CN1611457A - Method for treating or ganic waste water with nigh concentration - Google Patents
Method for treating or ganic waste water with nigh concentration Download PDFInfo
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- CN1611457A CN1611457A CNA2003101032232A CN200310103223A CN1611457A CN 1611457 A CN1611457 A CN 1611457A CN A2003101032232 A CNA2003101032232 A CN A2003101032232A CN 200310103223 A CN200310103223 A CN 200310103223A CN 1611457 A CN1611457 A CN 1611457A
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- waste water
- fenton reagent
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- organic wastewater
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- 239000002351 wastewater Substances 0.000 title claims abstract description 88
- 238000000034 method Methods 0.000 title claims abstract description 42
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 49
- 239000012028 Fenton's reagent Substances 0.000 claims abstract description 29
- 238000006386 neutralization reaction Methods 0.000 claims abstract description 15
- 230000003647 oxidation Effects 0.000 claims description 30
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 28
- 238000001556 precipitation Methods 0.000 claims description 15
- 238000004065 wastewater treatment Methods 0.000 claims description 12
- 230000001105 regulatory effect Effects 0.000 claims description 8
- 239000012467 final product Substances 0.000 claims description 2
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 abstract description 5
- 239000000126 substance Substances 0.000 abstract description 5
- 238000004062 sedimentation Methods 0.000 abstract 2
- 230000007423 decrease Effects 0.000 abstract 1
- 230000004907 flux Effects 0.000 abstract 1
- 239000003208 petroleum Substances 0.000 abstract 1
- 230000000694 effects Effects 0.000 description 15
- 238000005516 engineering process Methods 0.000 description 15
- 238000012545 processing Methods 0.000 description 14
- 238000006243 chemical reaction Methods 0.000 description 9
- 239000010802 sludge Substances 0.000 description 7
- 230000003197 catalytic effect Effects 0.000 description 6
- 230000000052 comparative effect Effects 0.000 description 4
- 229910001448 ferrous ion Inorganic materials 0.000 description 4
- 239000000243 solution Substances 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 150000001299 aldehydes Chemical class 0.000 description 3
- 238000011049 filling Methods 0.000 description 3
- 150000002576 ketones Chemical class 0.000 description 3
- 238000012856 packing Methods 0.000 description 3
- 150000003254 radicals Chemical class 0.000 description 3
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 238000005273 aeration Methods 0.000 description 2
- 238000010790 dilution Methods 0.000 description 2
- 239000012895 dilution Substances 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 230000002255 enzymatic effect Effects 0.000 description 2
- 238000000855 fermentation Methods 0.000 description 2
- 230000004151 fermentation Effects 0.000 description 2
- 239000000945 filler Substances 0.000 description 2
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 230000000813 microbial effect Effects 0.000 description 2
- 239000010813 municipal solid waste Substances 0.000 description 2
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N phenol group Chemical group C1(=CC=CC=C1)O ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 2
- 238000003672 processing method Methods 0.000 description 2
- 238000007348 radical reaction Methods 0.000 description 2
- 230000035484 reaction time Effects 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000000706 filtrate Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000007172 homogeneous catalysis Methods 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 230000007269 microbial metabolism Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000002574 poison Substances 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 230000035939 shock Effects 0.000 description 1
- 230000001954 sterilising effect Effects 0.000 description 1
- 239000002562 thickening agent Substances 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- Y02W10/12—
Landscapes
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The invention relates to a kind of treatment method of high concentration organic wastewater. The invention takes anaerobic organism filter tank- Fenton reagent oxidization - contact oxidization method (A-F-O method) as the core. After adjusting PH of high concentration organic wastewater, it runs through bottom of anaerobic organism filter tank (AF), and then overflows into Fenton reagent oxidization reactor from top of AF. After reacting by some time, it runs into neutralization sedimentation tank. When having removed vestigial Fe2+ in the wastewater, it gets into contact oxidization system, then control by regular hour, and last, flux through quadratic sedimentation tank. Treated by this method, COD of high concentration organic wastewater can decline to lower than 80mg/L, so it can achieve national discharge standard. The invention has stable and reliable treating effictiveness, convenient and steerable operation, low running cost, so that it adapts to treat high concentration organic wastewater discharged by petroleum chemical enterprise and other analogous enterprises.
Description
Technical field
The present invention relates to a kind of processing method of industrial waste water, is a kind of treatment process of high concentrated organic wastewater furtherly.
