CN104926016A - High-salt epoxy wastewater treatment method - Google Patents
High-salt epoxy wastewater treatment method Download PDFInfo
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- CN104926016A CN104926016A CN201510241166.7A CN201510241166A CN104926016A CN 104926016 A CN104926016 A CN 104926016A CN 201510241166 A CN201510241166 A CN 201510241166A CN 104926016 A CN104926016 A CN 104926016A
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Abstract
The invention discloses a high-salt epoxy wastewater treatment method. According to the invention, with a sequencing batch manner, wastewater is sequentially processed through hydrolysis, acidification, anaerobic, hyperoxia and hypoxia processes. Insoluble pollutants are dissolved in a hydrolysis tank (3); macromolecules and refractory pollutants are converted into small molecules in an acidification tank (4); in an anaerobic tank (5), B/C is further improved, and water quality biodegradability is further improved; in a hyperoxia tank (7), a large amount of degradable organics are degraded into inorganic small molecules; and in a hypoxia tank (8), residual organics are further decomposed, and outlet water quality is stabilized. Sludge in different sections is refluxed separately, such that flora mixing is avoided, and impact resistance is improved. With the method, wastewater pollutants with different properties are gradually decomposed with the sequencing batch manner; unit treatment efficiency is high; and organic pollutant reduction rate is high.
Description
Technical field
The present invention relates to a kind of Fine Chemistry Wastewater treatment process technology, refer to specifically and adopt sequence batch (acidication-aerobic biochemical process, namely by the process combination of " hydrolysis-acidifying-oxygen-hyperoxia-hypoxemia of holding concurrently ", the gradient of organic concentration decline and the kind of microflora in waste water are mated with quantity is collaborative, thus obtains stable, efficient processing efficiency.
Background technology
Carry out washing because adopting boiling water in epoxy resin production to purify, the waste water given off is that temperature is higher, and this waste water is high-concentration salt-containing wastewater, and its component is more complicated, mainly can be divided three classes:
1 organism: comprise the macromole intermediate product of polycondensation generation, excessive raw material ECH and hydrolysate, volatile phenol, organic solvent benzene series thing and aged resin.
2 mineral ions: as Na
+, Cl
-, OH
-deng.
3 water: the tap water introduced in resin washing.
Production technique is different, and the concentration of the generation of waste water and wherein each pollutent is also variant.As basic type epoxy resin liquid-state epoxy resin factory effluent generation is about 3.65 ~ 4.15m
3/ t product; Solvent extration solid epoxy resin factory effluent generation is about 10m
3/ t product; WATER-WASHING METHOD solid epoxy resin factory effluent generation is about 20 ~ 22m
3/ t product.The difference of pass is applied mechanically, the general 8000 ~ 10000mg/L of the general 2000 ~ 3500mg/L of liquid-state epoxy resin factory effluent COD, solid epoxy resin factory effluent COD according to washing water; Epoxy resin production waste-water Cl
-concentration generally at more than 5000mg/L, pH value is greater than 9.
Known to sum up analyzing, epoxy resin waste-water has that inorganic salinity is high, organic contamination substrate concentration is high, complicated component, biodegradability are poor, alkalescence is strong, temperature high, its intractability is larger, processing cost is higher, and epoxy wastewater treatment technology present situation has govern the sound development of China's epoxy resin industry.
Produce the method that evaporative desalination generally taked by saturated strong brine in epoxy resin production process, four, five, six times washing water repeats to apply mechanically, one, two, three time washing water as factory effluent, this waste water need process up to standard after can arrange outward.At present, the Technology that this kind of waste water mainly adopts " coagulating sedimentation-acidication-aerobic biochemical-precipitation-discharge ", the organism of this technique to epoxy wastewater has certain reduction effect, but also there are some problems:
1 effluent COD concentration reaches 300 ~ 500 mg/L, is difficult to meet emission standard or adapter requirement;
In 2 waste water, salinity fluctuation is larger on system stable operation impact;
The cell processing efficiency such as 3 hydrolysis, biochemistry are undesirable.
