CN102515433A - Synthetic rubber wastewater treatment process - Google Patents
Synthetic rubber wastewater treatment process Download PDFInfo
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- CN102515433A CN102515433A CN201110418681XA CN201110418681A CN102515433A CN 102515433 A CN102515433 A CN 102515433A CN 201110418681X A CN201110418681X A CN 201110418681XA CN 201110418681 A CN201110418681 A CN 201110418681A CN 102515433 A CN102515433 A CN 102515433A
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Abstract
The invention relates to a synthetic rubber wastewater treatment process, belonging to the field of chemical wastewater treatment. The process comprises the following steps: firstly introducing rubber wastewater to a pre-settling tank for homogenizing and settling, conveying to an adjusting tank through a pipeline, lifting the wastewater treated by the adjusting tank to a floatation tank, then entering a cavitation air floatation machine to remove suspended particles and colloid substances from wastewater, lifting to a high-efficacy dissolved air floatation machine by a pump, then introducing to a biochemical treatment system, discharging to an anoxic/aerobic oxidation tank, then introducing to a secondary settling tank, settling, introducing the supernatant to a catalytic oxidation unit water collecting tank, then entering a catalytic oxidation reactor by a pipeline, entering reacted wastewater into an oxidation flocculating tank, and finally entering a third settling tank for settling and then discharging. According to the invention, a floatation unit is arranged as follows: a first-stage floatation system adopts the cavitation air floatation machine and the second-stage floatation system adopts the high-efficacy dissolved air floatation machine, thus the gumming problem of a dissolved air tank can be effectively avoided and the floatation treatment effect is simultaneously guaranteed.
Description
Technical field
The present invention relates to a kind of viton sewage treatment process, belong to the chemical engineering sewage process field.
Background technology
Along with the sustainable growth of home market viton demand, built in China becomes many cover rubber production devices.Because of the rubber quantity of wastewater effluent is big, organic pollutant content is high, generally need supporting independently Sewage treatment systems.Because of adding multiple auxiliary chemicals in the rubber production technology, in polyreaction, produce a large amount of different molecular weight low-grade polymers again simultaneously, these chemical pollutants belong to the bio-refractory material mostly, cause rubber WWT difficulty up to standard big.The rubber production device according to production technique, to produce product different, institute's sewer water quality has bigger difference, and is wherein bigger with styrene-butadiene rubber(SBR), paracril WWT difficulty.
The domestic rubber Sewage treatment systems of having built up adopts " air supporting-bio-oxidation " treatment process basically at present, and water outlet CODcr is 120-150mg/L basically.In recent years, control puts more effort to the petrochemical enterprise total amount of pollutants discharged along with country, and chemical enterprise sewage drainage standard is strict further, and conventional rubber sewage treatment process can not satisfy existing sewage qualified discharge standard.For example, though Shandong rubber plant of branch office sewage-farm through repeatedly technological transformation, its effluent quality still far can not reach " integrated wastewater discharge standard " (GB8978-1996) requirement of petrochemical complex industry first discharge standard CODcr≤60mg/L.
Summary of the invention
According to the deficiency of prior art, the technical problem that the present invention will solve is: a kind of viton sewage treatment process is provided, makes elastomeric sewage discharge meet discharging standards, avoid the pollution of environment.
The technical solution adopted for the present invention to solve the technical problems is: a kind of viton sewage treatment process is provided, and its characteristic may further comprise the steps: rubber sewage at first gets into preliminary sedimentation tank and spares the matter deposition, and sewage is delivered to equalizing tank through post precipitation through pipeline; Sewage after equalizing tank is regulated is promoted to through pipeline in the reaction coagulation tank in the air-flotation system, in the reaction coagulation tank, adds Poly aluminum Chloride (PAC) (PAC) and SEPIGEL 305 (PAM), gets into air flotation turbo then; In air flotation turbo, remove suspended particle and colloidalmaterial in the sewage, promote through pump then and send into efficient air-dissolving air-float machine, sewage gets into the hydrolysis acidification pool of biochemical treatment system again; Under the effect of acidication bacterium, with macromolecular substance in the sewage, be difficult to biodegradable material and be converted into and be easy to biodegradable small-molecule substance, sewage is discharged entering anoxic/aerobic oxidation pond, back through hydrolysis acidification pool; Biological degradation through mikrobe is removed organic pollutant in the sewage; Effluent stream is to second pond then, flow to the catalytic oxidation unit water collecting basin through the supernatant of post precipitation, gets into catalyst oxidation reactor through pipeline again; At first in catalyst oxidation reactor, add SEPIGEL 305; And in catalyst oxidation reactor, add ferrous sulfate and ydrogen peroxide 50 reagent, produce the extremely strong hydroxyl radical free radical of oxidation capacity, with the most of oxidation removal of organic pollutant in the sewage; Reacted sewage gets into the oxidizing, flocculating pond; Add the further oxidation of oxygenant, add flocculation agent behind the complete oxidation, make reacted tiny alumen ustum further collide, flocculate; Enter into three heavy ponds at last and precipitate, but the water outlet qualified discharge.
