CN103787525A - Two-stage biochemical effluent in-depth treatment method for municipal sewage - Google Patents
Two-stage biochemical effluent in-depth treatment method for municipal sewage Download PDFInfo
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- CN103787525A CN103787525A CN201210427652.4A CN201210427652A CN103787525A CN 103787525 A CN103787525 A CN 103787525A CN 201210427652 A CN201210427652 A CN 201210427652A CN 103787525 A CN103787525 A CN 103787525A
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- 238000000034 method Methods 0.000 title claims abstract description 50
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- 238000007254 oxidation reaction Methods 0.000 claims abstract description 25
- 230000003647 oxidation Effects 0.000 claims abstract description 24
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 21
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- 235000008733 Citrus aurantifolia Nutrition 0.000 claims abstract description 14
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- 229920006395 saturated elastomer Polymers 0.000 claims description 6
- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 claims description 4
- 229910000360 iron(III) sulfate Inorganic materials 0.000 claims description 4
- 238000012856 packing Methods 0.000 claims description 4
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- Separation Of Suspended Particles By Flocculating Agents (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The invention discloses a two-stage biochemical effluent in-depth treatment and reuse method for municipal sewage. The method comprises the following treatment steps: (1) lime softening; (2) coagulation and precipitation; (3) oxidation; (4) filtering; and (5) ultrafiltration and reverse osmosis treatment. In the step (3), ozone is used as an oxidant for oxidation, and an adsorbent bed is arranged in an oxidation reactor. The method has the advantages of simple operation process, short flow, low treatment cost, applicability to municipal sewage treatment plant effluent with high contents of COD, chroma and salt, realization of resourceful utilization of sewage and industrial water conservation and accordance with requirements of circular economy, clean production and the like.
Description
Technical field
The present invention relates to a kind of method of advanced treatment of municipal effluent secondary biochemical effluent, be applicable to process the effluent of municipal sewage plant that COD, colourity, hardness and salts contg are higher.
Background technology
City sewage deep treatment reuse is to solve one of effective way of current Urban Water Shortage Problem of Cities.Municipal effluent is that reliable Ecology is stablized, supplied with to a kind of water yield, after conventional biochemical treatment, although BOD
5processed to 10mg/L, even below 5mg/L, but secondary biochemical effluent COD is still up to more than 100mg/L, contains part refractory organic, colourity and inorganic salt, cannot meet reuse and do the water quality requirement of industrial boiler water-supply.
Conventionally adopt " coagulation+clarification+filtration+sterilization " combined method to carry out advanced treatment to municipal wastewater treatment plant secondary biochemical effluent at present, its object is mainly used for suspended substance, the turbidity of water in removal and kills disease carrying germ in water, but the clearance to dissolved matter is lower, can not realize removing of COD, colourity, total dissolved solid and hardness, basicity, this method is not suitable for the Treatment for Reuse of the effluent of municipal sewage plant that COD, colourity and salts contg are higher.In order to guarantee that municipal wastewater treatment plant effluent reuse does industrial water supply,
cN101544448Aa kind of urban sewage recycling is proposed in the method for recirculated cooling water and boiler water feeding, the externally discharged waste water that municipal wastewater treatment plant is met to emission standard after second-stage treatment is sent into MBBR, in MBBR, BOD and ammonia nitrogen are degraded, water outlet enters coagulation, air-dissolving air-float, multi-medium filtering processing successively, and water outlet after treatment is reuse after ultrafiltration and reverse osmosis desalination processing again.The method is before waste water enters two films, to rely on moving-bed membrane bioreactor (MBBR) and add flocculation medicament to remove bio-degradable organic matter and the larger molecular organics in water, make COD, suspended substance and turbidity in water quality meet two film water inlet control requirements, but it is large that MBBR biological treatment is taken up an area, invest high, do not possess the removal means to solubility difficult for biological degradation organic matter, colourity and hardness, basicity, be therefore unsuitable for the Treatment for Reuse of the municipal sewage plant secondary biochemical treatment water outlet higher with trade effluent proportion.