Background technology
Along with China's industrial expansion, the waste water of many industries, enterprise's discharging is increasingly sophisticated., good biodegradability comparatively simple for composition, the waste water that concentration is lower can reach comparatively ideal treatment effect by making up traditional technology.But also have some waste water, organic concentration is higher, biodegradability is relatively poor even also have to a certain degree bio-toxicity, and is bigger with the traditional technology intractability.
Handling at present this type of waste water adopts burning method more or handles the method that the big multiple in back dilutes biochemistry through simple materialization.
It is commonplace that burning method processing high concentrated organic wastewater is used abroad, and its treatment effect is reliable and stable, and floor space is also smaller.But because the facility investment and the running cost of burning method are very high, the producer of present domestic employing burning method processing high concentrated organic wastewater is also few.
Big multiple dilution biochemistry was the main method when the pre-treatment high concentrated organic wastewater after simple materialization was handled.The treatment effect of this method still can, but along with China's water situation is increasingly serious, adopt the method for dilution to waste a large amount of precious water resource undoubtedly, increased wastewater emission amount, do not tackle the problem at its root, do not meet environmental protection requirement yet.
So urgent need is developed economic, the effective high concentrated organic wastewater treatment technology of a cover at present.
Anaerobic biofilter is a kind of anaerobic reactor that loads filler.In anaerobic biofilter, anaerobion is grown in filter material surface with biomembranous form, and waste water is flooding and passing through in the process of filler, under the acting in conjunction that microbial film absorption, microbial metabolism and filtrate are held back, organism wherein is by microbial transformation, and just its pollution is removed.The advantage of anaerobic biofilter is that organic loading is higher, strong shock resistance, and equipment is simple, energy consumption is low.But the anaerobic biofilter in past is owing to stop up easily, uses lessly, and along with the development success of multiple high efficiency packing, this problem is solution substantially now.
Fenton (Fenton) reagent oxidation is one of common technology of handling organic used water difficult to degradate.It is that a kind of employing hydrogen peroxide is an oxygenant, is the homogeneous catalysis treatment process of catalyzer with the ferrous salt.Owing in reaction, can produce the very strong OH free radical of oxidation capacity, so its speed of reaction is fast, oxidation efficiency is high, can make organic C-C bond rupture, and under suitable condition the most at last oxidation operation become CO2 and H2O.
Contact oxidation method belongs to a kind of of aerobe membrane processing method, and it is simple to operate, and treatment effect is reliable and stable, is a widely used at home and abroad ripe treatment technology.
Mentioned a wastewater purification technology among U.S. Pat-4765901-1A.The core of this technology is an oxidation sterilizing, promptly before waste water carries out the anaerobic biological processing, adopts enzymatic oxidn to handle and eliminates the wherein toxicity of aldehydes matter.The characteristics of this technology be for can not form the precipitation of aldehydes matter in oxidising process, and can the biodegradability of waste water not impacted basically.Because the very high and complicated component of organic concentration of waste water of the present invention, the enzymatic oxidn reaction technology at aldehydes matter among the employing patent US-4765901-1A is also improper.
Mentioned a kind of treatment process of organic sludge among the Japanese Patent JP-7-24499A.This method adopts metal catalyst and oxygenant combination that the residual active sludge or the digested sludge that produce in the wastewater biochemical processing are handled, to realize the minimizing of mud.The characteristic of this technology is that the pH of reaction solution transfers to 2～8, and needs heating, needs simultaneously mud is carried out supersound process before oxide treatment.The oxide treatment treatment condition are primarily aimed at sludge treatment in this patent, can not directly apply mechanically for wastewater treatment.
Mentioned the treatment technology of a percolate from garbage filling field among the Japanese Patent JP-54-108459A.At first make the COD of percolate reduce to 100～300mg/L, carry out the Fenton reagent oxidation again and handle, effectively remove remaining suspended substance, organism and colourity with traditional biochemical processing.The focusing on of patent JP-54-108459A handled low concentration with Fenton reagent method waste water makes its qualified discharge, for high concentrated organic wastewater, adopts traditional biochemical technology to make it drop to relatively difficulty of scope that patent needs.
German patent DE-4119 144A1 has in addition also introduced the technology of oxide treatment in wastewater treatment among Japanese Patent JP-52-108654A, JP-57-19100A, JP-3-106498A, the U.S. Pat-5468628A.
To sum up, although above method has been introduced oxidation technology in handling all, and do not have at waste water poison, aspect such as sludge reduction carried out effective exploration, all do not relate to the treatment effect to high concentrated organic wastewater.Therefore, developing a cost-effective treatment technology handles high concentrated organic wastewater and is necessary.
