CN103708677A - Spraying paint wastewater treatment technology - Google Patents
Spraying paint wastewater treatment technology Download PDFInfo
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- CN103708677A CN103708677A CN201310695939.XA CN201310695939A CN103708677A CN 103708677 A CN103708677 A CN 103708677A CN 201310695939 A CN201310695939 A CN 201310695939A CN 103708677 A CN103708677 A CN 103708677A
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Abstract
The invention provides a spraying paint wastewater treatment technology, comprising the following steps: adjusting the pH value of the wastewater to below 4 to obtain an acidizing fluid; demulsifying the acidizing fluid to obtain a demulsified solution; carrying out biodegradation on the demulsified solution; adding tertiary amine cationic polyether to the acidizing fluid as a reverse demulsifier, so that the CODCr of the wastewater is less than 30000mg/L. The CODCr value of the wastewater processed by the method is reduced to below 300mg/L from 10000-25000mg/L, and achieves the GB8978-1996 three-level standard, and the required cost of the overall craft process is 20-100 yuan in per ton of wastewater.
Description
Technical field
The present invention relates to field of waste water treatment, especially, relate to a kind for the treatment of process to painting wastewater.
Background technology
Painting wastewater is mainly derived from wet type spray chamber and washes working district, paint spray booth air with water, paints thing and organic solvent and be transferred to and in water, form painting wastewater in air.In painting wastewater, contain suspended substance and the difficult for biological degradation larger molecular organicses such as a large amount of resins, tensio-active agent, organic solvent (as ethanol, acetone, lipid, benzene class) and auxiliary agent, the composition of pollutent is comparatively complicated, COD
cr(chemical oxygen demand that the potassium bichromate of usining records as oxygenant) concentration is high, and biodegradability is poor.The method of conventional process painting wastewater is dilution method and Coagulation Method at present.
Dilution method is for cleaning itself and workshop after the surface water, other workshop waste water and sanitary wastewater etc. mix and process, COD after mixed diluting
cr≤ 1000mg/L, hardly degraded organic substance concentration reduces, and biodegradability strengthens, then gets final product qualified discharge by further biological treatment.But because pending wastewater volume after dilution is excessive, need to add a large amount of medicaments, required treating pond floor space is also excessive, thereby processing cost is higher, is unsuitable for industrial applicability.Coagulation Method is directly to painting wastewater, to add coagulating agent and flocculation agent to carry out coagulating treatment, but effluent quality difficulty reaches safety dumping standard.
Summary of the invention
The object of the invention is to provide a kind of painting wastewater treatment process, to solve painting wastewater in prior art, cannot process at low cost the technical problem to qualified discharge.
For achieving the above object, according to the invention provides a kind of painting wastewater treatment process, waste water ph is adjusted to and below 4, obtains acidizing fluid; Acidizing fluid is carried out to breakdown of emulsion and obtain breakdown of emulsion liquid; Breakdown of emulsion liquid is carried out to biological degradation; Wherein, in breakdown of emulsion process, in acidizing fluid, add tertiary amine cation polyether; Waste water COD
crbe less than 30000mg/L.
Further, the add-on of tertiary amine cation polyether for to add 0.1～5g in every liter of acidizing fluid.
Further, breakdown of emulsion step for to add successively the coagulating agent of tertiary amine cation polyether, 0.01～10g and the flocculation agent of 0.1～5g in every liter of acidizing fluid.
Further, breakdown of emulsion liquid is scraped to oil treatment; To break ph value of emulsion and be adjusted to 6～9.
Further, biological degradation step comprises anerobe degraded.
Further, anerobe degradation condition is organic volumetric loading 10～12kgCOD/m
3.d, DO≤0.5mg/L.
Further, biological degradation step comprises the degraded of acidifying enzyme, anerobe degraded, aerobic degradation and the filtration of aeration and biological pond.
Further, aerobic degradation condition is organic volumetric loading 5～10kgCOD/m
3.d, DO>=3mg/L, draft speed 0.9～1.1m
3/ minute, gas-water ratio 19～21:1.
Further, after aerobic degradation step, also comprise solid-liquid separation step.
