CN103435217B - Treatment process for sulfuration printing and dyeing wastewater - Google Patents

Treatment process for sulfuration printing and dyeing wastewater Download PDF

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CN103435217B
CN103435217B CN201310343216.3A CN201310343216A CN103435217B CN 103435217 B CN103435217 B CN 103435217B CN 201310343216 A CN201310343216 A CN 201310343216A CN 103435217 B CN103435217 B CN 103435217B
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settling tank
oxidation
cod
treatment process
water outlet
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CN103435217A (en
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刘进龙
陆张昕
张立果
张德
杨宇
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Guangdong Bofang Environmental Protection Technology Group Co ltd
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GUANGZHOU BOFANG ENVIRONMENTAL PROTECTION TECHNOLOGY Co Ltd
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Abstract

The invention discloses a treatment process for sulfuration printing and dyeing wastewater. The treatment process adopts the comprehensive treatment method comprising the steps of preaeration catalyzed oxidation, physico-chemical desulfuration, UV-fenton catalyzed oxidation, hydrolytic acidification and contact oxidation, so that wastewater is enabled to achieve the first-level discharge standard and the cost and sludge quantity for complete pharmaceutical treatment of wastewater can be reduced. The wastewater treatment process disclosed by the invention is stable, the impact resistance is strong, and the wastewater reaches the standard stably and is discharged finally; moreover, the toxic gas is collected and processed, so that the whole process is environmentally friendly and the secondary pollution is not easy to cause.

Description

A kind for the treatment of process that vulcanizes dyeing waste water
Technical field
The invention belongs to environmental technology field, particularly a kind for the treatment of process that vulcanizes dyeing waste water.
Background technology
In dyeing waste water, contain dyestuff, slurry, auxiliary agent, finish, soda acid, fiber impurity, sand class material, inorganic salt etc., there is the water yield large, organic pollutant content is high, alkalescence is large, change of water quality is large, the features such as biodegradability is poor, belong to one of unmanageable trade effluent, especially the high density thioxine dyes waste water producing in the yarn slip of denim dyes process, wherein contain a large amount of thioxine dyess (as sulphur black, SULPHUR BLUE BRN 150, sulphur yellow brown etc.), Sodium Sulphide, polyvinyl alcohol (PVA), tensio-active agent, other dyeing and printing auxiliary etc. have toxicity, the pollutent of difficult degradation, water resources and atmospheric environment are caused to very serious pollution.
Process at present high density sulfuration dyeing waste water main method and have chemical flocculation precipitation method, oxidation style and biological process etc.If adopt separately chemical flocculation precipitation method, oxidation style is processed such waste water, cost is high, go out water unstable, sludge quantity is large, effluent color dilution easily turns black, adopt the method for materialization and biochemical combination to have certain effect to the sulfur-bearing waste water from dyestuff of lower concentration, but sulfur-bearing waste water from dyestuff concentration is high, when wastewater flow rate is large, physical chemistry method is wayward, cause biochemical paralysis, the anaerobic pond blackout that can make completely as untreated in sulfide, produce hydrogen sulfide stink, after entering Aerobic Pond, make microorganism intoxicating, cannot breed by normal growth, biofilm detachment etc., final outflow water blackout, COD etc. exceed standard.Simple such waste water of art breading such as anaerobic-aerobic or extended aeration that adopt, water outlet COD, colourity are all difficult to up to standard, and in the time that system water outlet adds strong oxidizer, sulfide can change into sulphur simple substance and separate out, water outlet is rare oyster white, and therefore colourity, COD are still difficult to qualified discharge.
Liu Rongzhan adopts coagulation air-float-Nei electrolysis-catalytic oxidation combination process to process Dyeing Wastewater Containing High Concentration Sulfurized Dyestuff, integrate coagulation, electrification, absorption, redoxomorphism, remarkable to removal effects such as sulfide, slurry, dyestuffs, water outlet reaches emission standard, and can realize part reuse (processing of Dyeing Wastewater Containing High Concentration Sulfurized Dyestuff and comprehensive utilization, Liu Rongzhan, chemical industry environmental protection, 01 phase in 2002); In patent application CN200810029835.4, adopt oxygenant to carry out desulfurization, then decolour with organic-inorganic discoloring agent, finally carry out biochemical treatment, reduce sludge quantity, make sewage qualified discharge.But the former processing costs is high, operation is difficult, and the latter, in actual application, goes out water unstable, and system impact resistance is poor, is more unfavorable for cleaner production and environmental protection requirement.
Summary of the invention
The object of the invention is to overcome the deficiencies in the prior art, a kind for the treatment of process that vulcanizes dyeing waste water is provided.
