CN102863117A - Process and device for treating high concentrated organic wastewater - Google Patents
Process and device for treating high concentrated organic wastewater Download PDFInfo
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Abstract
Provided are a process and a device for treating high concentrated organic wastewater. The device comprise a water collection tank, a pH adjusting tank, a dynamic micro-electrolysis reactor, an anaerobic tank, an aerobiotic tank, a deep biochemical tank and a secondary sedimentation tank which are sequentially connected. A deep aerobiotic tank and a deep biochemical tank are further connected behind the secondary sedimentation tank as required. Waste water is filled into the dynamic micro-electrolysis reactor after the pH value of the waste water is adjusted to be 2.0-5.5, and micro-electrolysis fillings are subjected to a micro-electrolysis reaction; outlet water is adjusted to be alkaline, is filled with coagulant aids and then enters the anaerobic tank, the aerobiotic tank, the deep biochemical tank and the deep aerobiotic tank to continue to be degraded, and the final outlet water reaches the nationally regulated industrial wastewater discharge standard. The process and the device for treating high concentrated organic wastewater are high in reliability, good in treatment effect, low in cost and wide in application, and belong to the technical field of environmental protection and pollution control.
Description
Technical field
The present invention relates to a kind of technique and device thereof of processing high concentrated organic wastewater, belong to the Industrial Wastewater Treatment field.
Background technology
High concentrated organic wastewater is maximum Pollutant Source in Aquatic Environment, wherein the high concentrated organic wastewater of the industry dischargings such as chemical industry, printing and dyeing, pharmacy, process hides, dyestuff is poisoned large, difficult degradation, be the primary pollution source of destroying water ecological environment, the technique of therefore seek economy, processing high concentrated organic wastewater efficiently is very important.
Adopting biochemical process degrading high concentration organic waste water is the typical method of processing high concentrated organic wastewater in the industry, the one, and both economical, the 2nd, treating processes meets the principle of environmental protection and energy saving.But in the succession that high concentrated organic wastewater contains, contain the composition of difficult for biological degradation, perhaps to the composition of biochemistry pool microorganisms harm, must before biochemical process, carry out pre-treatment.For high concentrated organic wastewater, in the situation that operational excellence adopts AO method (being anaerobic biological+aerobic biochemical) can reach the COD clearance of 80%-90%.But, only rely on the AO method directly to process high concentrated organic wastewater up to standard.For example: for the high-concentration waste water of former water COD value more than 10000mg/L, 10%COD is exactly more than the 1000mg/L, also considerably beyond the requirement of the wastewater discharge standard of national environmental protection section regulation.Even continue again to prolong the biochemistry pool residence time, generally also can not produce more obvious effect.
Summary of the invention
The object of the invention is to propose a kind of technique of processing high concentrated organic wastewater, with the pretreatment technology of dynamic little electrolysis before as high concentrated organic wastewater biochemistry, and after the AO method, increase advanced treatment process, be specially deep biochemical technique and deep oxidation technique, the use of can using separately according to circumstances or connect.
Another object of the present invention is to provide a kind of device of processing high concentrated organic wastewater.
A kind of device of processing high concentrated organic wastewater comprises the water collecting basin, pH regulator pond, dynamic micro-electrolysis reactor, anaerobic pond, Aerobic Pond, deep biochemical pond, second pond, the deep oxidation pond that connect successively.
Dynamically micro-electrolysis reactor comprises main reactor and the auxiliary reactor of series connection, wherein all fill micro-electrolysis stuffing, micro-electrolysis stuffing is solid material, profile is sheet, particulate state (diameter range is 0.01mm-15.0mm) or irregularly shaped, that iron and carbon mass ratio are the mixture of 0.10-100, specific surface area 800-200000.All be provided with whipping appts in main reactor and the auxiliary main reactor, make waste water fully mix, react with filler.Alr mode adopts mechanical stirring, or with the pneumatic blending of pressure, can stir with the water impact of pressure.
