CN104817140A - Acetonitrile-containing high-salinity wastewater recovery and treatment method in production process of total fluorine ketone - Google Patents
Acetonitrile-containing high-salinity wastewater recovery and treatment method in production process of total fluorine ketone Download PDFInfo
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Abstract
The invention discloses a wastewater treatment method, and is applicable to an acetonitrile-containing high-salinity wastewater recovery and treatment method in the production process of total fluorine ketone. The method mainly includes the steps: performing electrolytic oxidation for wastewater; directly inserting an anode electrode and a cathode electrode into the wastewater; leading low-voltage micro-current into the two electrodes for electrolytic oxidation, or firstly leading low-voltage conventional current into the two electrodes for preliminary electrolytic oxidation and then leading low-voltage micro-current for final electrolytic oxidation. According to the method, new pollutants are not generated while acetonitrile in the wastewater is removed. The conventional current is led into the wastewater without the acetonitrile to perform electrolysis, and sodium hypochlorite solution is obtained, can be reused for removing the acetonitrile and ammonia nitrogen in original acetonitrile wastewater and can also be used for disinfection and epidemic prevention of water bodies such as reclaimed water, industrial circulating water and hospital sewage. The method is simple to operate and low in running cost and can simultaneously realize high-toxicity wastewater treatment and high-salinity wastewater resource utilization.
Description
Technical field
The present invention relates to a kind of process for treating industrial waste water, particularly a kind for the treatment of process being applicable to the ethane nitrile wastewater produced in perfluor ketone production process, belongs to water-treatment technology field.
Background technology
Perfluor ketone (C
3f
6o) can produce the trade effluent containing high density acetonitrile in production process, the water quality of waste water is as follows:
；
Ethane nitrile wastewater is poisonous organic industry sewage, needs to carry out harmless treatment, just can enter next stage operation or qualified discharge.
The treatment process of ethane nitrile wastewater mainly contains materilization freatment method and the biochemical method process etc. such as distillation method, absorption method, extraction process, combustion method, hydrolysis method and chemical oxidization method (containing catalyzed oxidation).The method of materializing strategy, ordinary expenditure is higher, produces secondary pollution simultaneously.The method of biological treatment, usually use aerobic method to organonitrile compound process, organonitrile compound has high toxicity, and aerobic bioprocess can be limited usually; Aerobic method process needs aeration, and due to the high volatile volatile of organonitrile compound, aeration can accelerate the stripping of acetonitrile, and acetonitrile is corresponding carboxylic acid and ammonia by Aerobic biological process after domestication, and carboxylic acid can be further oxidized to carbonic acid gas and water.For the ethane nitrile wastewater of high density, the another one problem of aerobic treatment is the ammonia nitrogen producing high density, and nitrification and denitrification process adds processing costs greatly.In addition, the salt containing high density in waste water, also limit the application of biochemical treatment.Ozone and photochemical catalytic oxidation have been used to the degraded of organonitrile compound, but these methods are usually very expensive, produce poisonous secondary pollutant simultaneously.For the ethane nitrile wastewater of high density, react in an aqueous medium, the result of process is difficult to the emission standard reaching 2mg/L.
ZL200610095052.7 discloses a kind for the treatment of process of nitrile contained organic sewage difficult to degrade, nitrile organism is contained containing the difficult degradation such as hydroxyacetonitrile, aniline-acetonitrile in waste water, waste water adopts Fe-C weak electrolysis mechanism to process in acid condition, then adds ferrous sulfate and lime carries out precipitation process.In foregoing invention, the light electrolysis post of Fe-C is in use due to the consumption of Fe, hollow and phenomenon that is percolation can occur, and namely waste water directly flows out without the filler of Fe-C, and the phenomenon of solidifying caking can occur another part Fe-C post, be connected as a single entity with reactor, be difficult to mobile.In addition, waste water, after above-mentioned art breading, also can produce a large amount of precipitations, becomes dangerous solid waste, needs to process further.In foregoing invention, treatment effect is not good, only has the clearance of about 40%.
Summary of the invention
The present invention, in order to overcome the deficiency of above-mentioned technology, designs the treatment process of ethane nitrile wastewater in a kind of perfluor ketone production process, and the method does not produce new pollutent while being removed by the acetonitrile in waste water.