Summary of the invention
The object of the present invention is to provide a kind of treatment process of high concentrated organic wastewater, when reaching processing requirements, have treatment effect reliable and stable, be easy to outstanding features such as industrial applications.
The treatment process of high concentrated organic wastewater of the present invention is to realize like this.The present invention adopts anaerobic biofilter-Fenton reagent oxidation-contact oxidation method (A-F-O method) that high concentrated organic wastewater is handled.
The treatment process of high concentrated organic wastewater of the present invention may further comprise the steps:
1. high concentrated organic wastewater is regulated pH to 6.8～7.2, preferred 6.9～7.1 in equalizing tank;
2. the waste water behind the adjusting pH enters anaerobic biofilter, stops 3～10d, preferred 4～8d;
3. waste water enters the Fenton reagent oxidation reactor through anaerobic biofilter, according to H
2O
2: COD (W/W)
Be (3.5～10.0): 1 ratio, preferred (4.0～8.5): 1 ratio adds H
2O
2, Fe
2+: H
2O
2Be (0.06～0.12): 1, preferred (0.08～0.10): the ratio of 1 ratio adds Fe
2+, waste water stops 180～360min, preferred 200～320min in Fenton reagent oxidation reactor;
4. the waste water after the oxide treatment enters the neutralization precipitation pond, and the pH of control settling tank water outlet is 7.5～8.5, preferably pH is 7.8～8.2;
5. in and after waste water enter contact-oxidation pool, enter second pond after stopping 12～18h, preferred 14～16h;
6. waste water gets final product water outlet stop 2～5h in second pond after.
Technological line of the present invention is summarized as follows:
High concentrated organic wastewater is regulated after the pH, feed anaerobic biofilter (AF) bottom, and enter Fenton reagent oxidation reactor from the overflow of AF top, enter the neutralization precipitation pond after reaction for some time, after removing ferrous ion remaining in the waste water, enter contact oxidation reaction system, control certain residence time, through the second pond water outlet.
Technical characterictic of the present invention is as follows:
The high concentrated organic wastewater that relates among the present invention, COD are generally at 10000～30000mg/L.
Anaerobic reactor to the requirement of pH than higher, because the optimum pH growth scope of methanogen is 6.8～7.2, and the optimum pH growth scope of acid-producing bacteria is 4.0～7.0, if environment pH surpasses the best pH scope of methanogen, acid fermentation might surpass methane fermentation, to the induce reaction acidifying of device of result causes treatment effect to descend.Therefore need the control high concentrated organic wastewater (COD generally at the pH of 10000～30000mg/L) water inlets 6.8～7.2, preferred 6.9～7.1.
The residence time of waste water in anaerobic reactor be difference to some extent with the difference of water quality, is the effect that guarantees anaerobic treatment, generally will guarantee the residence time that 3d is above.Simultaneously because anaerobic treatment and do not require that water outlet reduces to very lowly, therefore, the general residence time of waste water in AF is controlled at 3～10d, preferred 4～8d.
H in the Fenton reagent react
2O
2Consumption be the key factor that influences reaction effect, along with H
2O
2The increase of consumption, the processing efficiency of waste water also promote thereupon, but also raising thereupon of processing cost, and if H
2O
2Use quantity not sufficient, do not reach the ideal treatment effect again, therefore control H
2O
2Addition be H
2O
2/ COD (W/W)=3.5～10.0, preferred 4.0～8.5.
Fe in the Fenton reagent react
2+Consumption press Fe
2+/ H
2O
2=0.06～0.12 (w/w) meter is preferably 0.08～0.10 (w/w).This is because if the addition of ferrous ion is excessive, though favourable to removing organism, increased processing costs, also to handle more molysite rubbish after the free radical reaction simultaneously; And if the addition of ferrous ion is too small, free radical reaction just can't be carried out smoothly.Ferrous salt of the present invention generally is selected from the solubility salt that contains ferrous ion, as FeSO
47H
2O etc.
The time of Fenton reagent react need be controlled at 180～360min.Because when the reaction times is less than 180min, H
2O
2Can not react completely, cause residually, will have a strong impact on follow-up biochemical treatment; And after the reaction times surpassed 360min, processing efficiency no longer improved.Therefore needing the control Fenton reagent react time is 180～360min, preferred 200～320min.
