CN104556559B - A kind of processing method reducing COD of sewage - Google Patents
A kind of processing method reducing COD of sewage Download PDFInfo
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- CN104556559B CN104556559B CN201410740093.1A CN201410740093A CN104556559B CN 104556559 B CN104556559 B CN 104556559B CN 201410740093 A CN201410740093 A CN 201410740093A CN 104556559 B CN104556559 B CN 104556559B
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Abstract
The invention discloses a kind of processing method reducing COD of sewage: (1) cooling oil removing；(2) microelectrolysis processing；(3) oil interceptor processes；(4) further oil slick；(5) UASB reactor for treatment: above-mentioned waste water adding lignin and the mixing of wollastonite powder, enters UASB reactor, carry out anaerobic treatment, for several times, the Organic substance of this spent process water changes into methane in circulation；(6) Aeration tank processes: above waste water pumps into Aeration tank and carries out Aerobic Process for Treatment, allows the COD content in waste water reduce further, and the sewage after then processing is discharged to second pond and precipitates, and discharges mud, is purified water.
Description
Technical field
The present invention relates to sewage treatment area, particularly relate to a kind of processing method reducing COD of sewage.
Background technology
Modern sewage treatment technology, is divided by degree for the treatment of, can be divided into one-level, two grades and tertiary treatment.Coagulation, mainly removes the solid pollution material in suspended state in sewage, and physical treatment process major part can be only done the requirement of coagulation.Through the sewage of coagulation, BOD the most removable about 30%, do not reach discharge standard.Coagulation belongs to the pretreatment of two stage treatment.Two stage treatment, main removes in sewage in colloid and the organic pollution materials (BOD, COD material) of dissolved state, and clearance, up to more than 90%, makes organic pollution reach discharge standard.Tertiary treatment, processes the Organic substance of difficult degradation, nitrogen and phosphorus etc. further and can result in the soluble inorganic matter etc. of body eutrophication.Main method has biological carbon and phosphorous removal method, coagulant sedimentation, sand coarse aggregate ratio method, active carbon adsorption, ion exchange and electric osmose analytic process etc..Whole process be by the raw sewage of coarse rack through sewage pump promote after, through grid or sieve rate device, enter setting pot afterwards, sewage through girt-water separation enters primary sedimentation pond, it is more than coagulation (i.e. physical treatment), the water outlet of preliminary sedimentation tank enters biological treating equipment, active sludge and biomembrance process, (wherein the reactor of activated sludge process has Aeration tank, oxidation ditch etc., biomembrance process includes biofilter, biological rotating disk, biological contact oxidation process and biological fluidized bed), the water outlet of biological treating equipment enters secondary sedimentation tank, the water outlet of second pond is through sterilization discharge or enters tertiary treatment, it is two stage treatment that coagulation terminates to this, tertiary treatment includes biological carbon and phosphorous removal method, coagulant sedimentation, sand filtration method, active carbon adsorption, ion exchange and electroosmose process.A mud part for second pond is back to primary sedimentation pond or biological treating equipment, is partly into sludge concentration tank, enters sludge digestion tank afterwards, and after dehydration and drying equipment, mud is finally utilized.
UASB (up flow anaerobic sludge blanket reactor) is the high efficiency anaerobic reactor being most widely used at present, and reactor includes following components: intake and water distribution system, the cell body of reactor and three phase separator.In UASB reactor, most important equipment is three phase separator, and this equipment is arranged on the top of reactor and reactor is divided into the reaction zone of bottom and the settling zone on top.In order to obtain in depositor on the sedimentation effect of satisfaction of mud flco/granule in up-flow, first main purpose of three phase separator is exactly to separate the biogas produced from Sludge Bed/layer as efficiently as possible, particularly in the case of high load capacity, below collection chamber, the effect of reflecting plate is to prevent biogas from escaping into mud chamber by the gap between collection chamber, and the liquid wadding that in additionally baffle plate also helps minimizing reative cell, high yield tolerance is caused is dynamic.
