CN103304008A - Method for treating organic wastewater by using ferroferric oxide particle electrode in cooperation with electrochemical oxidization - Google Patents
Method for treating organic wastewater by using ferroferric oxide particle electrode in cooperation with electrochemical oxidization Download PDFInfo
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- CN103304008A CN103304008A CN2013102884163A CN201310288416A CN103304008A CN 103304008 A CN103304008 A CN 103304008A CN 2013102884163 A CN2013102884163 A CN 2013102884163A CN 201310288416 A CN201310288416 A CN 201310288416A CN 103304008 A CN103304008 A CN 103304008A
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Abstract
The invention discloses a method for treating organic wastewater by using a ferroferric oxide particle electrode in cooperation with electrochemical oxidization, and belongs to the field of wastewater treatment. The method comprises the following steps of: in the presence of an external electric field, adding sodium sulfate serving as electrolyte to the organic wastewater, feeding ferroferric oxide into the organic wastewater, and introducing a current for reacting. The method is characterized in that the ferroferric oxide particle is taken as a particle electrode, so that the mass transfer rate of the electrochemical process is increased, the energy consumption is reduced and the removal rate of organic pollutants is increased.
Description
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Technical field
The invention belongs to field of waste water treatment, relate to the method for the collaborative electrochemicial oxidation organic waste water of a kind of Z 250 granule electrode.
Background technology
Industrial expansion has caused more and more serious ambient water to pollute, and in water body, mankind itself's health in a large amount of pollutent serious threats.In recent years, electrochemical water treating method has been subject to extensive concern.Utilize electrode process and correlated response thereof, by comprehensive actions such as direct or indirect redox, cohesion flocculation and collaborative conversions, the organic pollutant in water body is had to good removal effect.Due to electrochemical method, to have purification of water quality efficiency high, and non-secondary pollution is easy to use, the outstanding advantages such as is easy to control, and at aspects such as wastewater treatment and purification of water qualitys, obtained increasing application.
Electrochemistry oxygen is turned to a kind of of electrochemical method, can make pollutent at anode surface direct oxidation or the strong oxidizing property material that produced by anode and oxidation.In electrochemical oxidation process, electrode materials has a certain impact to the degraded tool of organic pollutant.At present, DSA anode (dimensionally stable anode, Dimensional stable anode) usually is applied in electrochemical oxidation process.The DSA anode mainly by matrix metal and plating there is the electro catalytic activity metal oxide surface active coating form.Metallic matrix plays skeleton and electric action, and surface active coating participates in the anode electrochemical reaction.The DSA anode has the advantages such as chemical stability height and long service life.And in electrochemical oxidation process, the DSA anode surface can produce hydroxyl radical free radical with strong oxidizing property (M (
.oH)), M (H
2o) → M (
.oH)+H
++ e
–thereby, the organic pollutant in oxidizing water.
Introduce conducting particles and can improve the processing efficiency of electrochemical oxidation to waste water in electric field.Short grained particle is introduced to electric field and can form countless charged microelectrodes, i.e. granule electrode.Because granule electrode has huge specific surface area and stronger electroconductibility, therefore can improve the rate of mass transfer of electrochemical oxidation process, and reduce energy consumption.
Summary of the invention
The object of the present invention is to provide the method for the collaborative electrochemicial oxidation organic waste water of a kind of Z 250 granule electrode, the method is usingd the DSA anode as anode, anti-corrosion electrode is degraded to the persistent pollutant in water body as negative electrode, and add ferriferrous oxide particles as granule electrode, improve the rate of mass transfer of electrochemical process, and reduced energy consumption.
Purpose of the present invention is achieved through the following technical solutions:
The method of the collaborative electrochemicial oxidation organic waste water of a kind of Z 250 granule electrode, comprise the following steps: under the existence of extra electric field, in organic waste water, add sodium sulfate as ionogen, Z 250 is added in organic waste water, pass into electric current, reacted; Described organic waste water is preferably the waste water containing orange beta-naphthol.