In the waste water that the Fenton reagent oxidation is handled, have residual Fe
2+, and Fe
2+Can influence the processing efficiency of contact-oxidation pool, therefore need before waste water enters the catalytic oxidation system, carry out neutralization precipitation and handle, to remove residual Fe
2+Take all factors into consideration the water inlet pH requirement of catalytic oxidation system, the water outlet pH in control neutralization precipitation pond is 7.5～8.5, preferred 7.8～8.2.
The residence time of contact-oxidation pool is long more, and treatment effect is good more, but the pond holds and also can correspondingly increase, and the residence time is too short, can not guarantee that again stable water outlet is up to standard, and therefore needing the residence time of control contact-oxidation pool is 12～18h, preferred 14～16h.
Second pond mainly plays the effect of stablizing effluent quality, so the residence time of waste water in second pond is unsuitable too short, generally is controlled at 2～5h.
Below in conjunction with accompanying drawing 1 detailed process of the present invention is described:
Since anaerobic reactor to the requirement of pH than higher, therefore need the control high concentrated organic wastewater (COD generally at the pH of 10000～30000mg/L) water inlets 6.8～7.2, preferred 6.9～7.1.Waste water can enter AF after regulating pH.Waste water enters from the bottom of AF, and flow out at the top, and filling medium-soft fibrous packing in the AF can also can form good anaerobe film by the effectively catching anaerobic sludge.The residence time of waste water in AF is long more, and treatment effect is good more, and the residence time of anaerobic treatment can not be less than 3d, otherwise treatment effect can't guarantee, therefore the residence time of waste water in AF is controlled at 3～10d, preferred 4～8d.Waste water enters Fenton reagent oxidation reactor through AF.By in Fenton reagent oxidation reactor, adding H
2O
2And Fe
2+Come waste water is carried out oxide treatment.H
2O
2Addition with H
2O
2/ COD (W/W, the pure substance weight ratio, down together)=3.5～10.0, be preferably 4.0～8.5.Fe
2+Addition with Fe
2+/ H
2O
2(W/W)=0.06～0.12, preferred 0.08～0.10.The residence time of waste water in oxidation reactor is controlled at 180～360min, is preferably 200～320min.In order to remove remaining Fe in the Fenton reagent react
2+, in order to satisfy the water inlet requirement of follow-up contact-oxidation pool, the waste water of oxide treatment enters contact-oxidation pool again after pH is regulated in the neutralization precipitation pond simultaneously, the pH of control neutralization precipitation pond water outlet is 7.5～8.5, be preferably 7.8～8.2, the available strong base solution of pH regulator agent, NaOH solution as 10%.Filling medium-soft fibrous packing in the contact-oxidation pool, distribution micro porous aeration head at the bottom of the pond is through the gas blower aeration.The residence time of waste water in contact-oxidation pool is controlled at 12～18h, preferred 14～16h.Contact-oxidation pool water outlet gravity flow enters second pond, stops 2～5h and can discharge afterwards.
The present invention adopts anaerobic biofilter-Fenton reagent oxidation-contact oxidation method (A-F-O method) as the basic skills of handling high concentrated organic wastewater.
Handle through present method, the COD of general high concentrated organic wastewater can reduce to below the 80mg/L, reaches the requirement of national wastewater discharge standard.
Description of drawings
Fig. 1 is the schema of wastewater treatment of the present invention
Among the figure: 1. equalizing tank, 2. flow lifting type anaerobic biofilter, 3. Fenton reagent reactor, 4. neutralization precipitation pond, 5. contact-oxidation pool, 6. second pond, 7. sludge thickener.
Embodiment
Further describe the present invention below in conjunction with embodiment, scope of the present invention is not subjected to the restriction of these embodiment.Scope of the present invention proposes in claims.
Embodiment 1
Getting certain chemical plant contains ketone waste water (COD 11680mg/L) and tests.Enter anaerobic biofilter after wastewater pH transfers to 8.0, the residence time is 3d, and waste water enters Fenton reagent oxidation reactor subsequently, according to H
2O
2/ COD (W/W)=3.5, Fe
2+/ H
2O
2(W/W)=0.08 ratio adds H
2O
2And Fe
2+, entering the neutralization precipitation pond behind the reaction 180min, water outlet pH in neutralization precipitation pond is 8.0, then carries out catalytic oxidation and handles, the residence time is 12h, and through the second pond water outlet.
Contain ketone waste water after above-mentioned processing, water outlet COD reduces to 55mg/L, reaches national wastewater discharge standard.
