CN113860644A - Fenton-based wastewater treatment system and method - Google Patents

Fenton-based wastewater treatment system and method Download PDF

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Publication number
CN113860644A
CN113860644A CN202111195991.XA CN202111195991A CN113860644A CN 113860644 A CN113860644 A CN 113860644A CN 202111195991 A CN202111195991 A CN 202111195991A CN 113860644 A CN113860644 A CN 113860644A
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tank
fenton
wastewater treatment
treatment system
zone
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刘晓永
张日亮
陈铭聪
王玉
陈琴
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Guangzhou Sinovast Energy Environmental Protection Group Co ltd
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Guangzhou Sinovast Energy Environmental Protection Group Co ltd
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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
    • C02F1/30—Treatment of water, waste water, or sewage by irradiation
    • C02F1/32—Treatment of water, waste water, or sewage by irradiation with ultraviolet light
    • 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
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
    • C02F1/56—Macromolecular compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/722—Oxidation by peroxides
    • 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
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • 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
    • C02F2101/00—Nature of the contaminant
    • C02F2101/30—Organic compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00—Specific treatment goals
    • C02F2303/04—Disinfection
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2305/00—Use of specific compounds during water treatment
    • C02F2305/02—Specific form of oxidant
    • C02F2305/026—Fenton's reagent
    • 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
    • C02F3/28—Anaerobic digestion processes
    • C02F3/2806—Anaerobic processes using solid supports for microorganisms
    • 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
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F7/00—Aeration of stretches of water

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  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
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  • Treatment Of Water By Oxidation Or Reduction (AREA)
  • Separation Of Suspended Particles By Flocculating Agents (AREA)

Abstract

The invention discloses a Fenton-based wastewater treatment system and a Fenton-based wastewater treatment method. The wastewater treatment system comprises a pretreatment system, a biochemical system and an advanced treatment system which are connected in sequence; the pretreatment system comprises a grit chamber and a homogenizing tank or a primary air floatation tank which are connected in sequence; the biochemical system comprises a hydrolysis acidification tank, an AO tank and a primary sedimentation tank which are connected in sequence; the advanced treatment system comprises a contact oxidation tank, a secondary sedimentation tank, a secondary air flotation tank, a biological activated carbon filter tank, a membrane filtration system and a heterogeneous Fenton reaction system which are connected in sequence; and a connecting pipeline is arranged between the heterogeneous Fenton reaction system and the hydrolysis acidification tank. When the wastewater treatment system based on Fenton provided by the invention is used for treating wastewater, the effluent quality meets the first-class A standard of discharge Standard of pollutants for municipal wastewater treatment plants, and the wastewater treatment cost is low.

Description

Fenton-based wastewater treatment system and method
Technical Field
The invention relates to the technical field of wastewater treatment, in particular to a Fenton-based wastewater treatment system and a Fenton-based wastewater treatment method.
Background
Along with the rapid development of social economy and chemical industry, the sewage amount and the sewage type of industrial park increase day by day, sewage treatment process equipment lags behind, along with the improvement of people's environmental consciousness and the growing severity of environmental pollution, higher and higher requirements are put forward to industrial park waste water treatment, but each enterprise's product variety is various in the industrial park, the waste water discharge is irregular, and the most of discharging in the production process is the organic pollutant that the structure is complicated, poisonous and harmful and biochemical is difficult to degrade, the processing degree of difficulty is big.
The prior art aims at the water treatment process technology and the method of the industrial park sewage, although most of the industrial sewage and the discharged water can be effectively treated, for some harmful substances which are difficult to dissolve in water and degrade, the original treatment process technology is difficult to complete the important tasks of recycling and purifying the water quality. Therefore, under the new development environment and requirements, the modification and improvement of the industrial park sewage treatment process technology and method are imminent, so that the treatment process method and technology can better adapt to the purposes of recycling and purifying industrial sewage generated in the new-age industrial development process.
Disclosure of Invention
In order to solve the problem that the prior art cannot meet the treatment requirement when the wastewater has complex components and contains substances which are difficult to degrade and have high toxicity, the invention aims to provide a Fenton-based wastewater treatment system and a Fenton-based wastewater treatment method.
In order to achieve the purpose, the technical scheme adopted by the invention is as follows:
a wastewater treatment system based on Fenton comprises a pretreatment system, a biochemical system and an advanced treatment system which are connected in sequence;
the pretreatment system comprises a grit chamber and a homogenizing tank or a primary air floatation tank which are connected in sequence;
the biochemical system comprises a hydrolysis acidification tank, an AO tank and a primary sedimentation tank which are connected in sequence;
the advanced treatment system comprises a contact oxidation tank, a secondary sedimentation tank, a secondary air flotation tank, a biological activated carbon filter tank, a membrane filtration system and a heterogeneous Fenton reaction system which are connected in sequence; and a connecting pipeline is arranged between the heterogeneous Fenton reaction system and the hydrolysis acidification tank.