The present invention has following beneficial effect:
Technique provided by the invention can be by the COD in painting wastewater
crvalue is down to and is less than 300mg/L from 10000～25000mg/L, reaches GB8978-1996 grade III Standard.Wastewater pH is adjusted to after acidity, breakdown of emulsion process Chinese medicine consumption declines to a great extent, be only of the prior art 1 ‰, making to adopt this technique wastewater treatment expense per ton is only 20～100 yuan (containing artificial, water power, medicament expense, depreciation of equipment), can greatly save enterprise's spending, be easy to be extended and applied.
Except object described above, feature and advantage, the present invention also has other object, feature and advantage.Below with reference to figure, the present invention is further detailed explanation.
Accompanying drawing explanation
The accompanying drawing that forms the application's a part is used to provide a further understanding of the present invention, and schematic description and description of the present invention is used for explaining the present invention, does not form inappropriate limitation of the present invention.In the accompanying drawings:
Fig. 1 is the schema of the preferred embodiment of the present invention.
Embodiment
Below in conjunction with accompanying drawing, embodiments of the invention are elaborated, but the multitude of different ways that the present invention can be defined by the claims and cover is implemented.
The invention provides a kind of painting wastewater treatment process, this technique is by being adjusted to acidity by waste water ph before breakdown of emulsion, breaks water oil balance in solution, makes the macromolecule organic that is present in water with emulsion droplet form separated with water, is convenient to subsequent disposal.This technique is simultaneously in conjunction with breakdown of emulsion and biodegradation method, by the COD in painting wastewater
crvalue reduction reaches emission standard.
Painting wastewater treatment process comprises:
1) regulate waste water ph to be less than 4 and obtain acidizing fluid;
2) breakdown of emulsion, removes and swims in surperficial oil phase, obtains breakdown of emulsion liquid;
3) regulating broken ph value of emulsion is 6～9, obtains adjusting back liquid;
4) successively readjustment liquid being carried out to the degraded of acidifying mattress extracellular enzyme, anerobe degraded, aerobic degradation, solid-liquid separation and aeration and biological pond filters.
Method provided by the present invention is unsuitable for processing COD
crbe greater than the waste water of 30000mg/L.The waste water that meets this standard mostly is painting wastewater.In painting wastewater, contain polymer substance and corresponding emulsifying agent, emulsifying agent molecule oriented adsorption form firm interfacial film on water-oil interface, in waste water, also contain the impurity such as dust, impurity absorption is on water oil interface, the net thickness of diffusion double layer, Potential distribution width and the steepness of electrostatic double layer have been increased, oil phase drop height is evenly dispersed in liquid phase, and quite stable.For this type of waste water, common process is direct breakdown of emulsion, by direct interpolation flocculation agent, coagulating agent, makes waste water breakdown of emulsion, but the method can not surely separate out most of oil phase drop is broken, thereby present inventor first turns down painting wastewater pH value before breakdown of emulsion.
The following acidizing fluid that obtains of painting wastewater pH regulator to 4.Regulate the available various conventional acid of pH value of waste water, as sulfuric acid etc., for the consideration of environment protection, be preferably nonvolatile strong acid.The mineral acid ionization adding in waste water produces proton H
+, in and the negative charge on oil phase drop surface electric double layer in acidizing fluid, reduce the electric charge on oil phase drop surface, make between two no longer two like magnetic poles repel each other of oil phase drop, and mutually draw close.Oil phase drop after drawing close, similar mixing, gathering attracts each other.After drop contacts with each other, form the drop of more volume, thereby acceleration oil phase drop is de-, surely separate out.Acidified waste water can make higher aliphatic acid or high-carbon fatty alcohol class tensio-active agent in waste water generate the materials such as water-soluble lipid acid or fatty alcohol with acid effect simultaneously, makes it lose emulsifying capacity.After these tensio-active agent sex change, cannot continue emulsifying waste water, formed drop unstability, promotes waste water breakdown of emulsion.By adopting this step to reduce greatly the add-on of follow-up breakdown of emulsion process Chinese medicine, greatly reduce processing cost, for enterprise reduces cost.