The technical solution used in the present invention is:
A kind for the treatment of process that vulcanizes dyeing waste water, it is characterized in that: sulfuration dyeing waste water is through the total system of grid, aerating regulation pond, physical reaction pond 1#, settling tank 1#, UV-Fenton's reaction pond 2#, settling tank 2#, hydrolysis acidification pool, two-stage contact-oxidation pool, settling tank 3#, carry out successively preaeration catalyzed oxidation, materialization desulfurization, UV-Fenton catalyzed oxidation, acidication, catalytic oxidation processing, after water outlet is up to standard, through the discharge of discharge pond, the mud that settling tank and hydrolysis acidification pool produce is transported outward after sludge thickener is processed.
Preferably, above-mentioned treatment process comprises following technical process:
1) preaeration catalyzed oxidation: sulfuration dyeing waste water enters aerating regulation pond after grid interception foreign material, regulates wastewater pH to 8.0~10.0, adds manganese oxide composite catalyst, and aeration, stirs, and stops 4~6h, and tail gas is carried out to collection and treatment;
2) materialization desulfurization: by the water outlet access physical reaction pond 1# in aerating regulation pond, add poly-ferric chloride aluminium water purifying agent, stir, regulate pH, occur slowing down and stirring after flco, add polyacrylamide flocculant, after coagulation, enter settling tank 1# and carry out mud-water separation;
3) UV-Fenton catalyzed oxidation: the water outlet access UV-Fenton's reaction pond 2# of settling tank 1#, regulate pH to 3.0~5.0, add Fenton reagent, utilize UV catalyzed oxidation, stop after 2~4h, regulate pH to 7.5~8.5, enter settling tank 2# and carry out mud-water separation;
4) acidication: the water outlet of settling tank 2# enters hydrolysis acidification pool, fully mixes with active sludge, acidication 4~6h;
5) catalytic oxidation: the water outlet of hydrolysis acidification pool directly enters two-stage contact-oxidation pool, fully mixes with active sludge, and control dissolved oxygen is 2~3mg/L, catalytic oxidation 8~10h;
6) qualified discharge: after catalytic oxidation is processed, in waste water, add polymerize aluminum chloride or polyaluminium sulfate, and polyacrylamide flocculant, after coagulation, enter settling tank 3# and carry out mud-water separation; After water outlet is up to standard, through the discharge of discharge pond, the mud that settling tank and hydrolysis acidification pool produce is transported outward after sludge thickener is processed.
Preferably, in step 1), the chemical feeding quantity of manganese oxide composite catalyst is 150~200mg/L.
Preferably, step 2) in, in poly-ferric chloride aluminium water purifying agent, the mass ratio of iron, aluminium is (4~5): 1, and its chemical feeding quantity is 1000~3000mg/L.
Preferably, step 2) in, the configuration concentration of polyacrylamide flocculant is 0.05~0.1wt%, its chemical feeding quantity is 1000~2000mg/L.
Preferably, in step 4), the inoculation culture method of active sludge is as follows: in hydrolysis acidification pool, add sanitary sewage, regulate COD crto 400~500mg/L, add carbon, nitrogen, phosphorus nutrition salt; Introduce active sludge, vexed exposing to the sun, COD crbe down to below 300mg/L, introduce continuously subsequently step 3) sewage after treatment, control COD crbe 300~400mg/L, dissolved oxygen DO is 2.0~3.0mg/L, water outlet COD in 1 week crbe stabilized in below 200mg/L, after this progressively improve influent load,, examine under a microscope meanwhile, survive and be after exponential phase or stationary phase growth and breeding until bacterium, controlling dissolved oxygen DO is 0.3~0.5mg/L, completes the inoculation culture of active sludge.
Preferably, introduce active sludge, make MLSS mass concentration reach 1000~2000mg/L.
Preferably, in step 5), the inoculation culture method of active sludge is as follows: in contact-oxidation pool, add sanitary sewage, regulate COD crto 400~500mg/L, add carbon, nitrogen, phosphorus nutrition salt; Introduce active sludge, vexed exposing to the sun, COD crbe down to below 300mg/L, introduce continuously subsequently step 4) sewage after treatment, control COD crbe 300~400mg/L, dissolved oxygen DO is 2.0~3.0mg/L, water outlet COD in 1 week crbe stabilized in below 200mg/L, after this, progressively improve influent load, meanwhile, microorganism is biofilm on contact-oxidation pool filler, and biofilm thickness reaches 1.5~2.0mm, and active sludge is inoculated successfully, then carries out sludge acclimatization and later stage operation.
Preferably, in step 6), the chemical feeding quantity of polymerize aluminum chloride or polyaluminium sulfate is 80~100 mg/L, and the chemical feeding quantity of polyacrylamide flocculant is 200~500mg/L.