Preferably, the wastewater treatment system based on Fenton further comprises a disinfection tank, the disinfection tank is arranged behind the membrane filtration system, and effluent of the membrane filtration system is discharged after passing through the disinfection tank; further preferably, the disinfection tank is one of a chemical disinfection tank, an ozone disinfection tank and an ultraviolet disinfection tank; still further preferably, the disinfection tank is one of an ozone disinfection tank and an ultraviolet disinfection tank; still more preferably, the disinfection tank is an ultraviolet disinfection tank.
Preferably, the pretreatment system of the wastewater treatment system based on Fenton comprises a grit chamber, a homogenizing tank and a primary air floatation tank which are connected in sequence; the homogenizing tank is used for mixing and adjusting water quality.
Further preferably, the grit chamber in the pretreatment system is an aeration grit chamber; still further preferably, the grit chamber is two aeration grit chambers connected in parallel; still more preferably, the aeration rate of the aeration grit chamber is 0.05-0.15m3/m3The hydraulic retention time of the sewage is 4-10 min; more preferably, the aeration rate of the aeration grit chamber is 0.1m3/m3The hydraulic retention time of the sewage is 6-8 min.
Further preferably, the grit chamber in the pretreatment system comprises a grid filter; still further preferably, the grid is a plate-type fine grid; still more preferably, the grid is a plate-type fine grid with a grid gap of 3 mm; the hair fiber and the flocculent impurities in the industrial sewage are intercepted and removed.
Further preferably, the length-width ratio of the homogenizing pool in the pretreatment system is (3-1): 1; still further preferably, the aspect ratio of the homogenizing pool in the pretreatment system is 2: 1; the effluent of the grit chamber flows into the homogenizing tank after being metered, the sewage is subjected to water quality and water quantity regulation in the homogenizing tank, and when the water quality and water quantity fluctuation is large, the load impact of the subsequent process can be reduced.
Preferably, the first-stage air flotation tank in the pretreatment system is a cavitation air flotation tank; still more preferably, the air flotation section load is 4-8m3/(h·m2) (ii) a Even more preferably, the air bearing section is loadedIs 6m3/(h·m2)。
Further preferably, the hydraulic retention time of a first-stage air floatation tank in the pretreatment system is 10-30 min; still further preferably, the hydraulic retention time of the first-stage air floatation tank is 20 min.
Further preferably, at least one of a coagulant and a flocculant is added into a primary floatation tank in the pretreatment system; still more preferably, the coagulant is PAC (polyaluminium chloride), and the flocculant is PAM (polyacrylamide); more preferably, the coagulant is PAC (polyaluminium chloride) with a mass concentration of 10%, and the flocculant is PAM (polyacrylamide) with a mass concentration of 2 ‰.
Preferably, in the fenton-based wastewater treatment system, dechlorination respiratory bacteria (dehaococcoides mccartyi) are added into a hydrolysis acidification tank; more preferably, the amount of the bacterial suspension added is 100g/m3。
Preferably, in the fenton-based wastewater treatment system, the uniform water distribution device is arranged at the bottom of the hydrolysis acidification tank.
Preferably, in the fenton-based wastewater treatment system, the hydrolysis acidification tank is internally provided with a filler; preferably, the hydrolysis acidification tank is internally provided with a fiber rope filler; still more preferably, the outer diameter of the fiber rope is 45 mm; even more preferably, the fiber rope filler has a density of 30m/m3(ii) a The hydrolytic acidification tank adopts hydraulic stirring to strengthen the hydraulic cutting effect on the wastewater, improve the hydrolytic acidification capability, decompose macromolecular organic matters which are difficult to be biochemically degraded into micromolecular organic matters which are easy to biochemically degrade in the hydrolytic acidification tank, and improve the biodegradability of the sewage.
Preferably, in the fenton-based wastewater treatment system, the AO tank satisfies at least one of the following conditions: the sludge concentration is more than or equal to 5000 mg/L; the content of dissolved oxygen is less than or equal to 2 mg/L; the internal reflux ratio is 200-300%.
Preferably, in the Fenton-based wastewater treatment system, the concentration of sludge in the AO pool is more than or equal to 5000 mg/L; further preferably, the concentration of the sludge in the AO pool is more than or equal to 6000 mg/L; still further preferably, the sludge concentration in the anaerobic zone in the AO cell is 8000mg/L, and the sludge concentration in the aerobic zone in the AO cell is 7000 mg/L.
Preferably, in the Fenton-based wastewater treatment system, the content of dissolved oxygen in the AO pool is less than or equal to 2 mg/L.
Preferably, in the Fenton-based wastewater treatment system, the internal reflux ratio of the AO pool is 200-300%; more preferably, the internal reflux ratio of the AO cell is 250%.