Described preliminary sedimentation tank front end is provided with the flocculation agitated pool.
The pH value of described sewage after equalizing tank is regulated is 6.5～8.0, and sewage is homogeneous 12-24h in equalizing tank.
The add-on of described Poly aluminum Chloride (PAC) is 20～100mg/L, and the add-on of SEPIGEL 305 is 1～5mg/L.
Be in series with efficient air-dissolving air-float machine behind the described air flotation turbo.
Described sewage stops 8～12h in hydrolysis acidification pool, stop 6～12h at the anoxic oxidation pond, stops 24～36h in the aerobic oxidation pond.
Described second pond surface load is 0.5～1.65m
3/ m
2.h.
The input amount of described ydrogen peroxide 50 (massfraction is 30%) is 0.1～0.4mg/L, and the input amount of ferrous sulfate is 50～200mg/L, and the add-on of SEPIGEL 305 is 1～2mg/L, and oxidation time is 5～10min.
The described flocculation reaction time is 20-40min.
Described three heavy pool surface loads are 0.5～1.65m
3/ m
2.h.
Mud in the preliminary sedimentation tank is connected to sludge sump through the mud pipeline simultaneously; Sludge sump connects sludge thickener; Second pond then directly is connected sludge thickener through the mud pipeline with three heavy ponds; Air flotation turbo in the air flotation cell also is connected the scum silica frost pond through the mud pipeline with efficient air-dissolving air-float machine simultaneously, and the scum silica frost pond connects sludge thickener through pipeline, and sludge thickener connects sludge dewatering system through pipeline.Second pond also connects mud backflow well through pipeline in addition, and mud backflow well is back to hydrolysis acidification pool and anoxic oxidation pond through pipe section, and the aerobic oxidation pond connects the anoxic oxidation pond through the mud pipeline.
The invention has the beneficial effects as follows:
(1) use at present comparatively widely that air-floating apparatus mainly contains cavitation air flotation system and air-dissolving air-float system, the cavitation air flotation system has and characteristics such as is difficult for stopping up, operational management is convenient; Air-dissolving air-float system to suspended substance in the sewage, colloidal type pollutant removal treatment effect is good but it is high that sewage quality is required, and contains a large amount of colloidal type materials in the rubber sewage, is easy to that polymerization causes its normal operation of congestion affects in dissolving.Technology of the present invention is arranged to the two-stage air-flotation system with air flotation cell, and the one-level air-flotation system adopts air flotation turbo, and the secondary air-floatation system adopts efficient air-dissolving air-float machine, can effectively avoid dissolving gum deposit problem, has guaranteed the air supporting treatment effect simultaneously.
(2) hydrolysis acidification pool of the present invention adopts the upflow sludge blanket form, and in the pond upper suspension semi soft packing, can effectively prevent the loss of mud when increasing the muddy water mixed effect.The follow-up biological oxidizing process of hydrolysis acidification pool adopts conventional anoxic/aerobic (A/O) biological treatment, and A/O technology not only can obtain satisfied denitrification effect, and through the anaerobic-aerobic cyclical operation, can obtain higher COD and BOD clearance equally.
