CN1170784C - Dry nitrilon waste water treating process - Google Patents
Dry nitrilon waste water treating process Download PDFInfo
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- CN1170784C CN1170784C CNB00129461XA CN00129461A CN1170784C CN 1170784 C CN1170784 C CN 1170784C CN B00129461X A CNB00129461X A CN B00129461XA CN 00129461 A CN00129461 A CN 00129461A CN 1170784 C CN1170784 C CN 1170784C
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Abstract
The present invention relates to a method for treating chemical fiber production waste water. The present invention adopts air flotation-AB biological treatment technology, and the section A of the air flotation-AB biological treatment technology is aerobic biological absorption, and the section B of the air flotation-AB biological treatment technology is anaerobic-anoxic-aerobic technology. By the present invention, waste water of which the COD concentration is 2500 mg/L, the turbidity is 50 mg/L and the concentration of sulfate is 1200 mg/L can be treated to meet the first-grade national discharge standard in the industry of acrylic fibers, namely that the concentration of COD is from 50 mg/L to 160 mg/L, and the concentration of NH3O is 15 mg/L. The present invention has the advantages of stable running and small occupation of land. The present invention is suitable for the treatment of organic waste water, such as waste water generated by dry production of the acrylic fibers, epoxy chloropropane waste water, etc. which has high turbidity and high concentration of colloid and sulfate and contains substances hard to biodegrade.
Description
Technical field
The invention belongs to the improvement method of chemical fibre factory effluent, relate in particular to the treatment process of the acrylic fibers waste water by dry process that adopts two sections biological treatments of air supporting pre-treatment-AB.
Background technology
The whole nation has five covers dry acrylic fiber production equipment of the same type at present, and they are respectively Qilu Petrochemical company Acrylic Fibers Plant, Fushun Petrochemical Company Acrylic Fibers Plant, Ningbo City's Acrylic Fibers Plant, Qinhuangdao Acrylic Fibers Plant and Maoming City Acrylic Fibers Plant.This five tame Acrylic Fibers Plant waste water treatment process is both the design of designing institute of the china textile Department of Industry, the employing anaerobic-aerobic-. activated carbon treatment technology, but because bio-chemical effluent COD350～600mg/L, the gac load is bigger, and activated carbon treatment technology can't come into operation.
Existing sewage water treatment method has certain treatment effect to organic pollutants such as vinyl cyanide, DMF, but lower to the processing efficiency of COD, EDTA, the waste discharge severe overweight.
Patent application CN99112488.X is improved to coagulating sedimentation-anaerobic digestion-Anoxybiotic-aerobic biologic denitrogenation-sand filtration-activated carbon treatment technology, but this technology still has long flow path, the higher shortcoming of processing cost.
Summary of the invention
The treatment process that the purpose of this invention is to provide the lower acrylic fibers waste water by dry process of a kind of COD clearance height, technical process weak point and running cost.
2000 the country according to the unmanageable practical situation of Nitrilon waste water from the new standard of having worked out, change the industry first discharge standard into COD≤160mg/L.For this reason, the present invention has carried out improving to patent application CN99112488.X again:
1. replace coagulation-settlement process with air-float technology.Induced-draft air float (pressure air-dissolving air-float) processing efficiency is higher than coagulating sedimentation on the whole, need not regulate pH in operational process, and it is few to add pharmaceutical quantities, and the COD clearance is high and stable.
2. cancel sand filtration and activated carbon treatment technology, greatly reduced running cost.
3. other waste water such as sanitary sewage and ground wash-down water is owing to COD≤600mg/L, and good biodegradability is directly advanced the anoxic section, thereby the corresponding water conservancy load that has reduced the anaerobism section, and need not add co-substrate and improve its biodegradability, reduce cost, improve the COD clearance of whole flow process.
The present invention implements by following technical proposals: the treatment process of developing a kind of acrylic fibers waste water by dry process, it is characterized in that adopting air supporting pre-treatment-AB biological treatment flow process, wherein the A section is biological absorption, and the B section is an anaerobic-anoxic-aerobic process, comprises following processing step:
The dry acrylic fiber processing wastewater is cooled to 50 ℃～65 ℃ through a grade cooling tower, in the pipeline coagulation device with polymerize aluminum chloride and commercial goods CP-937 cation high molecular quaternary flocculation agent (factory: dragon's fountain chemical plant, Zibo) mix, enter the pressure air-dissolving air-float pond, air supporting handle the back supernatant liquor by secondary cool enter equalizing tank and regulate pH5.5～6.5 to 35 ℃ after; Waste water enters aeration tank, the settling tank of A section biological treatment successively; Subsequently, waste water enters the anaerobic digestion operation, at the sulfate reduction acid-producing with produce methane reaction placed in-line while of independent reaction phase-splitting separately, increases the biological desulphurization step between the two, becomes sulfate reduction-biological desulphurization-product methane three-phase tandem process; At last, introduce sanitary sewage and produce peace and quiet water down in the anoxic section, waste water after Anoxybiotic-aerobic biologic denitrogenation operation is handled, qualified discharge; Wherein:
Pressure air-dissolving method or bleed method technology are adopted in the air supporting pre-treatment, remove low-molecular(weight)polymer in this waste water; The pretreated technology operating parameter of pressure air-dissolving method air supporting is: 50～65 ℃ of temperature, polymerize aluminum chloride injected volume 20～150mg/L, quaternary ammonium salt cationic flocculation agent injected volume 1～3mg/L, water pH value 6.0～7.5, dissolved-air pressure 0.25～0.3Mpa, gas-water ratio is 1: 3; The pretreated technology operating parameter of bleed method air supporting is: 50～65 ℃ of temperature, polymerize aluminum chloride injected volume 20～150mg/L, quaternary ammonium salt cationic flocculation agent injected volume 1～3mg/L, water pH value 6.0～7.5.
The COD clearance of the pretreated technology of above-mentioned pressure air-dissolving air-float is 25～35%, delivery turbidity≤10mg/L.
Above-mentioned A segment process parameter, the aeration tank mud load rate is 2～4kgCOD/kgMLSSd, hydraulic detention time 0.5～2h, dissolved oxygen 0.1～0.5mg/L, sludge concentration is 4000～6000mg/L, settling tank sedimentation time 2h, return sludge ratio is 20%～50%, COD clearance 25%～35%.
Above-mentioned technology operating parameter in the sulfate reduction acid-producing is: reflux ratio 200%, mixed liquor suspended solid, MLSS concentration 15～20g/L, pH4.5～6.5, dissolved oxygen 0.0mg/L, hydraulic detention time 8～16h.
Above-mentioned in the biological desulphurization step technology operating parameter be: pH5.5～6.5, dissolved oxygen 1.5～2.5mg/L, hydraulic detention time 0.15h.
Above-mentioned in methane-producing reactor the technology operating parameter be: mixed liquor suspended solid, MLSS concentration 15～20g/L, pH6.5～7.5, dissolved oxygen 0.0mg/L, hydraulic detention time 8～16h.