Preferably, in the Fenton-based wastewater treatment system, the hydraulic retention time of the anaerobic zone in the AO pool is 10-14 h; further preferably, the hydraulic retention time of the anaerobic zone in the AO cell is 11-13 h; still further preferred, the hydraulic retention time of the anaerobic zone in the AO-cell is 12 h.
Preferably, in the Fenton-based wastewater treatment system, the hydraulic retention time of the aerobic zone in the AO pool is 30-40 h; further preferably, the hydraulic retention time of the aerobic zone in the AO cell is 32-38 h; still further preferably, the hydraulic retention time of the aerobic zone in the AO-cell is 36 h.
Preferably, in the fenton-based wastewater treatment system, the primary sedimentation tank is a radial sedimentation tank; preferably, the primary sedimentation tank is a medium-in and medium-out radial flow sedimentation tank; still further preferably, a mud bucket is arranged at the center of the bottom of the radial flow type sedimentation tank, and the bottom slope of the slope mud bucket is 0.1.
Preferably, in the Fenton-based wastewater treatment system, the primary sedimentation tank is a radial sedimentation tank, the hydraulic retention time of the sludge area is 0.5-1.5h, and the hydraulic retention time of the clarification area is 2-4 h; further preferably, the hydraulic retention time of the sludge zone is 1h, and the hydraulic retention time of the clarification zone is 3 h.
Preferably, in the Fenton-based wastewater treatment system, the contact oxidation pond is of a cellular rectangular structure; more preferably, the contact oxidation pond is internally provided with fiber filler; still further preferably, the fibrous filler is vertically arranged in the contact oxidation tank; still further preferably, the height of the fibrous filler is 2 to 4 m; even more preferably, the height of the fibrous filler is 3 m.
Preferably, in the Fenton-based wastewater treatment system, the content of dissolved oxygen in the contact oxidation pond is 2-4 mg/L; further preferably, the dissolved oxygen content is 2.5-3.5 mg/L; more preferably, the dissolved oxygen content is 3 mg/L.
Preferably, in the fenton-based wastewater treatment system, PAC (polyaluminium chloride) is added into the secondary sedimentation tank as a coagulant; more preferably, the adding amount of PAC is 10-30 mg/L; still more preferably, the PAC is added in an amount of 15-25 mg/L; more preferably, PAC is added in an amount of 20 mg/L.
Preferably, in the fenton-based wastewater treatment system, PAM (polyacrylamide) is added into the secondary sedimentation tank as a flocculating agent; further preferably, the dosage of the PAM is 0.2-0.4 mg/L; still further preferred; the dosage of PAM is 0.25-0.35 mg/L; more preferably, the amount of PAM added is 0.3 mg/L.
Preferably, in the fenton-based wastewater treatment system, the secondary air flotation tank in the advanced treatment system is a cavitation air flotation tank; further preferably, the air floatation section load is 3-5m3/(h·m2) (ii) a Still further preferably, the air flotation section load is 4m3/(h·m2)。
Preferably, in the Fenton-based wastewater treatment system, the hydraulic retention time of a secondary air flotation tank in the advanced treatment system is 10-30 min; further preferably, the hydraulic retention time of the secondary air flotation tank is 12-18 min; still further preferably, the hydraulic retention time of the secondary air flotation tank is 15 min.
Preferably, in the Fenton-based wastewater treatment system, the biological activated carbon filter tank adopts columnar activated carbon; further preferably, the bulk density of the activated carbon is 400-600 g/L; still more preferably, the bulk density of the activated carbon is 480 g/L.
Preferably, in the Fenton-based wastewater treatment system, the height of a carbon bed of the biological activated carbon filter is 2-3 m; further preferably, the height of the carbon bed of the biological activated carbon filter is 2.5 m; still further preferably, the empty bed contact time of the biological activated carbon filter is 10-20 min; still more preferably, the empty bed contact time of the biological activated carbon filter is 15 min.
Preferably, in the Fenton-based wastewater treatment system, the dissolved oxygen concentration in the biological activated carbon filter is 3-9 mg/L; further preferably, the dissolved oxygen concentration in the biological activated carbon filter is 4-8 mg/L; still further preferably, the dissolved oxygen concentration in the biological activated carbon filter is 5-7 mg/L.
Preferably, in the Fenton-based wastewater treatment system, the particle size of the filler in the biological activated carbon filter is less than or equal to 1 mm; further preferably, the grain diameter of the filler in the biological activated carbon filter is less than or equal to 0.8 mm; still further preferably, the grain size of the filler in the biological activated carbon filter is less than 0.8 mm.
Preferably, in the Fenton-based wastewater treatment system, the filtration rate in the biological activated carbon filter is 3-6 m/h; further preferably, the filtering speed in the biological activated carbon filter is 3.5-5.5 m/h; still further preferably, the filtering speed in the biological activated carbon filter is 4-5 m/h.
