CN103420543A - Processing method of production waste water containing sulfo fluorescent whitening agent - Google Patents
Processing method of production waste water containing sulfo fluorescent whitening agent Download PDFInfo
- Publication number
- CN103420543A CN103420543A CN2013103517689A CN201310351768A CN103420543A CN 103420543 A CN103420543 A CN 103420543A CN 2013103517689 A CN2013103517689 A CN 2013103517689A CN 201310351768 A CN201310351768 A CN 201310351768A CN 103420543 A CN103420543 A CN 103420543A
- Authority
- CN
- China
- Prior art keywords
- reactor
- pond
- hydraulic detention
- water
- detention time
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Landscapes
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The invention relates to a processing method of production waste water containing sulfo fluorescent whitening agent and aims to solve the problem that the existing fluorescent whitening agent production waste water processing is high in cost and poor in effect. According to the technical scheme, the acidification-biochemistry-physico-chemistry-biochemistry processing method includes: an equalization tank, an acidification tank, a primary settling tank, a hydrolysis acidification reactor, an IC reactor, a Fenton oxidization reactor, a secondary settling tank, an A/O reactor, a third settling tank, an ozonization processing unit and a sludge thickening tank which are sequentially connected. The whole system can be operate stably and continuously. The processing method is low in cost and good in effect.
Description
Technical field
The present invention relates to a kind for the treatment of process containing the sulfonic group fluorescent brightener production wastewater.This method can effectively be degraded containing most of hardly degraded organic substance in the sulfonic group fluorescent brightener production wastewater and be removed ammonia nitrogen, is mainly used in the processing of the white dyes waste water that high salinity, high ammonia nitrogen and hazardous and noxious substances are many.
Background technology
White dyes is a class light colour photoluminescence dyestuff.Under UV-light-irradiation, white dyes can inspire indigo plant, purple light, complementary and have whitening effect with gold-tinted on painted matrix, in industries such as weaving, papermaking, washing, plastics, rubber, pigment and paint, is widely used.Wherein, the ratio of sulfonic acid fundamental mode white dyes (hereinafter to be referred as " white dyes ") in whole whitening agent field surpasses 80%, is the topmost classification of white dyes family.
The raw materials for production of white dyes or middle by-product mostly are hazardous and noxious substances, as DSD acid, cyanuric chloride, aniline, morpholine and aniline sulfonic acid etc., above-mentioned substance is because containing phenyl ring, amino or azepine aromatic nucleus functional group etc., make the Biostatic of this waste water strong, biodegradable performance variation.The BOD of this waste water
5/ COD
CrValue generally is no more than 0.3.In addition, in the white dyes production process, acid adjustment and adjust the alkali operation to cause in waste water sodium chloride concentration higher frequently, the concentration of sodium-chlor even surpasses 10000mg/L, higher sodium chloride concentration will cause the change of osmotic pressure in microorganism cells in biochemical treatment of wastewater, cause cell plasmolysis and death.The research of the fluorescent brightener production wastewater treatment process of highly effective has important practical significance.
At present, the treatment process of fluorescent brightener production wastewater has a variety of, mainly comprises following three classes: the materilization freatment methods such as iron-carbon micro-electrolysis, Wet Catalytic Oxidation Method, Ozonation, Fenton; Traditional biochemical processing methods such as Biological Contact Oxidation Process, A/O technique, SBR technique, UASB technique; The materialization-biochemistry combination treatment method.The materialization treatment process is the organism of difficult degradation in white dyes waste water effectively, but processing cost is high, and ammonia nitrogen is not had to removal effect mostly; Traditional biochemical processing process is difficult to bear high salinity, high Biostatic and Johnson & Johnson's thing toxicity, to the poor processing effect of hardly degraded organic substance.
The materialization-biochemistry combination treatment method formula main development direction that fluorescent brightener production wastewater is processed in recent years, have a small amount of relevant report.As: CN101423313A discloses the processing route of " aeration iron-carbon micro-electrolysis-acidication-aerobe processing-ozone oxidation ", CN101830601A discloses the processing route of " coagulating sedimentation-acidication-aerobic oxidation-ultrasonic degradation-membrane biological reaction is processed ", but the contradiction between the good cost of Balance Treatment and treatment effect, materialization stage organic matter removal and the supply of biochemical stage denitrification organic carbon source etc. is still the subject matter that this method need solve.