cN1796314Aa kind of city sewage deep treatment method is proposed, by to effluent adopting coagulation and filtration, ozone oxidation, biologic active carbon filtration, reverse-osmosis treated, reach and remove difficult degradation microorganism remaining in municipal wastewater treatment plant secondary biochemical effluent, bacterium, virus, colourity etc., realize the object of water security reuse in municipal administration.But this processing method is mainly applicable to the low concentration wastewater processing of COD≤50mg/L, colourity≤30 degree, is not suitable for and contains the trade effluent that refractory organics COD, colourity and hardness are higher.
cN101182084Apropose combined treating method for reclaimed water reuse, by municipal wastewater factory secondary biochemical effluent being adopted to ozone pre-oxidation coagulation, precipitation, sand filtration, millipore filtration, ozone oxidation, charcoal absorption, disinfecting, realize water reuse in municipal administration.Although but this processing method is selected ozone Oxidation Treatment, but in lower concentration and short residence time(SRT), ozone is difficult to permineralization organism, and do not possess desalination process, therefore, this method is mainly applicable to the municipal effluent secondary biochemical effluent that salts contg is lower, and water outlet conductivity after treatment, total salt cannot meet reuse does the water quality requirement of industrial boiler water-supply.
Based on above analysis, for with the higher municipal sewage plant's secondary biochemical treatment water outlet of trade effluent proportion, because difficult for biological degradation COD, colourity, hardness, basicity, specific conductivity are higher, there is no at present reliable processing reuse, particularly reuse and do the Technology of industrial boiler water-supply.
Summary of the invention
For the deficiencies in the prior art, the present invention proposes a kind of method of municipal wastewater treatment plant secondary biochemical effluent advanced treatment, is applicable to the effluent of municipal sewage plant that COD, colourity, hardness and salts contg are higher.Adopt the water outlet that this treatment process obtains to make industrial boiler water-supply by direct reuse.
A method for municipal effluent secondary biochemical effluent advanced treatment, comprises the softening processing of (1) lime successively; (2) coagulating sedimentation processing; (3) oxide treatment; (4) filtration treatment; (5) processing unit such as ultrafiltration and reverse-osmosis treated, concrete operation step is as follows:
(1) lime is softening processes, and fully mixes in line mixer from the bio-chemical effluent of municipal sewage plant with saturated milk of lime, controls pH of mixed value and reaches 9.5～10.5, makes the HCO in water
3 -with OH
-there is neutralization reaction and form CO
3 2-, with Ca
2+, Mg
2+plasma generates carbonate deposition, in precipitation process of coagulation subsequently, is removed, and has reduced water hardness.Mix water outlet and carry out coagulating sedimentation processing.
(2) coagulating sedimentation processing, the softening composite waste after treatment of step (1) lime directly enters coagulative precipitation tank, under the flocculation agent adding and the effect of remaining lime coagulant aids, the throw out in water and suspended substance to be removed by clarification, clarification and effluent carries out oxide treatment.The pH value of this unit keeps weakly alkaline always, need not regulate.Waste water is 10～30min at the hydraulic detention time of coagulative precipitation tank.Be conventional organic and inorganic type flocculation agent to the flocculation agent adding in coagulative precipitation tank, wherein organic floculant is polyacrylamide, and dosage is 1～5mg/L; Inorganic flocculating agent can adopt bodied ferric sulfate or iron trichloride, and dosage is 10～30mg/L.By this cell processing, the throw out that in waste water, original suspended substance and step (1) produce can obtain deep removal, goes out water suspension≤10 mg/L, turbidity≤5 NTU, goes out the water hardness≤150 mg/L(with CaCO
3meter), basicity≤150 mg/L(is with CaCO
3meter), colourity, COD also obtain part removal simultaneously.