For realizing above technical purpose, the present invention will take following technical scheme:
The treatment process of ethane nitrile wastewater in a kind of perfluor ketone production process, mainly electrolytic oxidation process is carried out to described waste water, specifically carry out according to following steps: the first step, except acetonitrile, in waste water, pass into the micro-electric current of low pressure carry out electrolytic oxidation, or in waste water, first pass into low pressure conventional current carry out preliminary electrolysis oxidation, and then pass into the micro-electric current of low pressure and carry out final electrolytic oxidation; Second step, extracts clorox, and the waste water removing acetonitrile passes into conventional current again and carries out electrolysis, directly obtains the chlorine bleach liquor that can be used for the water body disinfections such as middle water, industrial circulating water and hospital sewage and epidemic prevention dissipation.
The principle of foregoing invention is as follows:
Due to the high salinity of ethane nitrile wastewater in perfluor ketone production process, make waste water have higher conductivity, a part of nitrile compounds can move to the surface of electrode:
；
Cl in brine waste
-cl is converted at anode
2, and can hypochlorous acid be further converted to:
Hypochlorous acid is a kind of strong oxidizer inherently, the nitrile compounds in water can be oxidized,
In the micro-CURRENT OXIDATION electrolytic process of the high-salt wastewater of nitrile compounds, there is oxidizing reaction in the surface that part nitrile compounds can move to electrode, another part is chlorinated the hypochlorous acid oxidization that sodium electrolysis produces, and above-mentioned two kinds of electrochemical oxidation process are simultaneous.A part of direct oxidation is nitrogen, and another part first becomes ammonium radical ion, then is converted into nitrogen through ammonium radical ion.
Remove the waste water after acetonitrile under conventional current effect:
Cl in brine waste
-cl is converted at anode
2, and can hypochlorous acid be further converted to:
Absorb with alkali NaOH, can chlorine bleach liquor be obtained, with Ca (OH)
2absorb, can calcium hypochlorite solution be obtained.
The technical scheme that the present invention limits further is:
Further, treatment process divides three steps to carry out, and yin, yang interelectrode distance is set to 2 ~ 8cm by the first step, and it be current density is 1 ~ 20mA/cm that two interpolars first pass into low pressure conventional current design parameter
2(note: current density is the current density of electrode surface, lower same.), continued electrolysis 0 ~ 6h; Second step, it is current density 0.1 ~ 1mA/cm that two interpolars pass into the micro-electric current design parameter of low pressure again
2, the interelectrode distance 2 ~ 8cm at yin, yang the two poles of the earth, continued electrolysis 6 ~ 84h; 3rd step, two interpolars pass into conventional current again, and design parameter is: current density is 20 ~ 500 mA/cm
2, electrolysis 0.2 ~ 5h, obtaining effective chlorine density is the chlorine bleach liquor of 1 ~ 13%.
Further, treatment process is carried out in two steps, and the micro-current parameters of described electrolytic oxidation mesolow is: interelectrode for yin, yang the two poles of the earth spacing is set to 2 ~ 8cm, and current density is 0.1 ~ 1mA/cm
2, continued electrolysis 20 ~ 84h.Through electrolytic oxidation except after acetonitrile, two interpolars pass into conventional current again, and design parameter is: current density is 20 ~ 500 mA/cm
2, electrolysis 0.2 ~ 5h, obtaining effective chlorine density is the chlorine bleach liquor of 1 ~ 13%.
Further, treatment process is carried out in wastewater electrolytic device, wastewater electrolytic device mainly comprises AC/DC changeover switch, cathode electrode, anode electrode, electrolyzer and power supply, ethane nitrile wastewater is placed in electrolyzer, the working end of cathode electrode, anode electrode is immersed in ethane nitrile wastewater, and the receiving end of electrode to be electrically connected power supply by AC/DC changeover switch.
Further, the conventional current parameter extracting clorox is: interelectrode for yin, yang the two poles of the earth spacing is set to 2 ~ 8cm, and current density is 20 ~ 500mA/cm2, electrolysis 0.2 ~ 5h, the gas of generation is back to raw wastewater and removes acetonitrile; Or be 3 ~ 5% by wastewater dilution to salt concn, directly sending into hypochlorite generator's (market having finished product sell), to produce effective chlorine density be the clorox of 5 ~ 13%.
Further, anode electrode and cathode electrode can be single to electrode, also can be that multipair anode and single anticathode are in parallel.
Further, anode electrode and cathode electrode are single to electrode, and electrode form can be tubular pole, plate type electrode, net formula electrode.