A kind of technique of processing high concentrated organic wastewater is characterized in that:
(1) concentrate on high concentrated organic wastewater in the wastewater collecting basin, by pump delivery to pH value equalizing tank; Add acid or alkali by chemicals dosing plant, with the pH value of waste water to 2.0-5.5;
(2) waste water is transported in the dynamic micro-electrolysis reactor, carries out micro-electrolysis reaction with micro-electrolysis stuffing in the main reactor; Waste water is in the bottom inflow reactor of main reactor, after the micro-electrolysis stuffing reaction, upper part through dynamic little electrolysis main reactor is separated with micro-electrolysis stuffing, and upper strata waste water exports auxiliary reactor to from the top of main reactor, and micro-electrolysis stuffing turns back in the main reactor; Waste water in like manner reacts with filler in auxiliary reactor, discharges from the top of auxiliary reactor at last; The water outlet of micro-electrolysis reaction adds alkali and regulates the pH value to 8.0-10.0, adds the coagulant aids precipitation and removes the partial organic substances that contains in the water, with the BC ratio raising 20% to 200% of waste water;
(1) waste water enters anaerobic pond, stops 2d-20d (48 hours to 480 hours), better 3d-10d because the residence time less than 3d, then treatment effect is bad, COD removes rate variance; Greater than 10d, useful to improving the COD clearance, but the volume of anaerobic pond is excessive, and construction cost is too high, and the pH value remains on 6.0-9.5 in the anaerobic pond, and temperature remains on 20 ℃-45 ℃; The anaerobic pond of biochemical filler is not installed, and the water outlet of anaerobic pond need to be installed mud-water separation interlayer and sludge refluxing apparatus;
(2) the anaerobic pond water outlet enters Aerobic Pond, and 20 minutes-24 hours residence time, the Aerobic Pond temperature remains on 15 ℃-35 ℃, and continuous aeration, by the effect of aerobic microbiological population, significantly removes the organism composition in the waste water; The water outlet of Aerobic Pond must be carried out separating of active sludge and waste water through settling tank, and mud must reflux, and superfluous mud discharging is to sludge sump, and supernatant liquid drains into Aerobic Pond; The oxygenant that adds can adopt Feton reagent, hydrogen peroxide, hypochlorite;
(3) waste water is through the processing of Aerobic Pond, the COD value is in the 500mg/L-2000mg/L scope, then need to continue in the deep biochemical pond, to degrade, the deep biochemical pond is set to a plurality of partitions, waste water successively cycling stream is crossed the interior difference partition of pond body, in cutting off, each sets different DO values, the microbial species bacterium of turning out, for organism generation biological degradation residual in the waste water, in the end in partition, because the organic substance residues in the waste water seldom, after the long-time running, can growth phycophyta and small-sized floating plant in the biochemistry pool and on the pool wall can, final outflow water reaches the industrial wastewater discharge standard that meets national regulation; In the Aerobic Pond water outlet COD value 500mg/L, adopt the deep oxidation pond suitable.More than 1000mg/L, adopt the deep biochemical pond suitable.In the scope of Aerobic Pond water outlet COD value 500mg/L-1000mg/L, two kinds of selections are arranged, a kind of is direct deep oxidation, also can select to continue deep biochemical.
(4) be higher than emission standard for the water outlet of deep biochemical pond, continue by can reaching emission standard behind the degree of depth Aerobic Pond.
Processing method reliability of the present invention is high, treatment effect good, cost is low, be widely used.
The present invention can guarantee that high-concentration industrial-water effluent index (COD, colourity, suspended substance, tensio-active agent, ammonia nitrogen etc.) after treatment reaches the first discharge standard requirement of " wastewater discharge standard " of national environmental protection cloth promulgated by the ministries or commissions of the Central Government fully.
In the running cost of the present invention, the running cost of little electrolysis stage is 1 yuan to 3 yuan/tons waste water; The running cost of biochemical stage is 1 yuan/ton of waste water; The cost of deep oxidation is 1 yuan to 4 yuan/tons waste water.
Description of drawings
Fig. 1 is high concentrated organic wastewater assembled technological schema.
