CN1413928A - Treatment technology for acrylic fibers waste water by dry process - Google Patents
Treatment technology for acrylic fibers waste water by dry process Download PDFInfo
- Publication number
- CN1413928A CN1413928A CN 02135650 CN02135650A CN1413928A CN 1413928 A CN1413928 A CN 1413928A CN 02135650 CN02135650 CN 02135650 CN 02135650 A CN02135650 A CN 02135650A CN 1413928 A CN1413928 A CN 1413928A
- Authority
- CN
- China
- Prior art keywords
- sludge
- waste water
- dissolved oxygen
- anaerobic
- coagulation
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Landscapes
- Water Treatment By Electricity Or Magnetism (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
Abstract
A process for treating the sewage generated by preparing acrylic fibre by dry method includes such steps as regulating pH value, coagulation-deposition to remove suspended substance and colloid, cooling supernatant, flowing in conditioning pool, active mud-microeletrolyzing stemp while providing oxygen to the active mud, anaerobic acidifying while introducing life sewage for removing EDTA and Na salt, and anaerobic-aerobic step for biologic denitrifying. Its advantages are high effect and easy operation.
Description
Technical field
The invention belongs to the multiple-stage treatment category of trade effluent, be specifically related to a kind of acrylic fibers waste water by dry process treatment process.
Background technology
The whole nation has five covers dry acrylic fiber production equipment of the same type at present, and they are respectively Fushun Petrochemical Company Acrylic Fibers Plant, gold river in Zhejiang Province, Zhejiang Acrylic Fibers Plant, Qinhuangdao Acrylic Fibers Plant, Maoming City Acrylic Fibers Plant and Qilu Petrochemical company Acrylic Fibers Plant.This five tame Acrylic Fibers Plant waste water treatment process is both the design of designing institute of the china textile Department of Industry, adopts anaerobic-aerobic-biological active carbon treatment process.
With Qilu Petrochemical company Acrylic Fibers Plant is example, and the waste water in its sewage-farm is mainly derived from acrylic fibers processing wastewater, sanitary sewage, acid-bearing wastewater and ground wash-down water etc.Figure of description 2 is seen in its technical process;
Existing sewage-farm is to vinyl cyanide, DMF (Dimethyl formamide, dimethyl formamide) etc. organic pollutant has certain treatment effect, but to COD, EDTA (Ethylene diamine teraacetic acid, ethylenediamine tetraacetic acid (EDTA)) processing efficiency is lower, the waste discharge severe overweight.
The subject matter of the normal operation in restriction sewage-farm has:
(1) the high and low polymers molecular weight of the influence of high and low polymers is big, and difficulty is degraded by microorganisms, and oligopolymer has very strong adhesive, the soft-filler of anaerobic pond and Aerobic Pond parcel, microbial film is gone to pot, and the sewage-farm processing efficiency sharply descends;
(2) sulfate radical produces substrate competition to anaerobic disadvantageous effect sulfate radical reduction bacterium and methanobacteria, has reduced microorganism to organic degradation capability, has formed the impact to anaerobic treatment;
(3) influencing of auxiliary agent added more than 20 kind of auxiliary agent in the dry acrylic fiber production, contains the material of difficult for biological degradation in the waste water;
(4) system defect is because there is defective (as water distribution etc.) in anaerobic system, thereby makes anaerobic system not bring into play its distinctive effect;
(5) mud reflux problem.The sewage-farm with regard to not considering the ammonia nitrogen problem, is back to anaerobic pond with second pond mud when initial design, can't guarantee the sludge retention time of Aerobic Pond, makes system lose the ability of ammonia nitrogen removal;
(6) accident pool and equalizing tank problem.The ability that present equalizing tank is regulated water quality a little less than, owing to when initial design, accident pool is not arranged, cause the instability of whole biochemical system operation again;
(7) the shunting sanitary sewage biochemical of considering to remove contamination is better, advance anaerobism after, it has increased the hydraulic load of anaerobic pond on the one hand, has reduced the degraded of recalcitrant substance on the other hand;
(8) bio-chemical effluent COD350～600mg/L contains recalcitrant substance in the waste water, biological activated carbon is handled does not almost have effect.
Fushun petrochemical industry research institute once carried out biochemical degradation research to Nitrilon waste water, adopt intermittent activated sludge process (Sequencing Batch Reactor respectively, SBR), traditional activated sludge process, three kinds of different process of biological contact oxidation process, water outlet COD300～500mg/L, conclude: have recalcitrant substance in this waste water, this material is water miscible and is difficult to rich amassing, therefore can't confirm.For Nitrilon waste water, COD concentration 1500～2500mg/L should adopt anaerobic biological treatment in theory.Three kinds of technologies that Fushun petrochemical industry research institute adopts in fact all are aerobic biological treatment processes, so the be beyond one's reach emission standard (COD concentration 160mg/L) of regulation of its bio-chemical effluent.
Carried out anaerobism, anoxic, aerobic six kinds of various combination technologies and the experiment of many-sided advanced treatment in 1998, conclude: contain the material of difficult for biological degradation in the acrylic fibers waste water by dry process really, these materials mainly are EDTA, macromole recalcitrant substance and organic sulfonate.The Anoxybiotic-aerobic biologic treatment effect is better, and water outlet COD can reach 280～320mg/L.
In having the flow test of anaerobic unit owing to contain the vitriol of 300～1200mg/L in the Nitrilon waste water, in the waste water sulfate concentration fluctuation bigger, cause the anaerobic reactor can not normally stable operation.1999, we carried out the research of coagulating sedimentation-anaerobic digestion-anaerobic-aerobic-sand filtration-activated carbon process processing Nitrilon waste water, have applied for patent, application number 99112488.X; This technology is the technology of taking at national grade one discharge standard COD≤100mg/L, Nitrilon waste water can be reached national grade one discharge standard, but the shortcoming of this technology mainly is to have adopted activated carbon process, the cost for wastewater treatment height.
Country had worked out standard again according to the unmanageable practical situation of Nitrilon waste water in 2000, changed the industry first discharge standard into COD≤160mg/L.For this reason, optimize original technical process, adopted air supporting-adsorption biodegradation-sulfate reduction-biological desulphurization-products methane three to be in series-research of anoxic-aerobic process processing Nitrilon waste water, also applied for patent, application number 00129461.X; Though this technology can reach national grade one discharge standard, exist that operational path is long, sulfate reduction and produce shortcomings such as methane control condition harshness, biological desulphurization corrodibility are big, industrial implementation difficulty in the anaerobism section.
Summary of the invention
The objective of the invention is to propose a kind of high efficiency treatment process that contains the trade effluent of recalcitrant substance, be applicable to the acrylic fibers waste water by dry process treatment process.This ratio juris is equally applicable to dyeing waste water, textile waste and other petrochemical wastewater.
For achieving the above object, the present invention has taked following technical scheme:
Develop a kind of treatment process of acrylic fibers waste water by dry process, it is characterized in that this technical process comprises coagulation-sedimentation unit, active sludge-little electrolysis cells, anaerobic acidification unit and the anaerobic-aerobic unit of combination successively;
After dry acrylic fiber processing wastewater, acid-bearing wastewater and ground wash-down water mix, enter suspended substance and colloidalmaterial in coagulation-sedimentation unit removal waste water behind the adjusting pH; Coagulation-settled supernatant liquor enters equalizing tank and regulates the water quality and the water yield by cooling, enter active sludge-little electrolysis cells then, carry out electrolytic reaction and simultaneously provide oxygen, make that microorganism is easier in the mud decomposes the organism in the system, reduce waste water COD to active sludge; Enter chemical structure and biodegradability that the anaerobic acidification unit changes hardly degraded organic substance subsequently; At last, introduce sanitary sewage in the anoxic section, improve the removal effect of biological denitrification process to recalcitrant substance EDTA and sodium salt thereof, waste water reaches the industry emission standard after Anoxybiotic-aerobic biologic denitrogenation operation is handled.