Summary of the invention
The objective of the invention is to overcome the deficiency of existing fluorescent brightener production wastewater treatment technology, a kind for the treatment of process containing the sulfonic group fluorescent brightener production wastewater is provided.
The technical scheme that the present invention takes for achieving the above object is:
A kind for the treatment of process containing the sulfonic group fluorescent brightener production wastewater, comprise: homogeneous pond, acid out pond, preliminary sedimentation tank, reactor for hydrolysis and acidification, IC reactor, Fenton oxidation reactor, second pond, A/O reactor, three heavy pond, ozonation treatment unit and sludge thickeners, described homogeneous pond, acid out pond, preliminary sedimentation tank, reactor for hydrolysis and acidification, IC reactor, Fenton oxidation reactor, second pond, A/O reactor, three heavy ponds, ozonation treatment unit are connected successively with sludge thickener, the operation of whole system steady and continuous; Concrete steps are as follows:
(1), the factory effluent that contains the sulfonic group white dyes of variant production all entered to the homogeneous pond mix, the hydraulic detention time in the homogeneous pond is 1d～7d;
(2), the waste water in step (1) homogeneous pond is entered to the acid out pond, with acid, be adjusted to acidity, the hydraulic detention time in acid out pond is 20min～60min;
(3), after the water outlet in acid out pond adds coagulating agent, enter preliminary sedimentation tank, the hydraulic detention time of preliminary sedimentation tank is 3h～20h, and wherein coagulating agent is polyacrylamide or polymerize aluminum chloride, and the consumption of polyacrylamide or polymerize aluminum chloride is 0.5～30mg/L;
(4), the preliminary sedimentation tank water outlet enters reactor for hydrolysis and acidification, the temperature of regulating waste water in reactor for hydrolysis and acidification is 10 ℃～40 ℃, hydraulic detention time is 1.5d～5d;
(5), after 0.5～2 times of the water outlet of reactor for hydrolysis and acidification dilution, add nutritive substance, enter the IC reactor, the temperature of regulating waste water in the IC reactor is 20 ℃～40 ℃, hydraulic detention time is 1.5d～5d, and water part is back to water inlet place of IC reactor, and reflux ratio is 0%～300%; Sanitary sewage, excrement of animals water or the glucose of wherein said nutritive substance for the carbon nutrient is provided; The potassium primary phosphate of phosphorus nutrient is provided, and the urea of nitrogen nutrient is provided, but the dosage of nutritive substance is according to being the water quality biochemical values (B/C value) >=25% of controlling the IC water inlet;
(6), the water outlet of IC reactor enters the Fenton oxidation reactor, by drug feeding pipeline, adds acid, ferrous sulfate, hydrogen peroxide, Fe
2+Concentration be 0.001mol/L～0.02mol/L, H
2O
2And Fe
2+Mol ratio be 1～10:1;
(7), the water outlet of Fenton oxidation reactor through in alkali lye and after, adding polyacrylamide to its concentration is 0.5～50mg/L, then enters second pond, the hydraulic detention time of second pond is 3h～20h;
(8), the second pond water outlet enters the A/O reactor, the temperature of regulating waste water in the A/O reactor is 10 ℃～40 ℃, hydraulic detention time is 1.5d～5d, water part is back to water inlet place of A/O reactor, reflux ratio is 100%～300%;
(9), the water outlet of A/O reactor enters three heavy ponds, the hydraulic detention times in three heavy ponds are 3h～20h;
(10), the water outlets in three heavy ponds enter the ozonation treatment unit, the ozone-depleting amount is 0.003g/Lmin～0.18g/Lmin, hydraulic detention time is 1min～60min;
(11), the mud in preliminary sedimentation tank, second pond and three heavy ponds is all entered to sludge thickener;
(12), the mud in sludge thickener after the mechanism filter-pressing dehydration, dry mud is transported to sludge ultimate disposal ground outward, sewage backflow is to the acid out pond.