Preferably, in the Fenton-based wastewater treatment system, the hydraulic retention time of wastewater in the biological activated carbon filter is more than 10 min; further preferably, the hydraulic retention time of the wastewater in the biological activated carbon filter is more than or equal to 15 min; still further preferably, the hydraulic retention time of the wastewater of the biological activated carbon filter is 15-60 min.
Preferably, in the Fenton-based wastewater treatment system, the turbidity of the effluent of the biological activated carbon filter is less than 0.2 NTU.
Preferably, in the Fenton-based wastewater treatment system, the membrane cut-off molecular weight in the membrane filtration system is 100-300 Da; further preferably, the membrane cut-off molecular weight in the membrane filtration system is 120-250 Da; still further preferably, the membrane cut-off in the membrane filtration system is 150-200 Da.
Preferably, in the fenton-based wastewater treatment system, the maximum operating pressure of the membrane filtration system is 30-50 bar; further preferably, the maximum operating pressure of the membrane filtration system is 35-45 bar; still further preferably, the maximum operating pressure of the membrane filtration system is 40-42 bar; even more preferably, the maximum operating pressure of the membrane filtration system is 41 bar.
Preferably, in the Fenton-based wastewater treatment system, the water yield of the membrane filtration system is 80-95%; further preferably, the water yield of the membrane filtration system is 83-92%; still further preferably, the water production rate of the membrane filtration system is 85-90%.
Preferably, the membrane filtration system has a salt rejection of < 50% in such a fenton based wastewater treatment system.
Preferably, in the fenton-based wastewater treatment system, the heterogeneous fenton reaction system comprises an acid regulation zone, a heterogeneous fenton reaction zone, an intermediate precipitation zone, a primary alkali regulation zone and a coagulating precipitation zone which are connected in sequence.
Preferably, in the fenton-based wastewater treatment system, the heterogeneous fenton reaction system further comprises a secondary alkali regulation zone; the effluent of the coagulating sedimentation zone enters a secondary alkali adjusting zone, and the effluent of the secondary alkali adjusting zone enters a hydrolysis acidification pool; further preferably, the pH of the effluent of the secondary alkali adjusting zone is 6-7.
Further preferably, in the heterogeneous Fenton reaction system, the pH value of the acid adjusting area is 2-4; still further preferably, the pH value of the acid adjusting region is 2.5-3.5; even more preferably, the pH in the acid adjustment zone is 3.
Further preferably, in the heterogeneous Fenton reaction system, the hydraulic retention time of the acid regulating area is 6-15 min; still further preferably, the hydraulic retention time of the acid adjusting pool is 8-12 min; more preferably, the hydraulic retention time of the acid adjusting pond is 10 min.
Further preferably, in the heterogeneous fenton reaction system, the heterogeneous fenton reaction zone is of a multi-folded plate horizontal plug-flow structure.
Further preferably, the heterogeneous fenton reaction zone in the heterogeneous fenton reaction system contains a catalyst; the concentration of the catalyst is more than or equal to 3 g/L; still more preferably, the concentration of the catalyst is more than or equal to 4 g/L; even more preferably, the concentration of the catalyst is 4-10 g/L; the catalyst can be a conventional Fenton catalyst.
Further preferably, in the heterogeneous fenton reaction system, an aeration pipeline is arranged at the bottom of the heterogeneous fenton reaction zone.
Further preferably, in the heterogeneous fenton reaction system, the top of the heterogeneous fenton reaction zone is provided with a stirrer, so that the sufficient flowing state of the catalyst in the heterogeneous fenton reaction zone is ensured.
Further preferably, in the heterogeneous Fenton reaction system, the hydraulic retention time of the heterogeneous Fenton reaction zone is 2-6 h; still further preferably, the hydraulic retention time of the heterogeneous Fenton reaction zone is 3-5 h; even more preferably, the hydraulic retention time of the heterogeneous Fenton reaction zone is 4 h.
Further preferably, in the heterogeneous Fenton reaction system, H is added into the heterogeneous Fenton reaction zone2O2，H2O2The molar mass ratio of the addition amount to the COD is (0.8-1.2) to 1; still further preferably, H2O2The molar mass ratio of the addition amount to the COD is 1: 1.
Preferably, in the heterogeneous Fenton reaction system, a reflux pipeline is arranged between the intermediate precipitation zone and the heterogeneous Fenton reaction zone, the intermediate precipitation zone partially refluxes the catalyst to a water inlet at the front section of the heterogeneous Fenton reaction zone, and the reflux amount of the catalyst is 6-15%; still more preferably, the reflux amount of the catalyst is 8 to 12%; still more preferably, the reflux amount of the catalyst is 10%.
Further preferably, in the heterogeneous Fenton reaction system, the hydraulic retention time of the intermediate settling zone is 0.5-2 h; still further preferably, the hydraulic retention time of the intermediate settling zone is 1-1.5 h; even more preferably, the hydraulic retention time of the intermediate settling zone is 1 h.