Preferably, regulate waste water ph with unslaked lime.
The invention has the beneficial effects as follows:
The present invention adopts the integrated conduct method of preaeration catalyzed oxidation, materialization desulfurization, UV-Fenton catalyzed oxidation, acidication, catalytic oxidation to vulcanize the processing of dyeing waste water, improved the clearance of sulfide by preaeration catalyzed oxidation, reduce sludge quantity, for subsequent disposal operation is saved dosing; By physico-chemical precipitation and UV-Fenton advanced oxidation, thoroughly remove the pollutent of the toxicity such as sulfide, difficult degradation, make the biodegradability of waste water obtain maximizing raising, provide top condition for entering follow-up biochemical treatment; Utilize the remaining organic pollutant of the further degrading waste water of acidication and catalytic oxidation, make waste water reach first discharge standard, and reduce the expense and the sludge quantity that use chemicals treatment waste water completely.
Waste water treatment process of the present invention is stable, strong shock resistance, the final stably reaching standard discharge of waste water; And owing to carrying out the collection and treatment of toxic gas, whole technological process environmental protection, is difficult for producing secondary pollution.
Brief description of the drawings
Fig. 1 is the processing technological flow figure that the present invention vulcanizes dyeing waste water.
Embodiment
Further set forth content of the present invention below in conjunction with accompanying drawing 1 and specific embodiment.
A kind for the treatment of process that vulcanizes dyeing waste water, it is characterized in that: sulfuration dyeing waste water is through the total system of grid, aerating regulation pond, physical reaction pond 1#, settling tank 1#, UV-Fenton's reaction pond 2#, settling tank 2#, hydrolysis acidification pool, two-stage contact-oxidation pool, settling tank 3#, carry out successively preaeration catalyzed oxidation, materialization desulfurization, UV-Fenton catalyzed oxidation, acidication, catalytic oxidation processing, after water outlet is up to standard, through the discharge of discharge pond, the mud that settling tank and hydrolysis acidification pool produce is transported outward after sludge thickener is processed.
Preferably, above-mentioned treatment process comprises following technical process:
1) preaeration catalyzed oxidation: sulfuration dyeing waste water enters aerating regulation pond after grid interception foreign material, regulates wastewater pH to 8.0~10.0, adds manganese oxide composite catalyst, and aeration, stirs, and stops 4~6h, and tail gas is carried out to collection and treatment;
2) materialization desulfurization: by the water outlet access physical reaction pond 1# in aerating regulation pond, add poly-ferric chloride aluminium water purifying agent, stir, regulate pH, occur slowing down and stirring after flco, add polyacrylamide flocculant, after coagulation, enter settling tank 1# and carry out mud-water separation;
3) UV-Fenton catalyzed oxidation: the water outlet access UV-Fenton's reaction pond 2# of settling tank 1#, regulate pH to 3.0~5.0, add Fenton reagent, utilize UV catalyzed oxidation, stop after 2~4h, regulate pH to 7.5~8.5, enter settling tank 2# and carry out mud-water separation;
4) acidication: the water outlet of settling tank 2# enters hydrolysis acidification pool, fully mixes with active sludge, acidication 4~6h;
5) catalytic oxidation: the water outlet of hydrolysis acidification pool directly enters two-stage contact-oxidation pool, fully mixes with active sludge, and control dissolved oxygen is 2~3mg/L, catalytic oxidation 8~10h;
6) qualified discharge: after catalytic oxidation is processed, in waste water, add polymerize aluminum chloride or polyaluminium sulfate, and polyacrylamide flocculant, after coagulation, enter settling tank 3# and carry out mud-water separation; After water outlet is up to standard, through the discharge of discharge pond, the mud that settling tank and hydrolysis acidification pool produce is transported outward after sludge thickener is processed.
Preferably, in step 1), the chemical feeding quantity of manganese oxide composite catalyst is 150~200mg/L.In manganese oxide composite catalyst, contain 30~65wt%MnO 2, 10~40wt%Fe 2o 3, also contain a small amount of other metal oxides.
Preferably, step 2) in, in poly-ferric chloride aluminium water purifying agent, the mass ratio of iron, aluminium is (4~5): 1, and its chemical feeding quantity is 1000~3000mg/L.
Preferably, step 2) in, the configuration concentration of polyacrylamide flocculant is 0.05~0.1wt%, its chemical feeding quantity is 1000~2000mg/L.