Acid in described step (2) is one or more in sulfuric acid, hydrochloric acid and nitric acid, the PH:5.0 of waste water～6.5 after acid adjustment.
In described step (3), the hydraulic detention time of preliminary sedimentation tank is 8h～12h.
The temperature of regulating waste water in reactor for hydrolysis and acidification in described step (4) is 28 ℃～35 ℃, and hydraulic detention time is 2.5d～4d.
In described step (5), the temperature of the interior waste water of IC reactor is 32 ℃～38 ℃, and hydraulic detention time is 2.5d～4d; IC reactor water part is back to water inlet place of IC reactor, and reflux ratio is 100%～200%.
Fe in described step (6)
2+Concentration be 0.002mol/L～0.005mol/L, H
2O
2And Fe
2+Mol ratio be 2:1～4:1.
In described step (7), the hydraulic detention time of second pond is 8h～12h.
In described step (8), the temperature of the interior waste water of A/O reactor is 25 ℃～33 ℃, and hydraulic detention time is 2.5d～4d, and water part is back to water inlet place of A/O reactor, and reflux ratio is 100%～200%.
In described step (9), the hydraulic detention time in three heavy ponds is 8h～12h.
In described step (10), ozonation treatment unit consumption ozone amount is 0.006g/Lmin～0.03g/Lmin, and hydraulic detention time is 2min～10min.
The characteristics that the sulfonic group compound is easily separated out in pH value reduction situation, the present invention is by simple acid out coprecipitation mode, can remove this part sulfonic group compound, the biodegradability of waste water be improved significantly, its water outlet is diluted with after reducing salts contg through suitable, then removes a large amount of COD through anaerobic biological processing cheaply; Treat anaerobic effluent remaining be mainly in the material situation of bad biochemistry, then, by the strong oxidizing reaction of Fenton, again promote BOD
5Value, with A/O biochemical system cheaply, processed again, to remove COD and most ammonia nitrogen of most of surplus, thus the contradiction between Balance Treatment cost and treatment effect etc. well, in alap cost situation, realized good water treatment effect.
The accompanying drawing explanation
Fig. 1 is the schema for the treatment of process of the present invention.
Embodiment
Embodiment 1
(1) 71
#, VBL, 31
#, the fluorescent brightener production wastewater such as BA and APC enters the homogeneous pond and mixes, pH value is 8～10, waste water COD and ammonia nitrogen are respectively 7500mg/L, 38mg/L; Hydraulic detention time is 3d;
(2) homogeneous pond waste water is entered to the acid out pond with the flow continuous self-flowing of 18～24t/h, with the vitriol oil, waste water PH is adjusted to 6.0～6.5, the hydraulic detention time in acid out pond is 30min;
(3) after the water outlet of acid out pond adds the polyacrylamide of 20mg/L, with the flow continuous self-flowing of 18～24t/h, enter preliminary sedimentation tank, the hydraulic detention time of preliminary sedimentation tank is 8h;
(4) the preliminary sedimentation tank water outlet is carried by pump, with the flow of 18～24t/h, enters anaerobic hydrolysis acidification reactor, and in reactor for hydrolysis and acidification, the temperature of waste water is 28 ℃～35 ℃, and hydraulic detention time is 3d;
(5) the reactor for hydrolysis and acidification water outlet is diluted with the clear water of 1.2 times, the sanitary sewage and the dirty swine ight soil water that add 36～48Kg/ hour, the flow of carrying with 39～53t/h by pump enters the IC reactor, in the IC reactor, the temperature of waste water is 32 ℃～38 ℃, hydraulic detention time is 3d, IC reactor water part is back to water inlet place of IC reactor, and reflux ratio is 200%;
(6) water outlet of IC reactor enters the Fenton oxidation reactor continuously with the flow gravity flow of 39～53t/h, by drug feeding pipeline, adds acid, ferrous sulfate and hydrogen peroxide, and the control pH value is 3, Fe
2+Concentration be 0.003mol/L, H
2O
2And Fe
2+Mol ratio be 3:1;
(7) water outlet of Fenton oxidation reactor through with in 30% sodium hydroxide solution and after, adding polyacrylamide to its concentration is 20mg/L, with the gravity flow of the flow of 39～53t/h, enters second pond, the hydraulic detention time of second pond is 8h;
(8) flow that the second pond water outlet is carried with 39～53t/h by pump enters the A/O reactor, and in the A/O reactor, the temperature of waste water is 25 ℃～33 ℃, and hydraulic detention time is 3d, and A/O reactor water part is back to water inlet place of A/O reactor, and reflux ratio is 200%;
(9) water outlet of A/O reactor enters three heavy ponds continuously with the flow gravity flow of 39～53t/h, and the hydraulic detention time in three heavy ponds is 12h;
(10) three sinking pool effluents enter the ozonation treatment unit continuously with the flow gravity flow of 39～53t/h, and the ozone-depleting amount is 0.013g/Lmin, and hydraulic detention time is 6min;
(11) mud in preliminary sedimentation tank, second pond and three heavy ponds all enters sludge thickener;
(12) after the dehydration of sludge thickener mud mechanism filter-pressing, dry mud is transported to sludge ultimate disposal ground outward, and sewage backflow is to the acid out pond.