In above-mentioned coagulation-sedimentation unit, operating parameter is: 60～95 ℃ of temperature, and in the composite flocculation agent that polymeric aluminum and quaternary ammonium salt cation flocculation agent are formed, polymeric aluminum consumption 30～200mg/L, quaternary ammonium salt cation flocculation agent consumption is 0.3～1.5mg/L;
In above-mentioned active sludge-little electrolysis cells, the carbon steel suspension member is set in the active sludge system, operating parameter is: pH3.5～9.0, hydraulic detention time 2～18h, dissolved oxygen 0.5～7.0mg/L, sludge concentration 2～4g/L, sludge retention time 8～12d, return sludge ratio 50%～200%;
In the above-mentioned anaerobic acidification unit, operating parameter is: pH5.5～6.5, hydraulic detention time 8～25h, dissolved oxygen 0～0.2mg/L, sludge concentration 5～10g/L;
In the above-mentioned anaerobic-aerobic unit, operating parameter is: anoxic section pH6.5～7.5, hydraulic detention time 6～10h, dissolved oxygen 0～0.5mg/L, sludge concentration 2～4g/L, sludge retention time 15～30d; Aerobic section pH6.5～7.5, hydraulic detention time 13～25h, dissolved oxygen 2.0～7.0mg/L, sludge concentration 2～4g/L, sludge retention time 15～30d;
Available coagulation-air flotation cell replaces coagulation-sedimentation unit, coagulation-air supporting operating parameter is: 60～95 ℃ of temperature, in the composite flocculation agent that polymeric aluminum and quaternary ammonium salt cation flocculation agent are formed, polymeric aluminum consumption 30～200mg/L, quaternary ammonium salt cation flocculation agent consumption 0.3～1.5mg/L, water pH value 5.5～8.5, dissolved-air pressure 0.2～0.5Mpa, gas-water ratio is 1: 4～1: 1;
Above-mentioned coagulation-sedimentation unit and active sludge-little electrolysis cells order can exchange;
Above-mentioned anaerobic acidification unit is two-phase anaerobic acidification also, i.e. sulfate reduction acid-producing and produce methane reaction two-phase anaerobic acidification;
In above-mentioned anoxic～aerobic unit, can add Powdered Activated Carbon 10～100mg/L at aerobic section, preferred gac dosage is 50mg/L;
Above-mentioned original acrylic fibers waste water by dry process COD 1500 ± 300mg/L, BOD 450 ± 100mg/L, ammonia nitrogen 45 ± 20mg/L, turbidity 50 ± 30mg/L, pH6.3 ± 1,65 ± 30 ℃ of temperature, EDTA 180 ± 80mg/L, sulfate radical 320 ± 150mg/L, inferior sulfate radical is 580 ± 300mg/L, handles COD 50～160mg/L, NH
3-N is less than the acrylic fiber industry national grade one discharge standard of 15mg/L.
Characteristics of the present invention are to have adopted following reasonable process:
1. coagulation-sedimentation:
Contain a large amount of low-molecular(weight)polymers in the acrylic fibers waste water by dry process, they exist with the suspension colloidal form, are difficult to natural subsidence and remove, and oligopolymer not only influences the normal operation of biochemical system after entering biochemical system, and has increased the organic matter degradation load; Oligopolymer easily stops up filler simultaneously, reduces the specific surface area of filler, has increased the wastewater biochemical intractability.Therefore, it is necessary at first removing low-molecular(weight)polymer, the composite flocculation agent that the present invention adopts polymerize aluminum chloride and quaternary ammonium salt cation flocculation agent to form, adopt coagulation-sedimentation process to remove the oligopolymer colloid, providing for the normal operation of biochemical treatment is part, has reduced the load of biochemical treatment effectively.The main purpose of this step is to remove high and low polymkeric substance, though coagulation-sedimentation effect a little less than air-float technology, coagulation-sedimentation process power consumption is little, simple to operate, also can achieve the goal.When processing wastewater carried out coagulant precipitation, test temperature should be greater than 60 ℃, and comparatively suitable coagulated agent is the composite flocculation agent that polymeric aluminum and quaternary ammonium salt cation flocculation agent are formed, and using dosage is respectively 30～200mg/L and greater than 0.3～1.5mg/L.The processing wastewater delivery turbidity is less than 15mg/L at this moment, and most of polymkeric substance can be removed.The ground wash-down water is introduced in the processing wastewater, can remove high low-grade polymer in the wash-down water of ground by coagulation-sedimentation.Contain a large amount of inferior sulfate radicals in the processing wastewater, contain a large amount of sulfate radicals in the acid-bearing wastewater,, regulate pH with lime and can remove a part of inferior sulfate radical by acid-bearing wastewater is introduced in the processing wastewater.
2. active sludge-little electrolysis:
According to number 01142858.9 active sludge-micro-electrolysis method that provides is provided in the patent, acrylic fibers waste water by dry process is carried out Processing Test.Be included in the common active sludge system carbon steel suspension member is set, pH value in conditioned reaction district is 3.5～9, and hydraulic detention time is greater than 2 hours, and dissolved oxygen is greater than 0.5mg/L, sludge concentration 2～4g/L, sludge retention time 8～12d, return sludge ratio 50～200%.In above-mentioned system, iron is reducing substances, and when oxidized, its two electronics that provide have the organic structure function of destruction, even can chain rupture by electrode reaction.The product Fe of electrode reaction
2+Also have more intense reductibility, help Fe
3+Generation, produce the very strong Fe (OH) of cohesive force
3Colloid, the organism in the absorption waste water.The hydraulic detention time that equalizing tank is unnecessary transform active sludge-little electrolysis as, when this system and the coexistence of active sludge system, pass through aeration, can play on the one hand and stir and the effect of minimizing concentration polarization, the carrying out of accelerating electrode reaction, simultaneously provide oxygen, make that microorganism is easier in the active sludge decomposes the organism in the system, reduce waste water COD to active sludge.
3. anaerobic acidification
Transform the anaerobic system of prior art as the anaerobic acidification treatment system.The anaerobic acidification preconditioning technique has carried out comparatively deep research at present as a kind of economy, convenience, practical Technology.Advantages such as the anaerobic acidification preconditioning technique has can improve the wastewater biochemical degradation property, energy consumption is low, the residence time is short and investment cost is low are more a kind of novel wastewater processing technologies of development at present.When organism carries out anaerobic digestion, mainly experience two stages: acid fermentation and alkaline fermentation stage.Anaerobic acidification is as pre-treatment, and main foundation is exactly two stage theories of anaerobically fermenting.And acid-producing bacteria and methanogen are relatively, have of a great variety, the phase is short from generation to generation, accretion rate is fast, adaptability is strong and to envrionment conditions requirement characteristic such as strictness very not.The product acid phase of anaerobic acidification and two-phase anaerobism (being sulfate reduction acid-producing and the product methane reaction technology of application number 00129461.X) has similar part, all is acid fermentation, but incomplete same.The two-phase anaerobic produces acid phase must be decomposed into organism formic acid, acetate and the H that can supply methanobacteria to utilize
2/ CO
2Deng, and anaerobic acidification will all not change into low molecular organic acids by organism, main purpose is chemical structure and the biodegradability that changes hardly degraded organic substance, so that follow-up aerobic treatment.
4. Anoxybiotic-aerobic biologic denitrogenation
Transform aerobic system as the anaerobic-aerobic system, organonitrogen, inorganic nitrogen in the waste water are had higher removal effect, this law ammonia nitrogen removal frank height can reach 100%; Sanitary sewage is directly put into aerobic system as co-substrate, both can prolong the hydraulic detention time of equalizing tank and anaerobic pond, also can improve removal effect EDTA; Introduce sanitary sewage in the anoxic section, instrument has not improved the biodegradability of Nitrilon waste water, has reduced the hydraulic load of anaerobism section, and has guaranteed the higher nitric efficiency of Anoxybiotic-aerobic biologic denitrification process.Because nitrogenous substances is more in the Nitrilon waste water, after active sludge-little electrolysis and anaerobic acidification processing, the ammonia-nitrogen content in the waste water will raise significantly, is further to remove organism and ammonia nitrogen, needs to adopt anoxic to carry out with the aerobic processing mode that combines.Aerobic system can utilize present facility, is anoxic and aerobic two portions by changing aeration with system divides, improves the removal effect of aerobic system to COD, ammonia nitrogen.
