CN101434445A - Processing system and operation method for phosphor-containing organic wastewater - Google Patents
Processing system and operation method for phosphor-containing organic wastewater Download PDFInfo
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Abstract
The invention relates to a treatment system and an operation method of phosphorus-containing organic wastewater. A chemical phosphorus removal system is combined with an aerobic biochemical system, thus forming a system that removes phosphate and organic matters in the effluent of an aerobic removal system. The chemical phosphorus removal system consists of a chemicals feeding system, a mixed reaction pool, a sedimentation pool, a residual sludge refluxing system and a chemical sludge refluxing system. The aerobic biochemical system consists of an aerobic contact oxidation system and an aerobic activated sludge system. During the process of chemical phosphorus removal, sulfide and part of the organic matters can be removed simultaneously, thus causing the subsequent aerobic process to run stably and reducing running cost thereof. The residual sludge of the aerobic biochemical system is subjected to aeration and then refluxes to the chemical phosphorus removal system, and flocculation is absorbed and chemical sludge flocculating constituents are settled by utilizing residual activated sludge, thus improving chemical phosphorus removal efficiency. Part of the chemical phosphorus removal sludge refluxes after aeration, thus reducing the feeding amount of chemicals and reducing running cost. The treatment system and the operation method can cause organic wastewater with high phosphorus concentration to reach strict discharge standard after being treated.
Description
Technical field
A kind of treatment process of handling phosphor-containing organic wastewater belongs to environment protection and technical field of waste water processing.Specifically, be to adopt the chemical dephosphorization method and the combination technique of aerobe technology to handle the treatment system and the working method of the phosphor-containing organic wastewater of anaerobic system discharge.
Background technology
Anaerobic Microbiological Treatment Technology has obtained widespread use in the high concentrated organic wastewater process field of industries such as fermentation alcohol discharging.But because anaerobion cell proliferation is very slow, requirement to nitrogen phosphorus nutrition thing is few, so anaerobic system is very limited to the removal of phosphorus and nitrogen in the waste water, the concentration of organism and phosphorus and nitrogen does not still reach discharging standards in the anaerobism water outlet, also needs further to handle.For the water outlet of the system for anaerobic treatment of high density organic waste waters such as fermentation alcohol, its organic content higher (COD concentration 500～5000mg/L), total phosphorus concentration more than 15～70mg/L, ammonia nitrogen 20～60mg/L, TN30～160mg/L, basicity 1500-2000mgCaCO
3More than/the L, and also contain in the waste water the virulent sulfide of aerobic microbiological.How this waste water being carried out cost-effective improvement and make it reach emission standard, is the problem that presses for solution.
The method of handling phosphor-containing organic wastewater has biological process, chemical method two big classes.Biological process comprises that biomembrance process, activated sludge processes such as catalytic oxidation are (as anaerobic/anoxic dephosphorization process, A
2SBR modification technologies such as/O and improved technology thereof, CAST and UNITANK and oxidation ditch process etc.), or microbial film and activated sludge process process combined.The chemistry rule is mainly chemical dephosphorization method, coagulant sedimentation etc.Biological process is being removed the organic while, and a part of phosphorus can be converted into microorganism cells and contains phosphorus component (as nuclear substance, poly-phosphorus particle etc.) and remove with the excess sludge system that discharges in the sewage.Practical operating experiences both domestic and external shows, adopts biological process that the removal amount of phosphorus is generally BOD
53.5%～4.5%, the content of phosphorus generally is no more than 5% in the mud.(be lower than 5～8mg/L), then biological process system effluent quality can satisfy emission request if the content of phosphorus is not high in the waste water; If phosphorus content is higher in the waste water, exceeded the limit value that biological process can be removed, just must combine biological process and chemical method dephosphorization, just can make the organism of final outflow water and the concentration of phosphorus reach emission request.At present, existing independent employing aerobe treatment measures or chemical dephosphorization measure can not guarantee the organism and the phosphorus while qualified discharge of the phosphor-containing organic wastewater that anaerobic system is discharged.Therefore, the improvement of this waste water need combine aerobe method and chemical method dephosphorization.
Biological process and chemical method dephosphorization process combined have many, for example Phostrip technology, the biological earlier technology of handling the back chemical dephosphorization etc. that the dephosphorization medicament is added to the first chemical dephosphorization artifact treatment process of (as the preliminary sedimentation tank water inlet) before the biological treatment tank, the dephosphorization medicament is added in the biological treatment process of aeration tank the technology of chemical dephosphorization simultaneously and the dephosphorization medicament is added to (as the second pond water outlet) after the biological treatment.Adopt which kind of combination process to need to determine as the case may be in the real work.