The reason of above defect: 1. the hydraulic retention distribution of acidication, each unit of aerobic biochemical is improper, in most technique, hydrolytic acidification time is shorter than the aerobic biochemical time, part Recalcitrant chemicals and insoluble pollutent fail to be degraded to small-molecule substance at acidication unit, cause aerobic biochemical unit efficiencies greatly to decline; 2. acidication, aerobic biochemical structures neglect height suddenly to pollutent along journey degradation rate, and in structures, microbial profile is uneven or there is concentration gradient, handle biological concentration distribution well to contaminant degradation efficiency Research on Interactive Problem in technique; 3. mud or mixed-liquor return improper, cause microbial population mixed and disorderly; 4. acidication, aerobic biochemical unit lack good waterpower adjustment, and system stablizes adaptive faculty difference to salinity fluctuation, microflora.
The present invention is intended to develop a kind of high salt epoxy wastewater treatment process technology newly, adopt sequence batch (acidication-aerobic biochemical process, acidication is divided into three sections of hydrolysis-acidifyings-hold concurrently oxygen, series connection, and each section all distributes dominant microflora, takes corresponding controling parameters according to Flora distribution; Aerobic biochemical is divided into two sections of hyperoxia-hypoxemia, series connection, takes different operating parameters for every section, makes contaminant degradation efficiency best; Acidication and aerobic biochemical end arrange settling tank respectively, and mud or mixed solution reflux separately, avoid flora to mix.This technology effectively can work in coordination with mating of Pollutant levels and microflora's quantity, and improve the degree that system tolerates salinity, effluent COD concentration is less than 50mg/L.
summary of the invention:
The present invention is to provide a kind of sequence batch (acidication-aerobic biochemical process, namely the Technology of " hydrolysis-acidifying-oxygen-hyperoxia-hypoxemia of holding concurrently ", system effectively can work in coordination with microorganism, salinity, pollutent triadic relation, makes treatment system efficient, stable.
Principal feature of the present invention is: first equalizing tank receives Workshop Production waste water, start lift pump, waste water lifting, to coagulative precipitation tank, adds PAC and PAM to coagulative precipitation tank, open stirrer simultaneously, after coagulation 10-15min, waste water is from sedimentation tank, and settling tank supernatant liquor is from flowing into hydrolytic tank, bottom settlings thing delivers to the dehydration of mud sheet frame by sludge pump, for preventing equalizing tank from depositing, intermittent aeration at the bottom of pond, originates from from gas blower; Secondly waste water is after hydrolytic tank completes hydrolysis, and gravity flow enters acidification pool, adds sodium bicarbonate during acidifying in waste water; The waste water obtained flows into oxygen compatibility pool and degrades to the macromole in waste water further, opens air door B, carries out intermittent air blast aeration, and excess sludge delivers to the dehydration of mud sheet frame by sludge pump, and upper clear supernate gravity flow is to hyperoxia pond; Carry out high strength blast aeration in hyperoxia pond, maintain the metabolism that aerobic microbiological is vigorous, waste water COD declines fast; Hypoxemia pond, carries out low intensity aeration, maintains microorganism concn and does not decline, and waste water COD is stable to decline; In Aerobic Pond, mixed solution enters second pond solid-liquid separation, and mud is carried by sludge pump, partial reflux, and excess sludge delivers to the dehydration of mud sheet frame; Aerobic Pond dissolved oxygen concentration is by C, D valve regulation, and return sludge ratio is by H, I valve regulation; Waste water from second pond is entered second coagulation settling tank, adds PAC and PAM to coagulation basin, open stirrer simultaneously, after coagulation 5-10min, waste water is from sedimentation tank, and settling tank supernatant liquor is from flowing into discharge pond, and bottom settlings thing delivers to the dehydration of mud sheet frame by sludge pump; If it is up to standard finally to discharge pond water outlet, then opens I valve and arrange outward; If not up to standard, then open the backflow of K valve again to process, waste water is successively through hydrolysis-acidifying-oxygen-hyperoxia-hypoxemia operation of holding concurrently, insoluble pollutent dissolves at hydrolytic tank, macromole, Recalcitrant chemicals are converted into small molecules at acidification pool, the B/C of oxygen compatibility pool improves further, and water quality biochemical is improved further; Hyperoxia pond is by a large amount of labile organic compounds degraded inorganic molecules, and residual organic matter is decomposed further in hypoxemia pond, stablizes effluent quality.
Principal feature of the present invention is: medium sediment pool of connecting after oxygen compatibility pool, and precipitating sludge is back to hydrolysis-acidifying-oxygen of holding concurrently by sludge pump, and sludge reflux position and quantity of reflux control flexibly by reverse flow valve E, F, G; Connect behind hypoxemia pond second pond, mud is carried by sludge pump, partial reflux, and excess sludge delivers to the dehydration of mud sheet frame; Dissolved oxygen concentration in hyperoxia pond and hypoxemia pond is by C, D valve regulation, and return sludge ratio is by H, I valve regulation; Each section of mud refluxes separately, avoids flora to mix, enhances impact resistance.