Further, anode electrode is the one in graphite cake, titanium base painting ruthenium electrode, titanium base painting iridium electrode, cathode electrode the moon is adopted as the one in graphite cake, titanium plate, titanium net, stainless steel plate, aluminium sheet, and table 1 is the impact of anode electrode sheet material on acetonitrile removal effect:
；
As seen from the above table, anode uses Ti-Ru electrode and anode to use titanium painting iridium electrode to be better than Graphite Electrodes, it is suitable that Ti-Ru electrode and titanium are coated with iridium electrode, can find under same current density simultaneously, uses the voltage 2.3V of titanium painting ruthenium pole plate lower than the 2.6V of Graphite Electrodes.Mean that the running cost of use titanium ruthenium electrode can be lower than Graphite Electrodes by more than 10%; But the procurement price of Graphite Electrodes will well below titanium ruthenium electrode, and Graphite Electrodes is due to its loose physical structure, when its surface-coated Gai Shihui peels off voluntarily, so without the need to carrying out surface cleaning to it, titanium ruthenium electrode then must routine cleaning surface, so how choice electrode needs the demand different according to client to determine, can certainly the multi items efficiency ensureing electrolysis in parallel.
Further, in ethane nitrile wastewater handled in perfluor ketone production process, muriatic mass percent is 6 ~ 40%, and the present invention selects 500mg/L ethane nitrile wastewater to be subjects, tests the electrolytical impact of different concns under identical concentration;
The different electrolyte concentration of table 2 is to the result of ethane nitrile wastewater
；
As seen from the above table, within the specific limits, improving the concentration of salt can increase substantially electrolytic efficiency, saves the time of electrolysis, and coincidentally in this waste water, the content of salt is in this range.
The initial p H scope of waste water is 2-13, acetonitrile concentration <45000mg/L, and the different pH of table 3 is to the result of ethane nitrile wastewater:
；
As seen from the above table, when the point value that pH=4 and pH=13 these two is concrete, the removal effect of acetonitrile is best; PH is at neutral environment, and the removal efficiency of acetonitrile is relatively low; This may be because different with the mechanism of degradation of alkaline environment at sour environment, in sour environment, and H
+first the N of attack C ≡ N key, at alkaline environment, OH
-the C of first attack C ≡ N key, makes C ≡ N triple bond become C=N double bond, is more easily degraded by OH free-radical oxidn.
Further, muriate is NaCl.
The present invention is owing to taking above technical scheme, and tool has the following advantages: the ammonium radical ion that 1) acetonitrile in waste water and electrolytic oxidation can be produced synchronously is removed, and does not produce new pollutent, significantly saves energy simultaneously; 2) utilize in this waste water, salts contg own is higher, the feature conducted electricity very well; 3) to determine the ionogen of loss in electrolytic process considerably less for the physicochemical property of low pressure micro-current electroanalysis self, and therefore this treatment process is omnidistance without the need to additionally adding supplies; (4) electrolysis is removed the high-salt wastewater of acetonitrile and can be continued electrolysis and obtain the sterilizing agent such as hypochlorite, dioxide peroxide byproduct.
Embodiment
Embodiment one:
The voltage of reaction is controlled by D.C. regulated power supply; Negative electrode in electrolyzer adopts Graphite Electrodes, anode to adopt Graphite Electrodes, interelectrode distance 5cm, also adjustable;
Concrete operations are as follows:
Cell dimension is: 200*150*80(unit cm), add the actual acetonitrile industrial sewage of 1.3L, in sewage, acetonitrile concentration is 20453mg/L, this sewage saltiness is 40%, is mainly NaCl, regulates pH value to be 12, regulating voltage be 2.8V as operating voltage, now current density is 1mA/cm
2, the area of anode electrode is 140cm
2, the acetonitrile concentration of electrolysis waste water after 20 hours can drop to below 2mg/L.
Remove the high slat-containing wastewater wastewater dilution 5 times of acetonitrile, pass into the electric current that current density is 500mA/cm2, electrolysis 0.2 hour, the chlorine bleach liquor that effective chlorine density is 5% can be obtained.
Embodiment two:
Cell dimension is: 200*150*80(unit cm), add the actual acetonitrile industrial sewage of 1.3L, in sewage, acetonitrile concentration is 21454mg/L, and salt concn is 19%, is mainly sodium-chlor; Be initial voltage and electric current with 1.2V, take graphite as anode, titanium plate is negative electrode, and positive plate area is 280cm
2, negative plate area is 140cm
2; Interelectrode distance is 8cm, and electrolysis result is as follows:
；
As seen from the above table: using acetonitrile and ammonia nitrogen in the method waste water of electrolysis, total nitrogen, can synchronously the removing of nitre nitrogen, is 0.01mA/cm in anodic current density
2under, acetonitrile can reach below 2mg/L at 35 hours, and ammonia nitrogen reached greatly the level of 20mg/L about 21 hours.Remove the high slat-containing wastewater wastewater dilution 5 times of acetonitrile, pass into the electric current that current density is 20mA/cm2, electrolysis 5 hours, the chlorine bleach liquor that effective chlorine density is 2% can be obtained.