The improvement of the phosphor-containing organic wastewater of discharging for system for anaerobic treatment, if the chemical dephosphorization operation is placed before the biochemical treatment operation, then in the chemical dephosphorization process, can be in the waste water species precipitate such as the virulent sulfide of microorganism being removed, can also remove the organic loading that a part of organism reduces generate subsequent chemical industry preface in addition, reduce working cost effectively.Therefore, for the phosphor-containing organic wastewater that system for anaerobic treatment is discharged, we adopt and carry out contained phosphorus, sulfide and a part of organism of chemical dephosphorization removal waste water earlier, just carry out the improvement thinking that aerobe is handled then.The chemical dephosphorization method combined with the aerobe technology forms the novel process system, and has carried out relevant optimization, has realized the phosphor-containing organic wastewater that anaerobic system is discharged is effectively administered, and makes the target of its qualified discharge.The invention relates to the novel process system of this combination and optimize the result who uses.
Summary of the invention
The object of the present invention is to provide a kind of method of handling phosphor-containing organic wastewater, effectively and economically remove phosphoric acid salt and organism in the system for anaerobic treatment water outlet, make it finally reach emission standard or reuse requirements in water quality.
A kind of system that handles phosphor-containing organic wastewater of the present invention is that chemical phosphorus removal system is combined with the aerobe system, forms phosphoric acid salt and the organic system removed in the anaerobic system water outlet.
Described chemical phosphorus removal system is made up of mixture 2 and dosing system, mixed reaction pond 3, settling tank 4, residual sludge reflux system and the chemical sludge return-flow system of molysite or molysite and aluminium salt.
Described aerobe system's employing aerobic contact oxidation and aerobic activated sludge system are in series; Aerobic contact oxidation adopts catalytic oxidation 5, aerobic activated sludge system to adopt activated sludge tank 6, residual sludge reflux system to adopt the modified groove 8 of excess sludge, chemical sludge return-flow system to adopt chemical sludge pond 9.
The working method of the system of processing phosphor-containing organic wastewater of the present invention, phosphor-containing organic wastewater 1 enters the mixed reaction pond 3 of hydraulic detention time 20～40min successively, the settling tank 4 of hydraulic detention time 2.0～4.0h, the aerobic contact oxidation pond 5 of hydraulic detention time 4.5～9.0h and the aerobic activated sludge pond 6 of hydraulic detention time 21.0～42.0h are discharged or reuse at last; The ratio 1.3%-3.3% of residual sludge reflux flow and flooding velocity, the surplus sludge volume of backflow is about 1:3～2:3 (m/m) with the ratio of the chemical sludge amount of generation; The ratio 2.0%-4.0% of chemical sludge return flow and flooding velocity.
Described phosphor-containing organic wastewater 1 enters in the mixed reaction pond 3, with the mixture 2 of the molysite that adds or molysite and aluminium salt, from the next body refuse thorough mixing of sludge sump 9 backflows, phosphorus in the waste water and molysite generation chemical reaction generate the insoluble precipitate of phosphorus, precipitate simultaneously the virulent sulfide of aerobic microbiological.Then, waste water that mixed reaction pond 3 is discharged and throw out mix with the excess sludge that refluxes from the modified groove 8 of excess sludge, and flow into together and carry out mud-water separation in the settling tank 4.
Described molysite is FeCl
3Or bodied ferric sulfate; Aluminium salt is Tai-Ace S 150 or aluminium chlorohydroxide.
Waste water behind the described settling tank 4 effusive chemical dephosphorizations enters contact-oxidation pool 5, is degraded to carbonic acid gas and water at this a part of organism.The water outlet of contact-oxidation pool 5 enters activated sludge tank 6 then, and organism and phosphorus are further degraded and transformed removal, and activated sludge tank 6 effluent qualities reach standard-required, are discharged or reuse; Settling tank 4 sedimentary body refuses enter chemical sludge pond 9, and the mud of sludge sump 9 is carried out aeration, make that wherein DO is back to mixed reaction pond 3 with a part of body refuse then at 0.2-2.5mg/L, and all the other body refuses are discharged to sludge treating system 10 and handle.
