CN114853285A - High-standard sewage treatment process for treating seaweed processing wastewater - Google Patents
High-standard sewage treatment process for treating seaweed processing wastewater Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 45
- 230000008569 process Effects 0.000 title claims abstract description 43
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- 239000002351 wastewater Substances 0.000 title claims abstract description 26
- 238000012545 processing Methods 0.000 title claims abstract description 24
- 241001474374 Blennius Species 0.000 title claims abstract description 17
- 238000011282 treatment Methods 0.000 title claims abstract description 14
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 32
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 25
- 230000003647 oxidation Effects 0.000 claims abstract description 20
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 20
- 238000009300 dissolved air flotation Methods 0.000 claims abstract description 5
- 230000014759 maintenance of location Effects 0.000 claims description 26
- 238000004062 sedimentation Methods 0.000 claims description 19
- 230000003197 catalytic effect Effects 0.000 claims description 13
- 238000001914 filtration Methods 0.000 claims description 13
- 238000004659 sterilization and disinfection Methods 0.000 claims description 12
- 241000195493 Cryptophyta Species 0.000 claims description 8
- 238000005273 aeration Methods 0.000 claims description 8
- 229920002401 polyacrylamide Polymers 0.000 claims description 5
- 239000002245 particle Substances 0.000 claims description 4
- 238000000926 separation method Methods 0.000 claims description 4
- 238000005189 flocculation Methods 0.000 claims description 3
- 230000016615 flocculation Effects 0.000 claims description 3
- 238000011221 initial treatment Methods 0.000 claims description 3
- 239000000463 material Substances 0.000 claims description 3
- 230000005855 radiation Effects 0.000 claims description 3
- 230000035484 reaction time Effects 0.000 claims description 3
- 238000002834 transmittance Methods 0.000 claims description 3
- 150000001450 anions Chemical class 0.000 claims 1
- 238000012360 testing method Methods 0.000 abstract description 12
- 238000004519 manufacturing process Methods 0.000 abstract description 7
- 230000004888 barrier function Effects 0.000 abstract description 2
- 230000007774 longterm Effects 0.000 abstract description 2
- 238000012423 maintenance Methods 0.000 abstract description 2
- IXPNQXFRVYWDDI-UHFFFAOYSA-N 1-methyl-2,4-dioxo-1,3-diazinane-5-carboximidamide Chemical compound CN1CC(C(N)=N)C(=O)NC1=O IXPNQXFRVYWDDI-UHFFFAOYSA-N 0.000 description 7
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- 229960001126 alginic acid Drugs 0.000 description 3
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- 150000004781 alginic acids Chemical class 0.000 description 3
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- 239000003344 environmental pollutant Substances 0.000 description 3
- 231100000719 pollutant Toxicity 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 125000000129 anionic group Chemical group 0.000 description 2
- 238000006065 biodegradation reaction Methods 0.000 description 2
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- 229910000360 iron(III) sulfate Inorganic materials 0.000 description 2
- 239000010841 municipal wastewater Substances 0.000 description 2
- 238000002791 soaking Methods 0.000 description 2
- 238000000108 ultra-filtration Methods 0.000 description 2
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
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- OKHHGHGGPDJQHR-YMOPUZKJSA-L calcium;(2s,3s,4s,5s,6r)-6-[(2r,3s,4r,5s,6r)-2-carboxy-6-[(2r,3s,4r,5s,6r)-2-carboxylato-4,5,6-trihydroxyoxan-3-yl]oxy-4,5-dihydroxyoxan-3-yl]oxy-3,4,5-trihydroxyoxane-2-carboxylate Chemical compound [Ca+2].O[C@@H]1[C@H](O)[C@H](O)O[C@@H](C([O-])=O)[C@H]1O[C@H]1[C@@H](O)[C@@H](O)[C@H](O[C@H]2[C@H]([C@@H](O)[C@H](O)[C@H](O2)C([O-])=O)O)[C@H](C(O)=O)O1 OKHHGHGGPDJQHR-YMOPUZKJSA-L 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
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- 239000000084 colloidal system Substances 0.000 description 1
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- 229910052757 nitrogen Inorganic materials 0.000 description 1
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- 239000000546 pharmaceutical excipient Substances 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
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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
- C02F1/30—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
- C02F1/52—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
- C02F1/72—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
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/26—Nature of the water, waste water, sewage or sludge to be treated from the processing of plants or parts thereof
-
- 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
- C02F3/302—Nitrification and denitrification treatment
-
- 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
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/30—Wastewater or sewage treatment systems using renewable energies
- Y02W10/37—Wastewater or sewage treatment systems using renewable energies using solar energy
Abstract
A sewage treatment process for treating seaweed processing wastewater with high standard belongs to the technical field of municipal sewage treatment. Based on the difficulties that COD in the seaweed wastewater has high concentration, low proportion of biodegradable COD, and high hydrophilicity, stability and gelling property, I determines the process flow and process parameters based on the long-term production data of the current water plant and repeated small and medium test tests. Through pilot test, the process route and the process parameters of the application are obtained. The flow and parameter setting of the dissolved air flotation process and the ozone oxidation process break through the barrier that no parameter can be used for reference in the prior art, and the purposes that the project investment and operation and maintenance cost are economical and reasonable and the effluent stably reaches the standard can be realized only by mutually matching parameters of all process links in the complete process flow of the project.