Processing by step 1～12, the COD of fluorescent brightener production wastewater, ammonia nitrogen and colourity have obtained effective removal, three sinking pool effluent COD, ammonia nitrogen and colourity are respectively 98mg/L, 5mg/L and 22, and the COD of system and the clearance of ammonia nitrogen are respectively 97.4% and 86.8%.
Embodiment 2
Step (5) reactor for hydrolysis and acidification water outlet is diluted with the clear water of 1.5 times, and the corresponding flow from step (5) beginning water becomes 45～60t/h, and other step is identical with example 1.
By the processing of step 1～12, the COD of fluorescent brightener production wastewater, ammonia nitrogen and colourity are respectively 87mg/L, 8mg/L and 25, and the COD of system and the clearance of ammonia nitrogen are respectively 97.7% and 78.9%.
Embodiment 3
Step (10) ozone-depleting amount is 0.026g/Lmin, and other step is identical with example 1.
By the processing of step 1～12, the COD of fluorescent brightener production wastewater, ammonia nitrogen and colourity are respectively 79mg/L, 5mg/L and 22, and the COD of system and the clearance of ammonia nitrogen are respectively 97.9% and 86.8%.
Claims (10)
1. the treatment process containing the sulfonic group fluorescent brightener production wastewater, it is characterized in that comprising: homogeneous pond, acid out pond, preliminary sedimentation tank, reactor for hydrolysis and acidification, IC reactor, Fenton oxidation reactor, second pond, A/O reactor, three heavy pond, ozonation treatment unit and sludge thickeners, described homogeneous pond, acid out pond, preliminary sedimentation tank, reactor for hydrolysis and acidification, IC reactor, Fenton oxidation reactor, second pond, A/O reactor, three heavy ponds, ozonation treatment unit are connected successively with sludge thickener, the operation of whole system steady and continuous; Concrete steps are as follows:
(1), the factory effluent that contains the sulfonic group white dyes of variant production all entered to the homogeneous pond mix, the hydraulic detention time in the homogeneous pond is 1d～7d;
(2), the waste water in step (1) homogeneous pond is entered to the acid out pond, with acid, be adjusted to acidity, the hydraulic detention time in acid out pond is 20min～60min;
(3), after the water outlet in acid out pond adds coagulating agent, enter preliminary sedimentation tank, the hydraulic detention time of preliminary sedimentation tank is 3h～20h, and wherein coagulating agent is polyacrylamide or polymerize aluminum chloride, and the consumption of polyacrylamide or polymerize aluminum chloride is 0.5～30mg/L;
(4), the preliminary sedimentation tank water outlet enters reactor for hydrolysis and acidification, the temperature of regulating waste water in reactor for hydrolysis and acidification is 10 ℃～40 ℃, hydraulic detention time is 1.5d～5d;
(5), after 0.5～2 times of the water outlet of reactor for hydrolysis and acidification dilution, add nutritive substance, enter the IC reactor, the temperature of regulating waste water in the IC reactor is 20 ℃～40 ℃, hydraulic detention time is 1.5d～5d, and water part is back to water inlet place of IC reactor, and reflux ratio is 0%～300%; Sanitary sewage, excrement of animals water or the glucose of wherein said nutritive substance for the carbon nutrient is provided; The potassium primary phosphate of phosphorus nutrient is provided, and the urea of nitrogen nutrient is provided, but the dosage of nutritive substance is according to being the water quality biochemical values (B/C value) >=25% of controlling the IC water inlet;