The excess sludge that described activated sludge tank 6 is discharged enters the modified groove 8 of excess sludge, and the mud of the modified groove 8 of excess sludge is carried out aeration, makes that wherein DO is at 0.2-2.5mg/L; A part of then excess sludge is back to water outlet place of mixed reaction pond 3, and mixes with the water that goes out of mixed reaction pond 3, then enters settling tank 4 together and carries out mud-water separation, to improve the removal efficient of 4 pairs of chemical precipitation flcos of settling tank and other suspended substance.
The present invention is a kind of technology of handling phosphor-containing organic wastewater, and its advantage and purposes are:
1) chemical dephosphorization method and aerobic biological treatment process are effectively made up, the chemical dephosphorization means are placed on the technical process head end, have guaranteed that the waste water of high phosphorus concentration can reach strict emission control standards after processing; Remove in the time of chemical dephosphorization the virulent sulfide of aerobe and a part of organism, guarantee the steady running of aerobic process and the working cost of reduction aerobic process system;
2) the aerobic treatment operation behind the chemical dephosphorization is divided into two sections of catalytic oxidation and active sludge, and catalytic oxidation reduces organic loading to remove COD, for having created condition in follow-up suspension active sludge unit; The active sludge unit then adopts underrun, realizes effective removal of remaining organism and nitrogen phosphorus, thereby has effectively guaranteed the up to standard of outlet water organic substance and nitrogen phosphorus.
3) the insoluble phosphorus compound precipitation flco of chemical dephosphorization unit generation is more less, and they are comparatively difficult with effectively separating of waste water in settling tank.The excess sludge that the active sludge unit produces also has good adsorption flocculation and sedimentation function, after it is back in the mixed reaction pond water outlet, can get up insoluble chemical sludge flco adsorption-flocculation, effectively separates with waste water in settling tank afterwards.Here, the backflow utilization of excess sludge has improved the mud-water separation efficient of settling tank effectively.
4) behind the residual sludge reflux, residual active sludge can obtain concentrating to a certain degree in settling tank.
5) a part of body refuse that settling tank is discharged is back to mixed reaction pond, makes full use of wherein to have active metal ion, thereby can reduce the dosage of chemical precipitation agent, has reduced the running cost of chemical dephosphorization.
Description of drawings
Fig. 1: the process flow sheet of handling phosphor-containing organic wastewater;
Number in the figure is: 1-water inlet, 2-molysite or molysite and aluminium salt mixture, 3-mixed reaction pond, 4-settling tank, 5-contact-oxidation pool, 6-activated sludge tank, 7-water outlet, the modified groove of 8-excess sludge, 9-chemical sludge pond, 10-sludge treating system.
Embodiment
The present invention is described in further detail below in conjunction with embodiment:
Technical process as shown in drawings.Phosphor-containing organic wastewater 1 enters mixing reactor 3 successively, with the molysite (FeCl that adds
3Or bodied ferric sulfate) or the mixture 2 of molysite and aluminium salt (Tai-Ace S 150 or aluminium chlorohydroxide), from sludge sump 9 the body refuse thorough mixing of coming that refluxes.Phosphorus in the waste water and molysite or aluminium salt generation chemical reaction generate the insoluble precipitate of phosphorus, precipitate simultaneously the virulent sulfide of aerobic microbiological.Then, waste water that mixing reactor 3 is discharged and throw out mix with the excess sludge that refluxes from the modified groove 8 of excess sludge, and flow into together and carry out mud-water separation in the settling tank 4.Waste water behind the settling tank 4 effusive chemical dephosphorizations enters contact-oxidation pool 5, is degraded to carbonic acid gas and water at this a part of organism.The water outlet of contact-oxidation pool 5 enters activated sludge tank 6 then, and organism and phosphorus are further degraded and transformed removal.The effluent quality of activated sludge tank 6 reaches standard-required, is discharged or reuse.
The excess sludge that activated sludge tank 6 is discharged enters the modified groove 8 of excess sludge, mud to the modified groove 8 of excess sludge carries out aeration, make that wherein DO is at 0.2-2.5mg/L, a part of then excess sludge is back to water outlet place of mixed reaction pond 3, and mix with the water that goes out of mixed reaction pond 3, then enter settling tank 4 together and carry out mud-water separation, to improve the removal efficient of 4 pairs of chemical precipitation flcos of settling tank and other suspended substance.
Settling tank 4 sedimentary body refuses enter chemical sludge pond 9, and the mud of sludge sump 9 is carried out aeration, make that wherein DO is back to mixing reactor 3 with a part of body refuse then at 0.2-2.5mg/L, and rest part is discharged to sludge treating system 10 and handles.