Embodiment three:
Cell dimension is: 200*150*80(unit cm), add the actual acetonitrile industrial sewage of 1.3L, in sewage, acetonitrile concentration is 21485mg/L, and salt concn is 19%, is mainly sodium-chlor.Be coated with iridium electrode for anode with titanium base, graphite is negative electrode, and positive plate area is 280cm
2, negative plate area is 140cm
2, interelectrode distance is 2cm; The first regulating voltage 2.2V of the first step, control current density are 20mA/cm
2, interelectrode distance 2cm, waste water pH value 4, electrolysis treatment 6h is carried out to waste water; Second step; Regulating voltage 1.5V, control current density are 0.1mA/cm
2, interelectrode distance 2cm, waste water pH value 4, electrolysis treatment 84h is carried out to waste water;
；
Using acetonitrile and ammonia nitrogen in the method waste water of electrolysis, total nitrogen, can synchronously the removing of nitre nitrogen, is 0.1mA/cm in anodic current density
2under, acetonitrile can be issued to below 2mg/L at 84h, and ammonia nitrogen reached greatly the level of 23mg/L about 42 hours, the direct processing cost about 18 watt-hour (WH) of every premium on currency.Therefore, the liberation of hydrogen using micro-electric current significantly can reduce similar technique to bring, the high energy consumption problem that the side reactions such as oxygen bring is analysed.
Remove the high slat-containing wastewater wastewater dilution 5 times of acetonitrile, pass into commercially available hypochlorite generator, the chlorine bleach liquor that effective chlorine density is 5% can be obtained.
Embodiment four:
Cell dimension is: 200*150*80(unit cm), add the actual acetonitrile industrial sewage of 1.3L, in sewage, acetonitrile concentration is 21243mg/L, salt concn is 19%, is mainly sodium-chlor, is coated with iridium electrode for anode with titanium base, stainless steel plate is negative electrode, and positive plate area is 280cm
2, negative plate area is 140cm
2, interelectrode distance is 2cm; With 1.2V potential electrolysis.
Electrolysis result is as follows: electrolysis under the condition of pH=5;
；
Using acetonitrile and ammonia nitrogen in the method waste water of electrolysis, total nitrogen, can synchronously the removing of nitre nitrogen, is 0.357mA/cm in anodic current density
2under, acetonitrile can be issued to below 2mg/L at 64h, and ammonia nitrogen reached greatly the level of 20mg/L about 42 hours, the direct processing cost about 10 watt-hour (WH) of every premium on currency.Therefore, the liberation of hydrogen using micro-electric current significantly can reduce similar technique to bring, the high energy consumption problem that the side reactions such as oxygen bring is analysed.
Remove the high slat-containing wastewater wastewater dilution 2 times of acetonitrile, pass into commercially available hypochlorite generator, the chlorine bleach liquor that effective chlorine density is 13% can be obtained.
Embodiment five:
Cell dimension is: 200*150*80(unit cm), add the actual acetonitrile industrial sewage of 1.3L, in sewage, acetonitrile concentration is 42485mg/L, and salt concn is 17%, is mainly sodium-chlor.Be coated with ruthenium electrode for anode with titanium base, titanium net is negative electrode, and positive plate area is 280cm
2, negative plate area is 140cm
2, interelectrode distance is 5cm; Regulating voltage 1.2V, control current density is 0.1mA/cm
2, interelectrode distance 2cm, waste water pH value 2, electrolysis treatment 84h is carried out to waste water;
；
Using acetonitrile and ammonia nitrogen in the method waste water of electrolysis, total nitrogen, can synchronously the removing of nitre nitrogen, is 0.1mA/cm in anodic current density
2under, acetonitrile can be issued to below 2mg/L at 120h.Therefore, micro-electric current is used the acetonitrile in waste water can be removed.The high slat-containing wastewater removing acetonitrile controls current density Direct Electrolysis, and the gas of generation absorbs with former ethane nitrile wastewater, and confined reaction 12h can reduce the time of raw wastewater micro-current electroanalysis.This example is after clorox is applied mechanically in this way, and the time of raw wastewater electrolysis can be reduced to 48 hours.