(6), the water outlet of IC reactor enters the Fenton oxidation reactor, by drug feeding pipeline, adds acid, ferrous sulfate, hydrogen peroxide, Fe
2+Concentration be 0.001mol/L～0.02mol/L, H
2O
2And Fe
2+Mol ratio be 1～10:1;
(7), the water outlet of Fenton oxidation reactor through in alkali lye and after, adding polyacrylamide to its concentration is 0.5～50mg/L, then enters second pond, the hydraulic detention time of second pond is 3h～20h;
(8), the second pond water outlet enters the A/O reactor, the temperature of regulating waste water in the A/O reactor is 10 ℃～40 ℃, hydraulic detention time is 1.5d～5d, water part is back to water inlet place of A/O reactor, reflux ratio is 100%～300%;
(9), the water outlet of A/O reactor enters three heavy ponds, the hydraulic detention times in three heavy ponds are 3h～20h;
(10), the water outlets in three heavy ponds enter the ozonation treatment unit, the ozone-depleting amount is 0.003g/Lmin～0.18g/Lmin, hydraulic detention time is 1min～60min;
(11), the mud in preliminary sedimentation tank, second pond and three heavy ponds is all entered to sludge thickener;
(12), the mud in sludge thickener after the mechanism filter-pressing dehydration, dry mud is transported to sludge ultimate disposal ground outward, sewage backflow is to the acid out pond.
2. a kind for the treatment of process containing the sulfonic group fluorescent brightener production wastewater according to claim 1, it is characterized in that: the acid in described step (2) is one or more in sulfuric acid, hydrochloric acid and nitric acid, the PH:5.0 of waste water～6.5 after acid adjustment.
3. a kind for the treatment of process containing the sulfonic group fluorescent brightener production wastewater according to claim 1, it is characterized in that: in described step (3), the hydraulic detention time of preliminary sedimentation tank is 8h～12h.
4. a kind for the treatment of process containing the sulfonic group fluorescent brightener production wastewater according to claim 1, it is characterized in that: the temperature of regulating waste water in reactor for hydrolysis and acidification in described step (4) is 28 ℃～35 ℃, and hydraulic detention time is 2.5d～4d.
5. a kind for the treatment of process containing the sulfonic group fluorescent brightener production wastewater according to claim 1 is characterized in that: in described step (5) in the IC reactor temperature of waste water be 32 ℃～38 ℃, hydraulic detention time is 2.5d～4d; IC reactor water part is back to water inlet place of IC reactor, and reflux ratio is 100%～200%.
6. a kind for the treatment of process containing the sulfonic group fluorescent brightener production wastewater according to claim 1, is characterized in that: Fe in described step (6)
2+Concentration be 0.002mol/L～0.005mol/L, H
2O
2And Fe
2+Mol ratio be 2:1～4:1.
7. a kind for the treatment of process containing the sulfonic group fluorescent brightener production wastewater according to claim 1, it is characterized in that: in described step (7), the hydraulic detention time of second pond is 8h～12h.
8. a kind for the treatment of process containing the sulfonic group fluorescent brightener production wastewater according to claim 1, it is characterized in that: in described step (8), the temperature of the interior waste water of A/O reactor is 25 ℃～33 ℃, hydraulic detention time is 2.5d～4d, water part is back to water inlet place of A/O reactor, and reflux ratio is 100%～200%.
9. a kind for the treatment of process containing the sulfonic group fluorescent brightener production wastewater according to claim 1, it is characterized in that: in described step (9), the hydraulic detention times in three heavy ponds are 8h～12h.
