CN1899986A - Method for treating printing and dyeing waste water by high pressure cavitation jet combined with fenton reagent - Google Patents
Method for treating printing and dyeing waste water by high pressure cavitation jet combined with fenton reagent Download PDFInfo
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Abstract
The present invention relates to treatment of printing and dyeing waste water. The process of treating printing and dyeing waste water includes the following steps: regulating pH value with acid, oxidizing with the Fenton reagent, cavitation treating with high pressure jet, coagulating sedimentation, adsorbing with fly ash and regulating pH value before exhausting. The present invention features the organic combination of high pressure cavitation jet and the Fenton reagent in treating printing and dyeing waste water. The present invention has obviously raised COD eliminating rate and decolorizing rate, high energy utilizing rate and other advantages.
Description
Technical field
The present invention relates to a kind of method of treatment of dyeing and printing.
Background technology
Textile printing and dyeing industry is one of industrial sector that China's water consumption is big, quantity discharged is big, and dyeing waste water accounts for 80% of whole trade effluents, and according to incompletely statistics, China's dyeing waste water discharges 300-400 ten thousand m3 every day.The pH value of dyeing waste water changes greatly, is generally 6-13, and colourity is dark, can reach 1000 times, and biodegradability is poor, and COD is 400-4000mg/L, and BOD is 100-150mg/L.Dyeing waste water water quality complexity contains a large amount of slurries and auxiliary agent, and especially activity, azoic dyestuff etc. also contain various carcinogenic, mutagenic toxic pollutants, as the aniline of groups such as phenyl ring, amido, azo, oil of mirbane, o-benzoic acid class etc.The dyeing waste water biodegradability is poor, and contains poisonous hard-degraded substance again, and therefore undesirable with the biological process treatment effect, variation water quality is big, and technical process is long, energy consumption height, complex management.If dyeing waste water directly discharges or handle defective discharging, can work the mischief to environment and human body health.
At present, the Chinese invention patent application number is 200310111518.4, and its denomination of invention is " a kind of advanced oxidation treatment process of waste water from dyestuff ", and this method adopts Fenton process to decoloring dye waste water earlier, handles with ultra-sonic oscillation then.The Chinese invention patent application number is 200510041020.4, its denomination of invention is " difficult biochemistry, high pollution trade effluent quick degrading process and a specific equipment thereof ", and this method employing high-pressure hydraulic pump sprays into waste water and carries out circular treatment in the reactor through the swirling flow divergent nozzle.Japanese patent application No. is 06-182362, its denomination of invention is " Treatment of dyeing waste water (treatment of dyeing wastewater) ", this method adopts Fenton process that waste water from dyestuff is carried out oxide treatment earlier, flocculates and precipitation process with aluminium flocculating agent and polymeric flocculant again.
Because the flyash processing power is limited, ultrasonic energy utilization ratio and penetration coefficient are all low, Fenton reagent is handled still not thorough, can only destroy the colour developing group of substance that show color in the waste water or macromole is resolved into secondary molecule, organism thoroughly can not be degraded, though adopting high-pressure hydraulic pump that waste water is sprayed into through the swirling flow divergent nozzle carries out circular treatment organism is had Degradation in the reactor, but organic degradation capability is compared with cavitation jet, its degradation capability is very little, and weak effect, therefore these methods are limited to the treatment effect of dyeing waste water, particularly bad to the macromolecular substance treatment effect of difficult degradation in the dyeing waste water.
Summary of the invention
The objective of the invention is at the deficiencies in the prior art, a kind of method for the treatment of printing and dyeing waste water by high pressure cavitation jet combined with fenton reagent is provided, this method has not only solved the processing of dyeing waste water, and has solved dyeing waste water COD and colourity and handle thoroughly and the low problem of clearance.