Embodiment six:
Cell dimension is: 200*150*80(unit cm), add the actual acetonitrile industrial sewage of 1.3L, in sewage, acetonitrile concentration is 2548mg/L, and salt concn is 17%, is mainly sodium-chlor.Be coated with ruthenium electrode for anode with titanium base, aluminium sheet is negative electrode, and positive plate area is 140cm
2, negative plate area is 140cm
2, interelectrode distance is 1cm; Regulating voltage 12V, control current density is 20mA/cm
2, waste water pH value 13, electrolysis treatment 4h is carried out to waste water;
；
Use high current density 20mA/cm
2acetonitrile in waste water can be removed, the content reducing acetonitrile fast reaches emission standard.Remove the high slat-containing wastewater wastewater dilution 2 times of acetonitrile, pass into commercially available hypochlorite generator, current density regulates 400mA/cm2, can obtain the chlorine bleach liquor that effective chlorine density is 13%.
Claims (10)
1. the treatment process of ethane nitrile wastewater in a perfluor ketone production process, mainly electrolytic oxidation process is carried out to described waste water, it is characterized in that, carry out according to following steps: the first step, except acetonitrile, in waste water, pass into the micro-electric current of low pressure carry out electrolytic oxidation, or in waste water, first pass into low pressure conventional current carry out preliminary electrolysis oxidation, and then pass into the micro-electric current of low pressure and carry out final electrolytic oxidation; Second step, extracts clorox, and the waste water removing acetonitrile passes into conventional current again and carries out electrolysis, directly obtains the chlorine bleach liquor that can be used for the water body disinfections such as middle water, industrial circulating water and hospital sewage and epidemic prevention dissipation.
2. the treatment process of ethane nitrile wastewater in perfluor ketone production process according to claim 1, it is characterized in that, described treatment process divides three steps to carry out, the first step, yin, yang interelectrode distance is set to 2 ~ 8cm, and it be current density is 1 ~ 20mA/cm that two interpolars first pass into low pressure conventional current design parameter
2, continued electrolysis 0 ~ 6h; Second step, it is current density 0.1 ~ 1mA/cm that two interpolars pass into the micro-electric current design parameter of low pressure again
2, the interelectrode distance 2 ~ 8cm at yin, yang the two poles of the earth, continued electrolysis 6 ~ 84h; 3rd step, two interpolars pass into conventional current again, and design parameter is: current density is 20 ~ 500 mA/cm
2, electrolysis 0.2 ~ 5h, obtaining effective chlorine density is the chlorine bleach liquor of 1 ~ 13%.
3. the treatment process of ethane nitrile wastewater in perfluor ketone production process according to claim 1, it is characterized in that, described treatment process is carried out in two steps, and the micro-current parameters of described electrolytic oxidation mesolow is: interelectrode for yin, yang the two poles of the earth spacing is set to 2 ~ 8cm, and current density is 0.1 ~ 1mA/cm
2, continued electrolysis 20 ~ 84h; Through electrolytic oxidation except after acetonitrile, two interpolars pass into conventional current again, and design parameter is: current density is 20 ~ 500 mA/cm
2, electrolysis 0.2 ~ 5h, obtaining effective chlorine density is the chlorine bleach liquor of 1 ~ 13%.
4. the treatment process of ethane nitrile wastewater in the perfluor ketone production process according to the arbitrary claim of claim 1-3, it is characterized in that, described treatment process is carried out in wastewater electrolytic device, described wastewater electrolytic device mainly comprises AC/DC changeover switch, cathode electrode, anode electrode, electrolyzer and power supply, described ethane nitrile wastewater is placed in electrolyzer, the working end of described cathode electrode, anode electrode is immersed in described ethane nitrile wastewater, and the receiving end of described electrode to be electrically connected power supply by AC/DC changeover switch.
5. the treatment process of ethane nitrile wastewater in the perfluor ketone production process according to Claims 2 or 3, it is characterized in that, the conventional current parameter extracting clorox is: interelectrode for yin, yang the two poles of the earth spacing is set to 2 ~ 8cm, and current density is 20 ~ 500mA/cm2, electrolysis 0.2 ~ 5h; Or be 3 ~ 5% by wastewater dilution to salt concn, directly send into commercially available hypochlorite generator, producing effective chlorine density is the clorox of 5 ~ 13%.