Above-mentioned in anoxic biological denitrificaion pond the technology operating parameter be: reflux ratio 100%～500%, mixed liquor suspended solid, MLSS concentration 4～6g/L, pH6.5～7.5, dissolved oxygen≤0.5mg/L, sludge retention time 5～10d, hydraulic detention time 6～12h.
Above-mentioned in the aerobic biological denitrification pond technology operating parameter be: mixed liquor suspended solid, MLSS concentration 2～6g/L, pH7.5～8.5, dissolved oxygen 〉=2.0mg/L, sludge retention time 5～10d, hydraulic detention time 6～12h, COD volumetric loading 0.5～1.0kgCOD/m
3D.
Above-mentioned discharging water quality after treatment can reach following index: COD 50～160mg/L, NH
3-N 15mg/L, SS 50mg/L, EDTA 6～10mg/L, pH 6～9.
Above-mentioned treatment process can add Powdered Activated Carbon 5～50ppm at aerobic section as the bio-chemical effluent phenomenon that exceeds standard occurring.
As sulfate concentration＞1000mg/L, waste water makes the water outlet sulfate concentration reduce to 200～500mg/L earlier by the Filter column of calcium oxide is housed to above-mentioned treatment process in the anaerobic digestion operation.
Above-mentioned treatment process is equally applicable to the processing of epoxy chloropropane trade effluent.
Characteristics of the present invention:
1. contain a large amount of low-molecular(weight)polymers in the air supporting acrylic fibers waste water by dry process, they exist with the suspension colloidal form, are difficult to natural subsidence and remove, and oligopolymer not only influences the normal operation of biochemical system after entering biochemical system, and has increased the organic matter degradation load; Oligopolymer easily stops up filler simultaneously, reduces the specific surface area of filler, has increased the wastewater biochemical intractability.Therefore, it is necessary at first removing low-molecular(weight)polymer, and the composite flocculation agent that the present invention adopts polymerize aluminum chloride and quaternary ammonium salt cationic flocculation agent to form adopts air-float technology to remove the oligopolymer colloid, providing for the normal operation of biochemical treatment is part, has reduced the load of biochemical treatment effectively.
2. sulfate reduction-biological desulphurization-product methane three is in series:
Higher sulphate content is the another characteristics of acrylic fibers waste water by dry process, and the vitriol of high density can produce the methane process to anaerobic digestion and have a negative impact, even causes anaerobic reactor operation failure.Adopt this three-phase tandem process, anaerobic process have been set up separately independently reactor, guaranteed that two big monoid bacteriums obtain preferable growth conditions in reactor separately, have avoided the matrix between two kinds of bacterium to strive unexpectedly.In the middle of acidogenic reactor and methane-producing reactor, set up desulfurizer simultaneously, can make sulfides from wastewater concentration, effectively weakened the toxic action of sulfide, improved the COD clearance of anaerobism section methanobacteria less than 1mg/L.
Because the imperfect stability of Industrial processes, the sulfate concentration fluctuation is bigger, if sulfate radical 200～500mg/L, biological desulfurization process can not need adopt.If sulfate radical 500～1000mg/L adopts above-mentioned three-phase tandem process,, can make in the waste water sulfate concentration less than 1000mg/L if sulfate concentration, can adopt calcium oxide precipitated sulfur acid group greater than 1000mg/L.
Biological desulfurization process is adopted in desulfurization, and this method is not only simple to operate, running cost is low, and recyclable elemental sulfur.
3. Anoxybiotic-aerobic biologic denitrogenation is introduced sanitary sewage in the anoxic section, has not only improved the biodegradability of Nitrilon waste water, has reduced the water conservancy load of anaerobism section, and has guaranteed the higher nitric efficiency of A/O technology.
4. add Powdered Activated Carbon in case of necessity
Because the imperfect stability of Industrial processes, the phenomenon if bio-chemical effluent exceeds standard can add Powdered Activated Carbon 5～50ppm at aerobic section, and the more effective waste water that guaranteed reaches the industry first discharge standard of national regulation.This is an innovation part of present technique, and the adding of Powdered Activated Carbon has not only improved the settling property of mud, and has guaranteed that waste water can qualified discharge.So just need not adopt operation and the higher post-processing technology of investment cost.
The present invention has the following advantages compared to existing technology:
1, air-float technology can be removed non-dissolving COD and the colloidalmaterial in the water effectively, compares with coagulation-settlement process, and not only the flocculation agent consumption is few, the pH range of application is wide, effective, stable, and the tensio-active agent in the waste water is had certain removal effect.
2, for high sulfate radical organic waste water, not only anaerobism clearance height, and recyclable elemental sulfur.
3, this technical process is to containing recalcitrant substance, and particularly tensio-active agent and complexone have higher removal effect.
4, the present invention has higher removal effect to organonitrogen, inorganic nitrogen in the waste water, and the ammonia nitrogen removal frank height can reach 100%.
5, technical process of the present invention is reasonable, and the economy height is its another principal feature.
Description of drawings
Fig. 1 is a technical process schematic block diagram of the present invention;
Fig. 2 is the technical process schematic block diagram of prior art.
Embodiment
The present invention is further elaborated below in conjunction with drawings and Examples:
Among the figure:
1. air supporting:
Adopt polymerize aluminum chloride and quaternary ammonium salt cationic flocculation agent as composite flocculation agent.The optimal operating parameter of pressure air-dissolving air-float technology is 60 ℃～80 ℃ of temperature, PAC (Poly aluminuium chloride, polymerize aluminum chloride) best dosage is 20～150mg/L, and quaternary ammonium salt cationic flocculation agent CP-937 dosage is 1mg/L, and the pH value is between 6.0～7.5.Dissolved-air pressure is 0.25～0.30MPa, and gas-water ratio is 1: 3.The COD clearance of pressure air-dissolving air-float technology is between 25%～35%, and delivery turbidity is lower than 5mg/L.The Induced-draft air float device that adopts U.S. AEROMIX to produce can reach the effect identical with pressure air-dissolving air-float.
2. AB biological treatment
The A section is the aerobe absorbing process, and the B section is an anaerobic-anoxic-aerobic process.
A segment process parameter, aeration tank mud load rate Ns is 2～4kgCOD/kgMLSS.d, hydraulic detention time 0.5～2h, DO 0.1～0.5mg/L, sludge concentration is 4000～6000mg/L, settling tank sedimentation time 2h, return sludge ratio is 20%～50%, COD clearance 25%～35%.
Anaerobic reactor is UASB (up-flow anaerobic sludge blanket) in the B segment process, and desulfurization pond, anoxic pond, Aerobic Pond are hybrid fully, and anoxic pond, Aerobic Pond are equipped with D type band soft cellulose filler, is provided with the perforation gas distribution pipe in the pond and carries out aeration.Be filled with in the desulfurization pond and draw western porcelain ring, settling tank is vertical sedimentation basin.