After acidifying, in waste water, most of oil phase drop unstability enters in solution, and under the traction of a plurality of drop molecular force, oil phase drop segregation, floats on acidizing fluid surface.Residual undecomposed oil phase drop also in acidizing fluid, now residual drop is and the compact drop of water, can be separated out by follow-up breakdown of emulsion means.The present invention's reverse-phase emulsifier used is tertiary amine cation polyether, tertiary amine cation polyether molecular chain length and with positive charge group, in acidified water, oil droplets covers one deck with the electrostatic double layer of negative charge, by absorption charge neutrality effect, the negative charge of oil droplets is neutralized by the positive charge of emulsion splitter, and oil phase drop is further de-steady.Under the coagulating agent adding after oil phase liquid after de-steady drops in and the effect of flocculation agent, attracting each other is gathered into oarse-grained oil droplet and moisture isolates.On tertiary amine cation polyether molecular chain with positive charge group, under acidic conditions, ionize out cationic polyelectrolyte, painting wastewater is water-in-oil-type, and oil droplets covers one deck with the electrostatic double layer of negative charge, to make oil droplet de-steady by adsorbing the effect of charge neutrality, thus separated with water.Be that oil droplet is electronegative, when pH value reduces, H
+concentration increases, and reverse-phase emulsifier is cationic polyelectrolyte, and under acidic conditions, reverse-phase emulsifier can better ionize out the positively charged ion of positively charged, by the effect of electrical neutralization, breaks the stability between oil droplet and oil droplet negative charge.Preferably promote drop to separate out, add and also can add after reverse-phase emulsifier the de-material that contributes to oily water separation that adds other after steady as flocculation agent and coagulating agent etc.Thereby coagulating agent and flocculation agent make to attract each other between olesome assemble separated with water.And pH value is too high, H
+concentration reduces, and suppresses the ionization reaction of reverse-phase emulsifier, and its positively charged quantity is reduced, and weaken, thereby demulsification weakens with the absorption charge neutrality effect of oil droplet.
Breakdown of emulsion step can be carried out according to a conventional method, adds after related agents, stirs breakdown of emulsion, and oil removing obtains breakdown of emulsion liquid.Medicament herein can only also can comprise coagulating agent and the flocculation agent of follow-up interpolation for tertiary amine cation polyether.Obviously can add according to a conventional method.Be preferably and add successively reverse-phase emulsifier, coagulating agent and flocculation agent.Coagulating agent and flocculation agent can be conventional medicament, are preferably coagulating agent and are wherein one or more of polymerize aluminum chloride (PAC), bodied ferric sulfate (PFS), polyaluminium sulfate (PAS), calcium chloride, magnesium chloride, magnesium sulfate, calcium sulfate; Flocculation agent is anionic polyacrylamide (PAM).Adding of flocculation agent and coagulating agent produces strong hydration to acidizing fluid, reduce the free water molecule in waste water, oil phase drop is produced to dehydration, destroyed hydration layer and the double electrical layers thereof of oil phase drop, neutralized the electrical of oil phase drop, oil phase drop unstability is assembled.The molecular chain of flocculation agent, by effects such as physics, chemistry, involves the oil phase drop of the dispersion after reverse-phase emulsifier breakdown of emulsion together, forms nettedly, between each particle, by passage connected with each other, merges gradually, makes oil droplet formation aggregate and separated with water.Preferred in breakdown of emulsion step to the tertiary amine cation polyether that adds 0.1～5g in acidizing fluid every liter described.Preferably to the tertiary amine cation polyether, the coagulating agent of 0.01～10g and the flocculation agent of 0.1～5g that add successively 0.1～5g in acidizing fluid every liter described.By this amount, add above-mentioned medicament, can make treated painting wastewater COD
crwaste water has reduced by 30～40% relatively, reaches subsequent biological treatment to waste water COD
crthe requirement of value, can avoid the waste to medicament again.Select tertiary amine cation polyether as reverse-phase emulsifier, at identical COD
crunder value requires, the add-on of this medicament can be down to minimum, can be cost-saving to greatest extent, can obtain required emulsifying effectiveness again simultaneously.
To acidizing fluid, oil removing obtains breakdown of emulsion liquid, and oil removing can be by artificial or mechanical means the oil slick of fluid surface is removed.