Fig. 2 is the organigram of dynamic little electrolysis.Wherein, the dynamic little electrolysis main reactor of 1-, the dynamic little electrolysis auxiliary reactor of 2-.
Fig. 3 is the technique course diagram of another kind of embodiment;
Embodiment
Micro-electrolysis stuffing in the presents is particulate solid available from filler factory.
Fig. 1 is high concentrated organic wastewater assembled technological schema.With reference to shown in Figure 1, a kind of device of processing high concentrated organic wastewater comprises the water collecting basin, pH regulator pond, dynamic little electrolysis main reactor, dynamic little electrolysis auxiliary reactor, anaerobic pond, Aerobic Pond, deep biochemical pond, the second pond that connect successively.
The tank body that can be steel reinforced concrete pool body or following material of pH value equalizing tank, main reaction pond, second pond is such as metal tin, plastics, glass reinforced plastic, sharp general tank etc.
Wherein, water collecting basin is that device is left standstill in high-concentration waste water collection, homogeneous, mixing; In the pH regulator pond, behind interpolation acid or the alkali pH value of waste water is adjusted to the scope of appointment; Dynamic little electrolysis main reaction and auxiliary reactor filling solid micro-electrolysis stuffing are also installed whipping appts, mix the anti-micro-electrolysis reaction of giving birth to by waste water and fully contacting of micro-electrolysis material and reach treatment effect, occur significantly descending through the pollutent indexs such as COD value, organic concentration, heavy metal content, colourity, suspended solid SS in the water outlet of micro-electrolysis reaction.
Fig. 2 is the organigram of dynamic little electrolysis.Wherein, dynamic little electrolysis main reactor 1 is connected with dynamic little electrolysis auxiliary reactor 2.
Waste water treatment process is as follows:
High concentrated organic wastewater is concentrated in the wastewater collecting basin, pump to pH value equalizing tank by pump;
Add acid or alkali in the pH value equalizing tank by chemicals dosing plant, with the pH value of waste water to 2.0-5.5;
Waste water behind the pH regulator is transported in the dynamic micro-electrolysis reactor, waste water and the micro-electrolysis stuffing of solid granular fully mix carry out micro-electrolysis reaction (hybrid mode comprise and be not limited to stir, water impact, with the air of pressure); Then waste water separates with micro-electrolysis stuffing through upper part of dynamic little electrolysis main reactor, and upper strata waste water flows out, and micro-electrolysis stuffing turns back in the reactor; The water outlet of micro-electrolysis reaction adds the alkali neutralization, regulates the pH value to 8.0-10.0, adds the coagulant aids precipitation and removes the partial organic substances that contains in the water, with BC ratio (BOD/COD value) raising 20% to 200% of waste water, improves simultaneously the bio-degradable of waste water;
Then waste water enters anaerobic pond, and the pH value remains in 6.0 to 9.5 scopes in the anaerobic pond, and temperature remains in 20 ℃ to the 45 ℃ scopes.The northern area winter temperature is lower than in 0 ℃ the situation for a long time, and anaerobic pond need to keep above-mentioned temperature range by adding gentle Insulation, otherwise anaerobic pond efficient will significantly descend.Waste water is controlled at 2d-20d (48 hours to 480 hours), better 3d-10d in the total residence time of anaerobic pond.The anaerobic pond of biochemical filler is not installed, and the water outlet of anaerobic pond need to be installed mud-water separation interlayer and sludge refluxing apparatus;
The anaerobic pond water outlet enters Aerobic Pond, and the Aerobic Pond continuous aeration by the effect of aerobic microbiological population, is significantly removed the organism composition in the waste water.The water outlet of Aerobic Pond must be carried out separating of active sludge and waste water through settling tank, and mud must reflux, and superfluous mud discharging is to sludge sump, and supernatant liquid drains into Aerobic Pond.The northern area winter temperature is lower than in 0 ℃ the situation for a long time, and Aerobic Pond need to keep in 15 ℃ to the 35 ℃ scopes by adding gentle Insulation, otherwise Aerobic Pond efficient will significantly descend.