Principal feature of the present invention is: adopt sequence batch (acidication-aerobic biochemical process, and acidication (hydrolysis-acidifying-oxygen of holding concurrently) and aerobic biochemical (hyperoxia-hypoxemia) residence time are respectively 14h and 9h.
Beneficial effect of the present invention is: in waste water, the pollutent of different in kind progressively decomposes according to sequence batch mode, and cell processing efficiency is high, and organic pollutant reduction rate is high, and stable water outlet is up to standard; Improve salinity tolerance degree, under steady running, salt concentration can reach 8000 ~ 10000 mg/L; Each unit structures are implemented precision to Pollutants in Wastewater and are decomposed, and system energy efficiency is high, reduces investment outlay; The oxygen supply of aerobic unit gradient, power consumption reduces greatly; Hydrolysis acidification pool gallery is implemented low energyization and is improved, and hydraulics is better, and stirring, thrust power consume low.
Accompanying drawing explanation
fig. 1 is process flow sheet of the present invention.
Embodiment
Below in conjunction with the drawings and specific embodiments, the present invention is described in further detail
As Fig. 1, a kind of high salt epoxy wastewater treatment process, key step is: first equalizing tank 1 receives Workshop Production waste water, starts lift pump 12, waste water lifting is to coagulative precipitation tank 2, add PAC and PAM to coagulative precipitation tank 2, open stirrer 18, after coagulation 10-15min simultaneously, waste water is from sedimentation tank, settling tank supernatant liquor is from flowing into hydrolytic tank 3, and bottom settlings thing delivers to mud sheet frame dehydration 21 by sludge pump 13, deposits for preventing equalizing tank 1, intermittent aeration at the bottom of pond, originates from from gas blower 14; Secondly waste water is after hydrolytic tank 3 completes hydrolysis, and gravity flow enters acidification pool 4, adds sodium bicarbonate during acidifying in waste water; The waste water obtained flows into oxygen compatibility pool 5 and degrades to the macromole in waste water further, opens air door B, carries out intermittent air blast aeration, and excess sludge delivers to mud sheet frame dehydration 21 by sludge pump 15, and upper clear supernate gravity flow is to hyperoxia pond 7; Carry out high strength blast aeration in hyperoxia pond 7, maintain the metabolism that aerobic microbiological is vigorous, waste water COD declines fast; Hypoxemia pond 8, carries out low intensity aeration, maintains microorganism concn and does not decline, and waste water COD is stable to decline; In Aerobic Pond, mixed solution enters second pond 9 solid-liquid separation, and mud is carried by sludge pump 16, partial reflux, and excess sludge delivers to mud sheet frame dehydration 21; Aerobic Pond dissolved oxygen concentration is by CD valve regulation, and return sludge ratio is by HI valve regulation; Waste water from second pond is entered second coagulation settling tank 10, adds PAC and PAM to coagulation basin, open stirrer 19 simultaneously, after coagulation 5 ~ 15min, waste water is from sedimentation tank, and settling tank supernatant liquor is from flowing into discharge pond 11, and bottom settlings thing delivers to mud sheet frame dehydration 21 by sludge pump 17; If it is up to standard finally to discharge pond 11 water outlet, then opens I valve and arrange outward; If not up to standard, then open the backflow of K valve again to process, waste water is successively through hydrolysis-acidifying-oxygen-hyperoxia-hypoxemia operation of holding concurrently, insoluble pollutent dissolves at hydrolytic tank 3, macromole, Recalcitrant chemicals are converted into small molecules at acidification pool 4, the B/C of oxygen compatibility pool 5 improves further, and water quality biochemical is improved further; Hyperoxia pond 7 is by a large amount of labile organic compounds degraded inorganic molecules, residual organic matter is decomposed further in hypoxemia pond 8, stablize effluent quality, series connection medium sediment pool 6 after oxygen compatibility pool 5, precipitating sludge is back to hydrolysis-acidifying-oxygen of holding concurrently by sludge pump 15, and sludge reflux position and quantity of reflux control flexibly by reverse flow valve EFG; Connect behind hypoxemia pond 8 second pond, mud is carried by sludge pump 16, partial reflux, and excess sludge delivers to mud sheet frame dehydration 21; Dissolved oxygen concentration in hyperoxia pond 7 and hypoxemia pond 8 is by CD valve regulation, and return sludge ratio is by HI valve regulation; Each section of mud refluxes separately, avoids flora to mix, enhances impact resistance, adopts sequence batch (acidication-aerobic biochemical process, and acidication hydrolysis-acidifying-double oxygen and aerobic biochemical hyperoxia-hypoxemia residence time are respectively 14h and 9h.