For achieving the above object, the present invention carries out according to the following steps:
(1) the pH value with acid adjusting dyeing waste water is 2.0～3.5;
(2) dyeing waste water of exchanging behind the pH carries out the Fenton reagent oxide treatment: low whipping speed is that 200～250r/min adds ferrous sulfate down, making the ferrous sulfate ionic concn is 0.009～0.015mol/L, add hydrogen peroxide then, making hydrogen peroxide concentration in dyeing waste water is 0.1～0.15mol/L, and the dyeing waste water behind the adding hydrogen peroxide is continued to stir 30～40 minutes;
(3) the pH value with the dyeing waste water after the sodium hydroxide adjusting oxide treatment is 8.0～10.0, add hydrogen peroxide therein, making hydrogen peroxide concentration therein is 0.01～0.05mol/L, stop to stir, be 8～12Mpa ram pump with this waste water by scaling type cavitating nozzle suction cavitation device with pump pressure then, the cavitation device internal pressure is 0.4～0.6Mpa, dyeing waste water from the Fenton reagent oxidation pond to cavitation device, be back to the Fenton reagent oxidation pond from cavitation device again, circulation cavitation 8～14 times;
(4) will enter coagulative precipitation tank through the dyeing waste water after the high pressure cavitation jet circular treatment, open stirrer, stirring velocity is 200～300r/min, add ferrous sulfate, making the concentration of ferrous sulfate ion in dyeing waste water is 250～350mg/L, after 1～3 minute, add polyacrylamide, making polyacrylamide concentration in this dyeing waste water is 0.3～0.7mg/L, stirs after 1～3 minute, makes stirring velocity reduce to 100～150r/min, stir after 2～3 minutes, make stirring velocity reduce to 50～80r/min, stir and stop after 20～30 minutes stirring, precipitate 30～50 minutes;
(5) carry out adsorption treatment with the clear liquid of flyash after: open stirrer to coagulating sedimentation, stirring velocity is 250～300r/min, transferring the pH value of clear liquid with acid is 2.0～3.5, be to add flyash to clear liquid in 1: 30～1: 50 by the mass ratio of flyash and clear liquid then, the flyash particle diameter is 0.10～0.15mm, continues to stir after 10～15 minutes, make stirring velocity reduce to 60～80r/min, stir after 30～50 minutes, stop to stir quiescent setting 20～35 minutes;
(6) clear liquid behind the quiescent setting being entered preparing pool, is 7.0～7.5 back dischargings with the sodium hydroxide adjust pH.
The present invention compared with prior art, the following technique effect that has:
1, high pressure cavitation jet organically is applied in the treatment of dyeing wastewater.The high pressure cavitation jet excellent wastewater treatment effect, can degrade contains the complicated larger molecular organics of phenyl ring, and the efficient height is thorough to organic matter degradation.General Fenton reagent oxidation, coagulating sedimentation and the flyash absorption combination treatment dyeing waste water of adopting, total COD clearance is 70～80%, chroma removal rate is 85～90%, is 95.1～96.0% and the present invention can make the total COD clearance of dyeing waste water, and chroma removal rate is 96.1～96.5%.After the dyeing waste water process Fenton reagent oxide treatment, organism has had preliminary degraded in the waste water under the general condition, and color removal is obvious, but COD does not still reach emission request, unless just increase dosage COD is further reduced.In order to save medicament expense usefulness, make COD and colourity reach emission request again, adopt high pressure cavitation jet that waste water is further handled, make COD reach emission request.Its detailed process is, after the Fenton reagent oxide treatment, adjust pH to 8.0～10.0, add hydrogen peroxide, making hydrogen peroxide concentration in waste water is 0.01～0.05mol/L, then with the high pressure cavitation jet system to the cavitation process that circulates of the supernatant liquor after staticly settling, pump pressure 8～12Mpa, the cavitation device internal pressure is 0.4～0.6Mpa, and nozzle is the scaling type cavitating nozzle, circulates 8～14 times.Under the high pressure cavitation conditions, produce cavity during waste water process cavitating nozzle, when crumbling and fall, cavity produces partial High Temperature High Pressure of moment, temperature can reach 1900K on the bubble wall, top temperature can reach 10000K in the bubble, pressure can reach more than the 50MPa, has formed the particular surroundings of a High Temperature High Pressure for organic degraded.Under such condition, can produce free radical, supercritical waters such as OH with strong oxidizing property and H, and direct heat Decomposition, thereby the organism in the waste water is further decomposed, hydrogen peroxide is under the promoter action under the high pressure cavitation conditions in addition, can produce free radicals such as a large amount of OH and H, thereby strengthen organic oxidation capacity.