10. a kind for the treatment of process containing the sulfonic group fluorescent brightener production wastewater according to claim 1, it is characterized in that: in described step (10), ozonation treatment unit consumption ozone amount is 0.006g/Lmin～0.03g/Lmin, and hydraulic detention time is 2min～10min.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310351768.9A CN103420543B (en) | 2013-08-13 | 2013-08-13 | Processing method of production waste water containing sulfo fluorescent whitening agent |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310351768.9A CN103420543B (en) | 2013-08-13 | 2013-08-13 | Processing method of production waste water containing sulfo fluorescent whitening agent |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103420543A true CN103420543A (en) | 2013-12-04 |
| CN103420543B CN103420543B (en) | 2014-07-23 |
Family
ID=49645984
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310351768.9A Active CN103420543B (en) | 2013-08-13 | 2013-08-13 | Processing method of production waste water containing sulfo fluorescent whitening agent |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103420543B (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103739157A (en) * | 2013-12-24 | 2014-04-23 | 中山市环保实业发展有限公司 | Method for processing middle and late period of landfill leachate |
| CN104193065A (en) * | 2014-09-17 | 2014-12-10 | 山西青山化工有限公司 | Treatment method for wastewater containing fluorescent whitening agent |
| CN104926019A (en) * | 2015-05-20 | 2015-09-23 | 安徽建筑大学 | Treatment system for high-carbon-and-nitrogen wastewater |
| CN105293839A (en) * | 2015-11-26 | 2016-02-03 | 山西青山化工有限公司 | Low-boiling point fraction treatment method for fluorescent brightener CBS wastewater |
| CN113307380A (en) * | 2021-05-24 | 2021-08-27 | 东华大学 | Underground water zero-valent iron-modified biochar composite packed column polyculture denitrification method and permeable reactive barrier |
| CN114105396A (en) * | 2020-08-31 | 2022-03-01 | 南京工大环境科技有限公司 | Process method for efficiently treating Lyocell short fiber wastewater |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20020017866A (en) * | 2000-08-31 | 2002-03-07 | 변기식 | The Wastewater Treatment Method and its System |
| CN101830601A (en) * | 2010-04-30 | 2010-09-15 | 浙江大学 | Biological treatment system and method thereof specific to industrial wastewater of fluorescent brightener |
| KR20110132709A (en) * | 2010-06-03 | 2011-12-09 | 한양대학교 산학협력단 | Magnetite nano particle-carrer complex, method for fabricating the same and sewage-pollution water purifying system including the same |
| JP2012040506A (en) * | 2010-08-19 | 2012-03-01 | Fuji Xerox Co Ltd | Water treatment apparatus and water treatment method |
| CN102951693A (en) * | 2012-11-21 | 2013-03-06 | 山西青山化工有限公司 | Method for processing and recycling production wastewater of fluorescent brightener CBS |
| CN202898159U (en) * | 2012-06-01 | 2013-04-24 | 中国石油天然气股份有限公司 | Sewage treatment device |
-
2013
- 2013-08-13 CN CN201310351768.9A patent/CN103420543B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20020017866A (en) * | 2000-08-31 | 2002-03-07 | 변기식 | The Wastewater Treatment Method and its System |
| CN101830601A (en) * | 2010-04-30 | 2010-09-15 | 浙江大学 | Biological treatment system and method thereof specific to industrial wastewater of fluorescent brightener |
| KR20110132709A (en) * | 2010-06-03 | 2011-12-09 | 한양대학교 산학협력단 | Magnetite nano particle-carrer complex, method for fabricating the same and sewage-pollution water purifying system including the same |
| JP2012040506A (en) * | 2010-08-19 | 2012-03-01 | Fuji Xerox Co Ltd | Water treatment apparatus and water treatment method |
| CN202898159U (en) * | 2012-06-01 | 2013-04-24 | 中国石油天然气股份有限公司 | Sewage treatment device |
| CN102951693A (en) * | 2012-11-21 | 2013-03-06 | 山西青山化工有限公司 | Method for processing and recycling production wastewater of fluorescent brightener CBS |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103739157A (en) * | 2013-12-24 | 2014-04-23 | 中山市环保实业发展有限公司 | Method for processing middle and late period of landfill leachate |