Along with industrial expansion, more and more superelevation COD value industrial wastewaters are discharged, and are badly in need of solving, and the present inventor, in long-term production practices, finds when Optimizing Process Parameters, process under technique specific, it is possible to low cost, easily operate, efficiently reduce COD of sewage.
Summary of the invention
The technical problem existed based on background technology, the invention provides a kind of new method reducing COD of sewage, by optimizing the condition of technique, can be with low cost, and the method the most operatively processing superelevation COD industrial wastewater.
Technical scheme is as follows:
A kind of processing method reducing COD of sewage, it is characterised in that its step is as follows:
(1) cooling oil removing: trade effluent is entered cooling oil slick pond, reaches the effect of cooling and oil removing；
(2) microelectrolysis processing: then enter micro cell and carry out microelectrolysis processing, described electrolyzer has magnesium cation and ferrum cation, light electrolysis produces organic substance in hydroxide ion and iron ion, with waste water and carries out oxidation reaction, tentatively reduces the numerical value of COD；
(3) oil interceptor processes: the waste water after electrolysis is processed enters oil interceptor, is neutralized reaction by Calx and removes sulfate radical, by the PH numerical control of water at 7-9；
(4) further oil slick: continue waste water to enter the further oil slick of oil slick regulating reservoir；
(5) UASB reactor for treatment: above-mentioned waste water adding lignin and the mixing of wollastonite powder, enters UASB reactor, carry out anaerobic treatment, for several times, the Organic substance of this spent process water changes into methane in circulation；
(6) Aeration tank processes: above waste water pumps into Aeration tank and carries out Aerobic Process for Treatment, allows the COD content in waste water reduce further, and the sewage after then processing is discharged to second pond and precipitates, and discharges mud, is purified water.
What described step (5) added lignin and wollastonite is preferably: according to mass percent, the lignin of 3-5 ‰, the wollastonite powder of 1-1.5%.
Described step (5) is preferably: circulate 4 times, each 2 hours.
The invention have benefit that:
1, the processing method of the present invention has the effect of highly significant to the industrial wastewater of high COD high pollution, can the most effectively reduce COD value, vegetable and animals oils, ammonia nitrogen, and float, protects environment, and waste water treatment efficiency is high.
2, highly useful methane has been produced in twice laid；
3, the present invention is simple to operation, is suitable for large-scale production, and processing cost is cheap；
4, present invention discover that addition lignin and wollastonite can reach synergy before sewage enters UASB, more rapidly and efficiently reduce COD value；
5, can efficiently to process COD value the highest for the method for the present invention, pollutes the most serious industrial wastewater.
Detailed description of the invention
Embodiment 1:
Handled sewage quality is: water temperature=12～28 DEG C, COD=5000mg/L, BOD5=180～250mg/L, SS=150～200mg/L, NH4+-N=80～90mg/L, NO2--N < 0.3mg/L, NO3--N < 1.5mg/L, TP=7mg/L, pH=9.0～10.0.
A kind of processing method reducing COD of sewage:
(1) cooling oil removing: above-mentioned sewage is entered cooling oil slick pond, reaches the effect of cooling and oil removing；
(2) microelectrolysis processing: then enter micro cell and carry out microelectrolysis processing, described electrolyzer has magnesium cation and ferrum cation, light electrolysis produces hydroxide ion and iron ion, oxidation reaction is carried out with organic substance in waste water, tentatively reducing the numerical value of COD, now COD value is about 4200；
(3) oil interceptor processes: the waste water after electrolysis is processed enters oil interceptor, is neutralized reaction by Calx and removes sulfate radical, by the PH numerical control of water at 7-8；
(4) further oil slick: continue above-mentioned waste water to enter the further oil slick of oil slick regulating reservoir；
(5) UASB reactor for treatment: above-mentioned waste water is added lignin and the mixing of wollastonite powder, enter UASB reactor (in reactor, sludge concentration is 6000～8000mg/L) and carry out anaerobic treatment, circulate 4 times, each 2 hours, the Organic substance of this spent process water changes into methane, and in water, the amount of removing of COD is up to 95%；
(6) Aeration tank processes: above waste water pumps into Aeration tank and carries out Aerobic Process for Treatment, allows the COD content in waste water reduce further, and the sewage after then processing is discharged to second pond and precipitates, and discharges mud, is purified water.