3. each unit main technologic parameters index:
Air flotation cell: 50～65 ℃ of temperature, best dosage 20～100mg/L of PAC, CP-937 dosage 1～3mg/L, pH6.0～7.5;
Biological absorbing unit: mud load rate Ns 2～4kgCOD/kgMLSS.d, hydraulic detention time 0.5～2h, dissolved oxygen 0.1～0.5mg/L, sludge concentration 4000～6000mg/L, settling tank 2h, return sludge ratio 20%～50%, acidogenic reactor: 30～35 ℃ of temperature, VSS/SS 50～55%, mixed liquor suspended solid, MLSS concentration 15～20g/L, pH5.5～6.5, hydraulic detention time 8～16h, gas production rate 0.050～0.075m
3/ kgCOD;
Methane-producing reactor: 30～35 ℃ of temperature, VSS/SS 50～55%, mixed liquor suspended solid, MLSS concentration 15～20g/L, pH 6.8～7.2, hydraulic detention time 8～16h, gas production rate 0.012～0.025m
3/ kgCOD;
The hypoxia response pond: 20～30 ℃ of temperature, VSS/SS 65～75%, mixed liquor suspended solid, MLSS concentration 4～6g/L, pH6.5～7.5, hydraulic detention time 6～12h, sludge retention time 5～10d, dissolved oxygen≤0.5mg/L;
The aerobic reaction pond: 20～30 ℃ of temperature, VSS/SS 65～75%, mixed liquor suspended solid, MLSS concentration 2～4g/L, pH7.5～8.5, hydraulic detention time 6～12h, sludge retention time 5～10d, dissolved oxygen 2.0mg/L.
The stable operation stage processing parameter
Reflux ratio MLSS DO SRT HRT COD volumetric loading
％ g/L mg/L hr hr kgCOD/m
3.d
Acidogenic reactor 200 15～20 0.0 8～16 1.5～3.5
Desulfurization pond 1.5～2.5 0.15～0.3
Medium sediment pool 2.0
Methane-producing reactor 15～20 0.0 8～16 1.0～1.5
Anoxic pond 100～500 4～6≤0.5 5～10 6～12 1.0～1.4
Aerobic Pond 4～6 〉=2.0 10 6～12 0.7～1.0
Settling tank 50～100 2.0
*MLSS (Mixed liquide suspended solid, mixed liquor suspended solid, MLSS concentration);
DO (Dissolved of oxygen, dissolved oxygen);
SRT (Sludge residence time, sludge retention time);
HRT (Hydraulic residence time, hydraulic detention time).
Among Fig. 1, waste water is removed oligopolymer colloid and excess sludge 11 discharges through air supporting 1 technology, waste water after the air supporting enters the aeration tank 2 of A section biological treatment successively, settling tank 3 (mud 12 has 3 backflows of 20～50% autoprecipitation ponds to return aeration tank 2), waste water continue the to flow through acidogenic reactor 4 (head and the tail return sludge ratio 200%) of B section anaerobic digestion, biological desulphurization pond 5, medium sediment pool 6 (reclaim elemental sulfur 14) and methane-producing reactor 7 (water outlet of methane-producing reactor 7 introduce sanitary sewage and produce peace and quiet under water 15), enter the anoxic pond 8 of B section anoxic-aerobic process biological denitrificaion operation successively, Aerobic Pond 9 (water outlet of Aerobic Pond 9 is to the return sludge ratio 300% of anoxic pond 8) and settling tank 10 (settling tank 10 is to the return sludge ratio 100% of anoxic pond 8) back qualified discharge.
Among Fig. 2, acrylic fibers processing wastewater 19 (1600m
3/ d) through cooling, coagulating sedimentation operation 20, flow into equalizing tank 21; Sanitary sewage (1100m
3/ d) descend water (330m with other
3/ d) 30 through pump well 31, lift pump 32, rotation grid 33 introducing equalizing tanks 21; Equalizing tank 21 water outlets are after lift pump 22 pumps into anaerobic pond 23, after entering Aerobic Pond 24, precipitation, sludge sump 25, charcoal tower 26, clean water basin 27 successively, clean in waste water 38, the power desalination and waste water 39 with power plant, after coming together in pumping station 28, enter pig dragon river 29, because of the defective workmanship discharging that often exceeds standard.Precipitation, sludge sump 25 part water outlets are promoted by lift pump 34, and a part passes back into anaerobic pond 23; A part is included in and is burned operation 36 after entering sludge dewatering system 35 dehydrations.Multistage centrifugal gas blower 37 is respectively to equalizing tank 21, Aerobic Pond 24 and 26 air blast of charcoal tower; The portion water of clean water basin 27 promotes the back flushing that is used for charcoal tower 26 through lift pump 40.
Embodiment 1
Dry acrylic fiber processing wastewater COD 1500-2000mg/L, turbidity 10～40mg/L, total nitrogen 100～300mg/L, sulfate radical 500～1000mg/L is cooled to 50 ℃～65 ℃ through a grade cooling tower, in the pipeline coagulation device with polymerize aluminum chloride 10～50mg/L, cation high molecular quaternary flocculation agent CP-937 1mg/L mixes, and water pH value 6.0～7.5 enters the pressure air-dissolving air-float pond, dissolved-air pressure 0.25～0.3Mpa, gas-water ratio is 1: 3; Supernatant liquor cools to about 35 ℃ by secondary, and the COD clearance of the pretreated technology of air-dissolving air-float is 25～35%, delivery turbidity≤10mg/L.Enter and enter biological adsorption tank after equalizing tank is regulated pH5.5～6.5, the aeration tank mud load rate is 2～4kgCOD/kgMLSSd, hydraulic detention time 0.5～1h, dissolved oxygen 0.1～0.3mg/L, sludge concentration is 4000～5000mg/L, settling tank sedimentation time 2h, return sludge ratio are 20%～40%, COD clearance 25%～35%.Water outlet enters acidogenic reactor, reflux ratio 200%, mixed liquor suspended solid, MLSS concentration 15～20g/L, pH5.5～6.5, dissolved oxygen 0.0mg/L, hydraulic detention time 8～10h, pH4.5～6.5; Water outlet enters the desulfurization pond, pH5.5～6.5, dissolved oxygen 1.5～2.0mg/L, hydraulic detention time 0.15h, after desulfurization, enter and produce methane pond pH control 6.5～7.5, mixed liquor suspended solid, MLSS concentration 15～20g/L, dissolved oxygen 0.0mg/L, hydraulic detention time 8～10h, other waste water such as water outlet and sanitary sewage are mixed into the Anoxybiotic-aerobic biologic denitrification system.Anoxic pond control reflux ratio 100～300%, mixed liquor suspended solid, MLSS concentration 4～6g/L, dissolved oxygen≤0.5mg/L, hydraulic detention time 6～8h, sludge retention time 5～10d; After the pH control 6.5～7.5, enter aerobic section then, mixed liquor suspended solid, MLSS concentration 2～6g/L, dissolved oxygen 〉=2mg/L, hydraulic detention time 6～8h, sludge retention time 5～10d, pH 7.5～8.5, COD volumetric loading 0.5～1.0kgCOD/m
3D; Return sludge ratio 50%～100%.Water outlet COD50～60mg/L, NH
3-N 15mg/L, suspended sediment concentration 50mg/L, EDTA 8～10mg/L, pH6～9 can reach national acrylic fiber industry first discharge standard.