Preferably, in step 4), the inoculation culture method of active sludge is as follows: in hydrolysis acidification pool, add sanitary sewage, regulate COD crto 400~500mg/L, add carbon, nitrogen, phosphorus nutrition salt; Introduce active sludge, vexed exposing to the sun, COD crbe down to below 300mg/L, introduce continuously subsequently step 3) sewage after treatment, control COD crbe 300~400mg/L, dissolved oxygen DO is 2.0~3.0mg/L, water outlet COD in 1 week crbe stabilized in below 200mg/L, after this progressively improve influent load,, examine under a microscope meanwhile, survive and be after exponential phase or stationary phase growth and breeding until bacterium, controlling dissolved oxygen DO is 0.3~0.5mg/L, completes the inoculation culture of active sludge.
Preferably, introduce active sludge, make MLSS mass concentration reach 1000~2000mg/L.
Preferably, in step 5), the inoculation culture method of active sludge is as follows: in contact-oxidation pool, add sanitary sewage, regulate COD crto 400~500mg/L, add carbon, nitrogen, phosphorus nutrition salt; Introduce active sludge, vexed exposing to the sun, COD crbe down to below 300mg/L, introduce continuously subsequently step 4) sewage after treatment, control COD crbe 300~400mg/L, dissolved oxygen DO is 2.0~3.0mg/L, water outlet COD in 1 week crbe stabilized in below 200mg/L, after this, progressively improve influent load, meanwhile, microorganism is biofilm on contact-oxidation pool filler, and biofilm thickness reaches 1.5~2.0mm, and active sludge is inoculated successfully, then carries out sludge acclimatization and later stage operation.
Preferably, in step 6), the chemical feeding quantity of polymerize aluminum chloride or polyaluminium sulfate is 80~100 mg/L, and the chemical feeding quantity of polyacrylamide flocculant is 200~500mg/L.
Preferably, regulate waste water ph with unslaked lime.
In step 1), utilize the special crystalline structure of manganese oxide composite catalyst material and catalytic activity, make to be adsorbed on surperficial H 2o and O 2produce hydroxyl radical free radical (OH), hydroxyl radical free radical has strong oxidizing property, and the larger molecular organicses such as energy sulfide oxidation and decomposition thioxine dyes molecule, make negative divalent sulfur be oxidized to sulphur simple substance and sulfate radical, and this step can reduce by 20~30% sulfide content.In this process, due to air aeration, the unnecessary gas entrainment hydrogen sulfide overflowing and other organic pollutants, so tail gas is carried out to collection and treatment, the present invention preferably adopts sealed construction to carry out preaeration catalyzed oxidation, collects waste gas from top, passes into lime pond.Certainly, those skilled in the art also can take according to practical situation other exhaust gas treating method.
Step 2) in, add poly-ferric chloride aluminium water purifying agent, unslaked lime, stir, regulate pH to 7.0~8.0, occur slowing down and stirring after flco, flco is not broken up, and add polyacrylamide flocculant (PAM), and allow the further change of flco be easy to greatly separate, be easy to dehydration; Then enter settling tank 1# and carry out mud-water separation.This step is carried out chemical coagulation and precipitation desulfurization by the effect of coagulation, precipitation, separation, and reaction formula is: S 2-+ Fe 2+=FeS ↓, S 2-+ Ca 2+=CaS ↓.The clearance of this step sulfide is 30~50%.Certainly, also available iron trichloride, polymerize aluminum chloride, Tai-Ace S 150 replace poly-ferric chloride aluminium water purifying agent, but consider that poly-ferric chloride aluminium water purifying agent is wide to the PH scope of waste water, formation flco maximum, and molysite has good precipitation removal effect to sulfide, preferably adds poly-ferric chloride aluminium water purifying agent.
In step 3), the water outlet of settling tank 1# enters reaction tank 2#, regulates pH to 2~4, and add the Fenton reagent of corresponding amount according to the size of COD, by UV device cyclic aeration, regulate pH to 7.5~8.5 with liming after completion of the reaction, then enter settling tank 2# and carry out mud-water separation.This step is utilized photochemistry and catalysed oxidation processes degradation of contaminant thereof, belongs to high-level oxidation technology, under the illuminate condition of UV-light, and ferrous catalysis H rapidly 2o 2generate hydroxyl radical free radical (OH).Concrete reaction process is shown in following reaction formula:
Fe 2++ H 2O 2 →Fe 3++·OH + OH
[Fe(OH)] 2+ Fe 2++HO· ,
[Fe(OOC―R)] 2+ Fe 2++R·+CO 2
HO·+RH→R·+H 2O ,
Fe 2++HO·→Fe 3++OH
The hydroxyl radical free radical of tool strong oxidizing property carries out oxygenolysis to organic pollutants such as the thioxine dyes in sulfur-containing waste water, PVA, organic additives, further remove sulfide, Persistent organic pollutants thing, polymer organic pollutant, reduce BOD and COD, make B/C ratio be greater than 0.45, improve the biodegradability of waste water.The clearance of this stage COD is 40~50%, and the clearance of sulfide reaches 20~50%.