In biological degradation step, need to use microorganism and enzyme, there is the bioactive material inactivation that is easily damaged under strong acid environment.Thereby first the pH value of breakdown of emulsion liquid is adjusted to neutrality, and be preferably 6～9, obtain adjusting back liquid, now just can give full play to the capacity of decomposition of biologically active substance.Can adopt conventional highly basic to regulate as sodium hydroxide etc.
Biological degradation step comprises anaerobic degradation or/and the method for other conventional biological degradation sewage, as aerobic bacteria degraded, aeration and biological degraded etc.Preferably comprise the degraded of acidifying enzyme, anerobe degraded, aerobic bacteria degraded and aeration and biological degraded.Obviously can in needs, to degradation solution, carry out solid-liquid separation, to reclaim solid spawn wherein, improve medicament service efficiency.Be specially after aerobic degradation treatment solution is carried out to solid-liquid separation, with the aerobic bacteria of reclaiming wherein, again utilize.
Acidifying enzyme degraded: larger molecular organics in breakdown of emulsion liquid is decomposed into small organic molecule under the effect of acidifying enzyme, improves the effect of follow-up anaerobic degradation step.Breakdown of emulsion liquid obtains the first treatment solution through the degraded of acidifying enzyme.
COD in the first treatment solution
crbe 10000～15000mg/L, cannot degradation of organic substances in case anerobe is poisoning.Adopt anaerobic degradation to process the first treatment solution.Anaerobic treatment step used is preferably IC (internal circulating anaerobic) edman degradation Edman.Anaerobic degradation step is to utilize anaerobion under oxygen-free environment, larger molecular organics in acidizing fluid remaining in the first treatment solution is decomposed into small organic molecule (as CH4 etc.), inorganics and a small amount of cellular material, and anaerobic process comprise the hydrolysed ferment stage, produce acetic acid and hydroformylation stage, product methane phase.Obtain the second treatment solution.Anaerobic degradation condition is organic volumetric loading 10～12kgCOD/m
3.d, DO≤0.5mg/L, degrades 1～20 hour.The required time of degrading is with this understanding the shortest, and reagent cost is minimum, and degradation effect is the most thorough.
The second treatment solution is carried out to aerobic degradation.Aerobic degradation is to make good use of oxygen animalcule under the condition of aerobic, and the respiration by the larger molecular organics in water by microorganism is decomposed into the inorganicss such as water and carbonic acid gas, thereby reduces the organism in water.In aerobic degradation, the packing specific area of reaction tank used is selected by conventional design, is beneficial to oxygen and enters in reaction tank, promotes microbial growth breeding, thereby improves the processing efficiency of aerobic degradation.Obtain the 3rd treatment solution.Aerobic degradation condition is organic volumetric loading 5～10kgCOD/m
3.d, DO>=3mg/L, draft speed 0.9～1.1m
3/ minute, gas-water ratio 19～21:1, degrades 1～20 hour.Degradation time can regulate according to the amount of processed waste water.The required time of degrading is with this understanding the shortest, and reagent cost is minimum, and degradation effect is the most thorough.
The 3rd treatment solution is carried out to solid-liquid separation, adopt ordinary method as tube settler, separated to the solid in the 3rd treatment solution.In the solid that separation obtains, comprise a large amount of aerobic degradation microbial films coming off, can be back in aerobic degradation reaction tank and recycle as active sludge, reduce costs.Obtain the 4th treatment solution.
Preferably also can carry out aeration and biological degraded to gained the 4th treatment solution, obtain the 5th treatment solution.To the further biological degradation of the 5th treatment solution, further reduce COD
crvalue, makes it to reach emission standard.
Embodiment
In following examples, material used and instrument are commercially available.COD in following examples
crdetection method carry out according to a conventional method.In following examples, tertiary amine cation polyether used is pressed CN91105181.3 preparation.
Embodiment 1
1. by 1 ton of painting wastewater (COD
crconcentration is 22630mg/L, pH=7) be placed in pH regulator pond, add the vitriol oil, stir, waste water ph is 2, and standing 5 minutes, oil-in-water system started to disperse de-steady, and profit is slowly separated, obtains acidizing fluid;
2. gained acidizing fluid is squeezed in breakdown of emulsion settling tank, every liter of acidizing fluid adds tertiary amine cation polyether reverse-phase emulsifier, the calcium chloride of 2g, 5 ‰ PAM of 1g of 0.1g successively, and rapid stirring is even, after standing 20 minutes by upper strata suspended substance frizing, separated and collected, obtains breakdown of emulsion liquid, now breakdown of emulsion liquid COD
crconcentration is 13790mg/L, pH=2.