Described step (5) adds lignin and wollastonite is: according to mass percent, the lignin of 3 ‰, the wollastonite powder of 1.5%.
To effluent quality after above-mentioned process it is: water temperature=12～28 DEG C, COD < 100mg/L, clearance more than 99%, BOD5=2mg/L, clearance more than 98%, SS < 1mg/L, almost all is removed, NH4+-N < 1mg/L, almost all is removed, TN < 10mg/L, and clearance is up to 90%, TP < 0.5mg/L, pH=7.0～8.0.
Embodiment 2:
Handled sewage quality is: water temperature=12～28 DEG C, COD=6000mg/L, BOD5=180～250mg/L, SS=150～200mg/L, NH4+-N=80～90mg/L, NO2--N < 0.3mg/L, NO3--N < 1.5mg/L, TP=7mg/L, pH=9.0～10.0.
A kind of processing method reducing COD of sewage:
(1) cooling oil removing: above-mentioned sewage is entered cooling oil slick pond, reaches the effect of cooling and oil removing；
(2) microelectrolysis processing: then enter micro cell and carry out microelectrolysis processing, described electrolyzer has magnesium cation and ferrum cation, light electrolysis produces hydroxide ion and iron ion, oxidation reaction is carried out with organic substance in waste water, tentatively reducing the numerical value of COD, now COD value is about 4900；
(3) oil interceptor processes: the waste water after electrolysis is processed enters oil interceptor, is neutralized reaction by Calx and removes sulfate radical, by the PH numerical control of water at 7-8；
(4) further oil slick: continue above-mentioned waste water to enter the further oil slick of oil slick regulating reservoir；
(5) UASB reactor for treatment: above-mentioned waste water is added lignin and the mixing of wollastonite powder, enter UASB reactor (in reactor, sludge concentration is 6000～8000mg/L) and carry out anaerobic treatment, circulate 4 times, each 2 hours, the Organic substance of this spent process water changes into methane, and in water, the amount of removing of COD is up to 95%；
(6) Aeration tank processes: above waste water pumps into Aeration tank and carries out Aerobic Process for Treatment, allows the COD content in waste water reduce further, and the sewage after then processing is discharged to second pond and precipitates, and discharges mud, is purified water.
Described step (5) adds lignin and wollastonite is: according to mass percent, the lignin of 5 ‰, the wollastonite powder of 1%.
To effluent quality after above-mentioned process it is: water temperature=12～28 DEG C, COD < 110mg/L, clearance more than 99%, BOD5=2mg/L, clearance more than 98%, SS < 1mg/L, almost all is removed, NH4+-N < 1mg/L, almost all is removed, TN < 10mg/L, and clearance is up to 90%, TP < 0.5mg/L, pH=7.0～8.0.
Embodiment 3:
Handled sewage quality is: water temperature=12～28 DEG C, COD=3000mg/L, BOD5=180～250mg/L, SS=150～200mg/L, NH4+-N=80～90mg/L, NO2--N < 0.3mg/L, NO3--N < 1.5mg/L, TP=7mg/L, pH=9.0～10.0.
A kind of processing method reducing COD of sewage:
(1) cooling oil removing: above-mentioned sewage is entered cooling oil slick pond, reaches the effect of cooling and oil removing；
(2) microelectrolysis processing: then enter micro cell and carry out microelectrolysis processing, described electrolyzer has magnesium cation and ferrum cation, light electrolysis produces hydroxide ion and iron ion, oxidation reaction is carried out with organic substance in waste water, tentatively reducing the numerical value of COD, now COD value is about 2500；
(3) oil interceptor processes: the waste water after electrolysis is processed enters oil interceptor, is neutralized reaction by Calx and removes sulfate radical, by the PH numerical control of water at 7-8；
(4) further oil slick: continue above-mentioned waste water to enter the further oil slick of oil slick regulating reservoir；
(5) UASB reactor for treatment: above-mentioned waste water is added lignin and the mixing of wollastonite powder, enter UASB reactor (in reactor, sludge concentration is 6000～8000mg/L) and carry out anaerobic treatment, circulate 4 times, each 2 hours, the Organic substance of this spent process water changes into methane, and in water, the amount of removing of COD is up to 95%；
(6) Aeration tank processes: above waste water pumps into Aeration tank and carries out Aerobic Process for Treatment, allows the COD content in waste water reduce further, and the sewage after then processing is discharged to second pond and precipitates, and discharges mud, is purified water.