In step 4), adopt bottom water inlet, the top overflow mode acidification that is hydrolyzed.Through previous step wastewater treatment operation, almost thoroughly remove sulfide, greatly improve the biodegradability of waste water, waste water fully mixes with activated sludge particles at hydrolysis acidification pool, utilizing a large amount of hydrolytic bacterias, the acidifying bacterium of inoculation culture is dissolved organic matter by insoluble hydrolysis of organic matter, the macromolecular substance of difficult for biological degradation is converted into the small-molecule substance of readily biodegradable, thereby further improves the biodegradability of waste water.The maintenance of hydrolysis acidification pool is according to normal procedure management maintenance.
In step 5), in two-stage contact-oxidation pool, the inoculation culture mode of active sludge is similar to hydrolysis acidification pool, and with hydrolysis acidification pool synchronized culture, accelerate the cultivation progress of whole biochemical system, acidication+catalytic oxidation is continuous, a synchronous biochemical treatment, to cultivate and synchronous operation within the shortest time, reduce environmental pollution, reduce production costs.The catalytic oxidation time is 8~10h.
In step 6), after acidication and contact oxidation technology processing, utilize hydraulic mixing, add polymerize aluminum chloride PAC or polyaluminium sulfate, and polyacrylamide flocculant PAM, chemical feeding quantity is respectively 80~100mg/L, 200~500mg/L; After coagulation, enter settling tank 3# and carry out mud-water separation; After water outlet is up to standard through discharge pond discharge, mud unified outward transport after sludge thickener is processed that three settling tanks and hydrolysis acidification pool produce.After catalytic oxidation, waste water still has a small amount of mud to enter settling tank, therefore this step adds water purification agent and flocculation agent to carry out further precipitate and separate, due to PAC, polyaluminium sulfate and PAM, to be applicable to turbidity low, pH value is low, large with the floss forming after pollutant reaction, speed is fast, and does not affect other indexs of water quality, is preferably PAC and PAM.Certainly, also can select polyaluminium sulfate to replace polymerize aluminum chloride according to practical situation.
Taking the treatment process of Zengcheng, Guangzhou making up plant dyeing waste water as example, treatment effect of the present invention is described below.Zengcheng, the Guangzhou cowboy of the making up plant sizing dyeing waste water water yield is 1000m 3/ d, every day, continuous operating time was 20 hours, this waste water complicated, biodegradability is poor, and former water leading indicator is as follows:
PH value Colourity (doubly) COD cr(mg/L) BOD 5(mg/L) SS(mg/L) S 2-(mg/L)
8.5~13 5500 3400 950 500 440
embodiment 1
Waste water treatment process is as follows:
1) preaeration catalyzed oxidation: dyeing waste water enters aerating regulation pond after grid interception foreign material, by liming adjusting wastewater pH to 8.0, the disposable manganese oxide composite catalyst that adds, chemical feeding quantity is 150mg/L, and continuous aeration stirs, stop 4h, adopt sealed construction to carry out preaeration catalyzed oxidation, waste gas is collected at top, passes into lime pond;
2) materialization desulfurization: the water outlet of aerating regulation pond being promoted to physical reaction pond 1# with lift pump, is 4:1 preparation poly-ferric chloride aluminium water purifying agent by iron, aluminium mass ratio, adds into reaction tank 1# by the chemical feeding quantity of 1500mg/L; Stir, adjust pH to 7.0 with liming, occur slowing down and stirring after flco, then be 0.05wt% by the configuration concentration that the chemical feeding quantity of 1000mg/L adds PAM(PAM), continue to stir, it is large that flco further becomes, and then enters settling tank 1# and carry out mud-water separation;
3) UV-Fenton catalyzed oxidation: the water outlet access UV-Fenton's reaction pond 2# of settling tank 1#, by liming adjusting pH value to 3.0, and add the Fenton reagent of corresponding amount according to the size of COD, by UV device cyclic aeration, stop 2h, after completion of the reaction, by liming adjusting pH value to 7.8, enter settling tank 2#.
4) acidication: settling tank 2# water outlet directly enters hydrolysis acidification pool, adopts bottom water inlet, and top overflow mode, fully mixes with active sludge, stops 6h;
5) catalytic oxidation: waste water directly enters two-stage contact-oxidation pool after acidication reaction, fully mixes with active sludge, adopts continuous aeration, and control dissolved oxygen is 3mg/L, stops 8h;
6) qualified discharge: 100 mg/L PAC and 200 mg/L PAM are added in contact-oxidation pool water outlet, after coagulation, enter settling tank 3# and carry out final step mud-water separation, after water outlet is up to standard, discharge through discharge pond, the mud that settling tank and hydrolysis acidification pool produce enters sludge thickener, after belt filter press is processed, transport outward mud, filtrate access settling tank 1# returns in technical process.