3. in breakdown of emulsion liquid per ton, add 1.5kg sodium hydroxide, stir, after standing 5 minutes, record COD
crconcentration is 13200mg/L, and pH=6 obtains adjusting back liquid.
4. readjustment liquid is squeezed into hydrolysis acidification pool, 30 minutes residence time, by the degraded of acidifying enzyme, obtain the first treatment solution.
5. the first treatment solution is squeezed into IC anaerobic reactor with lift pump, whirlwind-type water distribution in reactor, organic volumetric loading 11kgCOD/m
3d, DO (dissolved oxygen concentration)≤0.5mg/L.After 1.5 hours residence time, obtain the second treatment solution.
6. the second treatment solution is squeezed into aerobic treatment in Aerobic Pond, organic volumetric loading 6kgCOD/m in Aerobic Pond
3.d, DO>=3mg/L, draft speed 1.0m
3/ minute, gas-water ratio 20: 1,1.5 hours residence time, obtains the 3rd treatment solution.
7. the 3rd treatment solution is squeezed into vertical sedimentation basin and carry out secondary sedimentation, the mud part after precipitation is back to Aerobic Pond, and a part is evacuated to pressure filter and carries out thickening outward transport disposal, and gained liquid phase is the 4th treatment solution.
8. pair the 4th processing liquid pump enters BAF, COD load 1.25kgCOD/m in BAF
3.d, aerobic air demand 0.1m
3/ minute, gas-water ratio 5: 1, water outlet dissolved oxygen DO>=3mg/L, 1 hour residence time, obtains COD
crconcentration is 180mg/L, the 5th treatment solution of pH=7.
The required cost of whole process is only: the waste water electricity charge per ton are 10 yuan of 5 yuan+depreciation of equipment of 5 yuan+labour cost=24.5 yuan/t waste water for 4.5 yuan+medicament expense.
Embodiment 2
1. by 1 ton of painting wastewater (COD
crconcentration is 22630mg/L, pH=7) be placed in pH regulator pond, add the vitriol oil, stir, waste water ph is 3 standing 5 minutes, and oil-in-water system starts to disperse de-steady, and profit is slowly separated, obtains acidizing fluid;
2. gained acidizing fluid is squeezed in breakdown of emulsion settling tank, every liter of acidizing fluid adds tertiary amine cation polyether reverse-phase emulsifier, the calcium chloride of 0.01g, the PAM of the concentration 5g/L of 5g of 5g successively, rapid stirring is even, after standing 20 minutes by upper strata suspended substance frizing, separated and collected, obtain breakdown of emulsion liquid, now breakdown of emulsion liquid COD
crconcentration is 13790mg/L, pH=3.
3. in breakdown of emulsion liquid per ton, add 1.2kg sodium hydroxide, stir, after standing 5 minutes, record COD
crconcentration is 13200mg/L, and pH=6 obtains adjusting back liquid.
4. readjustment liquid is squeezed into hydrolysis acidification pool, 30 minutes residence time, by the degraded of acidifying enzyme, obtain the first treatment solution.
5. the first treatment solution is squeezed into IC anaerobic reactor with lift pump, whirlwind-type water distribution in reactor, organic volumetric loading 11kgCOD/m
3.d, DO (dissolved oxygen concentration)≤0.5mg/L.After 1 hour residence time, obtain the second treatment solution.
6. the second treatment solution is squeezed into aerobic treatment in Aerobic Pond, organic volumetric loading 6kgCOD/m in Aerobic Pond
3.d, DO>=3mg/L, draft speed 0.9m
3/ minute, gas-water ratio 19: 1,1 hour residence time, obtains the 3rd treatment solution.
7. the 3rd treatment solution is squeezed into vertical sedimentation basin and carry out secondary sedimentation, the mud part after precipitation is back to Aerobic Pond, and a part is evacuated to pressure filter and carries out thickening outward transport disposal, and gained liquid phase is the 4th treatment solution.