Embodiment 2
Dry acrylic fiber processing wastewater COD 2000-2500mg/L, turbidity 40～60mg/L, total nitrogen 100～300mg/L, sulfate radical 500～1000mg/L is cooled to 50 ℃～65 ℃ through a grade cooling tower, in the pipeline coagulation device with polymerize aluminum chloride 50～100mg/L, cation high molecular quaternary ammonium salt flocculation agent 2～3mg/L mixes, enter the pressure air-dissolving air-float pond, dissolved-air pressure 0.25～0.3Mpa, gas-water ratio is 1: 3; Supernatant liquor cools to about 35 ℃ by secondary, and the COD clearance of the pretreated technology of air-dissolving air-float is 25～35%, delivery turbidity≤10mg/L.Enter and enter biological adsorption tank after equalizing tank is regulated pH5.5～6.5, the aeration tank mud load rate is 2～4kgCOD/kgMLSSd, hydraulic detention time 1～2h, dissolved oxygen 0.3～0.5mg/L, sludge concentration is 5000～6000mg/L, settling tank sedimentation time 2h, return sludge ratio are 30%～50%, COD clearance 25%～35%.Water outlet enters acidogenic reactor, reflux ratio 200%, mixed liquor suspended solid, MLSS concentration 15～20g/L, pH4.5～6.5, hydraulic detention time 10～16h, pH4.5～6.5; Water outlet enters the desulfurization pond, pH5.5～6.5, dissolved oxygen 1.5～2.0mg/L, hydraulic detention time 0.15h, after desulfurization, enter and produce methane pond pH control 6.5～7.5, mixed liquor suspended solid, MLSS concentration 15～20g/L, hydraulic detention time 10～16h, other waste water such as water outlet and sanitary sewage are mixed into the Anoxybiotic-aerobic biologic denitrification system.Anoxic pond control reflux ratio 300～500%, mixed liquor suspended solid, MLSS concentration 4～6g/L, dissolved oxygen≤0.5mg/L, hydraulic detention time 8～12h, sludge retention time 5～10d; After the pH control 6.5～7.5, enter aerobic section then, mixed liquor suspended solid, MLSS concentration 2～6g/L, dissolved oxygen 〉=2mg/L, hydraulic detention time 8～12h, sludge retention time 10～15d, pH7.5～8.5, COD volumetric loading 0.5～1.0kgCOD/m
3D; Return sludge ratio 50%～100%.Water outlet COD 50～70mg/L, NH
3-N 15mg/L, suspended sediment concentration 50mg/L, EDTA 6～7mg/L, pH6～9 can reach national acrylic fiber industry first discharge standard.
Embodiment 3
Dry acrylic fiber processing wastewater COD 1500-2000mg/L, turbidity 10～40mg/L, total nitrogen 100～300mg/L, sulfate radical 500～1000mg/L, be cooled to 50 ℃～65 ℃ through a grade cooling tower, with polymerize aluminum chloride 100～150mg/L, cation high molecular quaternary flocculation agent CP-937 1mg/L mixes in the pipeline coagulation device, water pH value 6.0～7.5 enters bleed method air flotation pool; Supernatant liquor cools to about 35 ℃ by secondary, and the COD clearance of the pretreated technology of air-dissolving air-float is 25～35%, delivery turbidity≤10mg/L.Enter and enter biological adsorption tank after equalizing tank is regulated pH5.5～6.5, the aeration tank mud load rate is 2～4kgCOD/kgMLSSd, hydraulic detention time 0.5～1h, dissolved oxygen 0.1～0.3mg/L, sludge concentration is 4000～5000mg/L, settling tank sedimentation time 2h, return sludge ratio are 20%～40%, COD clearance 25%～35%.Water outlet enters acidogenic reactor, reflux ratio 200%, mixed liquor suspended solid, MLSS concentration 15～20g/L, pH5.5～6.5, dissolved oxygen 0.0mg/L, hydraulic detention time 8～10h, pH4.5～6.5; Water outlet enters the desulfurization pond, pH5.5～6.5, dissolved oxygen 1.5～2.0mg/L, hydraulic detention time 0.15h, after desulfurization, enter and produce methane pond pH control 6.5～7.5, mixed liquor suspended solid, MLSS concentration 15～20g/L, dissolved oxygen 0.0mg/L, hydraulic detention time 8～10h, other waste water such as water outlet and sanitary sewage are mixed into the Anoxybiotic-aerobic biologic denitrification system.Anoxic pond control reflux ratio 100～300%, mixed liquor suspended solid, MLSS concentration 4～6g/L, dissolved oxygen≤0.5mg/L, hydraulic detention time 6～8h, sludge retention time 5～10d; After the pH control 6.5～7.5, enter aerobic section then, mixed liquor suspended solid, MLSS concentration 2～6g/L, dissolved oxygen 〉=2mg/L, hydraulic detention time 6～8h, sludge retention time 5～10d, pH 7.5～8.5, COD volumetric loading 0.5～1.0kgCOD/m
3D; Return sludge ratio 50%～100%.Water outlet COD 50～60mg/L, NH
3-N 15mg/L, suspended sediment concentration 50mg/L, EDTA 6～9mg/L, pH6～9 can reach national acrylic fiber industry first discharge standard.