Further preferably, in the heterogeneous Fenton reaction system, the pH value of the primary alkali adjusting area is 7-8.5; still further preferably, the pH value of the first-stage alkali adjusting area is 7-8; even more preferably, the pH of the first alkalizing region is 7.5.
Further preferably, in the heterogeneous Fenton reaction system, the hydraulic retention time of the primary alkali regulation area is 3-8 min; still further preferably, the hydraulic retention time of the primary alkali regulation area is 4-6 min; still more preferably, the hydraulic retention time of the primary soda adjusting zone is 5 min.
Further preferably, in the heterogeneous Fenton reaction system, a stirring device is arranged in the coagulating sedimentation area; PFS (polyferric sulfate) with the mass fraction of 10% is used as a coagulant, and PAM (polyacrylamide) with the mass fraction of 2 per mill is used as a flocculant.
Further preferably, in the heterogeneous Fenton reaction system, the coagulating sedimentation zone is multi-lattice fractional sedimentation.
Preferably, in the heterogeneous Fenton reaction system, a reflux pipeline is arranged between the coagulating sedimentation area and the acid regulating area, the coagulating sedimentation area partially refluxes the catalyst to the acid regulating area, and the reflux amount of the catalyst is 3-12%; still more preferably, the reflux amount of the catalyst is 4 to 10%; more preferably, the amount of catalyst reflux is from 5 to 10%.
Further preferably, in the heterogeneous Fenton reaction system, the hydraulic retention time of a coagulation and precipitation zone is 30-50 min; still further preferably, the hydraulic retention time of the coagulating sedimentation zone is 35-45 min; even more preferably, the hydraulic retention time of the coagulation sedimentation zone is 40 min.
A wastewater treatment method for treating wastewater by adopting the Fenton-based wastewater treatment system specifically comprises the following steps: the wastewater enters the advanced treatment system after sequentially passing through the pretreatment system and the biochemical system, concentrated water of a membrane filtration system in the advanced treatment system enters the heterogeneous Fenton reaction system, effluent of the heterogeneous Fenton reaction system enters the hydrolysis acidification tank, and effluent of the membrane filtration system in the advanced treatment is discharged outside.
Preferably, the wastewater quality meets at least one of the following conditions: COD is less than or equal to 2000 mg/L; SS is less than or equal to 800 mg/L; TP is less than or equal to 6 mg/L; NH (NH)3-H is less than or equal to 240 mg/L; TN is less than or equal to 300 mg/L; biodegradability is less than or equal to 0.3.
Preferably, in the wastewater treatment method, COD in the wastewater quality is less than or equal to 2000 mg/L; further preferably, in the fenton-based wastewater treatment method, COD in the wastewater quality is less than or equal to 1500 mg/L; still further preferably, in the fenton-based wastewater treatment method, COD in the wastewater quality is less than or equal to 1000 mg/L.
Preferably, the biodegradability of the wastewater quality is less than or equal to 0.3; further preferably, the biodegradability of the wastewater quality is less than or equal to 0.25 in the Fenton-based wastewater treatment method; still more preferably, in the fenton-based wastewater treatment method, the biodegradability of the wastewater quality is less than or equal to 0.2.
Preferably, in the wastewater treatment method, the pH value of the effluent of the heterogeneous Fenton reaction system entering the hydrolysis acidification tank is 6-7.
The invention has the beneficial effects that:
the Fenton-based wastewater treatment system provided by the invention is used for treating wastewater, has the advantages of stable treatment effect, simplicity and convenience in operation and good controllability, and is easy to realize industrial application; the effluent quality meets the first-class A standard of pollutant discharge Standard of urban wastewater treatment plant (GB 18918-2002); the operation cost is low.
The invention improves the traditional AO pool, controls aeration and dissolved oxygen, reduces carbon source and aeration energy consumption; the invention adopts a directional membrane separation system, selectively intercepts organic matters, effectively controls membrane pollution and ensures that the effluent stably reaches the standard.
Compared with a Fenton system in a main process section, the Fenton-like reaction system is connected to a treatment process section of the membrane concentrated solution, so that the sewage treatment capacity can be greatly reduced, refractory organic matters in industrial wastewater are treated in a centralized manner, the treatment efficiency is improved, and the operation cost is reduced; compared with the traditional Fenton, the heterogeneous Fenton-like process is adopted, the production amount of the hazardous waste iron mud can be reduced by 90 percent, the operation cost is lower, and H is higher2O2The utilization rate is high.
Drawings
Fig. 1 is a flow diagram of a fenton-based wastewater treatment process.
Fig. 2 is a diagram of an embodiment of a fenton-based wastewater treatment system.