6. the treatment process of ethane nitrile wastewater in perfluor ketone production process according to claim 4, is characterized in that, described anode electrode and cathode electrode can be single to electrode, also can be that multipair anode and single anticathode are in parallel.
7. the treatment process of ethane nitrile wastewater in perfluor ketone production process according to claim 4, is characterized in that, described anode electrode and cathode electrode are single to electrode, and electrode form can be tubular pole, plate type electrode, net formula electrode.
8. the treatment process of ethane nitrile wastewater in perfluor ketone production process according to claim 4, it is characterized in that, described anode electrode is the one in graphite cake, titanium base painting ruthenium electrode, titanium base painting iridium electrode, and described cathode electrode is the one in graphite cake, titanium plate, titanium net, stainless steel plate, aluminium sheet.
9. the treatment process of ethane nitrile wastewater in the perfluor ketone production process according to the arbitrary claim of claim 1-3, it is characterized in that, in ethane nitrile wastewater handled in perfluor ketone production process, muriatic mass percent is 6 ~ 40%, initial p H scope is 2-13, acetonitrile concentration <45000mg/L.
10. the treatment process of ethane nitrile wastewater in perfluor ketone production process according to claim 9, it is characterized in that, described muriate is NaCl.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109550771A (en) * | 2018-12-11 | 2019-04-02 | 中化环境控股有限公司 | The minimizing technology and removal device of organic pollutant in industrial waste salt |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH10109093A (en) * | 1996-10-04 | 1998-04-28 | Sanden Corp | Drinking water sterilization device |
| US6096179A (en) * | 1997-10-06 | 2000-08-01 | Southeastern Trading, Llp | Carbon-reinforced electrode and method of making same |
| CN1907881A (en) * | 2006-08-23 | 2007-02-07 | 重庆紫光化工有限责任公司 | Processing method of nitrile contained organic sewage difficult to degrade |
| CN101037245A (en) * | 2007-02-14 | 2007-09-19 | 浙江工业大学 | Electrooxidation treatment technique for wastewater of chlorobenzene-containing compound |
| CN101767848A (en) * | 2008-12-30 | 2010-07-07 | 肖志邦 | Functional water preparation method and device by undivided micro-current electroanalysis |
| CN201809240U (en) * | 2010-08-13 | 2011-04-27 | 北京神州瑞霖环保科技有限公司 | Chemical fiber wastewater advanced treatment system |
| KR101256896B1 (en) * | 2008-04-23 | 2013-04-22 | 하얼빈 인스티튜 오브 테크놀로지 | A micro-current electrolysis sterilization algaecide device and method |
-
2015
- 2015-04-22 CN CN201510192836.0A patent/CN104817140B/en not_active Expired - Fee Related
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH10109093A (en) * | 1996-10-04 | 1998-04-28 | Sanden Corp | Drinking water sterilization device |
| US6096179A (en) * | 1997-10-06 | 2000-08-01 | Southeastern Trading, Llp | Carbon-reinforced electrode and method of making same |
| CN1907881A (en) * | 2006-08-23 | 2007-02-07 | 重庆紫光化工有限责任公司 | Processing method of nitrile contained organic sewage difficult to degrade |
| CN101037245A (en) * | 2007-02-14 | 2007-09-19 | 浙江工业大学 | Electrooxidation treatment technique for wastewater of chlorobenzene-containing compound |
| KR101256896B1 (en) * | 2008-04-23 | 2013-04-22 | 하얼빈 인스티튜 오브 테크놀로지 | A micro-current electrolysis sterilization algaecide device and method |
| CN101767848A (en) * | 2008-12-30 | 2010-07-07 | 肖志邦 | Functional water preparation method and device by undivided micro-current electroanalysis |
| CN201809240U (en) * | 2010-08-13 | 2011-04-27 | 北京神州瑞霖环保科技有限公司 | Chemical fiber wastewater advanced treatment system |
Non-Patent Citations (2)
| Title |
|---|
| 林莉等: "微电流电解对铜绿微囊藻的持续抑制研究", 《华中科技大学学报（自然科学版）》 * |
| 赵曙光等: "微电流电解消毒技术在海水维生***中的应用", 《水处理技术》 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109550771A (en) * | 2018-12-11 | 2019-04-02 | 中化环境控股有限公司 | The minimizing technology and removal device of organic pollutant in industrial waste salt |
| CN109550771B (en) * | 2018-12-11 | 2024-04-26 | 中化环境控股有限公司 | Method and device for removing organic pollutants in industrial waste salt |
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