Description
The technical field is as follows:
belongs to the technical field of municipal sewage treatment.
Background art:
the waste water from seaweed processing enterprises is discharged after being pretreated by each enterprise and meeting the industrial standard. Some indexes in the discharge standard of the seaweed processing industry do not meet the first-class A standard of discharge standard of pollutants for municipal wastewater treatment plants (GB18918-2002), and if the pollutants are directly discharged into natural water, the water environment pollution is caused. Therefore, under the current situation, each enterprise discharges the seaweed processing wastewater into a municipal sewage pipe network, mixes the seaweed processing wastewater with domestic sewage, and then enters a municipal sewage treatment plant for further treatment. At present, the municipal sewage plant adopts an AAO biological nitrogen and phosphorus removal, high-efficiency sedimentation tank and active sand filter tank advanced treatment process, and the quality of the outlet water is designed to reach the first-class A standard of pollutant discharge Standard of municipal sewage plant (GB 18918-2002).
Due to the needs of urban development and improvement of sewage resource utilization rate, the current water plant needs to be subjected to upgrading, the effluent of the sewage plant meets the IV-type standard in the quality standard of surface water environment (GB3838-2002), and the current water plant treatment process cannot meet the new upgrading requirement. At present, the municipal sewage plant case that the production wastewater of seaweed processing enterprises is mixed in the inlet water is not successfully solved in China to meet the effluent quality standard is used as reference, and the project is a difficult problem to be solved urgently in the field.
The main difficulty lies in the influence of the production wastewater of the seaweed processing enterprises on the standard of the COD of the effluent of the sewage plant. Before the standard is lifted, the COD of the effluent of the municipal sewage plant is less than or equal to 50mg/L, and the effluent of the sewage plant after the standard is lifted meets the condition that the COD is less than or equal to 30 mg/L.
The product of seaweed processing enterprises is alginic acid or sodium alginate, is mainly used as drugs for Gaiweiping and the like, is also used as excipient, adhesive, stabilizer and the like of tablets, and is commonly used as thickening agent and emulsifier in food and cosmetics.
The sodium alginate processing process is a pretreatment process, namely soaking the seaweed in water to remove impurities; then, through a digestion conversion process, converting insoluble sodium alginate into soluble sodium alginate by using alkali liquor; diluting and floating to obtain pure glue solution, filtering, calcification to convert sodium alginate into calcium alginate, extracting in water, decalcifying in decalcification system to obtain alginic acid, adding alkali to convert alginic acid into sodium alginate if sodium alginate is required, removing pigment, oven drying, and granulating.
The production process mainly comprises the steps of soaking, digesting, cleaning and calcification, and the water discharge is large, and the actual discharged COD peak value of each enterprise is over 1400-1500 mg/L. The waste water has the characteristics of unique thickening property, hydrophilicity, stability, gelling property and the like.