Described step (5) adds lignin and wollastonite is: according to mass percent, the lignin of 4 ‰, the wollastonite powder of 1.2%.
To effluent quality after above-mentioned process it is: water temperature=12～28 DEG C, COD < 30mg/L, clearance more than 99%, BOD5=2mg/L, clearance more than 98%, SS < 1mg/L, almost all is removed, NH4+-N < 1mg/L, almost all is removed, TN < 10mg/L, and clearance is up to 90%, TP < 0.5mg/L, pH=7.0～8.0.
Embodiment 4:
Handled sewage quality is: water temperature=12～28 DEG C, COD=8000mg/L, BOD5=180～250mg/L, SS=150～200mg/L, NH4+-N=80～90mg/L, NO2--N < 0.3mg/L, NO3--N < 1.5mg/L, TP=7mg/L, pH=9.0～10.0.
A kind of processing method reducing COD of sewage:
(1) cooling oil removing: above-mentioned sewage is entered cooling oil slick pond, reaches the effect of cooling and oil removing；
(2) microelectrolysis processing: then enter micro cell and carry out microelectrolysis processing, described electrolyzer has magnesium cation and ferrum cation, light electrolysis produces hydroxide ion and iron ion, oxidation reaction is carried out with organic substance in waste water, tentatively reducing the numerical value of COD, now COD value is about 6500；
(3) oil interceptor processes: the waste water after electrolysis is processed enters oil interceptor, is neutralized reaction by Calx and removes sulfate radical, by the PH numerical control of water at 7-8；
(4) further oil slick: continue above-mentioned waste water to enter the further oil slick of oil slick regulating reservoir；
(5) UASB reactor for treatment: above-mentioned waste water is added lignin and the mixing of wollastonite powder, enter UASB reactor (in reactor, sludge concentration is 6000～8000mg/L) and carry out anaerobic treatment, circulate 4 times, each 2 hours, the Organic substance of this spent process water changes into methane, and in water, the amount of removing of COD is up to 95%；
(6) Aeration tank processes: above waste water pumps into Aeration tank and carries out Aerobic Process for Treatment, allows the COD content in waste water reduce further, and the sewage after then processing is discharged to second pond and precipitates, and discharges mud, is purified water.
Described step (5) adds lignin and wollastonite is: according to mass percent, the lignin of 3 ‰, the wollastonite powder of 1%.
To effluent quality after above-mentioned process it is: water temperature=12～28 DEG C, COD < 300mg/L, clearance more than 99%, BOD5=2mg/L, clearance more than 98%, SS < 1mg/L, almost all is removed, NH4+-N < 1mg/L, almost all is removed, TN < 10mg/L, and clearance is up to 90%, TP < 0.5mg/L, pH=7.0～8.0.
Embodiment 5:
Handled sewage quality is: water temperature=12～28 DEG C, COD=2000mg/L, BOD5=180～250mg/L, SS=150～200mg/L, NH4+-N=80～90mg/L, NO2--N < 0.3mg/L, NO3--N < 1.5mg/L, TP=7mg/L, pH=9.0～10.0.