Described extra electric field is preferably usings the DSA anode as anode, and anti-corrosion electrode is as negative electrode; Described DSA anode is preferably Ti/RuO
2-IrO
2plate electrode, described anti-corrosion electrode is preferably the stainless steel flat plate electrode.
It is first 3.0～9.0 by its pH regulator that described organic waste water is preferably; Preferred, the pH value is adjusted to 3.0.
The concentration of described sodium sulfate is preferably 50 mmol/L.
The dosage of described Z 250 is preferably 0.2～0.8 g/L.
The intensity of described electric current is preferably 0.2～1.0 A.
The beneficial effect of the inventive method is:
(1) the Z 250 particle forms numerous microelectrode in can be in electrochemical reactor, thus reinforcing mass transfer, and the energy consumption of reduction, improved current efficiency;
(2) the Z 250 particle has magnetic, is easy to reclaim, effective solid-liquid separation after having guaranteed to process, and reusing is high;
(3) technological operation of the present invention is simple, and removal effect is better.
Embodiment
The azoic dyestuff pollutant is typical organic waste water, and azoic dyestuff is current most widely used synthetic dyestuff and is difficult to be biodegradable.Azoic dyestuff has toxicity and carinogenicity, and this makes the problem that is treated as the society extensive concern of waste water from dyestuff.Therefore, in embodiment, select the azoic dyestuff orange beta-naphthol as target contaminant.
Below by embodiment, the invention will be further described, illustrates outstanding feature of the present invention and marked improvement, only is the present invention is described and never is limited to the present invention.
Embodiment 1
Contrast (1) Z 250, (2) electrolysis and the impact of three kinds of systems of (3) Z 250 granule electrode electrochemical oxidation on the orange beta-naphthol degradation efficiency separately separately, each system operational condition and as follows to the result of orange beta-naphthol degraded.
(1) independent Z 250 system
Orange beta-naphthol strength of solution: 25 mg/L; Orange beta-naphthol wastewater volume: 200 mL; PH value: 3.0; Sodium sulfate concentration: 50 mmol/L; Z 250 dosage: 0.5 g/L.
(2) independent electrolysis system
Anode: Ti/RuO
2-IrO
2plate electrode; Negative electrode: stainless steel flat plate electrode; Electrode specification: 5 * 11.9 cm; Orange beta-naphthol strength of solution: 25 mg/L; Orange beta-naphthol wastewater volume: 200 mL; Sodium sulfate concentration: 50 mmol/L; PH value: 3.0; Power supply mode: direct current, 0.5 A.
(3) Z 250 granule electrode electrochemical oxidation system
Anode: Ti/RuO
2-IrO
2plate electrode; Negative electrode: stainless steel flat plate electrode; Electrode specification: 5 * 11.9 cm; Orange beta-naphthol strength of solution: 25 mg/L; Orange beta-naphthol wastewater volume: 200 mL; Sodium sulfate concentration: 50 mmol/L; PH value: 3.0; Z 250 dosage: 0.5 g/L; Power supply mode: direct current, 0.5 A.
The clearance of orange beta-naphthol under the different systems of table 1
Result shows: in independent Z 250 system, the orange beta-naphthol clearance is being 2.12% after reaction 60 min, and speed of reaction is slow; In independent electrolysis system, the clearance of orange beta-naphthol reaches 61.1% after reaction 60 min; In Z 250 granule electrode electrochemical oxidation system, the clearance of orange beta-naphthol after reaction 60 min is 82.7%, surpassed the clearance sum of the first two system, shows to have synergy between Z 250 granule electrode and electrochemical oxidation.
Embodiment 2
The impact of contrast different pH condition on the orange beta-naphthol clearance, be 3.0 at acid ph value respectively, pH neutral be 6.0 and the alkaline pH value Z 250 granule electrode electrochemical oxidation system that is 9.0 in the clearance of research orange beta-naphthol, operational condition and result are as follows in detail.