Wherein, in step 4), the inoculation culture method of active sludge is as follows: the inoculation culture method of active sludge is as follows: in hydrolysis acidification pool, add sanitary sewage, regulate COD crto 400~500mg/L, and m (BOD in mass ratio 5): m(N): m(P)=(200~300): add carbon, nitrogen, phosphorus nutrition salt at 5: 1; Introduce active sludge (taking from identical sink drainage sanitary sewage with active sludge), vexed exposing to the sun after 2~3d, COD near sink drainage crbe down to below 300mg/L, introduce continuously subsequently step 3) sewage after treatment, control COD crbe 300~400mg/L, dissolved oxygen DO is 2~3mg/L, water outlet COD in 1 week crbe stabilized in below 200mg/L; After this progressively improve influent load by increasing flooding quantity; , examine under a microscope meanwhile, survive and be after exponential phase or stationary phase growth and breeding until bacterium, controlling dissolved oxygen DO is 0.3~0.5mg/L, until reach COD clearance>=40%, completes the inoculation culture of active sludge.
In step 5), the inoculation culture method of active sludge is as follows: in the contact-oxidation pool of installing after combined stuffing, add the sanitary sewage of taking from identical sink drainage with active sludge, regulate COD crto 400~500mg/L, and m (BOD in mass ratio 5): m(N): m(P)=100: (4~5): 1 adds carbon, nitrogen, phosphorus nutrition salt; Introduce active sludge, vexed exposing to the sun after 2~3d, COD near sink drainage crbe down to below 300mg/L, introduce continuously subsequently sewage (through acidication sewage after treatment), control COD crbe 300~400mg/L, dissolved oxygen DO is 2.0~3.0mg/L, water outlet COD in 1 week crbe stabilized in below 200mg/L; After this progressively improve influent load by increasing flooding quantity; Meanwhile, microorganism is biofilm on contact-oxidation pool filler, and biofilm thickness is at 1.5~2mm, and micro-Microscopic observation has the protozoon of a small amount of activity, has a large amount of newborn zoogloeas to occur, with part thread fungus, better active.Through the cultivation of 1~3 month, domestication, water outlet is basicly stable, proceeds to subsequently trial run.In actually operating, after bacterium survives, nutritive salt composition just stops adding, and domestication finishes, and can start normal operation.
Detect by analysis, the leading indicator of discharge pond water outlet is as follows:
PH value Colourity (doubly) COD cr(mg/L) BOD 5(mg/L) SS(mg/L) S 2-(mg/L)
7.5 30 60 20 20 0.1
embodiment 2
Waste water treatment process is as follows:
1) preaeration catalyzed oxidation: dyeing waste water enters aerating regulation pond after grid interception foreign material, by liming adjusting wastewater pH to 10.0, the disposable manganese oxide composite catalyst that adds, chemical feeding quantity is 200mg/L, and continuous aeration stirs, stop 6h, adopt sealed construction to carry out preaeration catalyzed oxidation, waste gas is collected at top, passes into lime pond;
2) materialization desulfurization: the water outlet of aerating regulation pond being promoted to physical reaction pond 1# with lift pump, is 5:1 preparation poly-ferric chloride aluminium water purifying agent by iron, aluminium mass ratio, adds into reaction tank 1# by the chemical feeding quantity of 3000mg/L; Stir, adjust pH to 8.0 with liming, occur slowing down and stirring after flco, then be 0.1wt% by the configuration concentration that the chemical feeding quantity of 2000mg/L adds PAM(PAM), continue to stir, it is large that flco further becomes, and then enters settling tank 1# and carry out mud-water separation;
3) UV-Fenton catalyzed oxidation: the water outlet access UV-Fenton's reaction pond 2# of settling tank 1#, by liming adjusting pH value to 5.0, and add the Fenton reagent of corresponding amount according to the size of COD, by UV device cyclic aeration, stop 4h, after completion of the reaction, by liming adjusting pH value to 7.5, enter settling tank 2#.