Embodiment 4
Dry acrylic fiber processing wastewater COD 2000-2500mg/L, turbidity 0～60mg/L, total nitrogen 100～300mg/L, sulfate radical 500～1000mg/L, be cooled to 50 ℃～65 ℃ through a grade cooling tower, with polymerize aluminum chloride 50～100mg/L, cation high molecular quaternary ammonium salt flocculation agent 2～3mg/L mixes, and enters the Induced-draft air float pond in the pipeline coagulation device; Supernatant liquor cools to about 35 ℃ by secondary, and the COD clearance of the pretreated technology of air-dissolving air-float is 25～35%, delivery turbidity≤10mg/L.Enter and enter biological adsorption tank after equalizing tank is regulated pH5.5～6.5, the aeration tank mud load rate is 2～4kgCOD/kgMLSSd, hydraulic detention time 1～2h, dissolved oxygen 0.3～0.5mg/L, sludge concentration is 5000～6000mg/L, settling tank sedimentation time 2h, return sludge ratio are 30%～50%, COD clearance 25%～35%.Water outlet enters acidogenic reactor, reflux ratio 200%, mixed liquor suspended solid, MLSS concentration 15～20g/L, pH4.5～6.5, hydraulic detention time 10～16h, pH4.5～6.5; Water outlet enters the desulfurization pond, pH5.5～6.5, dissolved oxygen 1.5～2.0mg/L, hydraulic detention time 0.15h, after desulfurization, enter and produce methane pond pH control 6.5～7.5, mixed liquor suspended solid, MLSS concentration 15～20g/L, hydraulic detention time 10～16h, other waste water such as water outlet and sanitary sewage are mixed into the Anoxybiotic-aerobic biologic denitrification system.Anoxic pond control reflux ratio 300～500%, mixed liquor suspended solid, MLSS concentration 4～6g/L, dissolved oxygen≤0.5mg/L, hydraulic detention time 8～12h, sludge retention time 5～10d; After the pH control 6.5～7.5, enter aerobic section then, mixed liquor suspended solid, MLSS concentration 2～6g/L, dissolved oxygen 〉=2mg/L, hydraulic detention time 8～12h, sludge retention time 10～15d, pH 7.5～8.5, COD volumetric loading 0.5～1.0kgCOD/m
3D; Return sludge ratio 50%～100%.Water outlet COD 50～100mg/L, NH
3-N 15mg/L, suspended sediment concentration 40mg/L, EDTA 6～8mg/L, pH 6～9, reach national acrylic fiber industry first discharge standard.
Embodiment 5
Dry acrylic fiber processing wastewater COD 2000-2500mg/L, turbidity 40～60mg/L, total nitrogen 100～300mg/L, sulfate radical 500～1000mg/L, be cooled to 50 ℃～65 ℃ through a grade cooling tower, with polymerize aluminum chloride 50～100mg/L, cation high molecular quaternary ammonium salt flocculation agent 2mg/L mixes, and enters air flotation pool in the pipeline coagulation device.Supernatant liquor cools to about 35 ℃ by secondary, enter and enter biological adsorption tank after equalizing tank is regulated pH5.5～6.5, hydraulic detention time 0.5～1h, dissolved oxygen 0.1～0.3mg/L, sludge concentration is 4000～5000mg/L, settling tank sedimentation time 2h, return sludge ratio are 20%～40%, COD clearance 25%～35%.Water outlet enters acidogenic reactor, reflux ratio 200%, mixed liquor suspended solid, MLSS concentration 15～20g/L, pH5.5～6.5, dissolved oxygen 0.0mg/L, hydraulic detention time 8～10h, pH4.5～6.5; Water outlet enters the desulfurization pond, pH5.5～6.5, dissolved oxygen 1.5～2.0mg/L, hydraulic detention time 0.15h, after desulfurization, enter and produce methane pond pH control 6.5～7.5, mixed liquor suspended solid, MLSS concentration 15～20g/L, hydraulic detention time 8～10h, other waste water such as water outlet and sanitary sewage are mixed into the Anoxybiotic-aerobic biologic denitrification system.Anoxic pond control reflux ratio 100～300%, mixed liquor suspended solid, MLSS concentration 4～6g/L, dissolved oxygen≤0.5mg/L, hydraulic detention time 6～8h, sludge retention time 5～10d; After the pH control 6.5～7.5, enter aerobic section then, mixed liquor suspended solid, MLSS concentration 2～6g/L, dissolved oxygen 〉=2mg/L, hydraulic detention time 6～8h, sludge retention time 5～10d, pH 7.5～8.5, COD volumetric loading 0.5～1.0kgCOD/m
3D; Return sludge ratio 50%～100%.Water outlet COD 50～60mg/L, NH
3-N15mg/L, suspended sediment concentration 50mg/L, EDTA 6～8mg/L, pH6～9 can reach national acrylic fiber industry first discharge standard.All the other are with example 1.
Embodiment 6
Dry acrylic fiber processing wastewater COD 2000-2500mg/L, turbidity 40～60mg/L, total nitrogen 100～300mg/L, sulfate radical 500～1000mg/L is cooled to 50 ℃～65 ℃ through a grade cooling tower, in the pipeline coagulation device with polymerize aluminum chloride 50～100mg/L, cation high molecular quaternary ammonium salt flocculation agent 2～3mg/L mixes, enter the pressure air-dissolving air-float pond, dissolved-air pressure 0.25～0.3Mpa, gas-water ratio is 1: 3; Supernatant liquor cools to about 35 ℃ by secondary, and the COD clearance of the pretreated technology of air-dissolving air-float is 25～35%, delivery turbidity≤10mg/L.Enter and enter biological adsorption tank after equalizing tank is regulated pH5.5～6.5, the aeration tank mud load rate is 2～4kgCOD/kgMLSSd, hydraulic detention time 1～2 h, dissolved oxygen 0.3～0.5mg/L, sludge concentration is 5000～6000mg/L, settling tank sedimentation time 2h, return sludge ratio are 30%～50%, COD clearance 25%～35%.Water outlet enters acidogenic reactor, reflux ratio 200%, and mixed liquor suspended solid, MLSS concentration 15～20g/L, pH4.5～6.5, hydraulic detention time 10～16h, pH4.5～6. 5; Water outlet enters the desulfurization pond, pH5.5～6.5, dissolved oxygen 1.5～2.0mg/L, hydraulic detention time 0.15h, after desulfurization, enter and produce methane pond pH control 6.5～7.5, mixed liquor suspended solid, MLSS concentration 15～20g/L, hydraulic detention time 10～16h, other waste water such as water outlet and sanitary sewage are mixed into the Anoxybiotic-aerobic biologic denitrification system.Anoxic pond control reflux ratio 300～500%, mixed liquor suspended solid, MLSS concentration 4～6g/L, dissolved oxygen≤0.5mg/L, hydraulic detention time 8～12h, sludge retention time 5～10d; After the pH control 6.5～7.5, enter aerobic section then, mixed liquor suspended solid, MLSS concentration 2～6g/L, dissolved oxygen 〉=2mg/L, hydraulic detention time 8～12h, sludge retention time 10～15d, pH7.5～8.5, COD volumetric loading 0.5～1.0kgCOD/m
3D; Return sludge ratio 50%～100%.Water outlet COD 50～160mg/L, NH
3-N 15mg/L, suspended sediment concentration 50mg/L, EDTA 6～10mg/L, pH6～9 can reach national acrylic fiber industry first discharge standard.All the other are with example 2.