Operational condition: anode: Ti/RuO
2-IrO
2plate electrode; Negative electrode: stainless steel flat plate electrode; Electrode specification: 5 * 11.9 cm; Orange beta-naphthol strength of solution: 25 mg/L; Orange beta-naphthol wastewater volume: 200 mL; Sodium sulfate concentration: 50 mmol/L; PH value: 3.0,6.0,9.0; Z 250 dosage: 0.5 g/L; Power supply mode: direct current, 0.5 A.
The clearance of orange beta-naphthol under the different pH of table 2
Result shows: in above-mentioned pH scope, orange beta-naphthol all can effectively be removed, and under acidic conditions the clearance of orange beta-naphthol higher than the clearance of orange beta-naphthol under neutral and alkaline condition.
Embodiment 3
Contrast the impact of different strength of current conditions on the orange beta-naphthol clearance, the clearance of research orange beta-naphthol in the Z 250 granule electrode electrochemical oxidation system that is 0.2 A, 0.5 A and 1.0 A systems in strength of current respectively, operational condition and result are as follows in detail.
Operational condition: anode: Ti/RuO
2-IrO
2plate electrode; Negative electrode: stainless steel flat plate electrode; Electrode specification: 5 * 11.9 cm; Orange beta-naphthol strength of solution: 25 mg/L; Orange beta-naphthol wastewater volume: 200 mL; Sodium sulfate concentration: 50 mmol/L; PH value: 3.0; Z 250 dosage: 0.5 g/L; Power supply mode: direct current, 0.2 A, 0.5 A, 1.0 A.
The clearance of orange beta-naphthol under the different strength of current of table 3
Result shows: different current condition all have promoter action to reaction, and the clearance of the higher orange beta-naphthol of strength of current is higher.
Embodiment 4
The impact of contrast Z 250 dosage on the orange beta-naphthol clearance, the clearance of research orange beta-naphthol in the Z 250 granule electrode electrochemical oxidation system that is 0.2 g/L, 0.5 g/L and 0.8 g/L at the Z 250 dosage respectively, operational condition and result are as follows in detail.
Operational condition: anode: Ti/RuO
2-IrO
2plate electrode; Negative electrode: stainless steel flat plate electrode; Electrode specification: 5 * 11.9 cm; Orange beta-naphthol strength of solution: 25 mg/L; Orange beta-naphthol wastewater volume: 200 mL; Sodium sulfate concentration: 50 mmol/L; PH value: 3.0; Z 250 dosage: 0.2 g/L, 0.5 g/L, 0.8 g/L; Power supply mode: direct current, 0.5 A.
The clearance of orange beta-naphthol under table 4 Z 250 dosage
Result shows: Z 250 adds has promoter action to reaction, and the clearance of the higher orange beta-naphthol of dosage is the highest.
Above-described embodiment is preferably embodiment of the present invention; but embodiments of the present invention are not restricted to the described embodiments; other any do not deviate from change, the modification done under spirit of the present invention and principle, substitutes, combination, simplify; all should be equivalent substitute mode, within being included in protection scope of the present invention.
Claims (9)
1. the method for the collaborative electrochemicial oxidation organic waste water of Z 250 granule electrode, is characterized in that comprising the following steps: under the existence of extra electric field, in organic waste water, add sodium sulfate and Z 250, pass into electric current, reacted.
2. Z 250 granule electrode according to claim 1 is worked in coordination with the method for electrochemicial oxidation organic waste water, it is characterized in that: described organic waste water is the waste water containing orange beta-naphthol.
3. Z 250 granule electrode according to claim 1 is worked in coordination with the method for electrochemicial oxidation organic waste water, and it is characterized in that: described extra electric field is usingd the DSA anode as anode, and anti-corrosion electrode is as negative electrode.
4. Z 250 granule electrode according to claim 3 is worked in coordination with the method for electrochemicial oxidation organic waste water, and it is characterized in that: described DSA anode is Ti/RuO
2-IrO
2plate electrode, described anti-corrosion electrode is the stainless steel flat plate electrode.
5. Z 250 granule electrode according to claim 1 is worked in coordination with the method for electrochemicial oxidation organic waste water, and it is characterized in that: described organic waste water is first 3.0～9.0 by its pH regulator.