(3) catalyzed oxidation process using Fenton reagent oxidation of the present invention, H
2O
2At Fe
2+Katalysis decompose down and produce the hydroxyl radical free radical (OH) that high reaction activity is arranged, oxidation operation being resolved into small molecules even make micromolecular oxidation operation through approach such as transfer transports then is water and CO
2, indivedual direct mineralisings of organism.Simultaneously, Fe
2+Be oxidized to Fe
3+Produce coagulating sedimentation, remove large amount of organic, so Fenton reagent is that current collection chemical coagulation, chemical catalytic oxidation and materialization flocculation sediment are in the treatment process of one.The present invention adopts the neutral Fenton method of improvement, through the optimal drug binding site that control adds dose and in catalyst oxidation reactor, forms, uses minimum dose to reach best removal effect.Because need not regulate pH by preceding acid back alkali, so working cost reduces greatly, operation moves simpler and more direct, and last effect is better.
Description of drawings
Fig. 1 is a process flow diagram of the present invention;
1 is preliminary sedimentation tank among the figure; 2 is equalizing tank; 3 is air flotation turbo; 4 is efficient air-dissolving air-float machine; 5 is hydrolysis acidification pool; 6 is the anoxic oxidation pond; 7 is the aerobic oxidation pond; 8 is second pond; 9 is water collecting basin; 10 is catalyst oxidation reactor; 11 is the oxidizing, flocculating pond; 12 is three heavy ponds; 13 is sludge sump; 14 is sludge thickener; 15 is the scum silica frost pond; 16 is sludge dewatering system; 17 is mud backflow well.
Embodiment
Below in conjunction with accompanying drawing and embodiment the present invention is further specified.
The present invention is applied to 100,000 tons of/year butadiene product equipment Sewage treatment systemss of Zibo Qixiang Tengda Chemical Industry Co., Ltd.This device sewage effluent mainly comprises butylbenzene sewage, butyl rubber sewage, butadiene product equipment sewage, fitting room sewage, the suitable fourth device sewage of rare earth etc.The sewage-farm treatment scale is 520m
3/ h.The sewage-farm influent quality is CODcr:900mg/L, NH
3-N:40mg/L, SS:150mg/L.Treatment process is to be the treatment process of core with " pre-treatment+bio-oxidation+catalyzed oxidation ", and it is four processing units that whole process flow is divided into, and is respectively pretreatment unit, biochemical treatment unit, catalytic oxidation treatment unit and sludge treatment unit.Each cell process process description and main control parameters are following.
(1) pretreatment unit
Production equipment institute sewage effluent at first gets into preliminary sedimentation tank and spares the matter deposition, agitated pool is set and is equipped with soda acid dosing system control sewage pH value in the 6.5-8.0 scope at the preliminary sedimentation tank front end.From flowing to equalizing tank, hydraulic detention time is 24 hours to sewage through post precipitation.Sewage behind the homogeneous 12h is from flowing to the reaction coagulation tank in the cavitation air flotation system; In the reaction coagulation tank, add PAC and PAM; The PAC dosage is 20-50mg/L, and the PAM dosage is 1-3mg/L, is promoted to efficient air-dissolving air-float machine through pump then; SS in the sewage is further purified, and the sewage after the purification is from flowing to the biochemical treatment unit.
(2) biochemical treatment unit
From flowing to the unitary hydrolysis acidification pool of biochemical treatment, sewage with macromolecular substance, be difficult to biodegradable material and be converted into and be easy to biodegradable small-molecule substance, thereby improves the biodegradability of sewage under the effect of acidication bacterium through pretreated sewage.The hydrolysis acidification pool water outlet is from flowing to A/O (anoxic/aerobic oxidation pond) treatment system, and the A/O oxidation pond mainly is COD and NH in the degradation of sewage
3-N.Control mud 25-30d in age, dissolved oxygen 1-4mg/L, water temperature 30-35 ℃ of whole biochemical system, MLSS2.5-3.0g/1, pH7.2-7.8; Organism in the sewage obtains oxidative degradation at this element; The aeration tank water outlet is from flowing to second pond; Can be controlled in below the 105mg/l through the supernatant C OD of post precipitation, ammonia nitrogen is controlled at below the 15mg/l.Sewage after biochemical cell processing is from flowing to advanced treatment unit.