Embodiment 7 dry acrylic fiber processing wastewater COD 2000-2500mg/L, turbidity 40～60mg/L, total nitrogen 100～300mg/L, sulfate radical 200～500mg/L is because the COD/ sulfate radical can save greater than the sulfur removal technology between 4, two anaerobic reactors.Through cool-pneumatically supported Nitrilon waste water supernatant liquor cools to 35 ℃ by secondary about, enter and enter biological adsorption tank after equalizing tank is regulated pH5.5～6.5, hydraulic detention time 0.5hr, water outlet directly enters acidogenic reactor, hydraulic detention time 10～14h, pH4.8～6.5, water outlet enters produces methane pond pH control 6.5～7.5, hydraulic detention time 10～14h, other waste water such as water outlet and sanitary sewage are mixed into the Anoxybiotic-aerobic biologic denitrification system.Anoxic pond control dissolved oxygen is less than 0.5mg/L, hydraulic detention time 8～10h, sludge retention time 5～10d is after the pH control 6.5～7.5, enter aerobic section then, dissolved oxygen is greater than 2mg/L, hydraulic detention time 6～8h, sludge retention time 10～15d, pH7.5～8.5, effluent recycling is to anoxic pond, reflux ratio 300%～500%, return sludge ratio 50%～100%.Water outlet can reach national acrylic fiber industry first discharge standard.All the other are with example 3.
Embodiment 8
Dry acrylic fiber processing wastewater COD 1500-2000mg/L, turbidity 10～40mg/L, total nitrogen 100～300mg/L, sulfate radical 200～500mg/L is because the COD/ sulfate radical can remain greater than the sulfur removal technology between 4, two anaerobic reactors.Through cool-pneumatically supported Nitrilon waste water supernatant liquor cools to 35 ℃ by secondary about, enter and enter biological adsorption tank after equalizing tank is regulated pH5.5～6.5, hydraulic detention time 1.0h, water outlet enters acidogenic reactor, hydraulic detention time 8～10h, pH4.8～6.5, water outlet enters after the desulfurization of desulfurization pond produces methane pond pH control 6.5～7.5, hydraulic detention time 8～10h, other waste water such as water outlet and sanitary sewage are mixed into the Anoxybiotic-aerobic biologic denitrification system.Anoxic pond is controlled dissolved oxygen less than 0.5mg/L, hydraulic detention time 6～8h, sludge retention time 5～10d; After the pH control 6.5～7.5, enter aerobic section then, dissolved oxygen is greater than 2mg/L, and hydraulic detention time is less than 6h, sludge retention time 8～15d, and pH7.5～8.5, effluent recycling is to anoxic pond, reflux ratio 300%～500%, return sludge ratio 50%～100%.Water outlet reaches national acrylic fiber industry first discharge standard.Surplus with example 4.
Embodiment 9
Dry acrylic fiber processing wastewater COD2000-2500mg/L, turbidity 40～60mg/L, total nitrogen 100～300mg/L, sulfate radical 500～1000mg/L, be cooled to 50 ℃～65 ℃ through a grade cooling tower, with polymerize aluminum chloride 50～100mg/L, cation high molecular quaternary ammonium salt flocculation agent 1～3mg/L mixes, and enters air flotation pool in the pipeline coagulation device.Supernatant liquor cools to about 35 ℃ by secondary, through cooling-pneumatically supported Nitrilon waste water, enter and enter biological adsorption tank after equalizing tank is regulated pH5.5～6.5, hydraulic detention time 2.0h, water outlet enters acidogenic reactor, hydraulic detention time 12～16h, pH4.8～6.5, water outlet enters after the desulfurization of desulfurization pond produces methane pond pH control 6.5～7.5, hydraulic detention time 12～16h, and other waste water such as water outlet and sanitary sewage are mixed into the Anoxybiotic-aerobic biologic denitrification system.Anoxic pond is controlled dissolved oxygen less than 0.5mg/L, hydraulic detention time 6～8h, sludge retention time 5～10d; After the pH control 6.5～7.5, enter aerobic section then, dissolved oxygen is greater than 2mg/L, and hydraulic detention time is less than 6h, sludge retention time 8～15d, and pH7.5～8.5, effluent recycling is to anoxic pond, reflux ratio 300%～500%, return sludge ratio 50%～100%.Water outlet can reach national acrylic fiber industry first discharge standard.All the other are with example 1.
Embodiment 10
Dry acrylic fiber processing wastewater COD2000-2500mg/L, turbidity 40～60mg/L, total nitrogen 100～300mg/L, sulfate radical 500～1000mg/L, be cooled to 50 ℃～65 ℃ through a grade cooling tower, with polymerize aluminum chloride 50～100mg/L, cation high molecular quaternary ammonium salt flocculation agent 1～3mg/L mixes, and enters air flotation pool in the pipeline coagulation device.Through cool-pneumatically supported Nitrilon waste water supernatant liquor cools to 35 ℃ by secondary about, enter and enter biological adsorption tank after equalizing tank is regulated pH5.5～6.5, hydraulic detention time 1.0hr, water outlet enters acidogenic reactor, hydraulic detention time 12～16 hours, pH4.8～6.5, water outlet enters after the desulfurization of desulfurization pond produces methane pond pH control 6.5～7.5, hydraulic detention time 12～16 hours, other waste water such as water outlet and sanitary sewage are mixed into the Anoxybiotic-aerobic biologic denitrification system.Anoxic pond is controlled dissolved oxygen less than 0.5mg/L, hydraulic detention time 8～10 hours, sludge retention time 5～10 days; After the pH control 6.5～7.5, enter aerobic section then, dissolved oxygen is greater than 2mg/L, hydraulic detention time 8～10 hours, sludge retention time 8～15 days, pH 7.5～8.5, effluent recycling is to anoxic pond, reflux ratio 300%～500%, return sludge ratio 50%～100%.Water outlet can reach national acrylic fiber industry first discharge standard.All the other are with example 2.
Embodiment 11
Dry acrylic fiber processing wastewater COD2000-2500mg/L, turbidity 40～60mg/L, total nitrogen 100～300mg/L, sulfate radical 500～1000mg/L, be cooled to 50 ℃～65 ℃ through a grade cooling tower, with polymerize aluminum chloride 50～100mg/L, cation high molecular quaternary ammonium salt flocculation agent 1～3mg/L mixes, and enters air flotation pool in the pipeline coagulation device.Through cool-pneumatically supported Nitrilon waste water supernatant liquor cools to 35 ℃ by secondary about, enter and enter biological adsorption tank after equalizing tank is regulated pH5.5～6.5, hydraulic detention time 1.0hr, water outlet enters acidogenic reactor, hydraulic detention time 12～16 hours, pH4.8～6.5, water outlet enters after the desulfurization of desulfurization pond produces methane pond pH control 6.5～7.5, hydraulic detention time 12～16 hours, other waste water such as water outlet and sanitary sewage are mixed into the Anoxybiotic-aerobic biologic denitrification system.Anoxic pond is controlled dissolved oxygen less than 0.5mg/L, hydraulic detention time 10～12 hours, sludge retention time 5～10 days; After the pH control 6.5～7.5, enter aerobic section then, dissolved oxygen is greater than 2mg/L, hydraulic detention time 10～12 hours, sludge retention time 8～15 days, pH 7.5～8.5, effluent recycling is to anoxic pond, reflux ratio 300%～500%, return sludge ratio 50%～100%.Water outlet can reach national acrylic fiber industry first discharge standard.All the other are with example 3.