8. pair the 4th processing liquid pump enters BAF, COD load 1.25kgCOD/m in BAF
3.d, aerobic air demand 0.1m
3/ minute, gas-water ratio 5: 1, water outlet dissolved oxygen DO>=3mg/L, 1 hour residence time, obtains COD
crconcentration is 180mg/L, the 5th treatment solution of pH=7.
The required cost of whole process is only: the waste water electricity charge per ton are 10 yuan of 5 yuan+depreciation of equipment of 5.5 yuan+labour cost=25 yuan/t waste water for 4.5 yuan+medicament expense.
Embodiment 3
1. by 1 ton of painting wastewater (COD
crconcentration is 22630mg/L, pH=7) be placed in pH regulator pond, add the vitriol oil, stir, waste water ph is 4 standing 5 minutes, and oil-in-water system starts to disperse de-steady, and profit is slowly separated, obtains acidizing fluid;
2. gained acidizing fluid is squeezed in breakdown of emulsion settling tank, every liter of acidizing fluid adds tertiary amine cation polyether reverse-phase emulsifier, the calcium chloride of 10g, the PAM of the concentration 2g/L of 5g of 2g successively, rapid stirring is even, after standing 20 minutes by upper strata suspended substance frizing, separated and collected, obtain breakdown of emulsion liquid, now breakdown of emulsion liquid COD
crconcentration is 13790mg/L, pH=4.
3. in breakdown of emulsion liquid per ton, add 1.0kg sodium hydroxide, stir, after standing 5 minutes, record COD
crconcentration is 13200mg/L, and pH=7 obtains adjusting back liquid.
4. readjustment liquid is squeezed into hydrolysis acidification pool, 30 minutes residence time, by the degraded of acidifying enzyme, obtain the first treatment solution.
5. the first treatment solution is squeezed into IC anaerobic reactor with lift pump, whirlwind-type water distribution in reactor, organic volumetric loading 11kgCOD/m
3d, DO (dissolved oxygen concentration)≤0.5mg/L.After 2 hours residence time, obtain the second treatment solution.
6. the second treatment solution is squeezed into aerobic treatment in Aerobic Pond, organic volumetric loading 6kgCOD/m in Aerobic Pond
3.d, DO>=3mg/L, draft speed 1.0m
3/ minute, gas-water ratio 21:1,2 hours residence time, obtains the 3rd treatment solution.
7. the 3rd treatment solution is squeezed into vertical sedimentation basin and carry out secondary sedimentation, the mud part after precipitation is back to Aerobic Pond, and a part is evacuated to pressure filter and carries out thickening outward transport disposal, and gained liquid phase is the 4th treatment solution.
8. pair the 4th processing liquid pump enters BAF, COD load 1.25kgCOD/m in BAF
3.d, aerobic air demand 0.1m
3/ minute, gas-water ratio 5: 1, water outlet dissolved oxygen DO>=, 3mg/L, 1 hour residence time, obtains COD
crconcentration is 180mg/L, the 5th treatment solution of pH=7.
The required cost of whole process is only: the waste water electricity charge per ton are 10 yuan of 5 yuan+depreciation of equipment of 6 yuan+labour cost=25.5 yuan/t waste water for 4.5 yuan+medicament expense.
Embodiment 4
1. by 1 ton of painting wastewater (COD
crconcentration is 22630mg/L, pH=7) be placed in pH regulator pond, add the vitriol oil, stir, waste water ph is 1 standing 5 minutes, and oil-in-water system starts to disperse de-steady, and profit is slowly separated, obtains acidizing fluid;
2. gained acidizing fluid is squeezed in breakdown of emulsion settling tank, every liter of acidizing fluid adds tertiary amine cation polyether reverse-phase emulsifier, the calcium chloride of 4g, the PAM of the concentration 3g/L of 5g of 2g successively, rapid stirring is even, after standing 20 minutes by upper strata suspended substance frizing, separated and collected, obtain breakdown of emulsion liquid, now breakdown of emulsion liquid COD
crconcentration is 13790mg/L, pH=1.
3. in breakdown of emulsion liquid per ton, add 2.0kg sodium hydroxide, stir, after standing 5 minutes, record COD
crconcentration is 13200mg/L, and pH=6 obtains adjusting back liquid.