Embodiment 1:
Water-quality COD 〉=the 500mg/L of phosphor-containing organic wastewater 1, BOD
5〉=300mg/L, TP 〉=18mg/L, it enters mixing reactor 3 (hydraulic detention time 20min), with the FeCl that adds
3(dosage 90mg/L) molysite 2, from sludge sump 9 the body refuse thorough mixing of coming that refluxes, the insoluble precipitate of the phosphorus in the waste water and molysite generation chemical reaction generation phosphorus precipitates simultaneously to the virulent sulfide of aerobic microbiological.Then, waste water that mixing reactor 3 is discharged and throw out mix with the excess sludge that refluxes from the modified groove 8 of excess sludge, and flow into together in the settling tank 4 (hydraulic detention time 2.0h) and carry out mud-water separation.
Waste water behind the settling tank 4 effusive chemical dephosphorizations enters contact-oxidation pool 5 (hydraulic detention time 4.5h), is degraded to carbonic acid gas and water at this a part of organism.The water outlet of contact-oxidation pool 5 enters activated sludge tank 6 (hydraulic detention time 21.0h) then, organism remaining in the waste water further is degraded to carbonic acid gas and water and is carried out cell proliferation, phosphorus wherein then is converted into the proliferative cell component or is converted into poly-phosphorus particle in the polyP bacteria absorption cell, discharges with excess sludge then and removes.Effluent quality COD≤100mg/L, the BOD of activated sludge tank 6
5≤ 30mg/L, PO
4 3--P≤1mg/L is discharged.
The excess sludge that activated sludge tank 6 is discharged enters the modified groove 8 of excess sludge, mud to the modified groove 8 of excess sludge carries out aeration, make that wherein DO is at 0.2-2.5mg/L, a part of then excess sludge is back to water outlet place of mixed reaction pond 3, return flow is about 1.3% with the ratio of flooding velocity, and the surplus sludge volume of backflow is about 1:3 (m/m) with the ratio of the chemical sludge amount of generation; And mix with the water outlet and the throw out of mixed reaction pond 3, then enter settling tank 4 together and carry out mud-water separation, to improve the removal efficient of 4 pairs of chemical precipitation flcos of settling tank and other suspended substance.
Settling tank 4 sedimentary body refuses enter chemical sludge pond 9, mud to sludge sump 9 carries out aeration, makes that wherein DO is back to mixed reaction pond 3 with a part of body refuse then at 0.2-2.5mg/L, to reduce the consumption of chemical dephosphorization medicament, backflow body refuse flow is 2.0% with the ratio of flooding velocity; All the other body refuses are discharged to sludge treating system 10 and handle.
Embodiment 2:
Water-quality COD 〉=the 2500mg/L of phosphor-containing organic wastewater 1, BOD
5〉=1350mg/L, TP 〉=33mg/L, it enters mixing reactor 3 (hydraulic detention time 30min), with the FeCl that adds
3(dosage 180mg/L) molysite 2, from sludge sump 9 the body refuse thorough mixing of coming that refluxes, the insoluble precipitate of the phosphorus in the waste water and molysite generation chemical reaction generation phosphorus precipitates simultaneously to the virulent sulfide of aerobic microbiological.Then, waste water that mixing reactor 3 is discharged and throw out mix with the excess sludge that refluxes from the modified groove 8 of excess sludge, and flow into together in the settling tank 4 (hydraulic detention time 3.0h) and carry out mud-water separation.
Waste water behind the settling tank 4 effusive chemical dephosphorizations enters contact-oxidation pool 5 (hydraulic detention time 6.5h), is degraded to carbonic acid gas and water at this a part of organism.The water outlet of contact-oxidation pool 5 enters activated sludge tank 6 (hydraulic detention time 32.0h) then, organism remaining in the waste water further is degraded to carbonic acid gas and water and is carried out cell proliferation, phosphorus wherein then is converted into the proliferative cell component or is converted into poly-phosphorus particle in the polyP bacteria absorption cell, discharges with excess sludge then and removes.Effluent quality COD≤100mg/L, the BOD of activated sludge tank 6
5≤ 30mg/L, PO
4 3--P≤1mg/L is discharged.