The attached figure 2 marks:
100-a grit chamber, 110-a grid, 120-a grit zone, 200-a homogenizing tank, 300-a first-stage air flotation tank, 400-a hydrolysis acidification tank, 500-AO tank, 510-an anaerobic zone, 520-an aerobic zone, 600-a first-stage sedimentation tank, 700-a contact oxidation tank, 800-a second-stage sedimentation tank, 900-a second-stage air flotation tank, 1000-a biological activated carbon filter tank, 1100-a membrane filtration system, 1200-a heterogeneous Fenton reaction system, 1210-a acidity regulation zone, 1220-a heterogeneous Fenton reaction zone, 1230-a middle sedimentation zone, 1240-a first-stage alkalinity regulation zone, 1250-a coagulation sedimentation zone and 1300-a disinfection tank.
Detailed Description
The embodiments of the present invention will be described in detail below, and the embodiments described by referring to the drawings are exemplary only for the purpose of illustrating the present invention and are not to be construed as limiting the present invention.
The present invention will be described in further detail with reference to specific examples.
In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "connected" and "connected" are to be interpreted broadly, e.g., as a fixed connection, a detachable connection, or an integral connection; can be mechanically or electrically connected; they may be directly connected to each other, indirectly connected to each other through an intermediate member, or connected to each other through the inside of two members. The specific meanings of the above terms in the present invention can be understood by those skilled in the art according to specific situations.
The starting materials, reagents or equipment used in the examples are, unless otherwise specified, either conventionally commercially available or may be obtained by methods known in the art. Unless otherwise indicated, the testing or testing methods are conventional in the art.
As shown in fig. 1, the wastewater treatment system based on fenton comprises a pretreatment system, a hydrolysis acidification tank, an AO tank, a primary sedimentation tank, a contact oxidation tank, a secondary sedimentation tank, a secondary air flotation tank, a biological activated carbon filter tank, a membrane filtration system and a heterogeneous fenton reaction system which are connected in sequence, wherein concentrated water of the membrane filtration system enters the heterogeneous fenton reaction system, and discharged water of the membrane filtration system is discharged outside.
A fenton-based wastewater treatment system according to an embodiment of the present invention will be described with reference to fig. 2.
The wastewater treatment system based on Fenton in the embodiment of the invention comprises a grit chamber 100, a homogenizing tank 200, a primary air floatation tank 300, a hydrolysis acidification tank 400, an AO tank 500, a primary sedimentation tank 600, a contact oxidation tank 700, a secondary sedimentation tank 800, a secondary air floatation tank 900, a biological activated carbon filter 1000, a membrane filtration system 1100, a heterogeneous Fenton reaction system 1200 and a disinfection tank 1300.
In the fenton-based wastewater treatment system according to the embodiment of the present invention, the grit chamber 100 includes a grid 110 and a grit zone 120.
In a fenton-based wastewater treatment system according to an embodiment of the present invention, the AO-tank 500 includes an anaerobic zone 510 and an aerobic zone 520.
In the fenton-based wastewater treatment system according to the embodiment of the present invention, the heterogeneous fenton reaction system 1200 includes an acid adjusting zone 1210, a heterogeneous fenton reaction zone 1220, an intermediate precipitation zone 1230, a primary alkali adjusting zone 1240, and a coagulation precipitation zone 1250.
As shown in fig. 2, in an embodiment of the fenton-based wastewater treatment system, wastewater first enters a grit chamber 100, is trapped by a grid 110 to remove hair fibers and flocculent impurities in industrial wastewater, and is removed with sand through a grit zone 120; the effluent of the grit chamber 100 enters a homogenizing tank 200, and the quality and quantity of the wastewater are adjusted in the homogenizing tank 200; the water discharged from the homogenizing tank 200 enters a first-stage air floatation tank 300 to remove particles, colloid and the like in the water body; the water discharged from the first-stage air floatation tank 300 enters a hydrolysis acidification tank 400 for hydrolysis; the effluent of the hydrolysis acidification tank 400 enters an anaerobic zone 510 of the AO tank 500, the effluent of the anaerobic zone 510 enters an aerobic zone 520, the wastewater in the aerobic zone 520 flows back to the anaerobic zone 510, the effluent of the aerobic zone 520 enters a primary sedimentation tank 600, and part of sludge in the primary sedimentation tank 600 flows back to the anaerobic zone 510 of the AO tank 500; the effluent of the primary sedimentation tank 600 enters a contact oxidation tank 700, the effluent of the contact oxidation tank 700 enters a secondary sedimentation tank 800, the effluent of the secondary sedimentation tank 800 enters a secondary air flotation tank 900, the effluent of the secondary air flotation tank 900 enters a biological activated carbon filter 1000, and the effluent of the biological activated carbon filter 1000 enters a membrane filtration system 1100 and adopts a nanofiltration membrane; the concentrated water of the membrane filtration system 1100 enters a heterogeneous Fenton reaction system 1200, sequentially passes through an acid adjusting zone 1210, a heterogeneous Fenton reaction zone 1220, an intermediate precipitation zone 1230, a primary alkali adjusting zone 1240 and a coagulating sedimentation zone 1250, and the effluent of the coagulating sedimentation zone 1250 enters a hydrolysis acidification tank 400; the effluent of the membrane filtration system 1100 enters a disinfection tank 1300, and the effluent of the disinfection tank 1300 is discharged after reaching the standard.