5. add Powdered Activated Carbon in case of necessity
Because the imperfect stability of Industrial processes, the phenomenon if bio-chemical effluent exceeds standard can add Powdered Activated Carbon 10～100mg/L at aerobic section, and preferred gac dosage is 50mg/L; The more effective waste water that guaranteed reaches the industry first discharge standard of national regulation.The adding of Powdered Activated Carbon has not only improved the settling property of mud, and has guaranteed that waste water can qualified discharge.So just need not adopt operation and the higher post-processing technology of investment cost.
6. sanitary sewage is directly put into the biological degradation that aerobic system promotes EDTA as co-substrate
(the Ethylene diamine teraacetic acid of EDTA in the acrylic fibers waste water by dry process, ethylenediamine tetraacetic acid (EDTA)) and sodium salt be recalcitrant substance, the EDTA degradation rate can be brought up to 80% by adding the sodium acetate co-substrate, its major cause is the good biodegradability of sodium acetate, almost can be fully by biological degradation, during simultaneously as the carbon source of microorganism, sodium acetate has impelled the degraded of active sludge to EDTA at sodium acetate and EDTA.
As everyone knows, the good biodegradability of sanitary sewage, and contain various microbial strainss in the sanitary sewage, it is put in the waste water that contains EDTA, not only can improve the biodegradability of waste water, simultaneously, the various easy biochemical organism in the sanitary sewage also can impel EDTA further to decompose.
This law than the advantage that prior art has is:
1. technical process is reasonable, makes full use of the equipment of existing Sewage treatment systems, transform new treatment process as, has improved treatment effect, has reduced operation easier;
The present invention operate simple and easy, stable, industrial implementation is easy, is an effective new way handling acrylic fibers waste water by dry process.
Description of drawings
Fig. 1 is the processing technological flow block diagram of the acrylic fibers waste water by dry process after the present invention improves;
Fig. 2 is the processing technological flow block diagram of prior art acrylic fibers waste water by dry process.
Fig. 1 is the acrylic fibers waste water by dry process processing technological flow block diagram after the present invention improves. Among the figure, with acid-bearing wastewater and ground flushing Water is sneaked in the acrylic fibers technique waste water, under 60～95 ℃, uses CaCO3Carry out coagulation-sedimentation after regulating the pH value. Through cooling After enter the adjusting that regulating reservoir carries out water quality and the water yield. Technique waste water enters activated sludge-little electrolysis cells by number of patent application 01142858.9 method process after, pump into the anaerobic acidification pond and carry out anaerobic acidification and process. The anaerobic acidification water outlet is dirty with life Entering the anaerobic-aerobic section after water mixes processes. For improving the anaerobic-aerobic section to the removal effect of difficult for biological degradation material, Add Powdered Activated Carbon in the Aerobic Pond water inlet. HRT among the figure (Hydraulic residence time) is the hydraulic retention time.
Fig. 2 is the existing sewage treatment process block diagram of Qilu Petrochemical company Acrylic Fibers Plant. Among the figure, acrylic fibers technique waste water temperature up to About 80 ℃, enter cooling tower and about two-stage cools to 40 ℃, enter regulating reservoir. Acid-bearing wastewater is regulated pH through storing sour pond, Be delivered to the well that catchments by acidproof pump. Other waste water such as life sewage, ground flushing water directly enter the well that catchments, and carry through rotary grate Rise to regulating reservoir. Make waste water homogeneous and oxidation sulphite at regulating reservoir by aeration, pump into then the anaerobism section, overflow is to aerobic Section, the Aerobic Pond activated sludge returns anaerobic pond digestion through second pond precipitation rear section, burns after the dehydration of residue mud process mud. The second pond water outlet enters the clear water pond after biological charcoal is processed, mix with waste water in clear water pond and thermoelectric plant waste water and power desalination After enter pig Long He.
The present invention is further elaborated below in conjunction with embodiment for embodiment:
Embodiment 1 normal procedure is handled
Implement by Fig. 1 technical process, the dry acrylic fiber processing wastewater is with after acid-bearing wastewater and ground wash-down water mix, the waste water situation is: COD is 1500mg/L, BOD is 450mg/L, and ammonia nitrogen 45mg/L, turbidity are 50mg/L, pH is 6.3, temperature is 85～90 ℃, and EDTA is 320mg/L for the 180mg/L sulfate radical, and inferior sulfate radical is 580mg/L.Regulate pH with lime and 7.5 carry out coagulation-sedimentation.
In coagulation-sedimentation unit, the flocculation agent that adds is commodity polymeric aluminum (being polymerize aluminum chloride Aluminiumpolychloride) 100mg/L and cation polymeric flocculant (commodity CP-937) 0.8mg/L.Coagulation-sedimentation water outlet COD is 1400mg/L, and BOD is 450mg/L, and ammonia nitrogen 45mg/L, turbidity are 7.5mg/L, and pH is 7.3, and temperature is 60 ℃, and EDTA is 180mg/L, and sulfate radical is 340mg/L, and inferior sulfate radical is 300mg/L.Supernatant liquor enters equalizing tank and regulates by cooling to about 35 ℃, enters active sludge-little electrolysis cells then;
In active sludge-little electrolysis cells, the carbon steel suspension member is set in the active sludge system, pH is 5.5～6.5 in control, hydraulic detention time 12h, dissolved oxygen 2mg/L, sludge concentration 3g/L, sludge retention time 12d, return sludge ratio 100%.Active sludge-little electrolysis cells water outlet COD is 700mg/L, and BOD is 150mg/L, and ammonia nitrogen 65mg/L, pH are 5.5～6.0, and temperature is 30 ℃, and EDTA is 180mg/L, and sulfate radical is 850mg/L, and inferior sulfate radical is 5mg/L, enters the anaerobic acidification unit;
In the anaerobic acidification reactor, pH is 5.5～6.0 in control, and temperature is 30 ℃, hydraulic detention time 17.5h, sludge concentration 7g/L.Anaerobic acidification water outlet COD is 650mg/L, and BOD is 180mg/L, and ammonia nitrogen 120mg/L, pH are 5.5, and EDTA is 180mg/L.Anaerobic acidification water outlet and sanitary sewage are mixed into the Anoxybiotic-aerobic biologic denitrification system;
In the anaerobic-aerobic unit, anoxic pond control dissolved oxygen 0.3～0.5mg/L, hydraulic detention time 8h, sludge retention time 20d after pH is controlled at 6.5～7.5, enters aerobic section then, dissolved oxygen 2～4mg/L, hydraulic detention time 19h, sludge retention time 20d, pH is controlled at 6.5～7.5, effluent recycling is to anoxic pond, reflux ratio is 200%, and sludge concentration is controlled at 3g/L, and return sludge ratio is 50%～100%.The Powdered Activated Carbon dosage is 50mg/L in the Aerobic Pond.Thermoelectric and power desalination waste water COD is 10mg/L.Final outflow water COD is less than 140mg/L, and BOD is 5mg/L, and ammonia nitrogen 3mg/L, pH are 7.0, and EDTA is 25mg/L, reaches national acrylic fiber industry first discharge standard.
Embodiment 2 active sludge-little electrolysis cells and coagulation-sedimentation unit order exchanges
Implement by Fig. 1 technical process, the dry acrylic fiber processing wastewater is with after acid-bearing wastewater and ground wash-down water mix, the waste water situation is: COD is 1800mg/L, BOD is 550mg/L, and ammonia nitrogen 25mg/L, turbidity are 80mg/L, pH is 7.3, temperature is 85～90 ℃, and EDTA is 470mg/L for the 260mg/L sulfate radical, and inferior sulfate radical is 880mg/L.Regulate pH with lime and 7.5 carry out active sludge-little electrolysis earlier.