Embodiment 2
Getting certain chemical plant phenolic wastewater (COD 28960mg/L) tests.Enter anaerobic biofilter after wastewater pH transfers to 8.0, the residence time is 10d, and waste water enters Fenton reagent oxidation reactor subsequently, according to H
2O
2/ COD (W/W)=8.5, Fe
2+/ H
2O
2(W/W)=0.08 ratio adds H
2O
2And Fe
2+, entering the neutralization precipitation pond behind the reaction 280min, water outlet pH in neutralization precipitation pond is 8.0, then carries out catalytic oxidation and handles, the residence time is 16h, and through the second pond water outlet.
Phenolic wastewater is after above-mentioned processing, and water outlet COD reduces to 68mg/L, reaches national wastewater discharge standard.
Comparative Examples 1
The comparative example 1, and waste water directly enters the catalytic oxidation system after the Fenton reagent oxidation, and all the other conditions are identical.
With this understanding, the treatment effect of catalytic oxidation system continues to descend, and the phenomenon of mud occurs, and water outlet can not be up to standard.
Comparative Examples 2
The comparative example 1, and the residence time of waste water in contact-oxidation pool is controlled to be 10h, and all the other conditions are identical.
Contain ketone waste water after above-mentioned processing, water outlet COD is 120mg/L, surpasses discharging standards.
Claims (9)
1. the treatment process of high concentrated organic wastewater is characterized in that, it may further comprise the steps:
A. high concentrated organic wastewater is regulated pH to 6.8～7.2 in equalizing tank;
B. the waste water of regulating behind the pH enters anaerobic biofilter, stops 3～10d;
C. waste water enters the Fenton reagent oxidation reactor through anaerobic biofilter, according to H
2O
2: COD (W/W) is (3.5～10.0): 1 ratio adds H
2O
2, Fe
2+: H
2O
2Be (0.06～0.12): 1 ratio adds Fe
2+, waste water stops 180～360min in Fenton reagent oxidation reactor;
D. the waste water after the oxide treatment enters the neutralization precipitation pond, and the pH of control settling tank water outlet is 7.5～8.5;
E. in and after waste water enter contact-oxidation pool, enter second pond after stopping 12～18h;
F. waste water gets final product water outlet stop 2～5h in second pond after.
2. method of wastewater treatment according to claim 1 is characterized in that: wherein high concentrated organic wastewater is regulated pH to 6.9～7.1 in equalizing tank.
3. method of wastewater treatment according to claim 1 is characterized in that: wherein waste water stops 4～8d in anaerobic biofilter.
4. method of wastewater treatment according to claim 1 is characterized in that: wherein the Fenton reagent reactor is according to H
2O
2: COD (W/W) is (4.0～8.5): 1 ratio adds H
2O
2
5. method of wastewater treatment according to claim 1 is characterized in that: wherein the Fenton reagent reactor is according to Fe
2+: H
2O
2Be (0.08～0.10): 1 ratio adds Fe
2+
6. method of wastewater treatment according to claim 1 is characterized in that: wherein the residence time of waste water in the Fenton reagent oxidation reactor is 200～320min.
7. method of wastewater treatment according to claim 1 is characterized in that: wherein the water outlet pH in neutralization precipitation pond is controlled at 7.8～8.2.
8. method of wastewater treatment according to claim 1 is characterized in that: wherein the residence time of contact-oxidation pool is controlled at 14～16h.
