A standard of pollutant discharge Standard of urban wastewater treatment plant (GB18918-2002), and the water inlet condition of a recycling system is met.
The method has stable operation, high sludge concentration and large flow reflux, and makes the biochemical system more resistant to load impact.
The method really realizes the degradation of pollutants by deeply excavating the treatment potential of the activated sludge, and the dosing coupling precipitation can realize automatic dosing, so the operation is simple and the labor cost is saved.
Compared with the conventional Fenton method, the method has the advantages that the operation cost is low, the use amount of the medicament (especially the use amount of hydrogen peroxide and acid-base) of the oxidative coupling-precipitation technology is reduced by 50-75%, and the operation cost is greatly reduced.
The invention has wide application range, is easy to popularize and apply, and is suitable for the treatment of industrial wastewater which is difficult to degrade and toxic and the treatment of industrial park sewage with complex water quality.
It will be evident to those skilled in the art that the invention is not limited to the details of the foregoing illustrative embodiments, and that the present invention may be embodied in other specific forms without departing from the spirit or essential attributes thereof. The present embodiments are therefore to be considered in all respects as illustrative and not restrictive, the scope of the invention being indicated by the appended claims rather than by the foregoing description, and all changes which come within the meaning and range of equivalency of the claims are therefore intended to be embraced therein. Any reference sign in a claim should not be construed as limiting the claim concerned.
Claims (7)
1. A method for deeply removing COD in wastewater is characterized in that: comprises a biochemical treatment system (1) and a dosing coupling precipitation system (2);
the biochemical treatment system (1) comprises: the system comprises a hydrolysis tank (11), an aerobic tank (12) and a secondary sedimentation tank (13), wherein the hydrolysis tank (11) and the aerobic tank (12) are circulating water tanks, the sludge age in the aerobic tank (12) is maintained for 60-120 days, MLSS in the aerobic tank (12) is 8-15 g/L, the sludge load in the aerobic tank (12) is 0.05-0.1 gCOD/(gMLSS d), the sludge suspension state is maintained in the hydrolysis tank (11) in a hydraulic mixing or mechanical mixing mode, and the surface flow rate in the hydrolysis tank (11) is 0.3-0.5 m/s;
the dosing-coupled precipitation system (2) comprises: the device comprises a coagulation tank (21), a defoaming tank (22), a flocculation tank and a three-precipitation tank (24), wherein the coagulation tank (21), the defoaming tank (22), the flocculation tank (23) and the three-precipitation tank (24) are sequentially connected in series, and the two-precipitation tank (13) is communicated with the precipitation tank;
adding sewage into the hydrolysis tank (11), feeding the mixed liquor hydrolyzed by the hydrolysis tank (11) into an aerobic tank (12), wherein the mixed liquor at one end of the aerobic tank (12) far away from the hydrolysis tank (11) flows back into the hydrolysis tank (11), the mixed liquor in the aerobic tank (12) flows into a secondary sedimentation tank (13), and the sludge precipitated in the secondary sedimentation tank (13) flows back into the hydrolysis tank (11);
the water in the secondary sedimentation tank (13) enters the coagulation tank (21), ferrous sulfate and hydrogen peroxide are added into the coagulation tank (21), the water in the coagulation tank (21) flows into the defoaming tank (22), air is introduced into the defoaming tank (22), the water in the defoaming tank (22) flows into the flocculation tank (23), a flocculating agent is added into the flocculation tank (23), and mud-water separation is carried out in the tertiary sedimentation tank (24) to obtain clean outlet water.
2. The method for deeply removing COD in wastewater according to claim 1, which is characterized in that: the aeration intensity in the aerobic tank (12) is 0.7-1.0 m3/h/m3。
3. The method for deeply removing COD in wastewater according to claim 1, which is characterized in that: the reflux ratio of nitrifying liquid at the tail end of the aerobic tank (12) is (4-10): 1; the sludge reflux ratio of the secondary sedimentation tank (13) is (1-2): 1.
4. The method for deeply removing COD in wastewater according to claim 1, which is characterized in that: hydrogen peroxide (H)2O2) The molar ratio of the COD to the water is (0.5-1): 1.
5. The method for deeply removing COD in wastewater according to claim 1, which is characterized in that: hydrogen peroxide (H)2O2) With ferrous iron (Fe)2+) The molar ratio of (2-4) to (1).
6. The method for deeply removing COD in wastewater according to claim 1, which is characterized in that: the surface load of the three-sedimentation tank (24) is 0.8-1.0 m3/(m2·h)。
7. The method for deeply removing COD in wastewater according to claim 1, which is characterized in that: the ratio of gas to water of the defoaming tank (22) is (2-5) to 1.
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20020024253A (en) * | 2002-02-09 | 2002-03-29 | 서영진 | Treatment method for organic wastewater |
| CN103121756A (en) * | 2013-03-13 | 2013-05-29 | 华东理工大学 | Hydrolysis/aerobic cycle suspension activated sludge process and device for deep treatment of waste water |
| CN106045124A (en) * | 2016-07-15 | 2016-10-26 | 华东理工大学 | Method for removing residual organic matters from outlet water of biological reaction system |
| CN106145571A (en) * | 2016-09-30 | 2016-11-23 | 南京大学盐城环保技术与工程研究院 | A kind of chemical wastewater treatment station Tailwater Depth processing system and processing method |
| CN108675497A (en) * | 2018-05-24 | 2018-10-19 | 苏州苏沃特环境科技有限公司 | One kind being based on Fenton fluidized bed processing dyeing waste water minimum discharge devices and methods therefor |
| CN111620467A (en) * | 2020-06-03 | 2020-09-04 | 玖龙纸业（东莞）有限公司 | Sewage advanced treatment system and method |
-
2021
- 2021-10-29 CN CN202111268659.1A patent/CN113845275A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20020024253A (en) * | 2002-02-09 | 2002-03-29 | 서영진 | Treatment method for organic wastewater |
| CN103121756A (en) * | 2013-03-13 | 2013-05-29 | 华东理工大学 | Hydrolysis/aerobic cycle suspension activated sludge process and device for deep treatment of waste water |
| CN106045124A (en) * | 2016-07-15 | 2016-10-26 | 华东理工大学 | Method for removing residual organic matters from outlet water of biological reaction system |
| CN106145571A (en) * | 2016-09-30 | 2016-11-23 | 南京大学盐城环保技术与工程研究院 | A kind of chemical wastewater treatment station Tailwater Depth processing system and processing method |
| CN108675497A (en) * | 2018-05-24 | 2018-10-19 | 苏州苏沃特环境科技有限公司 | One kind being based on Fenton fluidized bed processing dyeing waste water minimum discharge devices and methods therefor |
| CN111620467A (en) * | 2020-06-03 | 2020-09-04 | 玖龙纸业（东莞）有限公司 | Sewage advanced treatment system and method |
Non-Patent Citations (1)
| Title |
|---|
| 王永广等: "水解酸化/好氧生化/Fenton氧化工艺处理制药废水的研究", 《环境工程学报》 * |
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