(3) oxide treatment, sends step (2) coagulating sedimentation waste water after treatment into oxidation reactor, and oxygenant is ozone.In oxidation reactor, arrange adsorbent bedly, sorbent material is haydite, gac or hard coal, and particle diameter is 5 ~ 10 mm, and packing ratio is reactor volume 50% ~ 75%.By add adsorbability material in oxidizing reaction, can absorb fast the organism of the difficult for biological degradation in waste water, it is rested in reactor, under alkaline condition, fully carry out oxidizing reaction until permineralization, improve greatly the removal efficiency of COD, and reduced the hydraulic detention time of waste water and the dosage of ozone.Organism on sorbent material generates CO after ozone oxidation
2and H
2o, has reached and has improved water quality and decolouring object; Sorbent material can recover again characterization of adsorption after ozone oxidation regeneration, and after processing, water outlet COD is lower without proceeding biochemical treatment.Detailed process is: after coagulating sedimentation is processed, water outlet enters oxidation reactor by bottom after fully mixing with ozone oxidation agent in line mixer, and the organism of the difficult for biological degradation such as the colourity in waste water is trapped within adsorption layer, and under alkaline condition, ozone forms
.oH can be by organism complete oxidation to CO
2and H
2o, reaches the colourity that removes waste water and the object that improves COD clearance.The ozone of this unit is provided by the ozonizer outside treatment unit, and the dosage of ozone is 5～20 mg/L waste water, is preferably 6～12 mg/L waste water, and the hydraulic detention time of waste water in oxidation reactor is 10 ~ 20min.By this cell processing, the colourity in waste water can remove more than 90%, effluent color dilution≤10 degree; Water outlet COD≤50 mg/L.
(4) filtration treatment, carries out filtration treatment by the water outlet after step (3) absorption ozonize, and after processing, uf processing is carried out in water outlet.Conventional filter plant can be selected in coarse filtration unit, as more medium filter, sand filtration, drift sand strainer or millipore filter etc.By waste water is carried out to filtration treatment, make water outlet SS≤20 mg/L, turbidity≤5 NTU, meet into ultrafiltration and reverse-osmosis treated requirement.
(5) ultrafiltration and reverse-osmosis treated, carries out ultrafiltration and reverse osmosis desalination processing by the water outlet after step (4) filtration treatment, and effluent reuse after treatment does industrial boiler water-supply.Ultrafiltration and reverse osmosis units can be selected conventional ultrafiltration and reverse osmosis equipment.Through step (1)～(4), waste water index after treatment can meet the water inlet index request into ultrafiltration and reverse osmosis, as COD≤50 mg/L, turbidity≤5 NTU, hardness≤150mg/L, basicity≤350mg/L, colourity≤30 degree, after this cell processing, effluent quality can meet reuse comprehensively and does the water quality requirement reuse of industrial boiler water-supply, and can keep the long-term operation of film.
Municipal sewage plant's secondary biochemical effluent that the inventive method is occupied larger proportion take industrial sewage is as object, adopt respectively that lime is softening, coagulating sedimentation, oxide treatment, filtration, ultrafiltration and reverse osmosis combined treatment flow process, treating processes is simple, flow process is short, working cost is low, the rear water outlet of processing can meet reuse and do the water quality requirement reuse of industrial boiler water-supply, and can guarantee the long-term operation of ultrafiltration and reverse osmosis membrane assembly.
The method that the present invention proposes can realize the advanced treatment of the effluent of municipal sewage plant higher containing COD, colourity, hardness and salts contg, make its reuse do industrial boiler water-supply, reach sewage recycling utilization and Industrial Water Saving object, meet the requirement of recycling industries and clean production etc.
Accompanying drawing explanation
Fig. 1 is the method process flow diagram of a kind of concrete municipal wastewater treatment plant secondary biochemical effluent advanced treatment of the present invention.
1-lime softens line mixer; 2-coagulative precipitation tank; 3-oxidation reactor; 4-strainer; 5-ultra-filtration equipment; 6-reverse osmosis unit.