2, after the Fenton reagent oxide treatment, adopt high pressure cavitation jet to handle, only need pump, encloses container, nozzle and some connecting tubes, valve, compare with biological treatment, saved huge bio-reaction system and other physico-chemical process ratio, equipment is simple, save medicament, handle thoroughly.The present invention makes the capital construction less investment of printing and dyeing wastewater treatment system, and the medicament expense is low in the operation, and it is few to produce waste.
3, flyash is a kind of porous medium, has good adsorption, and cheap, and advantages of good adsorption effect also reaches the purpose of waste recycling.
Description of drawings
Fig. 1 is a process flow diagram of the present invention; Fig. 2 is the block diagram of high pressure cavitation jet device, and 1 is the Fenton reagent oxidation pond in Fig. 2, and 2 is the water inlet pipe of ram pump, and 3 is ram pump, and 4 is the rising pipe of ram pump, and 5 is cavitation device, and 6 is the scaling type cavitating nozzle, and 7 is return line.
Embodiment
The method for the treatment of printing and dyeing waste water by high pressure cavitation jet combined with fenton reagent adopts Fenton reagent and high pressure cavitation jet combination treatment dyeing waste water.The embodiment of this method is as follows:
Example 1, processing COD are that 1385mg/L, colourity are that 658 times, pH value are undertaken by following concrete steps when being 6.0 dyeing waste water:
1, the pH value with hydrochloric acid adjusting dyeing waste water is 2.0;
2, the dyeing waste water of exchanging behind the pH carries out the Fenton reagent oxide treatment: low whipping speed is that 200r/min adds ferrous sulfate down, making the ferrous sulfate ionic concn is 0.009mol/L, add hydrogen peroxide then, making hydrogen peroxide concentration in dyeing waste water is 0.1mol/L, and the dyeing waste water behind the adding hydrogen peroxide is continued to stir 30 minutes
3, the pH value with the dyeing waste water after the sodium hydroxide adjusting oxide treatment is 8.0, add hydrogen peroxide therein, making hydrogen peroxide concentration therein is 0.01mol/L, stop to stir, then with pump pressure for the 8Mpa ram pump with this waste water by scaling type cavitating nozzle suction cavitation device, the cavitation device internal pressure is 0.4Mpa, dyeing waste water from the Fenton reagent oxidation pond to cavitation device, be back to the Fenton reagent oxidation pond from cavitation device again, circulation cavitation 8 times;
4, will enter coagulative precipitation tank through the dyeing waste water after the high pressure cavitation jet circular treatment, open stirrer, stirring velocity is 200r/min, add ferrous sulfate, making the concentration of ferrous sulfate ion in dyeing waste water is 250mg/L, after 1 minute, add polyacrylamide, making polyacrylamide concentration in this dyeing waste water is 0.3mg/L, stirs after 1 minute, make stirring velocity reduce to 100r/min, stir after 2 minutes, make stirring velocity reduce to 50r/min, stir after 20 minutes, stop to stir, precipitate 30 minutes;
5, carry out adsorption treatment with the clear liquid of flyash after: open stirrer to coagulating sedimentation, stirring velocity is 250r/min, transferring the pH value of clear liquid with hydrochloric acid is 2.0, be to clear liquid to add flyash at 1: 30 by the mass ratio of flyash and clear liquid then, the flyash particle diameter is 0.10mm, continues to stir after 10 minutes, make stirring velocity reduce to 60r/min, stir after 30 minutes, stop to stir quiescent setting 20 minutes;
6, the clear liquid behind the quiescent setting being entered preparing pool, is 7.0 back dischargings with the sodium hydroxide adjust pH.