Fig. 2 is the technique course diagram of another kind of embodiment, is in the increase deep oxidation pond, back of the second pond of the first process flow sheet, adds oxygenant in the body of pond.Waste water is through the processing of Aerobic Pond, and the COD value is in 500mg/L to the 2000mg/L scope, also surpasses the emission standard of national regulation, needs to continue to continue in the deep biochemical pond degraded.The design with common anaerobic pond or Aerobic Pond can not be adopted in the deep biochemical pond, need to cut off according to residence time design variable to be the pond body of a plurality of lattice, and every lattice are set different DO values, and adopt return of waste water and circulation.The different compartment in deep biochemical pond has different DO values, can cultivate and tame out special microbial species bacterium, and the organism generation biological degradation for residual in the waste water reaches processing intent.The deep biochemical pond of last compartment, because the organic substance residues in the waste water seldom, after the long-time running, phycophyta and small-sized floating plant occur and in biochemistry pool, grow with pool wall, finally reach the requirement of the industrial wastewater discharge standard that meets national regulation.
Although and not shown, but the present invention allows to replenish, add some slave parts and subsidiary function, increase pretreatment technology (air supporting, precipitation etc.) such as the front end at combination process, the rear end increases the physicochemical techniques such as filtration, can carry out various changes and reinforcement to the present invention, and these changes and strengthen all being comprised in the claim restricted portion of the present invention.
Case 1:
Employing is with reference to the technique of Fig. 1, and object is the trade effluent that the high density acrylate in chemical plant, Jiangsu Province is produced.Engineering was constructed in October, 2008, and be completed in January, 2009, and processing power is 100m
3Waste water/sky.It is 6000～10000mg/L that high density contains the former water COD of acrylate trade effluent value, and colourity is greater than 2000 times, pH3～4, and the COD value of water outlet behind the engineering operation is 60mg/L, each technique unit COD removal situation sees Table 1(2,009 7 monthly average values) unit: mg/L
Table 1
Case 2:
The dyestuff intermediate factory effluent of the high density chloride containing benzene oil of mirbane of the art breading Hebei province Chemical Group in the dynamic little electrolysis of this example employing Fig. 3 → efficient anaerobic pond → Aerobic Pond → deep biochemical pond → deep oxidation pond, former water COD value is 16000mg/L～25000mg/L, colourity is greater than 2000 times, pH2～6.Engineering was constructed in August, 2010, and be completed in January, 2011.Processing power is 300m
3Waste water/sky.The COD value of water outlet behind the engineering operation is 90mg/L, and each technique unit COD removes information slip such as table 2(2,012 4 monthly average values): unit: mg/L
Table 2
Claims (4)
1. a device of processing high concentrated organic wastewater is characterized in that comprising the water collecting basin, pH regulator pond, dynamic micro-electrolysis reactor, anaerobic pond, Aerobic Pond, deep biochemical pond, second pond, the deep oxidation pond that connect successively.
2. the device of processing high concentrated organic wastewater according to claim 1 is characterized in that dynamic micro-electrolysis reactor comprises mutual series connection and main reactor and the auxiliary reactor of whipping appts all are set, and wherein all fills micro-electrolysis stuffing.