(3) catalytic oxidation treatment unit
The water outlet of biochemical treatment unit gets into the buffering pond and gets into catalyst oxidation reactor after sewage promotes water pump pumps with tangential way.Add coagulating agent PAM simultaneously; Dosage is 1-3mg/L; Coagulating agent in having the catalyst oxidation reactor of larger ratio of height to diameter very with the mode and the water thorough mixing of eddy flow; Electrochemical reaction takes place simultaneously, and the sewage that has coagulating agent can contact with fenton reagent in the middle and upper part of catalyst oxidation reactor oxidizing reaction takes place, and Fenton reagent dosage is H
2O
2(30%) dosage is 0.1-0.4mL/L, FeSO
4Dosage is 50-200mg/L.Reacted sewage gravity flow enters into the oxidizing, flocculating pond; Reaction times is 20-30min, utilizes the further oxidation of oxygenant, finally reaches complete oxidation; Through adding flocculation agent; Make reacted tiny alumen ustum further collide, flocculate, then enter into three heavy ponds and precipitate, but the water outlet qualified discharge.
The invention effect
Zibo Qixiang Tengda Chemical Industry Co., Ltd sewage-farm final treat effluent index CODcr:40-50mg/L, NH
3-N:5-10mg/L, SS:5-20mg/L reach " integrated wastewater discharge standard " (GB8978-1996) petrochemical complex industry first discharge standard.
Claims (10)
1. viton sewage treatment process, its characteristic may further comprise the steps: rubber sewage at first gets into preliminary sedimentation tank and spares the matter deposition, and sewage is delivered to equalizing tank through post precipitation through pipeline; Sewage after equalizing tank is regulated is promoted to through pipeline in the reaction coagulation tank in the air-flotation system, in the reaction coagulation tank, adds Poly aluminum Chloride (PAC) and SEPIGEL 305, gets into air flotation turbo then; In air flotation turbo, remove suspended particle and colloidalmaterial in the sewage, promote through pump then and send into efficient air-dissolving air-float machine, sewage gets into the hydrolysis acidification pool of biochemical treatment system again; Under the effect of acidication bacterium, with macromolecular substance in the sewage, be difficult to biodegradable material and be converted into and be easy to biodegradable small-molecule substance, sewage is discharged entering anoxic/aerobic oxidation pond, back through hydrolysis acidification pool; Biological degradation through mikrobe is removed organic pollutant in the sewage, and effluent stream is to second pond then, flow to the catalytic oxidation unit water collecting basin through the supernatant of post precipitation; Get into catalyst oxidation reactor through pipeline again, at first in catalyst oxidation reactor, add SEPIGEL 305, and in catalyst oxidation reactor, add ferrous sulfate and ydrogen peroxide 50 reagent; Produce the extremely strong hydroxyl radical free radical of oxidation capacity; With the most of oxidation removal of organic pollutant in the sewage, reacted sewage gets into the oxidizing, flocculating pond, adds the further oxidation of oxygenant; Add flocculation agent behind the complete oxidation; Make reacted tiny alumen ustum further collide, flocculate, enter into three heavy ponds at last and precipitate, but the water outlet qualified discharge.
2. viton sewage treatment process according to claim 1 is characterized in that described preliminary sedimentation tank front end is provided with the flocculation agitated pool.
3. viton sewage treatment process according to claim 1 is characterized in that the pH value of described sewage after equalizing tank is regulated is 6.5～8.0, and sewage is homogeneous 12-24h in equalizing tank.
4. viton sewage treatment process according to claim 1, the add-on that it is characterized in that described Poly aluminum Chloride (PAC) is 20～100mg/L, the add-on of SEPIGEL 305 is 1～5mg/L.
5. viton sewage treatment process according to claim 1 is characterized in that being in series with efficient air-dissolving air-float machine behind the described air flotation turbo.
6. viton sewage treatment process according to claim 1 is characterized in that described sewage stops 8～12h in hydrolysis acidification pool, stops 6～12h at the anoxic oxidation pond, stops 24～36h in the aerobic oxidation pond.
7. viton sewage treatment process according to claim 1 is characterized in that described second pond surface load is 0.5～1.65m
3/ m
2.h.
8. viton sewage treatment process according to claim 1; The input amount that it is characterized in that described ydrogen peroxide 50 is 0.1～0.4mg/L; The input amount of ferrous sulfate is 50～200mg/L, and the add-on of SEPIGEL 305 is 1～2mg/L, and oxidation time is 5～10min.
9. viton sewage treatment process according to claim 1 is characterized in that the described flocculation reaction time is 20-40min.