The excess sludge that activated sludge tank 6 is discharged enters the modified groove 8 of excess sludge, mud to the modified groove 8 of excess sludge carries out aeration, make that wherein DO is at 0.2-2.5mg/L, a part of then excess sludge is back to water outlet place of mixed reaction pond 3, return flow is about 2.9% with the ratio of flooding velocity, and the surplus sludge volume of backflow is about 2: 3 (m/m) with the ratio of the chemical sludge amount of generation; And mix with the water outlet and the throw out of mixed reaction pond 3, then enter settling tank 4 together and carry out mud-water separation, to improve the removal efficient of 4 pairs of chemical precipitation flcos of settling tank and other suspended substance.
Settling tank 4 sedimentary body refuses enter chemical sludge pond 9, and a part of body refuse is back to mixing reactor 3, and to reduce the consumption of chemical dephosphorization medicament, the body refuse return flow is 2.9% with the ratio of flooding velocity; Rest part is discharged to sludge treating system and carries out processing such as thickening.
Embodiment 3:
Water-quality COD 〉=the 5000mg/L of phosphor-containing organic wastewater 1, BOD
5〉=3000mg/L, TP 〉=70mg/L, it enters mixing reactor 3 (hydraulic detention time 40min), with the FeCl that adds
3(dosage 400mg/L) molysite 2, from sludge sump 9 the body refuse thorough mixing of coming that refluxes, the insoluble precipitate of the phosphorus in the waste water and molysite generation chemical reaction generation phosphorus precipitates simultaneously to the virulent sulfide of aerobic microbiological.Then, waste water that mixing reactor 3 is discharged and throw out mix with the excess sludge that refluxes from the modified groove 8 of excess sludge, and flow into together in the settling tank 4 (hydraulic detention time 4.0h) and carry out mud-water separation.
Waste water behind the settling tank 4 effusive chemical dephosphorizations enters contact-oxidation pool 5 (hydraulic detention time 9.0h), is degraded to carbonic acid gas and water at this a part of organism.The water outlet of contact-oxidation pool 5 enters activated sludge tank 6 (hydraulic detention time 42.0h) then, organism remaining in the waste water further is degraded to carbonic acid gas and water and is carried out cell proliferation, phosphorus wherein then is converted into the proliferative cell component or is converted into poly-phosphorus particle in the polyP bacteria absorption cell, discharges with excess sludge then and removes.Effluent quality COD≤100mg/L, the BOD of activated sludge tank 6
5≤ 30mg/L, PO
4 3--P≤1mg/L is discharged.
The excess sludge that activated sludge tank 6 is discharged enters the modified groove 8 of excess sludge, mud to the modified groove 8 of excess sludge carries out aeration, make that wherein DO is at 0.2-2.5mg/L, a part of then excess sludge is back to water outlet place of mixed reaction pond 3, return flow is about 3.3% with the ratio of flooding velocity, and the surplus sludge volume of backflow is about 1:2 (m/m) with the ratio of the chemical sludge amount of generation; And mix with the water outlet and the throw out of mixed reaction pond 3, then enter settling tank 4 together and carry out mud-water separation, to improve the removal efficient of 4 pairs of chemical precipitation flcos of settling tank and other suspended substance.
Settling tank 4 sedimentary body refuses enter chemical sludge pond 9, mud to sludge sump 9 carries out aeration, makes that wherein DO is back to mixed reaction pond 3 with a part of body refuse then at 0.2-2.5mg/L, to reduce the consumption of chemical dephosphorization medicament, backflow body refuse flow is 4.0% with the ratio of flooding velocity; All the other body refuses are discharged to sludge treating system 10 and handle.
Embodiment 4:
Water-quality COD 〉=the 2500mg/L of phosphor-containing organic wastewater 1, BOD
5〉=1350mg/L, TP 〉=33mg/L add iron trichloride (FeCl
3) and the mixture of bodied ferric sulfate (PFS), wherein FeCl
3Dosage 120mg/L, PFS dosage are 165mg/L, and all the other are with embodiment 2.Effluent quality COD≤100mg/L, the BOD of activated sludge tank 6
5≤ 30mg/L, PO
4 3--P≤1mg/L is discharged.
Embodiment 5:
Water-quality COD 〉=the 2500mg/L of phosphor-containing organic wastewater 1, BOD
5〉=1350mg/L, TP 〉=33mg/L add iron trichloride (FeCl
3) and Tai-Ace S 150 (Al
2(SO
4)
3) mixture, FeCl wherein
3Dosage 120mg/L, Tai-Ace S 150 dosage are 100mg/L, and all the other are with embodiment 2.Effluent quality COD≤100mg/L, the BOD of activated sludge tank 6
5≤ 30mg/L, PO
4 3--P≤1mg/L is discharged.