6. Z 250 granule electrode according to claim 5 is worked in coordination with the method for electrochemicial oxidation organic waste water, and it is characterized in that: described organic waste water is first 3.0 by its pH regulator.
7. Z 250 granule electrode according to claim 1 is worked in coordination with the method for electrochemicial oxidation organic waste water, and it is characterized in that: the concentration of described sodium sulfate is 50 mmol/L.
8. Z 250 granule electrode according to claim 1 is worked in coordination with the method for electrochemicial oxidation organic waste water, and it is characterized in that: the dosage of described Z 250 is 0.2～0.8 g/L.
9. Z 250 granule electrode according to claim 1 is worked in coordination with the method for electrochemicial oxidation organic waste water, and it is characterized in that: the intensity of described electric current is 0.2～1.0 A.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105967427A (en) * | 2016-06-15 | 2016-09-28 | 烟台大学 | Photoelectric synergistic catalysis reactor |
| CN106365264A (en) * | 2016-11-21 | 2017-02-01 | 北京益清源环保科技有限公司 | Modified ferroferric oxide particle electrode with function of removing pyridine through electrocatalysis and preparation method |
| CN106365272A (en) * | 2016-11-21 | 2017-02-01 | 北京益清源环保科技有限公司 | Modified ferroferric oxide particle electrode with nitrobenzene electro-catalysis removal function and preparation method |
| CN106495280A (en) * | 2016-11-21 | 2017-03-15 | 北京益清源环保科技有限公司 | There is electro-catalysis to remove improved ferroferric oxide granule electrode and the preparation method of phenol function |
Citations (5)
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| US5565082A (en) * | 1993-10-27 | 1996-10-15 | Permelec Electrode Ltd. | Brine electrolysis and electrolytic cell therefor |
| CN1358672A (en) * | 2002-01-16 | 2002-07-17 | 中山大学 | Three-dimension electrode reactor and use for treating organic waste water |
| CN1850644A (en) * | 2006-05-26 | 2006-10-25 | 北京化工大学 | Three-dimensional electrode reactor for treating hard-degradeable organic waste water |
| CN102942243A (en) * | 2012-11-08 | 2013-02-27 | 沈阳建筑大学 | Wastewater treatment method combining three-dimensional electrode and electric Fenton |
| CN103121746A (en) * | 2013-03-20 | 2013-05-29 | 武汉大学 | Method for treating wastewater by complexly activating persulfate |
-
2013
- 2013-07-10 CN CN2013102884163A patent/CN103304008A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5565082A (en) * | 1993-10-27 | 1996-10-15 | Permelec Electrode Ltd. | Brine electrolysis and electrolytic cell therefor |
| CN1358672A (en) * | 2002-01-16 | 2002-07-17 | 中山大学 | Three-dimension electrode reactor and use for treating organic waste water |
| CN1850644A (en) * | 2006-05-26 | 2006-10-25 | 北京化工大学 | Three-dimensional electrode reactor for treating hard-degradeable organic waste water |
| CN102942243A (en) * | 2012-11-08 | 2013-02-27 | 沈阳建筑大学 | Wastewater treatment method combining three-dimensional electrode and electric Fenton |
| CN103121746A (en) * | 2013-03-20 | 2013-05-29 | 武汉大学 | Method for treating wastewater by complexly activating persulfate |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105967427A (en) * | 2016-06-15 | 2016-09-28 | 烟台大学 | Photoelectric synergistic catalysis reactor |
| CN106365264A (en) * | 2016-11-21 | 2017-02-01 | 北京益清源环保科技有限公司 | Modified ferroferric oxide particle electrode with function of removing pyridine through electrocatalysis and preparation method |
| CN106365272A (en) * | 2016-11-21 | 2017-02-01 | 北京益清源环保科技有限公司 | Modified ferroferric oxide particle electrode with nitrobenzene electro-catalysis removal function and preparation method |
| CN106495280A (en) * | 2016-11-21 | 2017-03-15 | 北京益清源环保科技有限公司 | There is electro-catalysis to remove improved ferroferric oxide granule electrode and the preparation method of phenol function |
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Application publication date: 20130918 |