A kind of processing method reducing COD of sewage:
(1) cooling oil removing: above-mentioned sewage is entered cooling oil slick pond, reaches the effect of cooling and oil removing；
(2) microelectrolysis processing: then enter micro cell and carry out microelectrolysis processing, described electrolyzer has magnesium cation and ferrum cation, light electrolysis produces hydroxide ion and iron ion, oxidation reaction is carried out with organic substance in waste water, tentatively reducing the numerical value of COD, now COD value is about 1600；
(3) oil interceptor processes: the waste water after electrolysis is processed enters oil interceptor, is neutralized reaction by Calx and removes sulfate radical, by the PH numerical control of water at 7-8；
(4) further oil slick: continue above-mentioned waste water to enter the further oil slick of oil slick regulating reservoir；
(5) UASB reactor for treatment: above-mentioned waste water is added lignin and the mixing of wollastonite powder, enter UASB reactor (in reactor, sludge concentration is 6000～8000mg/L) and carry out anaerobic treatment, circulate 4 times, each 2 hours, the Organic substance of this spent process water changes into methane, and in water, the amount of removing of COD is up to 95%；
(6) Aeration tank processes: above waste water pumps into Aeration tank and carries out Aerobic Process for Treatment, allows the COD content in waste water reduce further, and the sewage after then processing is discharged to second pond and precipitates, and discharges mud, is purified water.
Described step (5) adds lignin and wollastonite is: according to mass percent, the lignin of 4.5 ‰, the wollastonite powder of 1.1%.
To effluent quality after above-mentioned process it is: water temperature=12～28 DEG C, COD < 20mg/L, clearance more than 99%, BOD5=2mg/L, clearance more than 98%, SS < 1mg/L, almost all is removed, NH4+-N < 1mg/L, almost all is removed, TN < 10mg/L, and clearance is up to 90%, TP < 0.5mg/L, pH=7.0～8.0.
The above; it is only the present invention preferably detailed description of the invention; but protection scope of the present invention is not limited thereto; any those familiar with the art is in the technical scope that the invention discloses; according to technical scheme and inventive concept equivalent or change in addition thereof, all should contain within protection scope of the present invention.
Claims (1)
1. the processing method reducing COD of sewage, it is characterised in that its step is as follows:
(1) cooling oil removing: trade effluent is entered cooling oil slick pond, reaches the effect of cooling and oil removing；
(2) microelectrolysis processing: then enter micro cell and carry out microelectrolysis processing, has magnesium cation and ferrum cation in described electrolyzer, light electrolysis produces organic substance in hydroxide ion and iron ion, with waste water and carries out oxidation reaction, tentatively reduces the numerical value of COD；
(3) oil interceptor processes: the waste water after electrolysis is processed enters oil interceptor, is neutralized reaction by Calx and removes sulfate radical, by the pH numerical control of water at 7-9；
(4) further oil slick: continue waste water to enter the further oil slick of oil slick regulating reservoir；
(5) UASB reactor for treatment: above-mentioned waste water adding lignin and the mixing of wollastonite powder, enters UASB reactor, carry out anaerobic treatment, circulate 4 times, each 2 hours, the Organic substance of this spent process water changed into methane；
(6) Aeration tank processes: above waste water pumps into Aeration tank and carries out Aerobic Process for Treatment, allows the COD content in waste water reduce further, and the sewage after then processing is discharged to second pond and precipitates, and discharges mud, is purified water；
Described step (5) adds lignin and wollastonite is: according to mass percent, the lignin of 3-5 ‰, the wollastonite powder of 1-1.5%.
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| KR100703890B1 (en) * | 2006-05-26 | 2007-04-04 | (주)에코데이 | Plant for high concentration wastewater treatment by anaerobic and aerobic digestion |
| CN101376552A (en) * | 2008-09-19 | 2009-03-04 | 紫金矿业集团股份有限公司 | Process for processing high concentration refractory organic wastewater containing paratoluidine |
| CN101648762A (en) * | 2009-08-31 | 2010-02-17 | 江苏华能环境工程有限公司 | Coking wastewater treatment method |
| CN202671358U (en) * | 2012-07-16 | 2013-01-16 | 煤炭工业济南设计研究院有限公司 | Coating waste water processing device |
| CN203144244U (en) * | 2013-03-27 | 2013-08-21 | 重庆地质矿产研究院 | High-efficiency treatment system for industrial wastewater difficult to degrade |
| CN103599745A (en) * | 2013-12-04 | 2014-02-26 | 江南大学 | Modified calcium silicate and its application in sewage dephosphorization |
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