4) acidication: settling tank 2# water outlet directly enters hydrolysis acidification pool, adopts bottom water inlet, and top overflow mode, fully mixes with active sludge, stops 4h;
5) catalytic oxidation: waste water directly enters two-stage contact-oxidation pool after acidication reaction, fully mixes with active sludge, adopts continuous aeration, and control dissolved oxygen is 2mg/L, stops 10h;
6) qualified discharge: 80 mg/L PAC and 500 mg/L PAM are added in contact-oxidation pool water outlet, after coagulation, enter settling tank 3# and carry out final step mud-water separation, after water outlet is up to standard, discharge through discharge pond, the mud that settling tank and hydrolysis acidification pool produce enters sludge thickener, after belt filter press is processed, transport outward mud, filtrate access settling tank 1# returns in technical process.
Wherein, in step 4), step 5), the inoculation culture method of active sludge is with embodiment 1.
Detect by analysis, the leading indicator of discharge pond water outlet is as follows:
PH value Colourity (doubly) COD cr(mg/L) BOD 5(mg/L) SS(mg/L) S 2-(mg/L)
7.9 29 65 18 23 0.14
embodiment 3
Waste water treatment process is as follows:
1) preaeration catalyzed oxidation: dyeing waste water enters aerating regulation pond after grid interception foreign material, by liming adjusting wastewater pH to 9.0, the disposable manganese oxide composite catalyst that adds, chemical feeding quantity is 180mg/L, and continuous aeration stirs, stop 5h, adopt sealed construction to carry out preaeration catalyzed oxidation, waste gas is collected at top, passes into lime pond;
2) materialization desulfurization: the water outlet of aerating regulation pond being promoted to physical reaction pond 1# with lift pump, is 5:1 preparation poly-ferric chloride aluminium water purifying agent by iron, aluminium mass ratio, adds into reaction tank 1# by the chemical feeding quantity of 2000mg/L; Stir, adjust pH to 8.0 with liming, occur slowing down and stirring after flco, then be 0.08wt% by the configuration concentration that the chemical feeding quantity of 1500mg/L adds PAM(PAM), continue to stir, it is large that flco further becomes, and then enters settling tank 1# and carry out mud-water separation;
3) UV-Fenton catalyzed oxidation: the water outlet access UV-Fenton's reaction pond 2# of settling tank 1#, by liming adjusting pH value to 4.0, and add the Fenton reagent of corresponding amount according to the size of COD, by UV device cyclic aeration, stop 3h, after completion of the reaction, by liming adjusting pH value to 8.5, enter settling tank 2#.
4) acidication: settling tank 2# water outlet directly enters hydrolysis acidification pool, adopts bottom water inlet, and top overflow mode, fully mixes with active sludge, stops 5h;
5) catalytic oxidation: waste water directly enters two-stage contact-oxidation pool after acidication reaction, fully mixes with active sludge, adopts continuous aeration, and control dissolved oxygen is 2mg/L, stops 9h;
6) qualified discharge: 90 mg/L polyaluminium sulfates and 350 mg/L PAM are added in contact-oxidation pool water outlet, after coagulation, enter settling tank 3# and carry out final step mud-water separation, after water outlet is up to standard, discharge through discharge pond, the mud that settling tank and hydrolysis acidification pool produce enters sludge thickener, after belt filter press is processed, transport outward mud, filtrate access settling tank 1# returns in technical process.
Wherein, in step 4), step 5), the inoculation culture method of active sludge is with embodiment 1.
Detect by analysis, the leading indicator of discharge pond water outlet is as follows:
PH value Colourity (doubly) COD cr(mg/L) BOD 5(mg/L) SS(mg/L) S 2-(mg/L)
8.0 31 63 21 19 0.08
The present invention adopts the integrated conduct method of preaeration catalyzed oxidation, materialization desulfurization, UV-Fenton catalyzed oxidation, acidication, catalytic oxidation.Preaeration catalyzed oxidation, materialization desulfurization, UV-Fenton catalytic oxidation technique reduce COD in high-concentration sulfur-containing waste water from dyestuff, colourity, SS, sulfide etc., improve wastewater biodegradability, acidication, catalytic oxidation treatment process can remain organic pollutant by degrading waste water, make waste water reach first discharge standard, be pH value 6~9, COD cr≤ 100mg/L, BOD 5≤ 30mg/L, S 2-≤ 1mg/L, colourity≤40 times, SS≤70mg/L, final stably reaching standard discharge, and reduce the expense and the sludge quantity that reduces 10~30% that use chemicals treatment waste water completely.