2, wastewater source:
Wastewater source is in epoxy resin production plant washing step, and main water quality is as follows:
COD:5680mg/L, BOD5:1950mg/L, SS:950 mg/L, salinity: 7210mg/L, pH=9.5.
Basicity regulates and adopts sodium bicarbonate, technical grade.
3,
working condition:
1. production unit or structures comprise equalizing tank, coagulative precipitation tank, sequence batch (acidication-medium sediment pool-aerobic biochemical pool-second pond, coagulative precipitation tank, discharge pond, require as follows:
Equalizing tank: useful volume 12h factory effluent amount;
Coagulative precipitation tank: coagulation duration 10-15min, sedimentation time 3.0h;
Sequence batch (acidication-aerobic biochemical pool: hydrolysis-acidifying-oxygen hydraulic detention time of holding concurrently is respectively 6h-4h-4h, medium sediment pool residence time 3h; Hyperoxia-hypoxemia hydraulic retention is respectively 6h-3h, second pond residence time 4h;
Coagulative precipitation tank: coagulation duration 5-10min, sedimentation time 2.0h;
Discharge pond: useful volume 3h factory effluent amount.;
Coagulative precipitation tank adopts paddle agitator, power density 9kw/m
3;
Hydrolysis acidification pool adopts underwater scooter, power density 12kw/m
3;
Aeration uses gas blower, and blower air quantity configures variable ratio frequency changer according to gas/water than 25:1 and regulates;
Aerating system uses diaphragm type hole-variable aerator;
Sludge reflux pumping capacity is that wastewater flow rate 20-50% is adjustable;
Excess sludge adopts filter press dehydration;
Sodium bicarbonate is used for regulating waste water basicity, takes quantitative dosing method.
2. analytical test
COD detects and adopts GB GB11914 method; BOD5 detects and adopts GB GB7488 method; Salinity (muriate) adopts GB GB11896 method; PH value adopts GB GB6920 method to measure; GB7489 method is adopted to measure dissolved oxygen.
3. power supply facilities
3 phase power supplys, 380V; Possess gas blower, stirrer operational conditions.
four, water treatment effect:
Adopt sequence batch (acidication-aerobic biochemical process process epoxy resin production waste-water, the treatment effect of the every water-quality guideline in waste water is in table 1.
Table 1 each unit inlet/outlet water quality
Note: salinity: 7210mg/L.
Claims (3)
1. one kind high salt epoxy wastewater treatment process, key step is: first equalizing tank (1) receives Workshop Production waste water, start lift pump (12), waste water lifting is to coagulative precipitation tank (2), PAC and PAM is added to coagulative precipitation tank (2), open stirrer (18) simultaneously, after coagulation 15min, waste water is from sedimentation tank, settling tank supernatant liquor is from flowing into hydrolytic tank (3), and bottom settlings thing delivers to mud sheet frame dehydration (21) by sludge pump (13), deposits for preventing equalizing tank (1), intermittent aeration at the bottom of pond, originates from from gas blower (14); Secondly waste water is after hydrolytic tank (3) completes hydrolysis, and gravity flow enters acidification pool (4), adds sodium bicarbonate during acidifying in waste water; The waste water obtained flows into oxygen compatibility pool (5) and degrades to the macromole in waste water further, open air door (B), carry out intermittent air blast aeration, excess sludge delivers to mud sheet frame dehydration (21) by sludge pump (15), and upper clear supernate gravity flow is to hyperoxia pond (7); In hyperoxia pond (7), carry out high strength blast aeration, maintain the metabolism that aerobic microbiological is vigorous, waste water COD declines fast; Hypoxemia pond (8), carries out low intensity aeration, maintains microorganism concn and does not decline, and waste water COD is stable to decline; In Aerobic Pond, mixed solution enters second pond (9) solid-liquid separation, and mud is carried by sludge pump (16), partial reflux, and excess sludge delivers to mud sheet frame dehydration (21); Aerobic Pond dissolved oxygen concentration is by (C) (D) valve regulation, and return sludge ratio is by (H) (I) valve regulation; Waste water from second pond is entered second coagulation settling tank (10), PAC and PAM is added to coagulation basin, open stirrer (19) simultaneously, after coagulation 15min, waste water is from sedimentation tank, settling tank supernatant liquor is from flowing into discharge pond (11), and bottom settlings thing delivers to mud sheet frame dehydration (21) by sludge pump (17); Finally discharge pond (11) if water outlet is up to standard, then open (I) valve and arrange outward; If not up to standard, then open the backflow of (K) valve again to process, it is characterized in that: waste water is successively through hydrolysis-acidifying-oxygen-hyperoxia-hypoxemia operation of holding concurrently, insoluble pollutent dissolves at hydrolytic tank (3), macromole, Recalcitrant chemicals are converted into small molecules at acidification pool (4), the B/C of oxygen compatibility pool (5) improves further, and water quality biochemical is improved further; Hyperoxia pond (7) is by a large amount of labile organic compounds degraded inorganic molecules, and hypoxemia pond (8) decompose residual organic matter further, stablize effluent quality.