Result: after waste water was handled through above-mentioned steps, COD was 62mg/L, and colourity is 24 times, the pH value is 7.0, the CDO clearance is 95.5%, and percent of decolourization is 96.4%, and water quality reaches the first discharge standard of textile dyeing and finishing industrial water pollution thing emission standard (GB4287-1992).
Example 2, processing COD are that 1586mg/L, colourity are that 722 times, pH value are undertaken by following concrete steps when being 6.4 dyeing waste water:
1, the pH value with sulfuric acid adjusting dyeing waste water is 2.8;
2, the dyeing waste water of exchanging behind the pH carries out the Fenton reagent oxide treatment: low whipping speed is that 230r/min adds ferrous sulfate down, making the ferrous sulfate ionic concn is 0.012mol/L, add hydrogen peroxide then, making hydrogen peroxide concentration in dyeing waste water is 0.13mol/L, and the dyeing waste water behind the adding hydrogen peroxide is continued to stir 35 minutes;
3, the pH value with the dyeing waste water after the sodium hydroxide adjusting oxide treatment is 9.0, add hydrogen peroxide therein, making hydrogen peroxide concentration therein is 0.03mol/L, stop to stir, then with pump pressure for the 10Mpa ram pump with this waste water by scaling type cavitating nozzle suction cavitation device, the cavitation device internal pressure is 0.5Mpa, dyeing waste water from the Fenton reagent oxidation pond to cavitation device, be back to the Fenton reagent oxidation pond from cavitation device again, circulation cavitation 10 times;
4, will enter coagulative precipitation tank through the dyeing waste water after the high pressure cavitation jet circular treatment, open stirrer, stirring velocity is 250r/min, add ferrous sulfate, making the concentration of ferrous sulfate ion in dyeing waste water is 300mg/L, after 2 minutes, add polyacrylamide, making polyacrylamide concentration in this dyeing waste water is 0.5mg/L, stirs after 2 minutes, makes stirring velocity reduce to 120r/min, stirring made stirring velocity reduce to 60r/min after 2.5 minutes, stir after 25 minutes, stop to stir, precipitate 40 minutes;
5, carry out adsorption treatment with the clear liquid of flyash after: open stirrer to coagulating sedimentation, stirring velocity is 270r/min, transferring the pH value of clear liquid with sulfuric acid is 3.0, be to clear liquid to add flyash at 1: 40 by the mass ratio of flyash and clear liquid then, the flyash particle diameter is 0.12mm, continues to stir after 13 minutes, make stirring velocity reduce to 70r/min, stir after 40 minutes, stop to stir quiescent setting 30 minutes;
6, the clear liquid behind the quiescent setting being entered preparing pool, is 7.2 back dischargings with the sodium hydroxide adjust pH.
Result: after waste water was handled through above-mentioned steps, COD was 78mg/L, and colourity is 28 times, the pH value is 7.2, the CDO clearance is 95.1%, and percent of decolourization is 96.1%, and water quality reaches the first discharge standard of textile dyeing and finishing industrial water pollution thing emission standard (GB4287-1992).