Claims (9)

1. one kind is vulcanized the treatment process of dyeing waste water, it is characterized in that: sulfuration dyeing waste water is through the total system of grid, aerating regulation pond, physical reaction pond 1#, settling tank 1#, UV-Fenton's reaction pond 2#, settling tank 2#, hydrolysis acidification pool, two-stage contact-oxidation pool, settling tank 3#, carry out successively preaeration catalyzed oxidation, materialization desulfurization, UV-Fenton catalyzed oxidation, acidication, catalytic oxidation processing, after water outlet is up to standard, through the discharge of discharge pond, the mud that settling tank and hydrolysis acidification pool produce is transported outward after sludge thickener is processed; Specifically comprise following technical process:
1) preaeration catalyzed oxidation: sulfuration dyeing waste water enters aerating regulation pond after grid interception foreign material, regulates wastewater pH to 8.0~10.0, adds manganese oxide composite catalyst, and aeration, stirs, and stops 4~6h, and tail gas is carried out to collection and treatment;
2) materialization desulfurization: by the water outlet access physical reaction pond 1# in aerating regulation pond, add poly-ferric chloride aluminium water purifying agent, stir, regulate pH, occur slowing down and stirring after flco, add polyacrylamide flocculant, after coagulation, enter settling tank 1# and carry out mud-water separation;
3) UV-Fenton catalyzed oxidation: the water outlet access UV-Fenton's reaction pond 2# of settling tank 1#, regulate pH to 3.0~5.0, add Fenton reagent, utilize UV catalyzed oxidation, stop after 2~4h, regulate pH to 7.5~8.5, enter settling tank 2# and carry out mud-water separation;
4) acidication: the water outlet of settling tank 2# enters hydrolysis acidification pool, fully mixes with active sludge, acidication 4~6h;
5) catalytic oxidation: the water outlet of hydrolysis acidification pool directly enters two-stage contact-oxidation pool, fully mixes with active sludge, and control dissolved oxygen is 2~3mg/L, catalytic oxidation 8~10h;
6) qualified discharge: after catalytic oxidation is processed, in waste water, add polymerize aluminum chloride or polyaluminium sulfate, and polyacrylamide flocculant, after coagulation, enter settling tank 3# and carry out mud-water separation; After water outlet is up to standard, through the discharge of discharge pond, the mud that settling tank and hydrolysis acidification pool produce is transported outward after sludge thickener is processed.
2. treatment process according to claim 1, is characterized in that: in step 1), the chemical feeding quantity of manganese oxide composite catalyst is 150~200mg/L.
3. treatment process according to claim 1, is characterized in that: step 2) in, in poly-ferric chloride aluminium water purifying agent, the mass ratio of iron, aluminium is (4~5): 1, and its chemical feeding quantity is 1000~3000mg/L.
4. treatment process according to claim 1, is characterized in that: step 2) in, the configuration concentration of polyacrylamide flocculant is 0.05~0.1wt%, its chemical feeding quantity is 1000~2000mg/L.
5. treatment process according to claim 1, is characterized in that: in step 4), the inoculation culture method of active sludge is as follows: in hydrolysis acidification pool, add sanitary sewage, regulate COD crto 400~500mg/L, add carbon, nitrogen, phosphorus nutrition salt; Introduce active sludge, vexed exposing to the sun, COD crbe down to below 300mg/L, introduce continuously subsequently step 3) sewage after treatment, control COD crbe 300~400mg/L, dissolved oxygen DO is 2.0~3.0mg/L, water outlet COD in 1 week crbe stabilized in below 200mg/L, after this progressively improve influent load,, examine under a microscope meanwhile, survive and be after exponential phase or stationary phase growth and breeding until bacterium, controlling dissolved oxygen DO is 0.3~0.5mg/L, completes the inoculation culture of active sludge.
6. treatment process according to claim 5, is characterized in that: introduce active sludge, make MLSS mass concentration reach 1000~2000mg/L.
7. treatment process according to claim 1, is characterized in that: in step 5), the inoculation culture method of active sludge is as follows: in contact-oxidation pool, add sanitary sewage, regulate COD crto 400~500mg/L, add carbon, nitrogen, phosphorus nutrition salt; Introduce active sludge, vexed exposing to the sun, COD crbe down to below 300mg/L, introduce continuously subsequently step 4) sewage after treatment, control COD crbe 300~400mg/L, dissolved oxygen DO is 2.0~3.0mg/L, water outlet COD in 1 week crbe stabilized in below 200mg/L, after this, progressively improve influent load, meanwhile, microorganism is biofilm on contact-oxidation pool filler, and biofilm thickness reaches 1.5~2.0mm, and active sludge is inoculated successfully, then carries out sludge acclimatization and later stage operation.
8. treatment process according to claim 1, is characterized in that: in step 6), the chemical feeding quantity of polymerize aluminum chloride or polyaluminium sulfate is 80~100 mg/L, and the chemical feeding quantity of polyacrylamide flocculant is 200~500mg/L.
9. according to the treatment process described in claim 1~8 any one, it is characterized in that: regulate waste water ph with unslaked lime.
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