Example 1
The industrial sewage plant of Hunan Yueyang is located in the Yueyang Yunxi industrial area, and the design scale is 5000m3The wastewater of the chemical industry park adopts the common sewage treatment process of flocculation, hydrolytic acidification, AO biochemistry, air flotation, ozone oxidation treatment and BAF tank in advance, the medicament consumption is large, the operation cost is high, the ozone system is unstable, and the effluent water is dischargedThe COD fluctuation is large, the system has poor water quality and water quantity impact resistance, and the effluent can not meet the first-level A standard of pollutant discharge standard of urban sewage treatment plants.
The wastewater treatment process of the chemical industrial park is improved, the wastewater treatment system based on Fenton is adopted to treat wastewater, and the specific water quality parameters of the inlet water are as follows: COD less than or equal to 1000mg/L, BOD5≤200mg/L、pH＝6-9、SS≤400mg/L、TP≤3mg/L、NH3H is less than or equal to 120mg/L, TN and less than or equal to 150mg/L, petroleum is less than or equal to 10mg/L, and biodegradability is less than or equal to 0.2; the wastewater sequentially passes through a wastewater treatment system shown in the attached figure 2, and the process parameters of each device are as follows:
a grit chamber: a plate-type fine grid with 3mm grid gaps is adopted to intercept and remove hair fibers and flocculent impurities in the industrial sewage, 2 aeration grit chambers connected in parallel are adopted, and the aeration rate is 0.1m3/m3The sewage and the retention time are 6-8 min;
homogenizing in a homogenizing tank: by adopting the rectangular design of 2:1, the effluent of the grit chamber flows into the homogenizing tank after being metered, and the sewage is subjected to water quality and water quantity regulation in the homogenizing tank, so that the load impact of the subsequent process can be reduced when the water quality and water quantity fluctuate greatly;
a first-stage air floatation tank: adopting cavitation air flotation process to carry out physicochemical treatment, using 10% PAC (polyaluminium chloride) and 2 ‰ PAM (polyacrylamide) as reagents, and having air flotation section load of 6m3/(h·m2) The retention time is 20min, and particulate matters, colloid and the like in the water body are removed;
a hydrolysis acidification pool: adopting hydraulic stirring, uniformly distributing water at the bottom of the pool, and simultaneously arranging a fiber rope filler with the outer diameter of 45mm, wherein the filler density is 30m/m3The water power cutting function is strengthened to waste water, the hydrolytic acidification capability is improved, macromolecular organic matters which are difficult to be biochemically degraded are decomposed into micromolecular organic matters which are easy to biochemically degrade in a hydrolytic acidification tank, and the biodegradability of sewage is improved.
An AO cell: the residence time of the anaerobic zone and the aerobic zone is respectively 12 hours and 36 hours, the sludge amount of the anaerobic zone is 8000mg/L, the sludge amount of the aerobic zone is 7000mg/L, the dissolved oxygen of the aerobic zone is controlled below 2mg/L according to the simulation technology, the internal reflux ratio is 250 percent, and the COD, ammonia nitrogen and the like in water are effectively reduced through anaerobic denitrification and aerobic nitrification;
a first-stage sedimentation tank: a middle-in and periphery-out radial flow sedimentation tank is adopted, the residence time of a sludge zone is 1h, the residence time of a clarification zone is 3h, a mud bucket is arranged at the center of the bottom of the tank, the slope of the slope towards the bottom of the mud bucket is 0.1, the precipitated sludge partially flows back to an anoxic tank of a biochemical tank, and the rest sludge is sent to the sludge tank;
a contact oxidation pond: adopts a grid rectangular structure, adopts fiber filler and is vertically arranged, the filler layer is 3m, the dissolved oxygen is 3mg/L, and the residual COD and BOD can be effectively removed5；
A secondary sedimentation tank: PAC is used as a coagulant, PAM is used as a flocculant, the adding amount is respectively 20mg/L and 0.3mg/L, organic matters and chromaticity which can not be degraded at the biochemical tail end are removed, the water body is improved, and the water quality is purified;
a secondary air floatation tank: the physical and chemical treatment is carried out by adopting a cavitation air flotation process, and the load of an air flotation section is 4m3/(h·m2) The retention time is 15min, and suspended matters in the water body are further removed;
a biological activated carbon filter: the bulk density of the columnar activated carbon is 480g/L, the dissolved oxygen of inlet water is 6mg/L, the requirement of biodegradation on the dissolved oxygen is fully ensured, the height of a carbon bed is 2.5m, the contact time of an empty bed is 15min, and the turbidity of outlet water is less than 0.2 NTU;
a membrane filtration system: the maximum operating pressure (bar) is 41bar, the salt rejection rate is lower than 50 percent, the pH range is 3.0-9.0, the water yield is 85-90 percent, and the molecular weight cutoff is 150-200 Da;
heterogeneous fenton-like system: the system consists of an acid regulating area, a heterogeneous Fenton reaction area, an intermediate sedimentation tank area, a primary alkali regulating area and a coagulating sedimentation area, wherein the retention time of each area is respectively 10min, 4H, 1H, 5min and 40min, the initial pH of the Fenton reaction is 3.0, and H is2O2The molar mass ratio of the adding amount to COD is 1:1, the reflux rate of the catalyst in the intermediate precipitation zone is 10%, and the reflux rate of the coagulation precipitation zone is 10%;
in the embodiment, a solid-phase iron-based catalyst is adopted in the heterogeneous Fenton area, the catalyst is a conventional Fenton catalyst, the adding amount is 4g/L, and the repeated utilization rate is 10-20 times.