Example 3, processing COD are that 1733mg/L, colourity are that 844 times, pH value are undertaken by following concrete steps when being 6.6 dyeing waste water:
1, the pH value with sulfuric acid adjusting dyeing waste water is 3.5;
2, the dyeing waste water of exchanging behind the pH carries out the Fenton reagent oxide treatment: low whipping speed is that 250r/min adds ferrous sulfate down, making the ferrous sulfate ionic concn is 0.015mol/L, add hydrogen peroxide then, making hydrogen peroxide concentration in dyeing waste water is 0.15mol/L, and the dyeing waste water behind the adding hydrogen peroxide is continued to stir 40 minutes;
3, the pH value with the dyeing waste water after the sodium hydroxide adjusting oxide treatment is 10.0, add hydrogen peroxide therein, making hydrogen peroxide concentration therein is 0.05mol/L, stop to stir, then with pump pressure for the 12Mpa ram pump with this waste water by scaling type cavitating nozzle suction cavitation device, the cavitation device internal pressure is 0.6Mpa, dyeing waste water from the Fenton reagent oxidation pond to cavitation device, be back to the Fenton reagent oxidation pond from cavitation device again, circulation cavitation 14 times;
4, will enter coagulative precipitation tank through the dyeing waste water after the high pressure cavitation jet circular treatment, open stirrer, stirring velocity is 300r/min, add ferrous sulfate, making the concentration of ferrous sulfate ion in dyeing waste water is 350mg/L, add polyacrylamide after 3 minutes, making polyacrylamide concentration in this dyeing waste water is 0.7mg/L, stir after 3 minutes, make stirring velocity reduce to 150r/min, stir after 3 minutes, make stirring velocity reduce to 80r/min, stir after 30 minutes, stop to stir, precipitate 50 minutes;
5, carry out adsorption treatment with the clear liquid of flyash after: open stirrer to coagulating sedimentation, stirring velocity is 300r/min, transferring the pH value of clear liquid with sulfuric acid is 3.5, be to clear liquid to add flyash at 1: 50 by the mass ratio of flyash and clear liquid then, the flyash particle diameter is 0.15mm, continues to stir after 15 minutes, make stirring velocity reduce to 80r/min, stir after 50 minutes, stop to stir quiescent setting 35 minutes;
6, the clear liquid behind the quiescent setting being entered preparing pool, is 7.5 back dischargings with the sodium hydroxide adjust pH.
Result: after waste water was handled through above-mentioned steps, COD was 69mg/L, and colourity is 30 times, the pH value is 7.5, the CDO clearance is 96.0%, and percent of decolourization is 96.5%, and water quality reaches the first discharge standard of textile dyeing and finishing industrial water pollution thing emission standard (GB4287-1992).
Claims (4)
1, a kind of method for the treatment of printing and dyeing waste water by high pressure cavitation jet combined with fenton reagent is characterized in that this method carries out according to the following steps:
(1) the pH value with acid adjusting dyeing waste water is 2.0～3.5;
(2) dyeing waste water of exchanging behind the pH carries out the Fenton reagent oxide treatment: low whipping speed is that 200～250r/min adds ferrous sulfate down, making the ferrous sulfate ionic concn is 0.009～0.015mol/L, add hydrogen peroxide then, making hydrogen peroxide concentration in dyeing waste water is 0.1～0.15mol/L, and the dyeing waste water behind the adding hydrogen peroxide is continued to stir 30～40 minutes;
(3) the pH value with the dyeing waste water after the sodium hydroxide adjusting oxide treatment is 8.0～10.0, add hydrogen peroxide therein, making hydrogen peroxide concentration therein is 0.01～0.05mol/L, stop to stir, be 8～12Mpa ram pump with this waste water by scaling type cavitating nozzle suction cavitation device with pump pressure then, the cavitation device internal pressure is 0.4～0.6Mpa, dyeing waste water from the Fenton reagent oxidation pond to cavitation device, be back to the Fenton reagent oxidation pond from cavitation device again, circulation cavitation 8～14 times;
(4) will enter coagulative precipitation tank through the dyeing waste water after the high pressure cavitation jet circular treatment, open stirrer, stirring velocity is 200～300r/min, add ferrous sulfate, making the concentration of ferrous sulfate ion in dyeing waste water is 250～350mg/L, after 1～3 minute, add polyacrylamide, making polyacrylamide concentration in this dyeing waste water is 0.3～0.7mg/L, stirs after 1～3 minute, makes stirring velocity reduce to 100～150r/min, stir after 2～3 minutes, make stirring velocity reduce to 50～80r/min, stir and stop after 20～30 minutes stirring, precipitate 30～50 minutes;
(5) carry out adsorption treatment with the clear liquid of flyash after: open stirrer to coagulating sedimentation, stirring velocity is 250～300r/min, transferring the pH value of clear liquid with acid is 2.0～3.5, be to add flyash to clear liquid in 1: 30～1: 50 by the mass ratio of flyash and clear liquid then, the flyash particle diameter is 0.10～0.15mm, continues to stir after 10～15 minutes, make stirring velocity reduce to 60～80r/min, stir after 30～50 minutes, stop to stir quiescent setting 20～35 minutes;
(6) clear liquid behind the quiescent setting being entered preparing pool, is 7.0～7.5 back dischargings with the sodium hydroxide adjust pH.