Embodiment
Below in conjunction with accompanying drawing, the specific embodiment of the inventive method is described.
Secondary biochemical effluent from municipal sewage plant is squeezed into the softening line mixer 1 of lime continuously with pump, fully mix with saturated milk of lime, control the add-on of saturated milk of lime, the pH value of composite waste is remained on to 9.5～10.5, after calcium salt, magnesium salts in water reacted with milk of lime generation chemical precipitation, enter coagulative precipitation tank 2 and carry out flocculate and clarify separation.In coagulative precipitation tank 2, drop into continuously inorganic flocculating agent and organic floculant simultaneously, calcium, magnesium precipitate thing flocculation sediment under the effect of flocculation agent and excess hydrogen calcium oxide flocculating aids that original suspended substance in waste water and milk of lime softening process are produced, hardness, suspended substance and turbidity in waste water obtain deep removal, and colourity and COD also obtain part removal simultaneously.Water outlet after flocculate and clarify is sent into oxidation reactor 3 after fully mixing with from the ozone oxidation agent of ozonizer (unlisted in figure) in line mixer (unlisted in figure) and is processed.In oxidation reactor 3, the organism in waste water is attracted on the surface of sorbent material fast, and under alkaline condition, ozone produces hydroxyl radical free radical (HO after decomposing in water
.) etc. intermediate product, HO
.can, directly by the organism permineralization on sorbent material, generate CO
2and H
2o, recovers again its adsorption activity after adsorbent reactivation.Water outlet after adsorption and oxidation is sent into strainer 4 and is taken off suspended substance processing, and water outlet finally enters ultra-filtration equipment 5 again and reverse osmosis unit 6 carries out advanced desalination processing.In ultra-filtration equipment 5 and reverse osmosis unit 6, the various low concentration pollutants in waste water, inorganic salt even depth are removed, the water outlet (pure water) obtaining can meet industrial boiler water-supply water quality requirement and carry out reuse.Simultaneously, because waste water enters ultra-filtration equipment 5 and the front perfect preprocessing process above that passed through of reverse osmosis unit 6, main water inlet index COD≤50 mg/L, turbidity≤5 NTU, hardness≤150mg/L, basicity≤350mg/L, colourity≤30 degree, the long-time running that can keep ultrafiltration and reverse osmosis membrane assembly.
Adopt that inventive method adopts to occupy the secondary biochemical effluent of municipal sewage plant of larger proportion with industrial sewage that lime is softening, coagulating sedimentation, oxidation, filtration, ultrafiltration and the processing of reverse osmosis combination process, after processing, water outlet can reach reuse and do the water quality requirement of industrial boiler water-supply, and then realized municipal sewage as a resource utilization and the Industrial Water Saving object of high COD, colourity, hardness and salts contg, meet the requirement of recycling industries and clean production etc.
Further illustrate the inventive method and effect below by embodiment.
embodiment 1
Adopt treatment process of the present invention to carry out advanced treatment test to domestic certain municipal sewage plant's secondary biochemical effluent.In this municipal sewage plant's water inlet, because containing the pharmacy waste water of a large amount of difficult for biological degradation, after second-stage treatment, bio-chemical effluent COD 100～140 mg/L, pH 7.2 ~ 7.5, ammonia nitrogen 28-35 mg/L, colourity 175～200 are spent, BOD
50～5 mg/L, turbidity 10～25NTU, total hardness 380～520 mg/L, total alkalinity 350～400 mg/L, specific conductivity 3000～3200 μ s/cm.
Adopt method of the present invention, above-mentioned waste water is carried out to combined treatment test.Wastewater treatment scale is 1m
3/ h, main experimental device formation, operational conditions and the treatment effect of each processing unit are in table 1.After processing by method of the present invention, effluent index can meet reuse does the water quality requirement of oiler feed, i.e. turbidity≤0.3 NTU, COD
mn≤ 2 mg/L, ammonia nitrogen≤0.5 mg/L, specific conductivity≤100 μ s/cm, total hardness≤15mg/L are (with CaCO
3meter), total alkalinity≤20mg/L is (with CaCO
3meter), can substitute deionized water as industrial boiler water-supply reuse.