9. method of wastewater treatment according to claim 1 is characterized in that: wherein high concentrated organic wastewater is regulated pH to 6.9～7.1 in equalizing tank; Wherein waste water stops 4～8d in anaerobic biofilter; Wherein the Fenton reagent reactor is according to H
2O
2: COD (W/W) is (4.0～8.5): 1 ratio adds H
2O
2Wherein the Fenton reagent reactor is according to Fe
2+: H
2O
2Be (0.08～0.10): 1 ratio adds Fe
2+Wherein the residence time of waste water in the Fenton reagent oxidation reactor is 200～320min; Wherein the water outlet in neutralization precipitation pond is controlled at 7.8～8.2; Wherein the residence time of contact-oxidation pool is controlled at 14～16h.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2003101032232A CN1257853C (en) | 2003-10-30 | 2003-10-30 | Method for treating or ganic waste water with nigh concentration |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2003101032232A CN1257853C (en) | 2003-10-30 | 2003-10-30 | Method for treating or ganic waste water with nigh concentration |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1611457A true CN1611457A (en) | 2005-05-04 |
| CN1257853C CN1257853C (en) | 2006-05-31 |
Family
ID=34756572
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2003101032232A Expired - Lifetime CN1257853C (en) | 2003-10-30 | 2003-10-30 | Method for treating or ganic waste water with nigh concentration |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1257853C (en) |
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100366548C (en) * | 2006-03-09 | 2008-02-06 | 湖北大学 | Treating and reusing method for ramie degumming waste water |
| CN100368324C (en) * | 2006-03-09 | 2008-02-13 | 绵阳市勤生技术开发有限公司 | Method for treating high concentration organic waste water |
| CN100431977C (en) * | 2006-07-21 | 2008-11-12 | 中山大学 | Sterilizing method for hospital waste water |
| CN100494098C (en) * | 2007-03-09 | 2009-06-03 | 华南理工大学 | Fenton and air-float integral water treating method |
| WO2009124426A1 (en) * | 2008-04-08 | 2009-10-15 | 南京大学 | A method for treating pharmaceutical mixed wastewater in chemical industry park |
| CN101811767A (en) * | 2010-05-11 | 2010-08-25 | 沈阳建筑大学 | Admantadine waste water oxidation treatment method by Fenton reagent |
| CN102557345A (en) * | 2012-02-09 | 2012-07-11 | 湖南农业大学 | Treatment method of wastewater from processing of betel nuts |
| CN102921717A (en) * | 2012-10-19 | 2013-02-13 | 西安建筑科技大学 | In-situ remediation method aiming at dispersible petroleum-contaminated soil |
| CN102923901A (en) * | 2011-08-12 | 2013-02-13 | 中国石油化工股份有限公司 | Advanced treatment method of ethylene waste lye |
| CN103992009A (en) * | 2014-05-26 | 2014-08-20 | 南京工业大学 | PBOB treatment process for toxic organic chemical wastewater |
| CN107473524A (en) * | 2017-09-26 | 2017-12-15 | 江西沄沐环保科技有限公司 | A kind of high concentration organic acidity wastewater treatment system |
| CN110563253A (en) * | 2019-09-05 | 2019-12-13 | 北京环球中科水务科技有限公司 | treatment method of anisole organic wastewater |
-
2003
- 2003-10-30 CN CNB2003101032232A patent/CN1257853C/en not_active Expired - Lifetime
Cited By (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100368324C (en) * | 2006-03-09 | 2008-02-13 | 绵阳市勤生技术开发有限公司 | Method for treating high concentration organic waste water |
| CN100366548C (en) * | 2006-03-09 | 2008-02-06 | 湖北大学 | Treating and reusing method for ramie degumming waste water |
| CN100431977C (en) * | 2006-07-21 | 2008-11-12 | 中山大学 | Sterilizing method for hospital waste water |
| CN100494098C (en) * | 2007-03-09 | 2009-06-03 | 华南理工大学 | Fenton and air-float integral water treating method |
| WO2009124426A1 (en) * | 2008-04-08 | 2009-10-15 | 南京大学 | A method for treating pharmaceutical mixed wastewater in chemical industry park |
| CN101811767A (en) * | 2010-05-11 | 2010-08-25 | 沈阳建筑大学 | Admantadine waste water oxidation treatment method by Fenton reagent |
| CN102923901A (en) * | 2011-08-12 | 2013-02-13 | 中国石油化工股份有限公司 | Advanced treatment method of ethylene waste lye |
| CN102923901B (en) * | 2011-08-12 | 2014-07-09 | 中国石油化工股份有限公司 | Advanced treatment method of ethylene waste lye |
| CN102557345A (en) * | 2012-02-09 | 2012-07-11 | 湖南农业大学 | Treatment method of wastewater from processing of betel nuts |
| CN102557345B (en) * | 2012-02-09 | 2014-01-15 | 湖南农业大学 | Treatment method of wastewater from processing of betel nuts |
| CN102921717A (en) * | 2012-10-19 | 2013-02-13 | 西安建筑科技大学 | In-situ remediation method aiming at dispersible petroleum-contaminated soil |
| CN103992009A (en) * | 2014-05-26 | 2014-08-20 | 南京工业大学 | PBOB treatment process for toxic organic chemical wastewater |
| CN107473524A (en) * | 2017-09-26 | 2017-12-15 | 江西沄沐环保科技有限公司 | A kind of high concentration organic acidity wastewater treatment system |
| CN110563253A (en) * | 2019-09-05 | 2019-12-13 | 北京环球中科水务科技有限公司 | treatment method of anisole organic wastewater |
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