Through detection, the alga processing wastewater accounts for 35-45% of the current situation in the sewage plant inlet water, and other inlet water is domestic sewage, so that the COD of the project has the following characteristics compared with the conventional municipal sewage:
1) high COD content and high proportion of COD which is difficult to biodegrade. Before the wastewater is mixed into the seaweed processing wastewater, the COD peak value of the pure municipal wastewater is 450mg/L (the highest value of 90% probability of the daily average value in a production report), wherein the proportion of the difficultly biodegradable COD is less than 10%; after the seaweed processing wastewater is mixed, the peak value of COD is up to 840mg/L (the highest value of 90% probability of the daily mean value in a production report), the proportion of the difficultly biodegradable COD is increased to 20%, and the proportion of the granular difficultly biodegradable COD in the wastewater is more than 13%.
2) The COD hydrophilicity, the stability and the gelling property are increased, the COD biodegradation difficulty is high, and not only longer biodegradation time is needed, but also advanced oxidation and other modes are needed.
Disclosure of Invention
Based on the difficulties that COD in the seaweed wastewater has high concentration, low proportion of biodegradable COD, and high hydrophilicity, stability and gelling property, I determines the process flow and process parameters based on the long-term production data of the current water plant and repeated small and medium test tests. Through pilot test, the process route and the process parameters of the application are obtained. The flow and parameter setting of the dissolved air flotation process and the ozone oxidation process break through the barrier that no parameter can be used for reference in the prior art, and the purposes that the project investment and operation and maintenance cost are economical and reasonable and the effluent stably reaches the standard can be realized only by mutually matching parameters of all process links in the complete process flow of the project.
A high-standard sewage treatment process for treating seaweed processing wastewater is characterized by comprising the following steps:
municipal sewage mixed with the algae processing wastewater, wherein the volume of the algae processing wastewater accounts for 35-45%, and the rest is domestic sewage, and the municipal sewage and the algae processing wastewater sequentially pass through a pretreatment system → a biochemical system → a mixed sedimentation filtration system → a catalytic oxidation system → a disinfection system.
The components, technological parameters and functions of each system are as follows:
1) a pretreatment system:
the primary treatment system comprises the following components: coarse grid → lift pump station → medium and fine grids → aeration grit chamber → dissolved air floatation tank
Core parameters:
the grid gap of the coarse grid is 20mm, and the flow velocity of the passing grid under the maximum flow is 0.6-1.0 m/s;
the grid gap of the middle grid is 10mm, and the flow speed of the passing grid under the maximum flow is 0.6-1.0 m/s;
the grid gap of the fine grid is 3mm, and the flow velocity of the passing grid under the maximum flow is 0.6-1.0 m/s;
the aerated grit chamber stays for 5.0min at the maximum flow rate, and the horizontal flow rate at the maximum flow rate is 0.06-0.10 m/s;
the surface load of the separation area under the maximum flow of the dissolved air flotation tank is 20-30m 3 /m 2 H, the ratio of the amount of the backflow water entering the dissolved air tank for pressurizing dissolved air to the amount of the treated water is 10%, the reaction time of the flocculation zone is 11min, the dosage of a required medicament PFS (PFS is polymeric ferric sulfate with the effective content of more than or equal to 21%) is 175-205mg/L, and the dosage of anionic PAM is 0.27-0.44 mg/L.
2) A biochemical system:
consists of a biological pond and a rectangular sedimentation tank with a periphery inlet and a periphery outlet.
Core parameters:
the biological pond is sequentially provided with an anaerobic zone, a first anoxic zone, a first aerobic zone, an anoxic zone, a second anoxic zone and a second aerobic zone according to the water flow direction. The total hydraulic retention time is 24.0h, the hydraulic retention time of the anaerobic zone is 1.5h, the hydraulic retention time of the first anoxic zone is 5.0h, the hydraulic retention time of the first aerobic zone is 13.5h, the hydraulic retention time of the anoxic zone is 0.5h, the hydraulic retention time of the second anoxic zone is 3.0h, and the hydraulic retention time of the second aerobic zone is 0.5 h.
The periphery is put into a rectangular secondary sedimentation tank, the surface load under the average flow is 0.82-0.91 m 3 The hydraulic retention time is 4.0 h.
3) The mixed sedimentation filtering system consists of a high-efficiency sedimentation tank and a deep bed filtering tank;
core parameters:
the surface load of the maximum flow rate of the inclined pipe area of the high-efficiency sedimentation tank is 18.2-21m 3 /(m 2 .h)。
The deep bed filter adopts spherical ceramsite filter materials with the particle size of 2.0mm, the thickness of a filter layer is 1.5m, and the filtering speed under the average flow is 6.0-6.40 m/h.
4) Advanced oxidation system
An ozone catalytic oxidation contact tank is adopted, the ozone catalytic oxidation contact tank is provided with 3 stages, and the tank capacity is distributed in each stage according to the ratio of 2:1: 1; the hydraulic retention time under the average flow is 60min, the effective water depth of the contact pool is 6.0m, and the ozone adding amount is 15-22.5 mg/l.
5) Disinfection system
By adopting the ultraviolet disinfection channel process, the ultraviolet transmittance of the ultraviolet disinfection channel is not less than 65 percent, and the radiation dose is ensured to be more than 30mJ/cm 2 ) Ultraviolet irradiation time 20 s.
Detailed Description
Municipal sewage mixed with the algae processing wastewater (the algae processing wastewater accounts for 35-45% and the rest is domestic sewage) → a pretreatment system → a biochemical system → a mixed precipitation filtration system → a catalytic oxidation system → a disinfection system.
The components, technological parameters and functions of each system are as follows:
1) a pretreatment system:
the primary treatment system comprises the following components: coarse grid → lift pump station → medium and fine grids → aeration grit chamber → dissolved air floatation tank
Core parameters:
the grid gap of the coarse grid is 20mm, and the flow velocity of the passing grid under the maximum flow is 0.6-1.0 m/s;
the grid gap of the middle grid is 10mm, and the flow speed of the passing grid under the maximum flow is 0.6-1.0 m/s;
the grid gap of the fine grid is 3mm, and the flow velocity of the passing grid under the maximum flow is 0.6-1.0 m/s;
the aerated grit chamber stays for 5.0min at the maximum flow rate, and the horizontal flow rate at the maximum flow rate is 0.06-0.10 m/s;
the surface load of the separation area under the maximum flow of the dissolved air flotation tank is 20-30m 3 /m 2 H, the ratio of the amount of the backflow water entering the dissolved air tank for pressurizing dissolved air to the amount of the treated water is 10%, the reaction time of a flocculation zone is 11min, the dosage of PFS (polymeric ferric sulfate with the effective content being more than or equal to 21%) of the required added medicaments is 175-205mg/L, and the dosage of anionic PAM (polyacrylamide) is 0.27-0.44 mg/L.
The core parameter values of the grating and the aeration grit chamber are based on the years of operation experience of the current water plant, and the core parameter values of the dissolved air floatation tank come from field pilot experiments.
The method can effectively remove small floating and suspended impurities and sand grains (sand grains with the particle size of 0.2mm and the relative density of more than 2.65t/m 3) in the sewage, reduce the probability of blockage and equipment abrasion of subsequent treatment facilities and ensure the stability of a subsequent process system. The air floatation process is mainly responsible for removing part of colloid and difficultly-degraded COD in the sewage, thereby reducing the COD amount entering a biochemical system and saving the capacity of a biochemical tank and the aeration power consumption.
The removal rate of COD in the pretreatment process section is about 60-70%, and when the COD of the inlet water is 610-840mg/L, the COD of the outlet water is 252-336 mg/L.
The current situation is that a dissolved air floatation tank is not arranged behind an aeration grit chamber of a water plant. An air floatation process is added behind the aeration sand settling tank and in front of the biochemical tank, so that a part of granular refractory COD can be removed in advance, the tank capacity of the biochemical section is reduced, the aeration energy consumption of the biochemical tank is saved, and the ozone adding amount of the ozone catalytic oxidation section is saved; and the surface hydraulic load and the chemical dosage of the air floatation are determined through a pilot test.
Compared with the method without adopting the air floatation process, the COD entering the biochemical tank is reduced to 252-336 mg/L from 549-756, and the COD entering the ozone catalytic oxidation tank is reduced to 35-45mg/L from 45-55 mg/L.
The pilot test results of the surface hydraulic load and the medicament adding amount of the separation area of the air flotation tank are as follows:
along with the reduction of the hydraulic load of the air floatation tank and the increase of the dosage of the medicament, the removal rate of COD in the process section is gradually increased and the COD is dischargedThe proportion of the COD difficult to degrade in the water COD is gradually reduced. When the hydraulic load is 20-30.3m 3 /m 2 H, the dosage of the medicament is 175-205mg/L, the removal rate of COD by the process section is about 60-70%, and the COD of the effluent of the air floatation tank is 252-336 mg/L, wherein the COD which is difficult to biodegrade is 55-65 mg/L. Further reducing the hydraulic load or increasing the dosage of the medicament, and slowly increasing the removal rate of the difficultly degraded COD; and further reducing COD easily causes the shortage of denitrification carbon source of a biochemical system, and has the problems of carbon source supplement in a living pond and operation cost increase.
2) A biochemical system:
consists of a biological pond and a rectangular sedimentation tank with a periphery inlet and a periphery outlet.
Core parameters:
the biological pond is sequentially provided with an anaerobic zone, a first anoxic zone, a first aerobic zone, an anoxic zone, a second anoxic zone and a second aerobic zone according to the water flow direction. The total hydraulic retention time is 24.0h, the hydraulic retention time of the anaerobic zone is 1.5h, the hydraulic retention time of the first anoxic zone is 5.0h, the hydraulic retention time of the first aerobic zone is 13.5h, the hydraulic retention time of the anoxic zone is 0.5h, the hydraulic retention time of the second anoxic zone is 3.0h, and the hydraulic retention time of the second aerobic zone is 0.5 h.
The periphery is put into a rectangular secondary sedimentation tank, the surface load under the average flow is 0.82-0.91 m 3 The hydraulic retention time is 4.0 h.
The parameters are based on the years of operation experience of the water plant and pilot test data, and the COD of the effluent of the process section is 55-65 mg/L.
3) Mixing and settling filtering system:
consists of a high-efficiency sedimentation tank and a deep bed filter tank.
Core parameters:
the surface load of the inclined pipe area of the high-efficiency sedimentation tank at the maximum flow rate is 18.2-21m 3 /(m 2 .h)。
The deep-bed filter adopts spherical ceramsite filter materials with the particle size of 2.0mm, the thickness of a filter layer is 1.5m, and the filtering speed under the average flow is 6.0-6.40 m/h.
The parameters are based on the years of operation experience of the water plant in the current situation and pilot test data, and the COD of the effluent of the process section is 35-45 mg/L.
4) Advanced oxidation system
Catalytic oxidation contact tank adopting ozone
Core parameters:
the ozone catalytic oxidation contact pool is provided with 3 stages (the pool volume is distributed according to the proportion of 2:1:1 in each stage), the hydraulic retention time under the average flow is 60min, the effective water depth of the contact pool is 6.0m, and the ozone adding amount is 15-22.5 mg/l.
The pilot test is adopted to carry out the necessary selection on the deep bed filter tank post-advanced treatment process, and the comparison is respectively carried out as follows: adding a medium for coagulating sedimentation, adsorbing by activated carbon, adsorbing and filtering by activated coke, MBR, immersed ultrafiltration, ozone contact and catalytic oxidation by ozone:
the COD of the effluent water of the medium coagulating sedimentation, the active carbon, the active coke, the MBR and the immersion type ultrafiltration process can not reach the standard.
In the municipal sewage treatment, for COD which cannot be further difficultly degraded by the process, an ozone contact process is usually considered, but when the ozone addition amount is 15mg/L by adopting the ozone contact process, the COD is not obviously removed, and when the ozone addition amount is further increased to 22.5mg/L, the COD removal amount is only 5mg/L, so that the effluent cannot be guaranteed to stably reach the standard; further increasing the ozone adding amount to be more than 22.5mg/L, and leading the effluent chroma to be suddenly increased and exceed the limit value of the emission standard.
Therefore, in the test, catalyst filler is added, an ozone catalytic oxidation contact process is adopted, the catalyst reacts with ozone to form hydroxyl free radicals with stronger oxidability, and the oxidation effect of the difficultly-degraded COD is improved while the adding amount of ozone is not increased; when the ozone addition amount is 15-22.5 mg/L, COD is removed at 10-15 mg/L, the stable standard of the system effluent can be ensured, and the chromaticity of the effluent is not obviously changed.
5) Disinfection system
Ultraviolet disinfection channel process
Core parameters:
the ultraviolet transmittance of the ultraviolet disinfection channel is not less than 65 percent, and the radiation dose is ensured to reach the national standard (more than 30 mJ/cm) 2 ) Ultraviolet irradiation time 20 s.
Claims (1)
1. A high-standard sewage treatment process for treating seaweed processing wastewater is characterized by comprising the following steps:
municipal sewage mixed with the algae processing wastewater, wherein the volume of the algae processing wastewater accounts for 35-45%, and the rest is domestic sewage, and the municipal sewage and the algae processing wastewater sequentially pass through a pretreatment system → a biochemical system → a mixed sedimentation filtration system → a catalytic oxidation system → a disinfection system;
the components and technological parameters of each system are as follows:
1) a pretreatment system:
the primary treatment system comprises the following components: coarse grids → lift pump station → middle and fine grids → aeration grit chamber → dissolved air floatation tank;
the grid gap of the coarse grid is 20mm, and the flow velocity of the passing grid under the maximum flow is 0.6-1.0 m/s;
the grid gap of the middle grid is 10mm, and the flow speed of the passing grid under the maximum flow is 0.6-1.0 m/s;
the grid gap of the fine grid is 3mm, and the flow velocity of the passing grid under the maximum flow is 0.6-1.0 m/s;
the aerated grit chamber stays for 5.0min at the maximum flow rate, and the horizontal flow rate at the maximum flow rate is 0.06-0.10 m/s;
the surface load of the separation area under the maximum flow of the dissolved air flotation tank is 20-30m 3 /m 2 H, the ratio of the amount of the backflow water entering the dissolved air tank for pressurizing dissolved air to the amount of the treated water is 10%, the reaction time of a flocculation zone is 11min, the dosage of PFS (PFS) required to be added is 175-205mg/L, and the dosage of anion PAM (Polyacrylamide) is 0.27-0.44 mg/L;
2) a biochemical system:
consists of a biological tank and a rectangular sedimentation tank with a periphery inlet and a periphery outlet;
the biological pond is sequentially provided with an anaerobic zone, a first anoxic zone, a first aerobic zone, an anoxic zone, a second anoxic zone and a second aerobic zone according to the water flow direction; the total hydraulic retention time is 24.0h, the hydraulic retention time of the anaerobic zone is 1.5h, the hydraulic retention time of the first anoxic zone is 5.0h, the hydraulic retention time of the first aerobic zone is 13.5h, the hydraulic retention time of the anoxic zone is 0.5h, the hydraulic retention time of the second anoxic zone is 3.0h, and the hydraulic retention time of the second aerobic zone is 0.5 h;
the periphery is fed into a rectangular sedimentation tank, the surface load under the average flow is 0.82-0.91 m 3 The water retention time is 4.0 h;
4) the mixed sedimentation filtering system consists of a high-efficiency sedimentation tank and a deep bed filtering tank;
the surface load of the maximum flow rate of the inclined pipe area of the high-efficiency sedimentation tank is 18.2-21m 3 /(m 2 .h)；
The deep bed filter adopts spherical ceramsite filter materials with the particle size of 2.0mm, the thickness of a filter layer is 1.5m, and the filtering speed under the average flow is 6.0-6.40 m/h;
5) advanced oxidation system
An ozone catalytic oxidation contact tank is adopted, the ozone catalytic oxidation contact tank is provided with 3 stages, and the tank capacity is distributed in each stage according to the ratio of 2:1: 1; the hydraulic retention time under the average flow is 60min, the effective water depth of the contact pool is 6.0m, and the ozone adding amount is 15-22.5 mg/l;
6) disinfection system
By adopting the ultraviolet disinfection channel process, the ultraviolet transmittance of the ultraviolet disinfection channel is not less than 65 percent, and the radiation dose is ensured to be more than 30mJ/cm 2 Ultraviolet irradiation time 20 s.
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