The external drainage water quality indexes are as follows: COD is less than or equal to40mg/L、BOD5≤10mg/L、pH＝6-9、SS≤5mg/L、TP≤0.5mg/L、NH3H is less than or equal to 5mg/L, TN and less than or equal to 8mg/L, petroleum is less than or equal to 1mg/L, the standard reaches the first-class A standard of pollutant discharge standard of urban sewage treatment plants, and the operation cost of the whole system is relatively reduced from 16.8 yuan/ton to 11.6 yuan/ton.
Although the present invention has been described with reference to the above embodiments, it should be understood that the present invention is not limited thereto, and various changes, substitutions, and alterations can be made without departing from the spirit and scope of the invention.

Claims (10)

1. A Fenton-based wastewater treatment system is characterized by comprising a pretreatment system, a biochemical system and an advanced treatment system which are connected in sequence;
the pretreatment system comprises a grit chamber and a homogenizing tank or a primary air floatation tank which are connected in sequence;
the biochemical system comprises a hydrolysis acidification tank, an AO tank and a primary sedimentation tank which are connected in sequence;
the advanced treatment system comprises a contact oxidation tank, a secondary sedimentation tank, a secondary air flotation tank, a biological activated carbon filter tank, a membrane filtration system and a heterogeneous Fenton reaction system which are connected in sequence; and a connecting pipeline is arranged between the heterogeneous Fenton reaction system and the hydrolysis acidification tank.
2. A fenton-based wastewater treatment system according to claim 1, wherein the pretreatment system comprises a grit chamber, a homogenizing chamber and a primary air flotation chamber which are connected in sequence.
3. A fenton-based wastewater treatment system according to claim 1, wherein the AO-cell meets at least one of the following conditions: the sludge concentration is more than or equal to 5000 mg/L; the content of dissolved oxygen is less than or equal to 2 mg/L; the internal reflux ratio is 200-300%.
4. A fenton-based wastewater treatment system according to claim 1, wherein the membrane filtration system has a membrane cut-off of 100 and 300 Da.
5. A fenton-based wastewater treatment system according to claim 1, wherein the heterogeneous fenton reaction system comprises an acid regulation zone, a heterogeneous fenton reaction zone, an intermediate precipitation zone, a primary alkali regulation zone and a coagulation precipitation zone which are connected in sequence.
6. A Fenton-based wastewater treatment system according to claim 5, wherein the heterogeneous Fenton reaction zone comprises a catalyst; the concentration of the catalyst is more than or equal to 3 g/L.
7. A Fenton-based wastewater treatment system according to claim 5, wherein a return line is provided between the intermediate settling zone and the heterogeneous Fenton reaction zone.
8. A Fenton-based wastewater treatment system according to claim 5, wherein a return line is provided between the coagulation sedimentation zone and the acid regulation zone.
9. A wastewater treatment method characterized by treating wastewater using the fenton-based wastewater treatment system according to any one of claims 1 to 8.
10. The method of claim 9, wherein the wastewater quality satisfies at least one of the following conditions: COD is less than or equal to 2000 mg/L; SS is less than or equal to 800 mg/L; TP is less than or equal to 6 mg/L; NH (NH)3-H is less than or equal to 240 mg/L; TN is less than or equal to 300 mg/L; biodegradability is less than or equal to 0.3.
CN202111195991.XA 2021-10-14 2021-10-14 Fenton-based wastewater treatment system and method Pending CN113860644A (en)

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CN213446415U (en) * 2020-08-06 2021-06-15 中建环能科技股份有限公司 Reactor and wastewater treatment system
CN216639199U (en) * 2021-10-14 2022-05-31 广州华浩能源环保集团股份有限公司 Effluent disposal system based on fenton

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