Embodiment 12 dry acrylic fiber processing wastewater COD2000-2500mg/L, turbidity 40～60mg/L, total nitrogen 100～300mg/L, sulfate radical 500～1000mg/L, be cooled to 50 ℃～65 ℃ through a grade cooling tower, with polymerize aluminum chloride 50～100mg/L, cation high molecular quaternary ammonium salt flocculation agent 1～3mg/L mixes, and enters air flotation pool in the pipeline coagulation device.Through cool-pneumatically supported Nitrilon waste water supernatant liquor cools to 35 ℃ by secondary about, enter and enter biological adsorption tank after equalizing tank is regulated pH5.5～6.5, hydraulic detention time 1.0hr, water outlet enters acidogenic reactor, hydraulic detention time 12～16 hours, pH4.8～6.5, water outlet enters after the desulfurization of desulfurization pond produces methane pond pH control 6.5～7.5, hydraulic detention time 12～16 hours, other waste water such as water outlet and sanitary sewage are mixed into the Anoxybiotic-aerobic biologic denitrification system.Anoxic pond is controlled dissolved oxygen less than 0.5mg/L, hydraulic detention time 10～12 hours, sludge retention time 5～10 days; After the pH control 6.5～7.5, enter aerobic section then, dissolved oxygen is greater than 2mg/L, hydraulic detention time 10～12 hours, sludge retention time 8～15 days, pH7.5～8.5, effluent recycling is to anoxic pond, reflux ratio 100%～200%, return sludge ratio 50%～100%.Water outlet can reach national acrylic fiber industry first discharge standard.All the other are with example 4.
Embodiment 13 dry acrylic fiber processing wastewater COD2000-2500mg/L, turbidity 40～60mg/L, total nitrogen 100～300mg/L, sulfate radical 1000～2000mg/L, because sulfate concentration is greater than 1000mg/L, waste water is earlier by being equipped with the Filter column of calcium oxide, make water outlet sulfate concentration 200～500mg/L, enter a grade cooling tower then and be cooled to 50 ℃～65 ℃, in the pipeline coagulation device with polymerize aluminum chloride 50～100mg/L, cation high molecular quaternary ammonium salt flocculation agent 1～3mg/L mixes, and enters air flotation pool.Supernatant liquor cools to about 35 ℃ by secondary, through cool-pneumatically supported Nitrilon waste water supernatant liquor cools to 35 ℃ by secondary about, enter and enter biological adsorption tank after equalizing tank is regulated pH5.5～6.5, hydraulic detention time 1.0hr, water outlet enters acidogenic reactor, hydraulic detention time 12～16 hours, pH4.8～6.5, water outlet enters after the desulfurization of desulfurization pond produces methane pond pH control 6.5～7.5, hydraulic detention time 12～16 hours, other waste water such as water outlet and sanitary sewage are mixed into the Anoxybiotic-aerobic biologic denitrification system.Anoxic pond is controlled dissolved oxygen less than 0.5mg/L, hydraulic detention time 10～12 hours, sludge retention time 5～10 days; After the pH control 6.5～7.5, enter aerobic section then, dissolved oxygen is greater than 2mg/L, hydraulic detention time 10～12 hours, sludge retention time 8～15 days, pH 7.5～8.5, effluent recycling is to anoxic pond, reflux ratio 100%～200%, return sludge ratio 50%～100%.Water outlet can reach national acrylic fiber industry first discharge standard.
Embodiment 14 dry acrylic fiber processing wastewater COD 1500-2000mg/L, turbidity 10～40mg/L, total nitrogen 100～300mg/L, sulfate radical 500～1000mg/L, be cooled to 50 ℃～65 ℃ through a grade cooling tower, with polymerize aluminum chloride 10～50mg/L, cation high molecular quaternary flocculation agent 1mg/L mixes, and enters the pressure air-dissolving air-float pond in the pipeline coagulation device.Supernatant liquor cools to about 35 ℃ by secondary, enter and enter biological adsorption tank after equalizing tank is regulated pH5.5～6.5, hydraulic detention time 0.5hr, water outlet enters acidogenic reactor, hydraulic detention time 8～10 hours, pH4.8～6.5, water outlet enters after the desulfurization of desulfurization pond produces methane pond pH control 6.5～7.5, hydraulic detention time 8～10 hours, other waste water such as water outlet and sanitary sewage are mixed into the Anoxybiotic-aerobic biologic denitrification system.Anoxic pond is controlled dissolved oxygen less than 0.5mg/L, hydraulic detention time 6～8 hours, sludge retention time 5～10 days; After the pH control 6.5～7.5, enter aerobic section then, dissolved oxygen is greater than 2mg/L, hydraulic detention time is less than 6 hours, sludge retention time 8～15 days, pH7.5～8.5, effluent recycling is to anoxic pond, reflux ratio 300%～500%, return sludge ratio 50%～100%.Water outlet can reach national acrylic fiber industry first discharge standard.
Embodiment 15 dry acrylic fiber processing wastewater COD 1500-2000mg/L, turbidity 10～40mg/L, total nitrogen 100～300mg/L, sulfate radical 500～1000mg/L, be cooled to 50 ℃～65 ℃ through a grade cooling tower, with polymerize aluminum chloride 10～50mg/L, cation high molecular quaternary ammonium salt flocculation agent 1mg/L mixes, and enters the Induced-draft air float pond in the pipeline coagulation device.Supernatant liquor cools to about 35 ℃ by secondary, enter and enter biological adsorption tank after equalizing tank is regulated pH5.5～6.5, hydraulic detention time 0.5hr, water outlet enters acidogenic reactor, hydraulic detention time 8～10 hours, pH4.8～6.5, water outlet enters after the desulfurization of desulfurization pond produces methane pond pH control 6.5～7.5, hydraulic detention time 8～10 hours, other waste water such as water outlet and sanitary sewage are mixed into the Anoxybiotic-aerobic biologic denitrification system.Anoxic pond is controlled dissolved oxygen less than 0.5mg/L, hydraulic detention time 6～8 hours, sludge retention time 5～10 days; After the pH control 6.5～7.5, enter aerobic section then, dissolved oxygen is greater than 2mg/L, hydraulic detention time is less than 6 hours, sludge retention time 8～15 days, pH7.5～8.5, effluent recycling is to anoxic pond, reflux ratio 300%～500%, return sludge ratio 50%～100%.Water outlet can reach national acrylic fiber industry first discharge standard.