In active sludge-little electrolysis cells, the carbon steel suspension member is set in the active sludge system, pH is 6.5～7.5 in control, hydraulic detention time 12h, dissolved oxygen 5～7mg/L, sludge concentration 4g/L, sludge retention time 10d, return sludge ratio 200%.Active sludge-little electrolysis cells water outlet COD is 700mg/L, and BOD is 150mg/L, and ammonia nitrogen 65mg/L, pH are 5.5～6.0, and temperature is 30 ℃, and EDTA is 180mg/L, and sulfate radical is 850mg/L, and inferior sulfate radical is 5mg/L, enters the anaerobic acidification unit;
In coagulation-sedimentation unit, the flocculation agent that adds is commodity polymeric aluminum 200mg/L and cation polymeric flocculant (CP-937) 1.5mg/L.Coagulation-sedimentation water outlet COD is 1400mg/L, and BOD is 450mg/L, and ammonia nitrogen 45mg/L, turbidity are 7.5mg/L, and pH is 7.3, and temperature is 60 ℃, and EDTA is 180mg/L, and sulfate radical is 340mg/L, and inferior sulfate radical is 300mg/L.Supernatant liquor enters equalizing tank and regulates by cooling to about 35 ℃, enters active sludge-little electrolysis cells then; All the other are with example 1.
Embodiment 3 active sludge-little electrolysis cells and coagulation-sedimentation unit order exchanges
In active sludge-little electrolysis cells, pH is 6.5～7.5 in control, hydraulic detention time 18h, dissolved oxygen 0.5～1mg/L, sludge concentration 4g/L, sludge retention time 10d, return sludge ratio 50%.
In coagulation-sedimentation unit, the flocculation agent that adds is commodity polymeric aluminum 30mg/L and cation polymeric flocculant (CP-937) 0.3mg/L.All the other are with example 1.
Embodiment 4 usefulness coagulation-air flotation cell replaces coagulation-sedimentation unit
Coagulation-air supporting operating parameter is: 60～75 ℃ of temperature, in the composite flocculation agent that polymeric aluminum and quaternary ammonium salt cation flocculation agent are formed, polymeric aluminum consumption 200mg/L, quaternary ammonium salt cation flocculation agent consumption 1.5mg/L, water pH value 5.5～8.5, dissolved-air pressure 0.5Mpa, gas-water ratio is 1: 4～1: 1; All the other are with example 2.
Embodiment 5 usefulness coagulation-air flotation cell replaces coagulation-sedimentation unit
Coagulation-air supporting operating parameter is: 60～95 ℃ of temperature, in the composite flocculation agent that polymeric aluminum and quaternary ammonium salt cation flocculation agent are formed, polymeric aluminum consumption 30mg/L, quaternary ammonium salt cation flocculation agent consumption 0.3mg/L, water pH value 5.5～8.5, dissolved-air pressure 0.2Mpa, gas-water ratio is 1: 4～1: 1; All the other are with example 1.
Embodiment 6 anaerobic acidification unit adopt the two-phase anaerobic acidification, i.e. sulfate reduction acid-producing and product methane reaction two-phase anaerobic acidification (being sulfate reduction acid-producing and the product methane reaction technology of application number 00129461.X); All the other are with example 1.
Embodiment 7 coagulations-before being deposited in, active sludge-little electrolysis after
60～70 ℃ of coagulation-sedimentations, polymeric aluminum 30mg/L, quaternary ammonium salt cation flocculation agent 0.3mg/L;
Active sludge-little electrolysis, pH3.5～4.5, hydraulic detention time 2h, dissolved oxygen 0.5～1.0mg/L, sludge concentration 2g/L, sludge retention time 8d, return sludge ratio 50%;
Anaerobic acidification, pH5.5～6.0, hydraulic detention time 8h, dissolved oxygen 0mg/L, sludge concentration 5g/L;
Anaerobic-aerobic, anoxic section pH6.5～7.0, hydraulic detention time 6h, dissolved oxygen 0mg/L, sludge concentration 2g/L, sludge retention time 15d; Aerobic section pH6.5～7.0, hydraulic detention time 13h, dissolved oxygen 2.0mg/L, sludge concentration 2g/L, sludge retention time 15d;
Can add Powdered Activated Carbon 10mg/L at aerobic section; All the other are with example 1.
Embodiment 8 coagulations-before being deposited in, active sludge-little electrolysis after
70～80 ℃ of coagulation-sedimentations, polymeric aluminum 200mg/L, quaternary ammonium salt cation flocculation agent 1.5mg/L;
Active sludge-little electrolysis is provided with the carbon steel suspension member in the active sludge system, operating parameter is: pH4.5～5.5, hydraulic detention time 4h, dissolved oxygen 1.0～2.0mg/L, sludge concentration 3g/L, sludge retention time 9d, return sludge ratio 200%;
Anaerobic acidification, pH6.0～6.5, hydraulic detention time 25h, dissolved oxygen 0.1mg/L, sludge concentration 10g/L;
Anaerobic-aerobic, anoxic section pH7.0～7.5, hydraulic detention time 10h, dissolved oxygen 0.2mg/L, sludge concentration 3g/L, sludge retention time 30d; Aerobic section pH6.5～7.0, hydraulic detention time 25h, dissolved oxygen 7.0mg/L, sludge concentration 4g/L, sludge retention time 30d; Can add Powdered Activated Carbon 100mg/L at aerobic section; All the other are with example 1.
Embodiment 9 coagulations-before being deposited in, active sludge-little electrolysis after
80～95 ℃ of coagulation-sedimentations, polymeric aluminum 50mg/L, quaternary ammonium salt cation flocculation agent 0.5mg/L;
Active sludge-little electrolysis, pH5.5～6.5, hydraulic detention time 6h, dissolved oxygen 3～4mg/L, sludge concentration 4g/L, sludge retention time 10d, return sludge ratio 50%;
Anaerobic acidification, pH5.5～6.0, hydraulic detention time 20h, dissolved oxygen 0.2mg/L, sludge concentration 10g/L;
Anaerobic-aerobic, anoxic section pH7.0～7.5, hydraulic detention time 7h, dissolved oxygen 0.2mg/L, sludge concentration 3g/L, sludge retention time 20d; Aerobic section pH6.5～7.0, hydraulic detention time 15h, dissolved oxygen 3.0～4.0mg/L, sludge concentration 3g/L, sludge retention time 20d; Can add Powdered Activated Carbon 70mg/L at aerobic section; All the other are with example 1.
Embodiment 10 coagulations-before being deposited in, active sludge-little electrolysis after
80～90 ℃ of coagulation-sedimentations, polymeric aluminum 100mg/L, quaternary ammonium salt cation flocculation agent 0.8mg/L;
Active sludge-little electrolysis, pH7.5～8.5, hydraulic detention time 8h, dissolved oxygen 2～4mg/L, sludge concentration 2.5g/L, sludge retention time 11d, return sludge ratio 100%;
Anaerobic acidification, pH6.0～6.5, hydraulic detention time 15h, dissolved oxygen 0mg/L, sludge concentration 5g/L;
Anaerobic-aerobic, anoxic section pH7.0～7.5, hydraulic detention time 8h, dissolved oxygen 0.1mg/L, sludge concentration 4g/L, sludge retention time 25d; Aerobic section pH7.0～7.5, hydraulic detention time 20h, dissolved oxygen 4.0～5.0mg/L, sludge concentration 4g/L, sludge retention time 30d; All the other are with example 1.
Embodiment 11 coagulations-before being deposited in, active sludge-little electrolysis after
85～95 ℃ of coagulation-sedimentations, polymeric aluminum 80mg/L, quaternary ammonium salt cation flocculation agent 1.1mg/L;
Active sludge-little electrolysis, pH8.0～9.0, hydraulic detention time 10h, dissolved oxygen 5.0～7.0mg/L, sludge concentration 2g/L, sludge retention time 12d, return sludge ratio 150%;
In the anaerobic acidification unit, operating parameter is: pH6.0～6.5, hydraulic detention time 10h, dissolved oxygen 0mg/L, sludge concentration 5g/L;
Anaerobic-aerobic, anoxic section pH6.5～7.0, hydraulic detention time 9h, dissolved oxygen 0mg/L, sludge concentration 4g/L, sludge retention time 30d; Aerobic section pH6.5～7.0, hydraulic detention time 25h, dissolved oxygen 6.0～7.0mg/L, sludge concentration 2.5g/L, sludge retention time 25d; Can add Powdered Activated Carbon 50mg/L at aerobic section; All the other are with example 1.