4. readjustment liquid is squeezed into hydrolysis acidification pool, 30 minutes residence time, by the degraded of acidifying enzyme, obtain the first treatment solution.
5. the first treatment solution is squeezed into IC anaerobic reactor with lift pump, whirlwind-type water distribution in reactor, organic volumetric loading 11kgCOD/m
3d, DO (dissolved oxygen concentration)≤0.5mg/L.After 1.5 hours residence time, obtain the second treatment solution.
6. the second treatment solution is squeezed into aerobic treatment in Aerobic Pond, organic volumetric loading 6kgCOD/m in Aerobic Pond
3.d, DO>=3mg/L, draft speed 1.0m
3/ minute, gas-water ratio 20: 1,1.5 hours residence time, obtains the 3rd treatment solution.
7. the 3rd treatment solution is squeezed into vertical sedimentation basin and carry out secondary sedimentation, the mud part after precipitation is back to Aerobic Pond, and a part is evacuated to pressure filter and carries out thickening outward transport disposal, and gained liquid phase is the 4th treatment solution.
8. pair the 4th processing liquid pump enters BAF, COD load 1.25kgCOD/m in BAF
3.d, aerobic air demand 0.1m
3/ minute, gas-water ratio 5: 1, water outlet dissolved oxygen DO>=, 3mg/L, 1 hour residence time, obtains COD
crconcentration is 180mg/L, the 5th treatment solution of pH=7.
The required cost of whole process is only: the waste water electricity charge per ton are 10 yuan of 5 yuan+depreciation of equipment of 5.5 yuan+labour cost=25 yuan/t waste water for 4.5 yuan+medicament expense
Embodiment 5
1. by 1 ton of painting wastewater (COD
crconcentration is 22630mg/L, pH=7) be placed in pH regulator pond, add the vitriol oil, stir, waste water ph is 2 standing 5 minutes, and oil-in-water system starts to disperse de-steady, and profit is slowly separated, obtains acidizing fluid;
2. gained acidizing fluid is squeezed in breakdown of emulsion settling tank, every liter of acidizing fluid adds tertiary amine cation polyether reverse-phase emulsifier, the calcium chloride of 2g, the PAM of the concentration 4g/L of 0.1g of 2.2g successively, rapid stirring is even, after standing 20 minutes by upper strata suspended substance frizing, separated and collected, obtain breakdown of emulsion liquid, now breakdown of emulsion liquid COD
crconcentration is 13790mg/L, pH=2.
3. in breakdown of emulsion liquid per ton, add 1.2kg sodium hydroxide, stir, after standing 5 minutes, record COD
crconcentration is 13200mg/L, and pH=6 obtains adjusting back liquid.
4. readjustment liquid is squeezed into hydrolysis acidification pool, 30 minutes residence time, by the degraded of acidifying enzyme, obtain the first treatment solution.
5. the first treatment solution is squeezed into IC anaerobic reactor with lift pump, whirlwind-type water distribution in reactor, organic volumetric loading 11kgCOD/m
3d, DO (dissolved oxygen concentration)≤0.5mg/L.After 1.5 hours residence time, obtain the second treatment solution.
6. the second treatment solution is squeezed into aerobic treatment in Aerobic Pond, organic volumetric loading 6kgCOD/m in Aerobic Pond
3.d, DO>=3mg/L, draft speed 1.0m
3/ minute, gas-water ratio 20: 1,1.5 hours residence time, obtains the 3rd treatment solution.
7. the 3rd treatment solution is squeezed into vertical sedimentation basin and carry out secondary sedimentation, the mud part after precipitation is back to Aerobic Pond, and a part is evacuated to pressure filter and carries out thickening outward transport disposal, and gained liquid phase is the 4th treatment solution.
8. pair the 4th processing liquid pump enters BAF, COD load 1.25kgCOD/m in BAF
3.d, aerobic air demand 0.1m
3/ minute, gas-water ratio 5: 1, water outlet dissolved oxygen DO>=3mg/L, 1 hour residence time, obtains COD
crconcentration is 180mg/L, the 5th treatment solution of pH=7.