Embodiment 16 epoxy chloropropane processing wastewaters are handled
The epoxy chloropropane processing wastewater is higher owing to saltiness, and wherein contains the organic chloride of aerobic difficult for biological degradation, adopts coagulating sedimentation-diphasic anaerobic-aerobic process flow process, can make water outlet reach national grade one discharge standard.Epoxy chloropropane waste water COD 1500～2000mg/L, total salt 1.0%～1.5%, wherein owing to saltiness height in the waste water, the domestication process of mud takes longer.Aerobic not only treatment effect is good as adopting pure oxygen aeration, and the residence time is short.
Claims (12)
1. the treatment process of an acrylic fibers waste water by dry process is characterized in that adopting air supporting pre-treatment-AB biological treatment flow process, and wherein the A section is biological absorption, and the B section is anaerobism-anoxic-aerobic process, comprises following processing step:
The dry acrylic fiber processing wastewater is cooled to 50 ℃～65 ℃ through a grade cooling tower, in the pipeline coagulation device, mix with polymerize aluminum chloride and commercial goods CP-937 cation high molecular quaternary flocculation agent, enter air flotation pool, air supporting handle the back supernatant liquor by secondary cool enter equalizing tank and regulate pH5.5～6.5 to 35 ℃ after; Waste water enters aeration tank, the settling tank of the biological absorption of A section successively; Subsequently, waste water enters the anaerobic digestion operation, at the sulfate reduction acid-producing with produce methane reaction placed in-line while of independent reaction phase-splitting separately, increases the biological desulphurization step between the two, becomes sulfate reduction-biological desulphurization-product methane three-phase tandem process; At last, introduce sanitary sewage and produce peace and quiet water down in the anoxic section, waste water after anoxic-aerobic biological denitrification operation is handled, qualified discharge; Wherein:
Pressure air-dissolving method or bleed method technology are adopted in the air supporting pre-treatment, remove low-molecular(weight)polymer in this waste water; The pretreated technology operating parameter of pressure air-dissolving method air supporting is: 50～65 ℃ of temperature, polymerize aluminum chloride injected volume 20～150mg/L, quaternary ammonium salt cationic flocculation agent injected volume 1～3mg/L, water pH value 6.0～7.5, dissolved-air pressure 0.25～0.3Mpa, gas-water ratio is 1: 3; The pretreated technology operating parameter of bleed method air supporting is: 50～65 ℃ of temperature, polymerize aluminum chloride injected volume 20～150mg/L, quaternary ammonium salt cationic flocculation agent injected volume 1～3mg/L, water pH value 6.0～7.5.
2. according to the treatment process of the described acrylic fibers waste water by dry process of claim 1, the COD clearance that it is characterized in that the pretreated technology of pressure air-dissolving air-float is 25～35%, delivery turbidity≤10mg/L.
3. according to the treatment process of the described acrylic fibers waste water by dry process of claim 1, it is characterized in that: A segment process parameter, the aeration tank mud load rate is 2～4kgCOD/kgMLSSd, hydraulic detention time 0.5～2h, dissolved oxygen 0.1～0.5mg/L, sludge concentration is 4000～6000mg/L, settling tank sedimentation time 2h, return sludge ratio is 20%～50%, COD clearance 25%～35%.
4. according to the treatment process of the described acrylic fibers waste water by dry process of claim 1, it is characterized in that the technology operating parameter is in the sulfate reduction acid-producing: mixed liquor suspended solid, MLSS concentration 15～20g/L, pH4.5～6.5, dissolved oxygen 0.0mg/L, hydraulic detention time 8～16h.
5. according to the treatment process of claim 1 or 4 described acrylic fibers waste water by dry process, it is characterized in that the technology operating parameter is in the biological desulphurization step: pH5.5～6.5, dissolved oxygen 1.5～2.5mg/L, hydraulic detention time 0.15h.
6. according to the treatment process of claim 1 or 4 described acrylic fibers waste water by dry process, it is characterized in that the technology operating parameter is in producing methane reaction: mixed liquor suspended solid, MLSS concentration 15～20g/L, pH6.5～7.5, dissolved oxygen 0.0mg/L, hydraulic detention time 8～16h.
7. according to the treatment process of the described acrylic fibers waste water by dry process of claim 1, it is characterized in that the technology operating parameter is in the anoxic biological denitrificaion operation: mixed liquor suspended solid, MLSS concentration 4～6g/L, pH6.5～7.5, dissolved oxygen≤0.5mg/L, sludge retention time 5～10d, hydraulic detention time 6～12h.
8. according to the treatment process of the described acrylic fibers waste water by dry process of claim 1, it is characterized in that the technology operating parameter is in the aerobic biological denitrification operation: mixed liquor suspended solid, MLSS concentration 2～6g/L, pH7.5～8.5, dissolved oxygen 〉=2.0mg/L, sludge retention time 5～10d, hydraulic detention time 6～12h, COD volumetric loading 0.5～1.0kgCOD/m
3D.
9. according to the treatment process of the described acrylic fibers waste water by dry process of claim 1, it is characterized in that discharging after treatment water quality and can reach down
State index: COD 50～160mg/L, NH
3-N 15mg/L, suspended sediment concentration 50mg/L, EDTA 6～10mg/L, pH6～9.
10. according to the treatment process of claim 1 or 8 described acrylic fibers waste water by dry process, it is characterized in that to add Powdered Activated Carbon 5～50ppm at aerobic section as the bio-chemical effluent phenomenon that exceeds standard occurring.
11. according to the treatment process of the described acrylic fibers waste water by dry process of claim 1, it is characterized in that working as sulfate concentration＞1000mg/L in the anaerobic digestion operation, waste water makes the water outlet sulfate concentration reduce to 200～500mg/L earlier by the Filter column of calcium oxide is housed.
12., it is characterized in that this law is equally applicable to the processing of epoxy chloropropane trade effluent according to the treatment process of the described acrylic fibers waste water by dry process of claim 1.
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| CN101734791B (en) * | 2008-11-26 | 2011-07-27 | 孙光志 | Method for treating biological sewage |
| CN102115297A (en) * | 2011-01-14 | 2011-07-06 | 中国环境科学研究院 | Double-reflux denitrification membrane-bioreactor (MBR) process for treating dry acrylic fiber waste water |
| CN102276107B (en) * | 2011-05-30 | 2013-08-21 | 北京环利科环境工程技术有限公司 | Acrylic fiber sewage treatment technology through PHAOB method |
| CN105000751A (en) * | 2015-07-01 | 2015-10-28 | 江苏天成生化制品有限公司 | Integrated treatment method of aceto acetanilide wastewater and diketene wastewater |
| CN105439235B (en) * | 2016-01-13 | 2017-10-13 | 河北工业大学 | The method that two-stage froth flotation method pre-processes Nitrilon waste water |
| CN105776525B (en) * | 2016-03-01 | 2019-03-01 | 南京大学 | Integral type diphasic anaerobic desulfurization reactor and its wastewater treatment method |
| CN106495246A (en) * | 2016-11-21 | 2017-03-15 | 德宏电子(苏州)有限公司 | Fibrillation method for treating water |
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