3. technique of processing high concentrated organic wastewater is characterized in that:
(1) concentrate on high concentrated organic wastewater in the wastewater collecting basin, by pump delivery to pH value equalizing tank; By adding acid or alkali, with the pH value of waste water to 2.0-5.5;
(2) waste water is transported in the dynamic micro-electrolysis reactor, carries out micro-electrolysis reaction with micro-electrolysis stuffing in the main reactor; Waste water is in the bottom inflow reactor of main reactor, after the micro-electrolysis stuffing reaction, upper part through dynamic little electrolysis main reactor is separated with micro-electrolysis stuffing, and upper strata waste water exports auxiliary reactor to from the top of main reactor, and micro-electrolysis stuffing turns back in the main reactor; Waste water in like manner reacts with filler in auxiliary reactor, discharges from the top of auxiliary reactor at last; The water outlet of micro-electrolysis reaction adds alkali and regulates the pH value to 8.0-10.0, adds the coagulant aids precipitation and removes the partial organic substances that contains in the water, with the BC ratio raising 20% to 200% of waste water;
(3) waste water enters anaerobic pond, stops 2d-20d, and the pH value remains on 6.0-9.5 in the anaerobic pond, and temperature remains on 20 ℃-45 ℃;
(4) the anaerobic pond water outlet enters Aerobic Pond, and 20 minutes-24 hours residence time, the Aerobic Pond temperature remains on 15 ℃-35 ℃, and continuous aeration and interpolation oxygenant by the effect of aerobic microbiological population, are removed the organism composition in the waste water; The water outlet of Aerobic Pond is carried out separating of active sludge and waste water through settling tank, and mud must reflux, and superfluous mud discharging is to sludge sump;
(5) waste water, then needs to continue to continue to degrade in the deep biochemical pond if COD value is in the 500mg/L-2000mg/L scope through the processing of Aerobic Pond, and water outlet is discharged after meeting the industrial wastewater discharge standard of national regulation;
(6) be higher than emission standard for the water outlet of deep biochemical pond, continue by can reaching emission standard behind the degree of depth Aerobic Pond.
4. the technique of processing high concentrated organic wastewater according to claim 3 is characterized in that filling in the Aerobic Pond in the step (4) oxygenant Feton reagent, hydrogen peroxide, hypochlorite; Step (5) deep biochemical pond is set to a plurality of partitions, and waste water successively cycling stream is crossed the interior difference partition of pond body, sets different DO values in each cuts off.
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| CN103172219A (en) * | 2013-03-12 | 2013-06-26 | 南京大学 | Novel TAIC production wastewater treatment process and treatment system |
| CN103304076A (en) * | 2013-06-13 | 2013-09-18 | 谢武 | Catalytic micro-electrolysis water treatment equipment and process method thereof |
| CN103588353A (en) * | 2013-10-12 | 2014-02-19 | 沈阳建筑大学 | Modular combined treatment technique for small-size white wine plant wastewater |
| CN104803524A (en) * | 2015-05-13 | 2015-07-29 | 山东省环科院环境工程有限公司 | Method and system for treating leather retanning low-chromium wastewater through microelectroanalysis |
| CN106517487A (en) * | 2017-01-17 | 2017-03-22 | 中冶赛迪工程技术股份有限公司 | Modular multi-tube Fenton fluidized bed reactor |
| CN107176759A (en) * | 2017-06-21 | 2017-09-19 | 江苏蓝必盛化工环保股份有限公司 | A kind of method for handling fluorescent whitening agent waste water from dyestuff |
| CN111453928A (en) * | 2020-04-23 | 2020-07-28 | 珠海清扬打印耗材有限公司 | Industrial sewage treatment method and system for realizing same |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103172219A (en) * | 2013-03-12 | 2013-06-26 | 南京大学 | Novel TAIC production wastewater treatment process and treatment system |
| CN103304076A (en) * | 2013-06-13 | 2013-09-18 | 谢武 | Catalytic micro-electrolysis water treatment equipment and process method thereof |
| CN103588353A (en) * | 2013-10-12 | 2014-02-19 | 沈阳建筑大学 | Modular combined treatment technique for small-size white wine plant wastewater |
| CN104803524A (en) * | 2015-05-13 | 2015-07-29 | 山东省环科院环境工程有限公司 | Method and system for treating leather retanning low-chromium wastewater through microelectroanalysis |
| CN106517487A (en) * | 2017-01-17 | 2017-03-22 | 中冶赛迪工程技术股份有限公司 | Modular multi-tube Fenton fluidized bed reactor |
| CN107176759A (en) * | 2017-06-21 | 2017-09-19 | 江苏蓝必盛化工环保股份有限公司 | A kind of method for handling fluorescent whitening agent waste water from dyestuff |
| CN111453928A (en) * | 2020-04-23 | 2020-07-28 | 珠海清扬打印耗材有限公司 | Industrial sewage treatment method and system for realizing same |
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