2, the method for the treatment of printing and dyeing waste water by high pressure cavitation jet combined with fenton reagent according to claim 1 is characterized in that handling COD be that 1385mg/L, colourity are that 658 times, pH value carry out according to following steps when being 6.0 dyeing waste water:
(1) the pH value with hydrochloric acid adjusting dyeing waste water is 2.0;
(2) dyeing waste water of exchanging behind the pH carries out the Fenton reagent oxide treatment: low whipping speed is that 200r/min adds ferrous sulfate down, making the ferrous sulfate ionic concn is 0.009mol/L, add hydrogen peroxide then, making hydrogen peroxide concentration in dyeing waste water is 0.1mol/L, and the dyeing waste water behind the adding hydrogen peroxide is continued to stir 30 minutes
(3) the pH value with the dyeing waste water after the sodium hydroxide adjusting oxide treatment is 8.0, add hydrogen peroxide therein, making hydrogen peroxide concentration therein is 0.01mol/L, stop to stir, then with pump pressure for the 8Mpa ram pump with this waste water by scaling type cavitating nozzle suction cavitation device, the cavitation device internal pressure is 0.4Mpa, dyeing waste water from the Fenton reagent oxidation pond to cavitation device, be back to the Fenton reagent oxidation pond from cavitation device again, circulation cavitation 8 times;
(4) will enter coagulative precipitation tank through the dyeing waste water after the high pressure cavitation jet circular treatment, open stirrer, stirring velocity is 200r/min, add ferrous sulfate, making the concentration of ferrous sulfate ion in dyeing waste water is 250mg/L, after 1 minute, add polyacrylamide, making polyacrylamide concentration in this dyeing waste water is 0.3mg/L, stirs after 1 minute, make stirring velocity reduce to 100r/min, stir after 2 minutes, make stirring velocity reduce to 50r/min, stir after 20 minutes, stop to stir, precipitate 30 minutes;
(5) carry out adsorption treatment with the clear liquid of flyash after: open stirrer to coagulating sedimentation, stirring velocity is 250r/min, transferring the pH value of clear liquid with hydrochloric acid is 2.0, be to clear liquid to add flyash at 1: 30 by the mass ratio of flyash and clear liquid then, the flyash particle diameter is 0.10mm, continues to stir after 10 minutes, make stirring velocity reduce to 60r/min, stir after 30 minutes, stop to stir quiescent setting 20 minutes;
(6) clear liquid behind the quiescent setting being entered preparing pool, is 7.0 back dischargings with the sodium hydroxide adjust pH.