2. a kind of high salt epoxy wastewater treatment process according to claim 1, it is characterized in that: to connect afterwards medium sediment pool (6) at oxygen compatibility pool (5), precipitating sludge is back to hydrolysis-acidifying-oxygen of holding concurrently by sludge pump (15), and sludge reflux position and quantity of reflux control flexibly by reverse flow valve (E) (F) (G); To connect afterwards second pond in hypoxemia pond (8), mud by sludge pump (16) conveying, partial reflux, excess sludge delivers to mud sheet frame dehydration (21); Dissolved oxygen concentration in hyperoxia pond (7) and hypoxemia pond (8) is by (C) (D) valve regulation, and return sludge ratio is by (H) (I) valve regulation; Each section of mud refluxes separately, avoids flora to mix, enhances impact resistance.
3. a kind of high salt epoxy wastewater treatment process according to claim 1, is characterized in that: adopt sequence batch (acidication-aerobic biochemical process, and acidication (hydrolysis-acidifying-double oxygen) and aerobic biochemical (hyperoxia-hypoxemia) residence time are respectively 14h and 9h.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105712580A (en) * | 2016-03-07 | 2016-06-29 | 中蓝连海设计研究院 | Reduction treatment device and method for epoxy resin wastewater evaporative desalination mother liquor |
| CN108211771A (en) * | 2018-02-01 | 2018-06-29 | 重庆金茂达特种橡胶有限公司 | The waste gas processing method of rubber production technology |
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| CN104402166A (en) * | 2014-10-16 | 2015-03-11 | 滁州友林科技发展有限公司 | Industrial sewage treatment process |
| CN104478174A (en) * | 2014-12-19 | 2015-04-01 | 新疆环境工程技术有限责任公司 | High-salt-content dyeing wastewater treatment recovery zero discharge integration method |
-
2015
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Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
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| JP2014036959A (en) * | 2008-12-28 | 2014-02-27 | Metawater Co Ltd | Biological nitrogen removing device, water treatment system and carrier therefor |
| JP2010264440A (en) * | 2009-04-17 | 2010-11-25 | Nihon Hels Industry Corp | Phosphorus and nitrogen removing method by anaerobic, low-dissolved oxygen, and high-dissolved oxygen activated sludge process |
| CN104261633A (en) * | 2014-10-16 | 2015-01-07 | 滁州友林科技发展有限公司 | High-sludge industrial sewage treatment process |
| CN104402166A (en) * | 2014-10-16 | 2015-03-11 | 滁州友林科技发展有限公司 | Industrial sewage treatment process |
| CN104478174A (en) * | 2014-12-19 | 2015-04-01 | 新疆环境工程技术有限责任公司 | High-salt-content dyeing wastewater treatment recovery zero discharge integration method |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105712580A (en) * | 2016-03-07 | 2016-06-29 | 中蓝连海设计研究院 | Reduction treatment device and method for epoxy resin wastewater evaporative desalination mother liquor |
| CN108211771A (en) * | 2018-02-01 | 2018-06-29 | 重庆金茂达特种橡胶有限公司 | The waste gas processing method of rubber production technology |
| CN108211771B (en) * | 2018-02-01 | 2021-03-19 | 重庆金茂达特种橡胶有限公司 | Waste gas treatment method of rubber production process |
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