| CN104193065A (en) * | 2014-09-17 | 2014-12-10 | 山西青山化工有限公司 | Treatment method for wastewater containing fluorescent whitening agent |
| CN104926019A (en) * | 2015-05-20 | 2015-09-23 | 安徽建筑大学 | Treatment system for high-carbon-and-nitrogen wastewater |
| CN105293839A (en) * | 2015-11-26 | 2016-02-03 | 山西青山化工有限公司 | Low-boiling point fraction treatment method for fluorescent brightener CBS wastewater |
| CN114105396A (en) * | 2020-08-31 | 2022-03-01 | 南京工大环境科技有限公司 | Process method for efficiently treating Lyocell short fiber wastewater |
| CN113307380A (en) * | 2021-05-24 | 2021-08-27 | 东华大学 | Underground water zero-valent iron-modified biochar composite packed column polyculture denitrification method and permeable reactive barrier |
| CN113307380B (en) * | 2021-05-24 | 2023-04-21 | 东华大学 | Mixed culture denitrification method for groundwater zero-valent iron-modified biochar composite filler column and permeable reaction wall |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103420543B (en) | 2014-07-23 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103420543B (en) | Processing method of production waste water containing sulfo fluorescent whitening agent | |
| CN101381185B (en) | Denitrification processing method of coking wastewater and processing arrangement | |
| CN103224309A (en) | Leather waste water treatment system and treatment process | |
| CN104961304A (en) | High-concentration fluorine chemical wastewater treatment technology | |
| CN108033633B (en) | Triethylamine wastewater comprehensive treatment method | |
| CN106315977B (en) | A kind of printing-dyeing waste water treatment process | |
| CN109205954A (en) | Light electrolysis catalysis oxidation, biochemical treatment high-concentration waste hydraulic art | |
| CN108298762A (en) | A kind of combination SNAD techniques and bioreactor expose oneself the method for gas denitrogenation dephosphorizing | |
| CN111302560A (en) | Power plant sewage treatment method based on activated sludge process | |
| CN102616979A (en) | Treatment method for surface treatment liquid wastewater of metal processing | |
| KR100419827B1 (en) | Biological, pysical and chemical treatment method of waste water from livestock | |
| KR100386224B1 (en) | Advanced Piggery Wastewater Treatment System | |
| CN104817178A (en) | Short-range denitrification/dephosphorization device and method based on sludge side pretreatment | |
| CN206843294U (en) | A kind of dye wastewater treatment device | |
| CN105800873A (en) | Method for treating high-concentration ammonia nitrogen wastewater by autotrophic denitrification process | |
| Mulder et al. | Full-scale experience with the SHARON process through the eyes of the operators | |
| KR101360015B1 (en) | Method of reusing treated wastewater and system using the same | |
| CN101830601B (en) | Biological treatment system and method thereof specific to industrial wastewater of fluorescent brightener | |
| CN102329050B (en) | Process and device for efficiently treating wheat straw pulp intermediate wastewater by alkaline method | |
| CN215947051U (en) | Domestic sewage treatment device | |
| CN206069649U (en) | Integrated sewage disposal water cleaning systems | |
| CN115477388A (en) | Ammonium nitrate wastewater treatment device and method | |
| CN111747618B (en) | Efficient denitrification system and method based on two-stage AO oxidation ditch series connection | |
| CN113998848A (en) | Ammonia distillation, gas water seal, rainwater and sludge filtrate mixed wastewater treatment system and method | |
| CN207891216U (en) | A kind of processing system of high-concentration hardly-degradable pharmacy waste water |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20180308 Address after: 044100 Shanxi city of Yuncheng Province Linyi hi tech Industrial Park, No. 888 Patentee after: Shanxi Jinguang Chemical Co., Ltd. Address before: Hi tech Industrial Park, 044100 Shanxi city of Yuncheng Province Linyi County No. 888 Patentee before: Shanxi Kingsun Chemical Co., Ltd. |
|
| TR01 | Transfer of patent right |