The required cost of whole process is only: 10 yuan=25 yuan/ton waste water of 5 yuan+depreciation of equipment of 5.5 yuan+labour cost for 4.5 yuan+medicament expense of the waste water electricity charge per ton.
Comparative example 1
Be the pH value of waste water not to be adjusted to below 4 with the difference of embodiment 1, directly carry out breakdown of emulsion and biological degradation and process.
Waste water is the milk sap that oil and water mix, and profit does not obtain separation, cannot carry out follow-up biological degradation and process.
Comparative example 2
Be waste water not to be carried out to biological degradation with the difference of embodiment 1.
Waste water is COD after treatment
crfor 13200mg/L, can not reach emission standard.
Comparative example 3
Be that with the difference of embodiment 1 added tertiary amine cation polyether is 6g, the acidizing fluid pH value of painting wastewater is 5.
Through processing COD in painting wastewater
crfor 13000mg/L, can not reach emission standard.
Therefore method provided by the invention can be processed painting wastewater extremely can qualified discharge COD
crconcentration is 180mg/L, pH=7, and also cost is only 25 yuan/ton of waste water, expense is greatly reduced.And painting wastewater cannot be processed to and can discharge in comparative example 1～3, illustrate not according to method provided by the invention cannot obtain can qualified discharge waste water.Above embodiment and comparative example have fully proved acidifying pH value and the impact of tertiary amine cation polyether add-on on painting wastewater treating processes, if the pH value of acidizing fluid and tertiary amine cation polyether add-on change, cannot be by the emulsion droplet breakdown of emulsion in painting wastewater, and then cannot continue subsequent degradation step, waste water still cannot directly be discharged after treatment.
The foregoing is only the preferred embodiments of the present invention, be not limited to the present invention, for a person skilled in the art, the present invention can have various modifications and variations.Within the spirit and principles in the present invention all, any modification of doing, be equal to replacement, improvement etc., within all should being included in protection scope of the present invention.
Claims (8)
1. a painting wastewater treatment process, is characterized in that,
Described waste water ph is adjusted to and below 4, obtains acidizing fluid;
Described acidizing fluid is carried out to breakdown of emulsion and obtain breakdown of emulsion liquid;
Described breakdown of emulsion liquid is carried out to biological degradation; Wherein
In described breakdown of emulsion process, in described acidizing fluid, add tertiary amine cation polyether; Described waste water COD
crbe less than 30000mg/L.
2. method according to claim 1, is characterized in that, the add-on of described tertiary amine cation polyether for to add 0.1～5g in acidizing fluid every liter described.
3. method according to claim 2, is characterized in that, described breakdown of emulsion step for to add successively described tertiary amine cation polyether, the coagulating agent of 0.01～10g and the flocculation agent of 0.1～5g in acidizing fluid every liter described.
4. according to the method described in any one in claim 1～3, it is characterized in that, described biological degradation step comprises anerobe degraded.
5. method according to claim 4, is characterized in that, described anerobe degradation condition is organic volumetric loading 10～12kgCOD/m
3.d, DO≤0.5mg/L.
6. method according to claim 4, is characterized in that, described biological degradation step comprises the degraded of acidifying enzyme, anerobe degraded, aerobic degradation and the filtration of aeration and biological pond.
7. method according to claim 6, is characterized in that, described aerobic degradation condition is organic volumetric loading 5～10kgCOD/m
3.d, DO>=3mg/L, draft speed 0.9～1.1m
3/ minute, air water volume ratio 19～21:1.
8. according to the method for claim 7, it is characterized in that, after described aerobic degradation step, also comprise solid-liquid separation step.
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| CN109336311A (en) * | 2018-11-08 | 2019-02-15 | 天津磊峰实业有限公司 | A kind of processing method for electrophoretic painting sewage |
| CN114477629A (en) * | 2022-01-21 | 2022-05-13 | 南京高科环境科技有限公司 | Treatment system and treatment method for viscose flushing wastewater |
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| CN109336311A (en) * | 2018-11-08 | 2019-02-15 | 天津磊峰实业有限公司 | A kind of processing method for electrophoretic painting sewage |
| CN114477629A (en) * | 2022-01-21 | 2022-05-13 | 南京高科环境科技有限公司 | Treatment system and treatment method for viscose flushing wastewater |
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