Embodiment 6:
Water-quality COD 〉=the 2500mg/L of phosphor-containing organic wastewater 1, BOD
5〉=1350mg/L, TP 〉=33mg/L add iron trichloride (FeCl
3) and the mixture of aluminium chlorohydroxide, wherein FeCl
3Dosage 120mg/L, aluminium chlorohydroxide dosage are 85mg/L, and all the other are with embodiment 2.Effluent quality COD≤100mg/L, the BOD of activated sludge tank 6
5≤ 30mg/L, PO
4 3--P≤1mg/L is discharged.
Claims (9)
1. a system that handles phosphor-containing organic wastewater is characterized in that chemical phosphorus removal system is combined with the aerobe system, forms phosphoric acid salt and the organic system removed in the anaerobic system water outlet.
2. the system of processing phosphor-containing organic wastewater as claimed in claim 1 is characterized in that described chemical phosphorus removal system is made up of mixture (2) and dosing system, mixed reaction pond (3), settling tank (4), residual sludge reflux system and the chemical sludge return-flow system of molysite or molysite and aluminium salt.
3. the system of processing phosphor-containing organic wastewater as claimed in claim 1 is characterized in that described aerobe system's employing aerobic contact oxidation and aerobic activated sludge system are in series.
4. the system of processing phosphor-containing organic wastewater as claimed in claim 1 is characterized in that described aerobic contact oxidation adopts contact-oxidation pool (5), aerobic activated sludge system to adopt activated sludge tank (6), residual sludge reflux system to adopt the modified groove of excess sludge (8), chemical sludge return-flow system to adopt chemical sludge pond (9).
5. the working method of the system of claim 1,2,3 or 4 processing phosphor-containing organic wastewater, it is characterized in that phosphor-containing organic wastewater (1) enters the mixed reaction pond (3) of hydraulic detention time 20～40min successively, the settling tank of hydraulic detention time 2.0～4.0h (4), the aerobic contact oxidation pond (5) of hydraulic detention time 4.5～9.0h and the aerobic activated sludge pond (6) of hydraulic detention time 21.0～42.0h are discharged or reuse at last; Residual sludge reflux flow and flooding velocity are than 1.3%-3.3%, and the mass ratio of the chemical sludge amount of the surplus sludge volume of backflow and generation is 1:3～2:3; The chemical sludge return flow compares 2.0%-4.0% with flooding velocity.
6. working method as claimed in claim 5, it is characterized in that described phosphor-containing organic wastewater (1) enters in the mixing reactor (3), with the mixture (2) of the molysite that adds or molysite and aluminium salt, from the next body refuse thorough mixing of sludge sump (9) backflow, phosphorus in the waste water and molysite generation chemical reaction generate the insoluble precipitate of phosphorus, precipitate simultaneously the virulent sulfide of aerobic microbiological; Then, waste water that mixed reaction pond (3) is discharged and throw out mix with the excess sludge that refluxes from the modified groove of excess sludge (8), and flow into settling tank together and carry out mud-water separation in (4).
7. working method as claimed in claim 6 is characterized in that described molysite is FeCl
3Or bodied ferric sulfate; Aluminium salt is Tai-Ace S 150 or aluminium chlorohydroxide.
8. working method as claimed in claim 5 is characterized in that the waste water behind the effusive chemical dephosphorization of described settling tank (4) enters contact-oxidation pool (5), is degraded to carbonic acid gas and water at this a part of organism; The water outlet of contact-oxidation pool (5) enters activated sludge tank (6) then, and organism and phosphorus are further degraded and transformed removal, and activated sludge tank (6) effluent quality reaches standard-required, is discharged or reuse; The sedimentary body refuse of settling tank (4) enters chemical sludge pond (9), and the mud of sludge sump (9) is carried out aeration, makes that wherein DO is back to mixed reaction pond 3 with a part of body refuse then at 0.2-2.5mg/L, and all the other body refuses are discharged to sludge treating system (10) and handle.
9. working method as claimed in claim 5 is characterized in that the excess sludge that described activated sludge tank (6) is discharged enters the modified groove of excess sludge (8), and the mud of the modified groove of excess sludge (8) is carried out aeration, makes that wherein DO is at 0.2-2.5mg/L; A part of then excess sludge is back to water outlet place of mixed reaction pond (3), and mix with the water that goes out of mixed reaction pond (3), then enter settling tank (4) together and carry out mud-water separation, to improve the removal efficient of settling tank (4) chemical precipitation flco and other suspended substance.
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