Embodiment 12 coagulations-before being deposited in, active sludge-little electrolysis after
Coagulation-sedimentation, 80～90 ℃, polymeric aluminum, 150mg/L, quaternary ammonium salt cation flocculation agent, 1.3mg/L;
Active sludge-little electrolysis, pH3.5～5.0, hydraulic detention time 12h, dissolved oxygen 4～5mg/L, sludge concentration 3g/L, sludge retention time 8d, return sludge ratio 200%;
Anaerobic acidification, pH5.5～6.0, hydraulic detention time 18h, dissolved oxygen 0mg/L, sludge concentration 10g/L;
Anaerobic-aerobic, anoxic section pH6.5～7.0, hydraulic detention time 10h, dissolved oxygen 0mg/L, sludge concentration 3g/L, sludge retention time 15d; Aerobic section pH6.5～7.0, hydraulic detention time 25h, dissolved oxygen 5.5～7.0mg/L, sludge concentration 3.5g/L, sludge retention time 20d; Can add Powdered Activated Carbon 90mg/L at aerobic section; All the other are with example 1.
Embodiment 13 coagulations-before being deposited in, active sludge-little electrolysis after
Coagulation-sedimentation, 75～85 ℃, polymeric aluminum 180mg/L, quaternary ammonium salt cation flocculation agent 1.5mg/L;
Active sludge-little electrolysis, pH5～7, hydraulic detention time 16h, dissolved oxygen 5～6mg/L, sludge concentration 3.5g/L, sludge retention time 9d, return sludge ratio 100%;
Anaerobic acidification, pH6.0～6.5, hydraulic detention time 8h, dissolved oxygen 0.2mg/L, sludge concentration 10g/L;
Anaerobic-aerobic, anoxic section pH6.5～7.0, hydraulic detention time 10h, dissolved oxygen 0mg/L, sludge concentration 2g/L, sludge retention time 30d; Aerobic section pH6.5～7.0, hydraulic detention time 22h, dissolved oxygen 2.5～3.5mg/L, sludge concentration 4g/L, sludge retention time 18d; Can add Powdered Activated Carbon 30mg/L at aerobic section; All the other are with example 1.
Embodiment 14 coagulations-before being deposited in, active sludge-little electrolysis after
Coagulation-sedimentation, 60～75 ℃, polymeric aluminum 30mg/L, quaternary ammonium salt cation flocculation agent 0.3mg/L;
Active sludge-little electrolysis, pH6～8, hydraulic detention time 18h, dissolved oxygen 5～7mg/L, sludge concentration 4g/L, sludge retention time 10d, return sludge ratio 50%;
Anaerobic acidification, pH6.0～6.5, hydraulic detention time 8h, dissolved oxygen 0.2mg/L, sludge concentration 10g/L;
Anaerobic-aerobic, anoxic section pH7.0～7.5, hydraulic detention time 8h, dissolved oxygen 0.2mg/L, sludge concentration 3g/L, sludge retention time 25d; Aerobic section pH7.0～7.5, hydraulic detention time 20h, dissolved oxygen 2.0～4.0mg/L, sludge concentration 3g/L, sludge retention time 15d; Can add Powdered Activated Carbon 50mg/L at aerobic section; All the other are with example 1.
Embodiment 15 coagulations-before being deposited in, active sludge-little electrolysis after
85～90 ℃ of coagulation-sedimentations, polymeric aluminum 200mg/L, quaternary ammonium salt cation flocculation agent 1.5mg/L;
Active sludge-little electrolysis, pH6.5～7.5, hydraulic detention time 12h, dissolved oxygen 2～3mg/L, sludge concentration 2.5g/L, sludge retention time 11d, return sludge ratio 150%;
Anaerobic acidification, pH5.5～6.0, hydraulic detention time 8h, dissolved oxygen 0mg/L, sludge concentration 5g/L;
Anaerobic-aerobic, anoxic section pH6.5～7.0, hydraulic detention time 10h, dissolved oxygen 0mg/L, sludge concentration 2.5g/L, sludge retention time 20d; Aerobic section pH7.0～7.5, hydraulic detention time 25h, dissolved oxygen 2.0～4.0mg/L, sludge concentration 2g/L, sludge retention time 15d; All the other are with example 1.
Embodiment 16 coagulations-before being deposited in, active sludge-little electrolysis after
80～95 ℃ of coagulation-sedimentations, polymeric aluminum amount 100mg/L, quaternary ammonium salt cation flocculation agent 0.8mg/L;
Active sludge-little electrolysis, pH7.5～9.0, hydraulic detention time 14h, dissolved oxygen 0.5～2.0mg/L, sludge concentration 3.5g/L, sludge retention time 12d, return sludge ratio 200%;
Anaerobic acidification, pH5.5～6.0, hydraulic detention time 12h, dissolved oxygen 0mg/L, sludge concentration 5g/L;
Anaerobic-aerobic, anoxic section pH6.5～7.0, hydraulic detention time 7h, dissolved oxygen 0.1mg/L, sludge concentration 4g/L, sludge retention time 30d; Aerobic section pH7.0～7.5, hydraulic detention time 13h, dissolved oxygen 4.0～6.0mg/L, sludge concentration 2g/L, sludge retention time 20d; All the other are with example 1.
Embodiment 17 coagulations-before being deposited in, active sludge-little electrolysis after
85～95 ℃ of coagulation-sedimentations, polymeric aluminum 90mg/L, quaternary ammonium salt cation flocculation agent 1.2mg/L;
Active sludge-little electrolysis, pH8～9, hydraulic detention time 7h, dissolved oxygen 0.5～2.0mg/L, sludge concentration 2.5g/L, sludge retention time 8.5d, return sludge ratio 110%;
Anaerobic acidification pH5.5～6.0, hydraulic detention time 25h, dissolved oxygen 0mg/L, sludge concentration 10g/L;
Anaerobic-aerobic, anoxic section pH6.5～7.0, hydraulic detention time 7h, dissolved oxygen 0mg/L, sludge concentration 4g/L, sludge retention time 20d; Aerobic section pH6.5～7.0, hydraulic detention time 13h, dissolved oxygen 4.0～6.0mg/L, sludge concentration 2g/L, sludge retention time 20d; All the other are with example 1.
Embodiment 18 coagulations-before being deposited in, active sludge-little electrolysis after
80～90 ℃ of coagulation-sedimentations, polymeric aluminum 110mg/L, quaternary ammonium salt cation flocculation agent 0.6mg/L;
Active sludge-little electrolysis, pH3.5～4.5, hydraulic detention time 7.5h, dissolved oxygen 2.5～4.0mg/L, sludge concentration 2.5g/L, sludge retention time 9.5d, return sludge ratio 90%;
Anaerobic acidification, pH6.0～6.5, hydraulic detention time 8h, dissolved oxygen 0.2mg/L, sludge concentration 8g/L;
Anaerobic-aerobic, anoxic section pH7.0～7.5, hydraulic detention time 10h, dissolved oxygen 0mg/L, sludge concentration 4g/L, sludge retention time 30d; Aerobic section pH6.5～7.0, hydraulic detention time 25h, dissolved oxygen 5.0～7.0mg/L, sludge concentration 2g/L, sludge retention time 30d; All the other are with example 1.
Embodiment 19 coagulations-before being deposited in, active sludge-little electrolysis after
60～75 ℃ of coagulation-sedimentations, polymeric aluminum 75mg/L, quaternary ammonium salt cation flocculation agent 1.4mg/L;
Active sludge-little electrolysis, pH5.5～6.5, hydraulic detention time 16h, dissolved oxygen 0.5～2.0mg/L, sludge concentration 3.5g/L, sludge retention time 10.5d, return sludge ratio 80%;
Anaerobic acidification pH5.5～6.0, hydraulic detention time 10h, dissolved oxygen 0.2mg/L, sludge concentration 9g/L;
Anaerobic-aerobic, anoxic section pH6.5～7.0, hydraulic detention time 6h, dissolved oxygen 0mg/L, sludge concentration 3g/L, sludge retention time 15d; Aerobic section pH6.5～7.0, hydraulic detention time 13h, dissolved oxygen 6.0～7.0mg/L, sludge concentration 4g/L, sludge retention time 30d; All the other are with example 1.
