CN103274524B - Printing and dyeing wastewater pretreatment method based on anoxic zone phase separation technology - Google Patents
Printing and dyeing wastewater pretreatment method based on anoxic zone phase separation technology Download PDFInfo
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Abstract
The invention relates to a printing and dyeing wastewater pretreatment method based on an anoxic zone phase separation technology. According to the printing and dyeing wastewater pretreatment method, an anoxic zone is divided into a phase I and a phase II, namely a phase for hydrogen production and acid production through fermentation and a methanogenesis phase; an electron donor is provided by organic matters in the wastewater, and dye is effectively decolored in the phase I by using a sulfate reducing process and the reducing capacity of reduzate, namely the sulfide, therefore the biodegradability of the wastewater is improved; and the organic matters can be efficiently removed in the phase II. As an anoxic phase transformation technology in the printing and dyeing wastewater treatment course, the printing and dyeing wastewater pretreatment method is used for providing a two-phase anoxic system and carrying out pretreatment on the printing and dyeing wastewater; the chromaticity and the COD (Chemical Oxygen Demand) removal rates can be effectively increased, the biodegradability of the wastewater can be greatly improved, and the defects that a traditional anoxic process is instable in treatment effect, large in sludge yield and the like are overcome. The printing and dyeing wastewater pretreatment method can be used for effectively removing chromaticity and COD in the printing and dyeing wastewater, the removal rates of the chromaticity and the COD respectively reach more than 95 percent and 60 percent, and the organic loading to subsequent procedures is greatly reduced.
Description
Technical field
The invention belongs to Industrial Wastewater Treatment industry, specifically relate to a kind of dyeing waste water pretreatment process based on anaerobism section phase detachment technique.
Background technology
Dyeing is typical high water consumption industry, needs every year to consume the technique softening water of nearly hundred million tons.Dyeing waste water mainly contains dyestuff, slip, dyeing auxiliary and fiber impurity, finish, acid, alkali and inorganic salt etc., complicated component and quantity discharged are large, colourity is high, basicity is large, pH is higher, organic content is high, bio-refractory thing many and it is large to change, directly discharge brings very big harm to human health and living environment, cause the waste of water resources simultaneously, be acknowledged as one of main harmful waste water of refractory reason.
Organism in dyeing waste water is mainly derived from alkali decrement waste water and the desized wastewater of high density, and this part waste water is alkalescence, though the water yield little (account for total wastewater flow rate 10%), its COD concentration can be up to tens thousand of; Alkali decrement, desized wastewater main component are polyvinyl alcohol (PVA) and starch, and wherein PVA is difficult degradation organic polymer, and starch good biodegradability.In dyeing waste water, colourity is mainly derived from the waste water that dyeing process produces, and has certain toxicity and biological activity restraining effect, and wastewater biodegradability is lower.
Existing treatment of dyeing wastewater generally comprises: physico-chemical processes, chemical method and biological process, although physico-chemical processes and chemical method are effective, cost is large, and working cost is higher, and limited by applicable elements.At present, with biological treatment, especially aerobe is treated to master, and occupies the majority with catalytic oxidation and surperficial high-rate activated-sludge process both at home and abroad.Aerobe is processed obvious to BOD removal effect, generally can reach 80% left and right, but colourity and COD clearance are not high, especially as the widespread use of the chemical sizwes such as PVA, tensio-active agent, solvent and a cloth alkali Decrement Technique, not only make the COD of dyeing waste water reach 2000～3000mg/L, and BOD/COD also drops to below 0.2 by original 0.4～0.5, simple aerobe intractability is increasing, and water outlet is difficult to up to standard; In addition, the high working cost of aerobic method and excess sludge processing or handling problems are always the difficult problems that field of waste water treatment is not resolved.According to document announcement, external general sludge treatment or disposal costs account for 50%～70% of whole Sewage Plant expense, also account at home 40% left and right.For above-mentioned reasons, the Anaerobic Microbiological Treatment Technology of dyeing waste water starts to be subject to people's attention, and the treatment of dyeing wastewater new technology of seeking efficient, low consumption, reduced investment is day aobvious important.
Dyeing waste water is owing to existing the organic substance of a large amount of difficult for biological degradation, and biochemical is poor, for improving the biodegradability of waste water, often need before aeration and biological is processed, hydrolysis acidification pool be set and process as anaerobism section.Anaerobism section is processed to the pre-treatment as various biochemical treatments, can improve sewage biochemical property, reduce the load of subsequent biological treatment, thereby during the high food wastewater of chemical industry, papermaking and organic concentration that is widely used in difficult for biological degradation processes.
At present, in the anaerobism section treatment process of dyeing waste water biochemistry, conventionally adopt homogenous anaerobic system, however homogenous anaerobic system as the anaerobism section in treatment of dyeing wastewater process, zymophyte and methanogen complete the whole process of anaerobic digestion in homogeneous reaction device.Yet because the growth characteristics of this 2 class flora are very different, to envrionment conditions require widely differently, so homogenous anaerobic system cannot make zymophyte and methanogen all in best physiological ecological envrionment conditions, be difficult to performance optimum usefulness separately; In addition, in conventional art, often only pay attention to organic hydrolysis, and lack, starch, glucose fermentation are produced to the directed control technique of hydrogen.The COD clearance of homogenous anaerobic system is 20～40% at present, and chroma removal rate is 60～80%, and still larger to the organic loading pressure of follow-up aerobic section, colourity is also difficult to further removal.
Along with country and the local raising gradually to dyeing waste water emission standard, make recommendation technique in the past can not meet current discharge of wastewater and require the requirement with social economic environment, need badly and carry out upgrading.
Summary of the invention
In order to overcome anaerobism section in prior art, process the deficiency existing, the invention provides a kind of efficient, stable dyeing waste water pretreatment process based on anaerobism section phase detachment technique.
A dyeing waste water pretreatment process based on anaerobism section phase detachment technique, described dyeing waste water comprises alkali decrement waste water, desized wastewater and dyeing waste-water, described dyeing waste water pretreatment process comprises the steps:
(1) in alkali decrement waste water or desized wastewater, add 0.5～10g/L vitriol condensing agent, and in separator, reclaim PVA and carry out recycling;
(2) step (1) water outlet enters equalizing tank after mixing with dyeing waste-water, and in equalizing tank, with sulphur acid for adjusting pH to 5～8, the COD in the water outlet of control step (2) and sulfate radical mass ratio are between 1～10:1;
(3) step (2) water outlet enters anaerobism section I phase reactor and produces hydrogen acid process, reactor contains take the anaerobic activated sludge that zymophyte is dominant bacteria, in described I phase reactor, add redox mediator, described redox mediator is riboflavin, anthraquinone-2, a kind of in 6 stilbene-4,4'-bis-(1-azo-3, 4-dihydroxy-benzene)-2,2'-disulfonates, lawsone, regianin; The content of described redox mediator in waste water is 1～50 μ mol/L; After this step, the clearance of colourity and COD reaches respectively more than 90% and 20%;
(4) step (3) water outlet enters anaerobism section II phase reactor and produces methane process, and reactor contains take the anaerobic activated sludge that methanogen is dominant bacteria, and after this step, the clearance of colourity and COD reaches respectively more than 95% and 60%.
Preferably, described I phase reactor, II phase reactor are a kind of in sequence batch (anaerobic reactor, upflow anaerobic sludge blanket reactor, Anaerobic upflow reactor.
Preferably, in step (3), controlling pH is 5～7, and hydraulic detention time is 1～5h, and I phase reactor operating temperature is 10～35 ℃, and redox potential is less than-100 mV; In step (4), controlling pH is 6.5～7.5, and hydraulic detention time is 5～12h, and inner circulating reflux ratio is 100～300%, and II phase reactor operating temperature is 10～50 ℃, be less than-200mV of redox potential.
Preferably, described in step (1), vitriol is sodium sulfate, and its content in waste water is 2～10g/L.
Preferably, described in step (2), sulfuric acid is industrial waste sulfuric acid, and in step (2) water outlet, sulfate radical detection level is 100～1000 mg/L.Adopt industrial waste sulfuric acid to carry out pH regulator, thus efficent use of resources turn waste into wealth, cost-saving.
Preferably, in step (3), controlling pH is 5.5～6.5, and hydraulic detention time is 2～3h, and I phase reactor operating temperature is 15～30 ℃, and redox potential is-150～-250mV; In step (4), controlling pH is 6.8～7.2, and hydraulic detention time is 6～8h, and inner circulating reflux ratio is 100～150%, 25～35 ℃ of temperature, and redox potential is-300～-500mV.
Preferably, described Anaerobic upflow reactor employing particle diameter is 3～5mm volcanics, haydite or gac are filler.
Preferably, in described sequence batch (anaerobic reactor or upflow anaerobic sludge blanket reactor, be provided with diving mixer.Being provided with of diving mixer is beneficial to anaerobic activated sludge and extensively contacts with waste water.
Preferably, the described dyeing waste water pretreatment process based on anaerobism section phase detachment technique comprises the steps:
(1) in alkali decrement waste water or desized wastewater, add 5.2g/L sodium sulfate, and in separator, reclaim PVA and carry out recycling;
(2) step (1) water outlet enters equalizing tank after mixing with dyeing waste-water, and in equalizing tank, with sulphur acid for adjusting pH to 7, sulfate radical detection level is 500 mg/L, and COD and the sulfate radical mass ratio controlled in step (2) water outlet are 3.6;
(3) step (2) water outlet enters anaerobism section I phase reactor and produces hydrogen acid process, reactor is Anaerobic upflow reactor, it take haydite as filler, median size 3 mm, controlling pH is 6, hydraulic detention time is 2.5h, and I phase reactor operating temperature is 25 ℃, and redox potential is-150～-250mV; And add Riboflavin Tetrabutyrate 0 μ mol/L; After this step, chroma removal rate is that 93.8%, COD clearance is 25.8%;
(4) step (3) water outlet enters anaerobism section II phase reactor and produces methane process, and II phase reactor is upflow anaerobic sludge blanket reactor; The volume ratio of described I phase reactor and II phase reactor is 1:3; Controlling pH is 7, and hydraulic detention time is 8h, and inner circulating reflux ratio is 35 ℃ of 100%, the II phase reactor operating temperatures, and redox potential is-350～-450 mV; After this step, chroma removal rate is that 98.8%, COD clearance is 65.6%.
In step of the present invention (2), can add in right amount vitriol in step (1) and the sulfuric acid in step (2) according to COD content in waste water, reaching that PVA reclaims and the basis of pH regulator on, control waste water COD/SO
4 2-mass ratio is between 1～10:1.
The startup of I phase reactor is controlled by physical chemistry the form that method and kinetic control method combine and is realized.Starting period, adopting treatment of dyeing wastewater factory anaerobic activated sludge is seed sludge, anaerobic activated sludge in I phase reactor be take zymophyte as dominant bacteria, by pH value in on-line Control I phase reactor in slant acidity scope (in 5～7), control hydraulic detention time simultaneously and shorten gradually, progressively to improve organic sludge loading, and make zymogenic growth obtain ecological dominance, carry out fermentation and hydrogen production, the starting period is 10～30 days.The starting period of II phase reactor, the treatment of dyeing wastewater factory anaerobic activated sludge of take is seed sludge, anaerobic activated sludge in II phase reactor be take methanogen as dominant bacteria, by online pH meter, control wastewater pH in 6.5～7.5, hydraulic detention time is 5～12h, and inner circulating reflux ratio is 100～300%, and reactor operating temperature is 10～50 ℃, redox potential (ORP) <-200 mV, the starting period is 10～30 days.
The present invention is based on anaerobism section phase detachment technique, homogenous anaerobic system is divided into antibiotic wastewater, be about to anaerobism section and be divided into I phase (produce hydrogen and produce sour phase) and II phase (methanogenic phase), utilize the organism in waste water that electron donor is provided, utilize the reducing power of sulfate-reducing process and its reduzate sulfide, at I, realize mutually effective decolouring of dyestuff, improve wastewater biodegradability, and realize mutually organic efficient removal at II.Antibiotic wastewater is realized and being separated according to microbiological property, can reduce engineering construction cost, and reduce sludge yield and disposal costs.
The present invention can reduce follow-up aerobic section organic sludge loading, shortens hydraulic detention time, thereby reduces follow-up aerobic section sludge yield more than 20%, reduces follow-up aerobic section engineering construction cost more than 15%.
Know-why of the present invention is:
In equalizing tank, alkali decrement waste water, desized wastewater and dyeing waste-water mix, and carry out pH regulator with industrial waste sulfuric acid.Therefore, enter in the waste water of anaerobism section and mainly contain starch, dyestuff and vitriol.The present invention mainly undergoes technological transformation to anaerobism section, exploitation diphasic anaerobic treatment technology.
Anaerobism section I phase: produce hydrogen and produce sour phase.In anaerobism section I phase, the present invention utilizes zymogenic ecological dominance to carry out fermentation and hydrogen production, realizes the efficient decolorizing of waste water.H
2be the optimized electronic donor of dyestuff biological reducing decolouring in dyeing waste water, fermentation and hydrogen production is the basic reason that dyeing waste water has higher decoloration performance.Owing to containing a certain amount of vitriol in system, sulfate reduction and reducing dyes decolorization all can be utilized H
2, between this kind, hydrogen transmittance process can promote again starch, glucose fermentation process.In addition, in vitriol anaerobic reduction process, can produce sulfide, also can be used as dye decolored good reductive agent, and under the effect of redox mediator, decolorization rate is significantly improved.So, anaerobism section I mutually in, can realize the quick decolouring with the dyeing waste water of biological coupling interaction effect based on chemistry, realize effective organic matter fermentation simultaneously and produce hydrogen, produce acid, thus the substrate (VFA) that the suitable ecotope of providing smoothly of methane process is provided mutually and easily utilizes for anaerobism II.Dyeing waste water is after anaerobism section I processes mutually, realized the quick decolouring of dyestuff, and produce hydrogen and acid process by the orientation fermentation that hydrogen transfer function between the kind of sulfate reduction has been strengthened I phase starch, this provides favourable condition smoothly for II is mutually methanogenic, COD concentration significantly reduces simultaneously, and biodegradability is improved, and has reduced the organic loading to follow-up aerobic section, realize the shortening of whole hydraulic detention time (HRT), the total pond of engineering holds and capital cost also will significantly be cut down.
Anaerobism section II phase: methanogenic phase.Methanogen utilizes the VFA that previous step generates to produce methane, and described VFA is mainly volatility short chain fatty acid, than traditional anaerobic treatment process, and the methanogenic phase energy by-passing portions organic loading in diphasic anaerobic technique.Because the sludge yield containing the anaerobic activated sludge of methanogen is far below aerobic sludge, therefore, the present invention also can cut down sludge yield, solve or alleviate treatment of dyeing wastewater plant excess sludge and process handling problems, ensure that final outflow water meets discharge or reuse requirement, has larger environment and social effect.
Water outlet after the present invention processes enters conventional printing-dyeing waste water treatment process aerobic section, qualified discharge or reuse after penetration depth processing unit processes again after biochemical system is processed.
The present invention is as anaerobism section renovation technique in treatment of dyeing wastewater flow process, provide a kind of antibiotic wastewater to carry out pre-treatment to dyeing waste water, can effectively improve colourity and COD clearance, wastewater biodegradability significantly improves, and has overcome the problems such as traditional anaerobic technique treatment effect is unstable, sludge yield is large.The present invention can effectively remove colourity and the COD in dyeing waste water, and clearance can reach respectively more than 95% and 60%, significantly reduces the organic loading to subsequent handling.
Accompanying drawing explanation
Fig. 1 is the functional block diagram based on treatment of dyeing wastewater of the present invention.
Embodiment
Below in conjunction with the drawings and specific embodiments, the invention will be further described, but protection scope of the present invention is not limited to this.
Embodiment 1
With reference to Fig. 1, a kind of dyeing waste water pretreatment process based on anaerobism section phase detachment technique, described dyeing waste water comprises alkali decrement waste water, desized wastewater and dyeing waste-water, described dyeing waste water pretreatment process comprises the steps:
(1) alkali decrement, desized wastewater reclaim PVA and carry out recycling by adding 7.8g/L sodium sulfate in separator;
(2) after the waste water that step (1) water outlet produces with the dyeing process of printing and dyeing mill mixes, enter equalizing tank, in equalizing tank, with sulfur waste acid for adjusting pH value to 7, in system, sulfate radical detection level is 710 mg/L, COD/SO
4 2-mass ratio is 2.5;
(3) step (2) water outlet enters diphasic anaerobic technique I phase reactor, reactor is Anaerobic upflow reactor (AF), take volcanics as filler, median size 4 mm, controlling reactor water inlet pH value is 6.5, controlling hydraulic detention time (HRT) is 4 h, and I phase reactor operating temperature is 35 ℃, and redox potential (ORP) is-150～-250mV; And add anthraquinone-2,6 stilbene-4,4'-bis-(1-azo-3, 4-dihydroxy-benzene)-2,2'-disulfonate 10 μ mol/L; After this step, chroma removal rate is that 92.5%, COD clearance is 23.8%;
(4) step (3) water outlet enters II phase reactor, reactor is upflow anaerobic sludge blanket reactor (UASB), controlling pH value is 6.8, hydraulic detention time is 8 h, inner circulating reflux is than 100%, reactor operating temperature is 40 ℃, and redox potential (ORP) is between-300～-400mV, and sludge age is 150d; The volume ratio of described I phase reactor and II phase reactor is 1:3; After this step, chroma removal rate is that 98.3%, COD clearance is 64.4%.
The control group of antibiotic wastewater is the single-phase processing waste water of UASB reactor, controlling pH value is 7.0, hydraulic detention time is 12 h(anaerobism section phase-separation system I phases and the hydraulic detention time sum of II phase), inner circulating reflux is than 100%, and sludge age is 150d; Control group effluent color dilution clearance is that 74.1%, COD clearance is 32.5%.
According to above-mentioned steps, the Inlet and outlet water indices of antibiotic wastewater and control group is in Table 1.
Table 1
Water outlet after embodiment 1 processes enters conventional printing-dyeing waste water treatment process aerobic section, qualified discharge or reuse after penetration depth processing unit processes again after biochemical system is processed.
Embodiment 2
With reference to Fig. 1, a kind of dyeing waste water pretreatment process based on anaerobism section phase detachment technique, described dyeing waste water comprises alkali decrement waste water, desized wastewater and dyeing waste-water, and described anaerobism section comprises I phase and II phase, and described dyeing waste water pretreatment process comprises the steps:
(1) in alkali decrement waste water or desized wastewater, add 5.2g/L sodium sulfate, and in separator, reclaim PVA and carry out recycling;
(2) after the waste water that step (1) water outlet produces with other operation mixes, enter equalizing tank, in equalizing tank, with sulphur acid for adjusting pH to 7, sulfate radical detection level is 500 mg/L, COD/SO
4 2-mass ratio is 3.6;
(3) step (2) water outlet enters anaerobism section I phase reactor, and reactor is Anaerobic upflow reactor (AF), and it take haydite as filler, median size 3mm, controlling pH is 6, hydraulic detention time is 2.5h, I phase reactor operating temperature is 25 ℃, and ORP is-150～-250mV; And add Riboflavin Tetrabutyrate 0 μ mol/L; After this step, chroma removal rate is that 93.8%, COD clearance is 25.8%;
(4) step (3) water outlet enters anaerobism section II phase reactor, and II phase reactor is upflow anaerobic sludge blanket reactor (UASB); The volume ratio of described I phase reactor and II phase reactor is 1:3; Controlling pH is 7, and hydraulic detention time is 6h, and inner circulating reflux ratio is 100%, 35 ℃ of reactor operating temperatures, and ORP is between-350～-450mV, sludge age is 180d; After this step, chroma removal rate is that 98.8%, COD clearance is 65.6%.
The control group of antibiotic wastewater is the single-phase processing waste water of UASB reactor, and controlling pH value is 7.0, and hydraulic detention time is 8.5 h(I phases and the hydraulic detention time sum of II phase), inner circulating reflux is than 100%, and sludge age is 180d; Control group effluent color dilution clearance is that 72.5%, COD clearance is 31.5%.
According to above-mentioned steps, the Inlet and outlet water indices of antibiotic wastewater and control group is in Table 2.
Table 2
Water outlet after embodiment 2 processes enters conventional printing-dyeing waste water treatment process aerobic section, qualified discharge or reuse after penetration depth processing unit processes again after biochemical system is processed.
Embodiment 3
With reference to Fig. 1, a kind of dyeing waste water pretreatment process based on anaerobism section phase detachment technique, described dyeing waste water comprises alkali decrement waste water, desized wastewater and dyeing waste-water, described dyeing waste water pretreatment process comprises the steps:
(1) alkali decrement, desized wastewater reclaim PVA and carry out recycling by adding 2.9g/L sodium sulfate in separator;
(2) after the waste water that step (1) water outlet produces with the dyeing process of printing and dyeing mill mixes, enter equalizing tank, in equalizing tank, with sulfur waste acid for adjusting pH value to 6.8, in system, sulfate radical detection level is 220 mg/L, COD/SO
4 2-mass ratio is 8.2;
(3) step (2) water outlet enters diphasic anaerobic technique I phase reactor, and reactor is sequence batch (anaerobic reactor (ASBR), inside establishes submersible agitator; Mudpan is established in water outlet, and return sludge ratio is 150%; Controlling pH value in reactor is 6.5, and controlling hydraulic detention time is 3 h, and I phase reactor operating temperature is 15 ℃, and ORP is-150～-250mV, and sludge age is 15d; And add lawsone 40 μ mol/L; After this step, chroma removal rate is that 90.8%, COD clearance is 25.6%;
(4) step (3) water outlet enters II phase reactor, and reactor is UASB reactor, and controlling pH value is 7.2, and hydraulic detention time is 10h, and inner circulating reflux is than 150%, 30 ℃ of reactor operating temperatures, and ORP is between-350～-500mV, sludge age is 200d; II phase reactor effluent color dilution clearance is that 97.9%, COD clearance is 60.7%.
The control group of antibiotic wastewater is the single-phase processing waste water of UASB reactor, and controlling pH value is 7.0, and hydraulic detention time is 13 h(I phases and the hydraulic detention time sum of II phase), inner circulating reflux is than 150%, and sludge age is 200d; Control group effluent color dilution clearance is that 76%, COD clearance is 33.2%.
According to above-mentioned steps, the Inlet and outlet water indices of antibiotic wastewater and control group is in Table 3.
Table 3
Water outlet after embodiment 3 processes enters conventional printing-dyeing waste water treatment process aerobic section, qualified discharge or reuse after penetration depth processing unit processes again after biochemical system is processed.
Embodiment 4
With reference to Fig. 1, a kind of dyeing waste water pretreatment process based on anaerobism section phase detachment technique, described dyeing waste water comprises alkali decrement waste water, desized wastewater and dyeing waste-water, and described anaerobism section comprises I phase and II phase, and described dyeing waste water pretreatment process comprises the steps:
(1) alkali decrement, desized wastewater reclaim PVA and carry out recycling by adding 9.8g/L sodium sulfate in separator;
(2) after the waste water that step (1) water outlet produces with the dyeing process of printing and dyeing mill mixes, enter equalizing tank, in equalizing tank, with sulfur waste acid for adjusting pH value to 7.5, in system, sulfate radical detection level is 800 mg/L, COD/SO
4 2-mass ratio is 2.3;
(3) step (2) water outlet enters diphasic anaerobic technique I phase reactor, and reactor is upflow anaerobic sludge blanket reactor (UASB), inside establishes submersible agitator; Mudpan is established in water outlet, and return sludge ratio is 100%; Controlling pH value in reactor is 5.8, and hydraulic detention time is 2 h, and I phase reactor operating temperature is 30 ℃, and ORP is-150～-250mV, and sludge age is 20d; And add regianin 30 μ mol/L; After this step, chroma removal rate is that 93%, COD clearance is 29.2%;
(4) step (3) water outlet enters II phase reactor, and reactor is ASBR reactor, inside establishes submersible agitator, and controlling pH value is 7, and hydraulic detention time is 12 h, 45 ℃ of reactor operating temperatures, and ORP is between-350～-450mV, sludge age is 100d; II phase reactor effluent color dilution clearance is that 97.5%, COD clearance is 66.8%.
The control group of antibiotic wastewater is the single-phase processing waste water of ASBR reactor, inside establishes submersible agitator, and controlling pH value is 7.0, and hydraulic detention time is 14 h(I phases and the hydraulic detention time sum of II phase), system is spoil disposal not, and sludge age is 100d; Control group effluent color dilution clearance is that 69%, COD clearance is 37.2%.
According to above-mentioned steps, the Inlet and outlet water indices of antibiotic wastewater and control group is in Table 4.
Table 4
Water outlet after embodiment 4 processes enters conventional printing-dyeing waste water treatment process aerobic section, qualified discharge or reuse after penetration depth processing unit processes again after biochemical system is processed.
Claims (9)
1. the dyeing waste water pretreatment process based on anaerobism section phase detachment technique, described dyeing waste water comprises alkali decrement waste water, desized wastewater and dyeing waste-water, it is characterized in that: described dyeing waste water pretreatment process comprises the steps:
(1) in alkali decrement waste water or desized wastewater, add 2.9～9.8g/L sodium sulfate condensing agent, and in separator, reclaim PVA and carry out recycling;
(2) step (1) water outlet enters equalizing tank after mixing with dyeing waste-water, and in equalizing tank, with sulphur acid for adjusting pH to 5～8, the COD in the water outlet of control step (2) and sulfate radical mass ratio are between 2.3～8.2:1;
(3) step (2) water outlet enters anaerobism section I phase reactor and produces hydrogen acid process, reactor contains take the anaerobic activated sludge that zymophyte is dominant bacteria, in described I phase reactor, add redox mediator, described redox mediator is riboflavin, anthraquinone-2, a kind of in 6 stilbene-4,4'-bis-(1-azo-3, 4-dihydroxy-benzene)-2,2'-disulfonates, lawsone, regianin; The content of described redox mediator in waste water is 10～40 μ mol/L; After this step, the clearance of colourity and COD reaches respectively more than 90% and 20%;
(4) step (3) water outlet enters anaerobism section II phase reactor and produces methane process, and reactor contains take the anaerobic activated sludge that methanogen is dominant bacteria, and after this step, the clearance of colourity and COD reaches respectively more than 95% and 60%.
2. according to the dyeing waste water pretreatment process based on anaerobism section phase detachment technique described in claim 1, it is characterized in that: described I phase reactor, II phase reactor are a kind of in sequence batch (anaerobic reactor, upflow anaerobic sludge blanket reactor, Anaerobic upflow reactor.
3. according to the dyeing waste water pretreatment process based on anaerobism section phase detachment technique described in claim 1, it is characterized in that: in step (3), controlling pH is 5～7, and hydraulic detention time is 1～5h, I phase reactor operating temperature is 10～35 ℃, and redox potential is less than-100 mV; In step (4), controlling pH is 6.5～7.5, and hydraulic detention time is 5～12h, and inner circulating reflux ratio is 100～300%, and II phase reactor operating temperature is 10～50 ℃, be less than-200mV of redox potential.
4. according to the dyeing waste water pretreatment process based on anaerobism section phase detachment technique described in claim 1, it is characterized in that: described in step (1), vitriol is sodium sulfate, its content in waste water is 2～10g/L.
5. according to the dyeing waste water pretreatment process based on anaerobism section phase detachment technique described in claim 1, it is characterized in that: described in step (2), sulfuric acid is industrial waste sulfuric acid, in step (2) water outlet, sulfate radical detection level is 100～1000 mg/L.
6. according to the dyeing waste water pretreatment process based on anaerobism section phase detachment technique described in claim 3, it is characterized in that: in step (3), controlling pH is 5.5～6.5, hydraulic detention time is 2～3h, I phase reactor operating temperature is 15～30 ℃, and redox potential is-150～-250mV; In step (4), controlling pH is 6.8～7.2, and hydraulic detention time is 6～8h, and inner circulating reflux ratio is 100～150%, 25～35 ℃ of temperature, and redox potential is-300～-500mV.
7. according to the dyeing waste water pretreatment process based on anaerobism section phase detachment technique described in claim 2, it is characterized in that: it is filler that described Anaerobic upflow reactor adopts volcanics, haydite or the gac that particle diameter is 3～5mm.
8. according to the dyeing waste water pretreatment process based on anaerobism section phase detachment technique described in claim 2, it is characterized in that: in described sequence batch (anaerobic reactor or upflow anaerobic sludge blanket reactor, be provided with diving mixer.
9. according to the dyeing waste water pretreatment process based on anaerobism section phase detachment technique described in claim 3, it is characterized in that: comprise the steps:
(1) in alkali decrement waste water or desized wastewater, add 5.2g/L sodium sulfate, and in separator, reclaim PVA and carry out recycling;
(2) step (1) water outlet enters equalizing tank after mixing with dyeing waste-water, and in equalizing tank, with sulphur acid for adjusting pH to 7, sulfate radical detection level is 500mg/L, and COD and the sulfate radical mass ratio controlled in step (2) water outlet are 3.6;
(3) step (2) water outlet enters anaerobism section I phase reactor and produces hydrogen acid process, reactor is Anaerobic upflow reactor, it take haydite as filler, median size 3mm, controlling pH is 6, hydraulic detention time is 2.5h, and I phase reactor operating temperature is 25 ℃, and redox potential is-150～-250mV; And add Riboflavin Tetrabutyrate 0 μ mol/L; After this step, chroma removal rate is that 93.8%, COD clearance is 25.8%;
(4) step (3) water outlet enters anaerobism section II phase reactor and produces methane process, and II phase reactor is upflow anaerobic sludge blanket reactor; The volume ratio of described I phase reactor and II phase reactor is 1:3; Controlling pH is 7, and hydraulic detention time is 8h, and inner circulating reflux ratio is 35 ℃ of 100%, the II phase reactor operating temperatures, and redox potential is-350～-450mV; After this step, chroma removal rate is that 98.8%, COD clearance is 65.6%.
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| CN103964571B (en) * | 2014-04-14 | 2015-08-12 | 杭州电子科技大学 | A kind of biomass filler anaerobic filter tank processing oxidation state pollutent |
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