3, the method for the treatment of printing and dyeing waste water by high pressure cavitation jet combined with fenton reagent according to claim 1 is characterized in that handling COD be that 1586mg/L, colourity are that 722 times, pH value carry out according to following steps when being 6.4 dyeing waste water:
(1) the pH value with sulfuric acid adjusting dyeing waste water is 2.8;
(2) dyeing waste water of exchanging behind the pH carries out the Fenton reagent oxide treatment: low whipping speed is that 230r/min adds ferrous sulfate down, making the ferrous sulfate ionic concn is 0.012mol/L, add hydrogen peroxide then, making hydrogen peroxide concentration in dyeing waste water is 0.13mol/L, and the dyeing waste water behind the adding hydrogen peroxide is continued to stir 35 minutes;
(3) the pH value with the dyeing waste water after the sodium hydroxide adjusting oxide treatment is 9.0, add hydrogen peroxide therein, making hydrogen peroxide concentration therein is 0.03mol/L, stop to stir, then with pump pressure for the 10Mpa ram pump with this waste water by scaling type cavitating nozzle suction cavitation device, the cavitation device internal pressure is 0.5Mpa, dyeing waste water from the Fenton reagent oxidation pond to cavitation device, be back to the Fenton reagent oxidation pond from cavitation device again, circulation cavitation 10 times;
(4) will enter coagulative precipitation tank through the dyeing waste water after the high pressure cavitation jet circular treatment, open stirrer, stirring velocity is 250r/min, add ferrous sulfate, making the concentration of ferrous sulfate ion in dyeing waste water is 300mg/L, after 2 minutes, add polyacrylamide, making polyacrylamide concentration in this dyeing waste water is 0.5mg/L, stirs after 2 minutes, make stirring velocity reduce to 120r/min, stir after 2.5 minutes, make stirring velocity reduce to 60r/min, stir after 25 minutes, stop to stir, precipitate 40 minutes;
(5) carry out adsorption treatment with the clear liquid of flyash after: open stirrer to coagulating sedimentation, stirring velocity is 270r/min, transferring the pH value of clear liquid with sulfuric acid is 3.0, be to clear liquid to add flyash at 1: 40 by the mass ratio of flyash and clear liquid then, the flyash particle diameter is 0.12mm, continues to stir after 13 minutes, make stirring velocity reduce to 70r/min, stir after 40 minutes, stop to stir quiescent setting 30 minutes;
(6) clear liquid behind the quiescent setting being entered preparing pool, is 7.2 back dischargings with the sodium hydroxide adjust pH.
4, high pressure cavitation jet according to claim 1 is in conjunction with the method for Fenton agent treated dyeing waste water, it is characterized in that handling COD be that 1733mg/L, colourity are that 844 times, pH value carry out according to following steps when being 6.6 dyeing waste water:
(1) the pH value with sulfuric acid adjusting dyeing waste water is 3.5;
(2) dyeing waste water of exchanging behind the pH carries out the Fenton reagent oxide treatment: low whipping speed is that 250r/min adds ferrous sulfate down, making the ferrous sulfate ionic concn is 0.015mol/L, add hydrogen peroxide then, making hydrogen peroxide concentration in dyeing waste water is 0.15mol/L, and the dyeing waste water behind the adding hydrogen peroxide is continued to stir 40 minutes;
(3) the pH value with the dyeing waste water after the sodium hydroxide adjusting oxide treatment is 10.0, add hydrogen peroxide therein, making hydrogen peroxide concentration therein is 0.05mol/L, stop to stir, then with pump pressure for the 12Mpa ram pump with this waste water by scaling type cavitating nozzle suction cavitation device, the cavitation device internal pressure is 0.6Mpa, dyeing waste water from the Fenton reagent oxidation pond to cavitation device, be back to the Fenton reagent oxidation pond from cavitation device again, circulation cavitation 14 times;
(4) will enter coagulative precipitation tank through the dyeing waste water after the high pressure cavitation jet circular treatment, open stirrer, stirring velocity is 300r/min, add ferrous sulfate, making the concentration of ferrous sulfate ion in dyeing waste water is 350mg/L, after 3 minutes, add polyacrylamide, making polyacrylamide concentration in this dyeing waste water is 0.7mg/L, stirs after 3 minutes, make stirring velocity reduce to 150r/min, stir after 3 minutes, make stirring velocity reduce to 80r/min, stir after 30 minutes, stop to stir, precipitate 50 minutes;
(5) carry out adsorption treatment with the clear liquid of flyash after: open stirrer to coagulating sedimentation, stirring velocity is 300r/min, transferring the pH value of clear liquid with sulfuric acid is 3.5, be to clear liquid to add flyash at 1: 50 by the mass ratio of flyash and clear liquid then, the flyash particle diameter is 0.15mm, continues to stir after 15 minutes, make stirring velocity reduce to 80r/min, stir after 50 minutes, stop to stir quiescent setting 35 minutes;
(6) clear liquid behind the quiescent setting being entered preparing pool, is 7.5 back dischargings with the sodium hydroxide adjust pH.
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