Embodiment 20 coagulations-before being deposited in, active sludge-little electrolysis after
75～85 ℃ of coagulation-sedimentations, polymeric aluminum 70mg/L, quaternary ammonium salt cation flocculation agent 0.6mg/L;
Active sludge-little electrolysis, pH7.5～9.0, hydraulic detention time 2.5h, dissolved oxygen 2～4mg/L, sludge concentration 2.5g/L, sludge retention time 11.5d, return sludge ratio 70%;
Anaerobic acidification, pH5.5～6.0, hydraulic detention time 18h, dissolved oxygen 0mg/L, sludge concentration 7g/L;
Anaerobic-aerobic, anoxic section pH6.5～7.0, hydraulic detention time 6h, dissolved oxygen 0.5mg/L, sludge concentration 2g/L, sludge retention time 30d; Aerobic section pH6.5～7.0, hydraulic detention time 13h, dissolved oxygen 2.0～4.0mg/L, sludge concentration 4g/L, sludge retention time 30d; All the other are with example 1.
Embodiment 21 active sludge-little electrolysis cells is arranged at (order exchange) before coagulation-sedimentation unit
Active sludge-little electrolysis, pH8.0～9.0, hydraulic detention time 10h, dissolved oxygen 5.0～7.0mg/L, sludge concentration 2g/L, sludge retention time 12d, return sludge ratio 150%;
85～95 ℃ of coagulation-sedimentations, polymeric aluminum 80mg/L, quaternary ammonium salt cation flocculation agent 1.1mg/L;
In the anaerobic acidification unit, operating parameter is: pH6.0～6.5, hydraulic detention time 10h, dissolved oxygen 0mg/L, sludge concentration 5g/L;
Anaerobic-aerobic, anoxic section pH6.5～7.0, hydraulic detention time 9h, dissolved oxygen 0mg/L, sludge concentration 4g/L, sludge retention time 30d; Aerobic section pH6.5～7.0, hydraulic detention time 25h, dissolved oxygen 6.0～7.0mg/L, sludge concentration 2.5g/L, sludge retention time 25d; Can add Powdered Activated Carbon 50mg/L at aerobic section; All the other are with example 2.
Embodiment 22 active sludge-little electrolysis cells is arranged at before coagulation-sedimentation unit
Active sludge-little electrolysis, pH3.5～5.0, hydraulic detention time 12h, dissolved oxygen 4～5mg/L, sludge concentration 3g/L, sludge retention time 8d, return sludge ratio 200%;
Coagulation-sedimentation, 80～90 ℃, polymeric aluminum, 150mg/L, quaternary ammonium salt cation flocculation agent, 1.3mg/L;
Anaerobic acidification, pH5.5～6.0, hydraulic detention time 18h, dissolved oxygen 0mg/L, sludge concentration 10g/L;
Anaerobic-aerobic, anoxic section pH6.5～7.0, hydraulic detention time 10h, dissolved oxygen 0mg/L, sludge concentration 3g/L, sludge retention time 15d; Aerobic section pH6.5～7.0, hydraulic detention time 25h, dissolved oxygen 5.5～7.0mg/L, sludge concentration 3.5g/L, sludge retention time 20d; Can add Powdered Activated Carbon 90mg/L at aerobic section; All the other are with example 2.
Embodiment 23 active sludge-little electrolysis cells is arranged at before coagulation-sedimentation unit
Active sludge-little electrolysis, pH5～7, hydraulic detention time 16h, dissolved oxygen 5～6mg/L, sludge concentration 3.5g/L, sludge retention time 9d, return sludge ratio 100%;
Coagulation-sedimentation, 75～85 ℃, polymeric aluminum 180mg/L, quaternary ammonium salt cation flocculation agent 1.5mg/L;
Anaerobic acidification, pH6.0～6.5, hydraulic detention time 8h, dissolved oxygen 0.2mg/L, sludge concentration 10g/L;
Anaerobic-aerobic, anoxic section pH6.5～7.0, hydraulic detention time 10h, dissolved oxygen 0mg/L, sludge concentration 2g/L, sludge retention time 30d; Aerobic section pH6.5～7.0, hydraulic detention time 22h, dissolved oxygen 2.5～3.5mg/L, sludge concentration 4g/L, sludge retention time 18d; Can add Powdered Activated Carbon 30mg/L at aerobic section; All the other are with example 2.
Embodiment 24 active sludge-little electrolysis cells is arranged at before coagulation-sedimentation unit
Active sludge-little electrolysis, pH6～8, hydraulic detention time 18h, dissolved oxygen 5～7mg/L, sludge concentration 4g/L, sludge retention time 10d, return sludge ratio 50%;
Coagulation-sedimentation, 60～75 ℃, polymeric aluminum 30mg/L, quaternary ammonium salt cation flocculation agent 0.3mg/L;
Anaerobic acidification, pH6.0～6.5, hydraulic detention time 8h, dissolved oxygen 0.2mg/L, sludge concentration 10g/L;
Anaerobic-aerobic, anoxic section pH7.0～7.5, hydraulic detention time 8h, dissolved oxygen 0.2mg/L, sludge concentration 3g/L, sludge retention time 25d; Aerobic section pH7.0～7.5, hydraulic detention time 20h, dissolved oxygen 2.0～4.0mg/L, sludge concentration 3g/L, sludge retention time 15d; Can add Powdered Activated Carbon 50mg/L at aerobic section; All the other are with example 2.
Embodiment 25 active sludge-little electrolysis cells is arranged at before coagulation-sedimentation unit
Active sludge-little electrolysis, pH6.5～7.5, hydraulic detention time 12h, dissolved oxygen 2～3mg/L, sludge concentration 2.5g/L, sludge retention time 11d, return sludge ratio 150%;
85～90 ℃ of coagulation-sedimentations, polymeric aluminum 200mg/L, quaternary ammonium salt cation flocculation agent 1.5mg/L;
Anaerobic acidification, pH5.5～6.0, hydraulic detention time 8h, dissolved oxygen 0mg/L, sludge concentration 5g/L;
Anaerobic-aerobic, anoxic section pH6.5～7.0, hydraulic detention time 10h, dissolved oxygen 0mg/L, sludge concentration 2.5g/L, sludge retention time 20d; Aerobic section pH7.0～7.5, hydraulic detention time 25h, dissolved oxygen 2.0～4.0mg/L, sludge concentration 2g/L, sludge retention time 15d; All the other are with example 1.
Embodiment 26 active sludge-little electrolysis cells is arranged at before coagulation-sedimentation unit
Active sludge-little electrolysis, pH7.5～9.0, hydraulic detention time 14h, dissolved oxygen 0.5～2.0mg/L, sludge concentration 3.5g/L, sludge retention time 12d, return sludge ratio 200%;
80～95 ℃ of coagulation-sedimentations, polymeric aluminum amount 100mg/L, quaternary ammonium salt cation flocculation agent 0.8mg/L;
Anaerobic acidification, pH5.5～6.0, hydraulic detention time 12h, dissolved oxygen 0mg/L, sludge concentration 5g/L;
Anaerobic-aerobic, anoxic section pH6.5～7.0, hydraulic detention time 7h, dissolved oxygen 0.1mg/L, sludge concentration 4g/L, sludge retention time 30d; Aerobic section pH7.0～7.5, hydraulic detention time 13h, dissolved oxygen 4.0～6.0mg/L, sludge concentration 2g/L, sludge retention time 20d; All the other are with example 2.
Embodiment 27 active sludge-little electrolysis cells is arranged at before coagulation-sedimentation unit
Active sludge-little electrolysis, pH8～9, hydraulic detention time 7h, dissolved oxygen 0.5～2.0mg/L, sludge concentration 2.5g/L, sludge retention time 8.5d, return sludge ratio 110%;
85～95 ℃ of coagulation-sedimentations, polymeric aluminum 90mg/L, quaternary ammonium salt cation flocculation agent 1.2mg/L;
Anaerobic acidification pH5.5～6.0, hydraulic detention time 25h, dissolved oxygen 0mg/L, sludge concentration 10g/L;
Anaerobic-aerobic, anoxic section pH6.5～7.0, hydraulic detention time 7h, dissolved oxygen 0mg/L, sludge concentration 4g/L, sludge retention time 20d; Aerobic section pH6.5～7.0, hydraulic detention time 13h, dissolved oxygen 4.0～6.0mg/L, sludge concentration 2g/L, sludge retention time 20d; All the other are with example 2.