10. viton sewage treatment process according to claim 1 is characterized in that described three heavy pool surface loads are 0.5～1.65m
3/ m
2.h.
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| CN201110418681XA CN102515433A (en) | 2011-12-14 | 2011-12-14 | Synthetic rubber wastewater treatment process |
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|---|---|---|---|
| CN201110418681XA CN102515433A (en) | 2011-12-14 | 2011-12-14 | Synthetic rubber wastewater treatment process |
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103723883A (en) * | 2013-11-13 | 2014-04-16 | 安徽淮化股份有限公司 | Treatment method of synthetic rubber production waste water |
| CN104710077A (en) * | 2015-03-06 | 2015-06-17 | 天津市联合环保工程设计有限公司 | Treatment system and treatment method of synthetic rubber wastewater |
| CN106167331A (en) * | 2016-06-29 | 2016-11-30 | 云南康泰环保科技有限公司 | A kind of method of wastewater treatment during Oleoresin production |
| CN106698758A (en) * | 2017-02-20 | 2017-05-24 | 叶华天 | Method and device for using catalytic oxidant for treating chemical sewage |
| CN109111031A (en) * | 2018-08-28 | 2019-01-01 | 苏州爱源环境科技有限公司 | A kind of emulsion polymerization production of resins purification method for effluent |
| CN111348800A (en) * | 2020-02-28 | 2020-06-30 | 苏州仕净环保科技股份有限公司 | Natural rubber wastewater treatment process |
| CN111453931A (en) * | 2020-05-07 | 2020-07-28 | 山东济新环境工程有限公司 | Treatment process of rubber accelerator wastewater |
| CN114180696A (en) * | 2021-12-28 | 2022-03-15 | 张家港市清源水处理有限公司 | Sedimentation sludge discharge method of three-sedimentation tank |
| CN114772795A (en) * | 2022-05-25 | 2022-07-22 | 福建省金皇环保科技有限公司 | Catalytic oxidation coagulating sedimentation integrated sewage treatment process |
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Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103723883A (en) * | 2013-11-13 | 2014-04-16 | 安徽淮化股份有限公司 | Treatment method of synthetic rubber production waste water |
| CN104710077B (en) * | 2015-03-06 | 2017-03-01 | 天津市联合环保工程设计有限公司 | The processing system of synthetic rubber waste water and its processing method |
| CN104710077A (en) * | 2015-03-06 | 2015-06-17 | 天津市联合环保工程设计有限公司 | Treatment system and treatment method of synthetic rubber wastewater |
| CN106167331B (en) * | 2016-06-29 | 2019-03-12 | 昆明久昌生物科技有限公司 | A kind of wastewater treatment method during Oleoresin production |
| CN106167331A (en) * | 2016-06-29 | 2016-11-30 | 云南康泰环保科技有限公司 | A kind of method of wastewater treatment during Oleoresin production |
| CN106698758A (en) * | 2017-02-20 | 2017-05-24 | 叶华天 | Method and device for using catalytic oxidant for treating chemical sewage |
| CN109111031A (en) * | 2018-08-28 | 2019-01-01 | 苏州爱源环境科技有限公司 | A kind of emulsion polymerization production of resins purification method for effluent |
| CN111348800A (en) * | 2020-02-28 | 2020-06-30 | 苏州仕净环保科技股份有限公司 | Natural rubber wastewater treatment process |
| CN111453931A (en) * | 2020-05-07 | 2020-07-28 | 山东济新环境工程有限公司 | Treatment process of rubber accelerator wastewater |
| CN114180696A (en) * | 2021-12-28 | 2022-03-15 | 张家港市清源水处理有限公司 | Sedimentation sludge discharge method of three-sedimentation tank |
| CN114180696B (en) * | 2021-12-28 | 2023-11-24 | 张家港市清源水处理有限公司 | Sediment sludge discharge method of triple sedimentation tank |
| CN114772795A (en) * | 2022-05-25 | 2022-07-22 | 福建省金皇环保科技有限公司 | Catalytic oxidation coagulating sedimentation integrated sewage treatment process |
| CN114772795B (en) * | 2022-05-25 | 2024-01-02 | 福建省金皇环保科技有限公司 | Catalytic oxidation coagulation precipitation integrated sewage treatment process |
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Application publication date: 20120627 |