The main processing unit of table 1 embodiment 1 forms and treatment effect
| processing unit title | treatment unit scale and chief component | main operational conditions and control parameter | process water outlet or effect |
| 1 lime is softening | line mixer, material PVC. | wastewater flow 1m 3/ h; Add saturated milk of lime 500mg/L; PH of mixed value 9.80. | influent COD 120mg/L, pH 7.36, ammonia nitrogen 30 mg/L, colourity 180 are spent, BOD 52.0mg/L, turbidity 20NTU, total hardness 450mg/L, total alkalinity 680mg/L, specific conductivity 3100 μ s/cm. |
| 2 coagulative precipitation tanks | pVC material, volume 0.5m 3, built-in agitator stirs flocculation agent. | wastewater flow 1m
3/ h; Add bodied ferric sulfate inorganic flocculating agent 20 mg/L, |
water outlet COD 98mg/L, pH 9.62, colourity 125 are spent, turbidity 5 NTU, total hardness 200mg/L, total alkalinity 635mg/L. |
| 3 oxidation reactors | the tower cylindrical reactor of PVC material, useful volume 0.3m 3, external ozonizer, built-in adsorption layer, sorbent material is haydite, particle diameter 5 ~ 10 mm, packing ratio is 50%. | wastewater flow 1m 3/ h; Ozone dosage 6.58 mg/L; Retention time of sewage 10 min; PH of mixed value 9.62. | water outlet COD 48 mg/L, pH 7.85, total alkalinity 152 mg/L, ammonia nitrogen 1.5 mg/L, colourity 8 are spent, turbidity 4.5 mg/L. |
| 4 strainers | adopt multi-medium filtering post, material synthetic glass, size of main body is: diameter 300mm, high 2350mm; Interior filling quartz sand and ANTHRACITE FILTER MEDIA; Adopt upflowing water outlet. | wastewater flow 1m 3/ h; Every 2 days anti-cleanings once. | water outlet COD 42mg/L, turbidity 2.8NTU, SS≤5, pH 7.76, ammonia nitrogen 1.3 mg/L, colourity≤8 degree. |
| 5 ultrafiltration+reverse osmosis unit | adopt LG-DOW membrane module; Designing treatment amount 1.0 m 3/ h. | operate continuously, water rate 70% processed. | delivery turbidity 0.25 NTU, COD mn0.36 mg/L, ammonia nitrogen 0.3 mg/L, specific conductivity 58 μ s/cm, total hardness 13.5mg/L are (with CaCO 3meter), total alkalinity 15.2mg/L is (with CaCO 3meter) |
Adopt the treatment unit of embodiment 1, process the sewage identical with embodiment 1, the water treatment effect that the operational conditions of change each processing unit obtains is in table 2.
The main processing unit of table 2 embodiment 2 forms and treatment effect
| processing unit title | treatment unit scale and chief component | main operational conditions and control parameter | process water outlet or effect |
| 1 lime is softening | line mixer, material PVC. | wastewater flow 1m 3/ h; Add saturated milk of lime 650mg/L; PH of mixed value 10.50. | influent COD 140mg/L, pH 7.45, ammonia nitrogen 28 mg/L, colourity 200 are spent, BOD 52.5mg/L, turbidity 15NTU, total hardness 384mg/L, total alkalinity 980 mg/L, specific conductivity 3150 μ s/cm. |
| 2 coagulative precipitation tanks | pVC material, volume 0.5m 3, built-in agitator stirs flocculation agent. | wastewater flow 1m 3/ h; Add bodied ferric sulfate inorganic flocculating agent 25mg/L, polyacrylamide 3mg/L; PH of mixed value 10.30.Waste water hydraulic detention time 30min. | water outlet COD 115mg/L, pH 10.30, colourity 125 are spent, turbidity 6.5 NTU, total hardness 180 mg/L, total alkalinity 926 mg/L. |
| 3 oxidation reactors | the tower cylindrical reactor of PVC material, useful volume 0.3m 3, external ozonizer, built-in adsorption layer, sorbent material is haydite, particle diameter 5 ~ 10 mm, packing ratio is 75%. | wastewater flow 1m 3/ h; Ozone dosage 11.75mg/; Waste water hydraulic detention time 18min; PH of mixed value 10.30. | water outlet COD 42mg/L, pH 7.21, total alkalinity 56 mg/L, ammonia nitrogen 0.6 mg/L, colourity 5 are spent, turbidity 3.8 mg/L. |
| 4 strainers | adopt multi-medium filtering post, material synthetic glass, size of main body is: diameter 300mm, high 2350mm; Interior filling quartz sand and ANTHRACITE FILTER MEDIA; Adopt upflowing water outlet. | wastewater flow 1m 3/ h; Every 2 days anti-cleanings once. | water outlet COD 40mg/L, turbidity 2.3NTU, SS≤5, pH 7.35, ammonia nitrogen 0.55 mg/L, colourity≤5 degree. |
| 5 ultrafiltration+reverse osmosis unit | adopt LG-DOW membrane module; Designing treatment amount 1.0 m 3/ h. | operate continuously, water rate 70% processed. | delivery turbidity 0.2NTU, COD mn0.24mg/L, ammonia nitrogen 0.15 mg/L, specific conductivity 50 μ s/cm, total hardness 10.2 mg/L are (with CaCO 3meter), total alkalinity 12.4mg/L is (with CaCO 3meter) |
Claims (10)
1. a method for municipal effluent secondary biochemical effluent advanced treatment, is characterized in that: comprise following treatment step: (1) lime is softening to be processed; (2) coagulating sedimentation processing; (3) oxide treatment; (4) filtration treatment; (5) ultrafiltration and reverse-osmosis treated; Wherein, the described oxide treatment of step (3), take ozone as oxygenant, arranges adsorbent bed in oxidation reactor.
2. in accordance with the method for claim 1, it is characterized in that: in softening processing of lime of step (1), lime mixes in line mixer with waste water, controls the pH value 9.5～10.5 of waste water after mixing.
3. it is characterized in that in accordance with the method for claim 1: in the softening processing of step (1) lime, adopt saturated milk of lime.
4. it is characterized in that in accordance with the method for claim 1: in the processing of step (2) coagulating sedimentation, the hydraulic detention time of waste water in coagulative precipitation tank is 10～30min.
5. it is characterized in that in accordance with the method for claim 1: the flocculation agent that step (2) coagulating sedimentation adds in processing is organic floculant and inorganic flocculating agent.
6. in accordance with the method for claim 5, it is characterized in that: the inorganic flocculating agent that step (2) coagulating sedimentation adds in processing is bodied ferric sulfate or iron trichloride, and dosage is 10～30mg/L.
7. in accordance with the method for claim 5, it is characterized in that: the organic floculant that step (2) coagulating sedimentation adds in processing is polyacrylamide, and dosage is 1～5mg/L.
8. in accordance with the method for claim 1, it is characterized in that: the sorbent material that step (3) oxide treatment adopts is haydite, gac or hard coal, and particle diameter is 5 ~ 10 mm, packing ratio is reactor volume 50% ~ 75%.
9. in accordance with the method for claim 1, it is characterized in that: in step (3) oxide treatment, the dosage of ozone is 5～20 mg/L waste water, and the hydraulic detention time of waste water in oxidation reactor is 10 ~ 20min.
10. it is characterized in that in accordance with the method for claim 1: step (4) filtration treatment adopts multi-medium filtering, sand filtration, drift sand to filter or millipore filtration.
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