Embodiment 28 active sludge-little electrolysis cells is arranged at before coagulation-sedimentation unit
Active sludge-little electrolysis, pH3.5～4.5, hydraulic detention time 7.5h, dissolved oxygen 2.5～4.0mg/L, sludge concentration 2.5g/L, sludge retention time 9.5d, return sludge ratio 90%;
80～90 ℃ of coagulation-sedimentations, polymeric aluminum 110mg/L, quaternary ammonium salt cation flocculation agent 0.6mg/L;
Anaerobic acidification, pH6.0～6.5, hydraulic detention time 8h, dissolved oxygen 0.2mg/L, sludge concentration 8g/L;
Anaerobic-aerobic, anoxic section pH7.0～7.5, hydraulic detention time 10h, dissolved oxygen 0mg/L, sludge concentration 4g/L, sludge retention time 30d; Aerobic section pH6.5～7.0, hydraulic detention time 25h, dissolved oxygen 5.0～7.0mg/L, sludge concentration 2g/L, sludge retention time 30d; All the other are with example 2.
Embodiment 29 active sludge-little electrolysis cells is arranged at before coagulation-sedimentation unit
Active sludge-little electrolysis, pH5.5～6.5, hydraulic detention time 16h, dissolved oxygen 0.5～2.0mg/L, sludge concentration 3.5g/L, sludge retention time 10.5d, return sludge ratio 80%;
60～75 ℃ of coagulation-sedimentations, polymeric aluminum 75mg/L, quaternary ammonium salt cation flocculation agent 1.4mg/L;
Anaerobic acidification pH5.5～6.0, hydraulic detention time 10h, dissolved oxygen 0.2mg/L, sludge concentration 9g/L;
Anaerobic-aerobic, anoxic section pH6.5～7.0, hydraulic detention time 6h, dissolved oxygen 0mg/L, sludge concentration 3g/L, sludge retention time 15d; Aerobic section pH6.5～7.0, hydraulic detention time 13h, dissolved oxygen 6.0～7.0mg/L, sludge concentration 4g/L, sludge retention time 30d; All the other are with example 2.
Embodiment 30 active sludge-little electrolysis cells is arranged at before coagulation-sedimentation unit
Active sludge-little electrolysis, pH7.5～9.0, hydraulic detention time 2.5h, dissolved oxygen 2～4mg/L, sludge concentration 2.5g/L, sludge retention time 11.5d, return sludge ratio 70%;
75～85 ℃ of coagulation-sedimentations, polymeric aluminum 70mg/L, quaternary ammonium salt cation flocculation agent 0.6mg/L;
Anaerobic acidification, pH5.5～6.0, hydraulic detention time 18h, dissolved oxygen 0mg/L, sludge concentration 7g/L;
Anaerobic-aerobic, anoxic section pH6.5～7.0, hydraulic detention time 6h, dissolved oxygen 0.5mg/L, sludge concentration 2g/L, sludge retention time 30d; Aerobic section pH6.5～7.0, hydraulic detention time 13h, dissolved oxygen 2.0～4.0mg/L, sludge concentration 4g/L, sludge retention time 30d; All the other are with example 2.
Claims (10)
1. the treatment process of an acrylic fibers waste water by dry process is characterized in that this technical process comprises coagulation-sedimentation unit, active sludge-little electrolysis cells, anaerobic acidification unit and the anaerobic-aerobic unit of combination successively;
After dry acrylic fiber processing wastewater, acid-bearing wastewater and ground wash-down water mix, enter suspended substance and colloidalmaterial in coagulation-sedimentation unit removal waste water behind the adjusting pH; Coagulation-settled supernatant liquor enters equalizing tank and regulates the water quality and the water yield by cooling, enter active sludge-little electrolysis cells then, carry out electrolytic reaction and simultaneously provide oxygen, make that microorganism is easier in the mud decomposes the organism in the system, reduce waste water COD to active sludge; Enter chemical structure and biodegradability that the anaerobic acidification unit changes hardly degraded organic substance subsequently; At last, introduce sanitary sewage in the anoxic section, improve the removal effect of biological denitrification process to recalcitrant substance EDTA and sodium salt thereof, waste water reaches the industry emission standard after Anoxybiotic-aerobic biologic denitrogenation operation is handled.
2. according to the treatment process of the described acrylic fibers waste water by dry process of claim 1, it is characterized in that in described coagulation-sedimentation unit, operating parameter is: 60～95 ℃ of temperature, in the composite flocculation agent that polymeric aluminum and quaternary ammonium salt cation flocculation agent are formed, polymeric aluminum consumption 30～200mg/L, quaternary ammonium salt cation flocculation agent consumption is 0.3～1.5mg/L.
3. according to the treatment process of the described acrylic fibers waste water by dry process of claim 1, it is characterized in that in described active sludge-little electrolysis cells, the carbon steel suspension member is set in the active sludge system, operating parameter is: pH3.5～9.0, hydraulic detention time 2～18h, dissolved oxygen 0.5～7.0mg/L, sludge concentration 2～4g/L, sludge retention time 8～12d, return sludge ratio 50%～200%.
4. according to the treatment process of the described acrylic fibers waste water by dry process of claim 1, it is characterized in that operating parameter is in the described anaerobic acidification unit: pH5.5～6.5, hydraulic detention time 8～25h, dissolved oxygen 0～0.2mg/L, sludge concentration 5～10g/L.
5. according to the treatment process of the described acrylic fibers waste water by dry process of claim 1, it is characterized in that operating parameter is in the described anaerobic-aerobic unit: anoxic section pH6.5～7.5, hydraulic detention time 6～10h, dissolved oxygen 0～0.5mg/L, sludge concentration 2～4g/L, sludge retention time 15～30d; Aerobic section pH6.5～7.5, hydraulic detention time 13～25h, dissolved oxygen 2.0～7.0mg/L, sludge concentration 2～4g/L, sludge retention time 15～30d.
6. according to the treatment process of the described acrylic fibers waste water by dry process of claim 1, it is characterized in that available coagulation-air flotation cell replaces coagulation-sedimentation unit, coagulation-air supporting operating parameter is: 60～95 ℃ of temperature, in the composite flocculation agent that polymeric aluminum and quaternary ammonium salt cation flocculation agent are formed, polymeric aluminum consumption 30～200mg/L, quaternary ammonium salt cation flocculation agent consumption 0.3～1.5mg/L, water pH value 5.5～8.5, dissolved-air pressure 0.2～0.5Mpa, gas-water ratio is 1: 4～1: 1.
7. according to the treatment process of the described acrylic fibers waste water by dry process of claim 1, it is characterized in that described coagulation-sedimentation unit and active sludge-little electrolysis cells order can exchange.
8. according to the treatment process of the described acrylic fibers waste water by dry process of claim 1, it is characterized in that also two-phase anaerobic acidification of described anaerobic acidification, i.e. sulfate reduction acid-producing and produce methane reaction two-phase anaerobic acidification.
9. according to the treatment process of the described acrylic fibers waste water by dry process of claim 1, it is characterized in that to add Powdered Activated Carbon 10～100mg/L at aerobic section in the described anaerobic-aerobic unit preferred gac dosage 50mg/L.
10. according to the treatment process of the described acrylic fibers waste water by dry process of claim 1, it is characterized in that original acrylic fibers waste water by dry process COD1500 ± 300mg/L, BOD 450 ± 100mg/L, ammonia nitrogen 45 ± 20mg/L, turbidity 50 ± 30mg/L, pH6.3 ± 1,65 ± 30 ℃ of temperature, EDTA 180 ± 80mg/L, sulfate radical 320 ± 150mg/L, inferior sulfate radical is 580 ± 300mg/L, handles COD 50～160mg/L, NH
3-N is less than the acrylic fiber industry national grade one discharge standard of 15mg/L.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02135650 CN1210214C (en) | 2002-10-22 | 2002-10-22 | Treatment technology for acrylic fibers waste water by dry process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02135650 CN1210214C (en) | 2002-10-22 | 2002-10-22 | Treatment technology for acrylic fibers waste water by dry process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1413928A true CN1413928A (en) | 2003-04-30 |
| CN1210214C CN1210214C (en) | 2005-07-13 |
Family
ID=4748294
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 02135650 Expired - Fee Related CN1210214C (en) | 2002-10-22 | 2002-10-22 | Treatment technology for acrylic fibers waste water by dry process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1210214C (en) |
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100404441C (en) * | 2006-08-23 | 2008-07-23 | 重庆紫光化工股份有限公司 | Treatment method of high concentration undegradable nitrile containing organic waste water |
| CN101798160A (en) * | 2010-04-07 | 2010-08-11 | 东南大学 | Treatment device and pretreatment method of wastewater generated by producing acrylic fibers by using dry method |
| CN1994924B (en) * | 2006-12-05 | 2011-05-25 | 南开大学 | Printing and dyeing waste water deodorization biochemical processing method |
| CN102295389A (en) * | 2011-08-03 | 2011-12-28 | 句容宁武新材料发展有限公司 | Industrial waste water treating technology |
| CN101423312B (en) * | 2007-10-31 | 2012-05-30 | 中国石油化工股份有限公司 | Acrylon production waste water treatment method |
| CN102633402A (en) * | 2011-04-07 | 2012-08-15 | 上海问鼎水处理工程有限公司 | Method for treating chitin waste water |
| CN103359897A (en) * | 2013-08-07 | 2013-10-23 | 山东太平洋环保有限公司 | Process and device for treating high-concentration sulfate radical textile-dyeing wastewater |
| CN104961303A (en) * | 2015-07-10 | 2015-10-07 | 青岛小川环保设备有限公司 | Pump-free integrated wastewater deep treatment equipment |
| CN105461156A (en) * | 2014-09-03 | 2016-04-06 | 中国石油化工股份有限公司 | Treatment method for nitrile rubber production wastewater |
| CN105481205A (en) * | 2016-01-29 | 2016-04-13 | 杭州萧索环保科技有限公司 | Printing and dyeing wastewater treatment process |
| CN106830352A (en) * | 2017-01-16 | 2017-06-13 | 广州市广深环保科技有限公司 | A kind of multifunctional and composite type microbial bacteria group sewage treatment process |
| CN111470724A (en) * | 2020-04-20 | 2020-07-31 | 杭州师范大学钱江学院 | Deep purification treatment method for spandex industrial production wastewater |
-
2002
- 2002-10-22 CN CN 02135650 patent/CN1210214C/en not_active Expired - Fee Related
Cited By (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100404441C (en) * | 2006-08-23 | 2008-07-23 | 重庆紫光化工股份有限公司 | Treatment method of high concentration undegradable nitrile containing organic waste water |
| CN1994924B (en) * | 2006-12-05 | 2011-05-25 | 南开大学 | Printing and dyeing waste water deodorization biochemical processing method |
| CN101423312B (en) * | 2007-10-31 | 2012-05-30 | 中国石油化工股份有限公司 | Acrylon production waste water treatment method |
| CN101798160A (en) * | 2010-04-07 | 2010-08-11 | 东南大学 | Treatment device and pretreatment method of wastewater generated by producing acrylic fibers by using dry method |
| CN102633402A (en) * | 2011-04-07 | 2012-08-15 | 上海问鼎水处理工程有限公司 | Method for treating chitin waste water |
| CN102295389A (en) * | 2011-08-03 | 2011-12-28 | 句容宁武新材料发展有限公司 | Industrial waste water treating technology |
| CN102295389B (en) * | 2011-08-03 | 2012-10-10 | 句容宁武新材料发展有限公司 | Industrial waste water treating technology |
| CN103359897B (en) * | 2013-08-07 | 2014-12-24 | 山东太平洋环保有限公司 | Process and device for treating high-concentration sulfate radical textile-dyeing wastewater |
| CN103359897A (en) * | 2013-08-07 | 2013-10-23 | 山东太平洋环保有限公司 | Process and device for treating high-concentration sulfate radical textile-dyeing wastewater |
| CN105461156A (en) * | 2014-09-03 | 2016-04-06 | 中国石油化工股份有限公司 | Treatment method for nitrile rubber production wastewater |
| CN105461156B (en) * | 2014-09-03 | 2018-01-23 | 中国石油化工股份有限公司 | A kind of processing method of nitrile rubber production waste water |
| CN104961303A (en) * | 2015-07-10 | 2015-10-07 | 青岛小川环保设备有限公司 | Pump-free integrated wastewater deep treatment equipment |
| CN104961303B (en) * | 2015-07-10 | 2016-10-26 | 青岛小川环保设备有限公司 | Non-pump type degree of depth integrated equipment for sewage treatment |
| CN105481205A (en) * | 2016-01-29 | 2016-04-13 | 杭州萧索环保科技有限公司 | Printing and dyeing wastewater treatment process |
| CN105481205B (en) * | 2016-01-29 | 2018-01-09 | 杭州萧索环保科技有限公司 | A kind of printing-dyeing waste water treatment process |
| CN106830352A (en) * | 2017-01-16 | 2017-06-13 | 广州市广深环保科技有限公司 | A kind of multifunctional and composite type microbial bacteria group sewage treatment process |
| CN111470724A (en) * | 2020-04-20 | 2020-07-31 | 杭州师范大学钱江学院 | Deep purification treatment method for spandex industrial production wastewater |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1210214C (en) | 2005-07-13 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1668539A (en) | Method and facility for treatment of sludge derived from biological water purification facilities | |
| CN105417687B (en) | The method and apparatus of sewage and bed mud in a kind of Combined Treatment black-odor riverway | |
| CN1210214C (en) | Treatment technology for acrylic fibers waste water by dry process | |
| CN106430565B (en) | It is a kind of directly converted based on carbon source, the sewage low consumption processing of nitrogen biological eliminating and energy recovery combined treatment process | |
| CN103936225B (en) | The method of catalyzed internal electrocatalysis coupling two-stage biofilter advanced treatment on coking wastewater | |
| CN1778714A (en) | Adjusting method for A/O biological denitrification reactor and nitrification process, its on-line fuzzy controller and control thereof | |
| CN106277555B (en) | High-efficiency low-cost treatment method and system for coking wastewater | |
| CN101525207A (en) | Integrated pre-denitrification and denitrogenation biological filter sewerage treatment process | |
| CN1887740A (en) | Short-path deep biological denitrogenation method for city garbage percolate | |
| CN106673192A (en) | Technology for removing total nitrogen in garbage leachate by anammox and special device thereof | |
| CN1907889A (en) | Apparatus and method of treating city domestic refuse percolation liquid by two-stage UASB+A/O technique | |
| CN101935136A (en) | Zero energy consumption low sludge yield municipal sewage dephosphorization and denitrification treatment method | |
| CN110217949A (en) | A kind of process for treating high ammonia nitrogen waste water | |
| CN1164513C (en) | Method for treating acrylonitrile and acrylic waste water | |
| CN100345771C (en) | Process of micro electrolysis pretreating PTA waste water | |
| CN1067227A (en) | Gas dissolving and releasing liquid treatment system | |
| CN101823814A (en) | Method and system of integrated denitrifying phosphorus and nitrogen removal | |
| CN101781056B (en) | Treatment method of waste papermaking water | |
| CN1688513A (en) | Method and apparatus for treating organic waste | |
| CN109867352B (en) | Method for realizing autotrophic deep denitrification of nitrogen-containing wastewater by utilizing anaerobic MBR (membrane bioreactor) | |
| CN1562808A (en) | Biological denitrification technique for waste water of bean products and fuzzy control device and method | |
| CN101050020A (en) | Method for treating wastewater by technique of sludge decrement type biomembrane piled ball packing | |
| CN1488584A (en) | Method for treaing uaste water containing aminopolycanboxylic acid | |
| CN1188743A (en) | Comprehensive effluent disposal technology for wet spinning acrylic fibers industry | |
| CN206486350U (en) | Full biological denitrificaion and mud decrement system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |