CN110845055B - Sectional type electrochemical water treatment device and method for treating water by adopting same - Google Patents
Sectional type electrochemical water treatment device and method for treating water by adopting same Download PDFInfo
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/467—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction
- C02F1/4672—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction by electrooxydation
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/463—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrocoagulation
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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Abstract
The invention discloses a sectional type electrochemical water treatment device and a treatment method adopting the same, and the device comprises an electrolytic tank consisting of a cathode and an anode, wherein an electrolytic channel is formed between the cathode and the anode and is divided into a front section and a rear section, the front section of the electrolytic channel is filled with carbon-based loaded metal oxide and/or corresponding carbon-based loaded metal, the rear section of the electrolytic channel is filled with carbon-based loaded metal and/or iron particles, and the front section of the electrolytic channel is also internally provided with an aeration device. The treatment method comprises the steps of adjusting the conductivity and the pH value of the wastewater, starting the aeration device and the electrolytic tank, reacting the wastewater sequentially through the front section and the rear section of the electrolytic tank, standing and centrifuging. The device realizes the in-situ generation of strong oxidizing radicals and adsorption flocs in sections by filling different catalytic particle electrodes in the continuous electrolytic channel in sections, thereby improving the removal rate of refractory organic matters; meanwhile, the treatment method can overcome the problem of anode passivation to a certain degree and reduce energy consumption.
Description
Technical Field
The invention belongs to the field of wastewater treatment, and particularly relates to a sectional type electrochemical water treatment device and a sectional type electrochemical water treatment method.
Background
The electric flocculation technology is a green and low-cost wastewater treatment technology. The principle of the electric flocculation is that a soluble metal anode generates metal cations (Al) under the action of an external electric field3+Or Fe2+Etc.), cathode generation of H2And surface hydroxyl (. OH) groupsThe hydroxide and the polynuclear hydroxyl complex are combined in the solution to form hydroxide flocs rich in surface hydroxyl groups. The formed floc can adsorb pollutants such as heavy metal ions, organic matters, suspended particles and the like in water through the effects of exclusive adsorption, net capture, rolling, sweeping, adsorption bridging and the like in a solution. One part of floc adsorbs pollutants with higher density and then sinks to the bottom of the reactor, and the other part of floc is attached to H generated by the cathode2Air floatation is carried out on the bubbles, and the purpose of removing pollutants is achieved after solid-liquid separation. Meanwhile, the electrochemical oxidation in the electric flocculation process can also be cooperated with the flocculation process to remove pollutants.
The electric flocculation technology integrates the advantages of chemical flocculation and electrochemistry, the pollutant removal efficiency is high, the equipment is simple, and secondary pollution can not be caused. However, the removal efficiency of the pollutants is affected by the limitation of the free radicals with strong oxidizing property generated in the electric flocculation process.
Disclosure of Invention
The purpose of the invention is as follows: the first purpose of the invention is to provide a sectional type electrochemical water treatment device which can effectively improve the removal rate of refractory organic matters;
a second object of the invention is to provide a method for treatment with the device.
The technical scheme is as follows: the sectional type electrochemical water treatment device comprises an electrolytic bath consisting of a cathode and an anode, wherein an electrolytic channel is formed between the cathode and the anode and is divided into a front section and a rear section, the electrolytic channel of the front section is filled with carbon-based load metal oxide and/or corresponding carbon-based load metal, the electrolytic channel of the rear section is filled with carbon-based load metal and/or iron particles, and the electrolytic channel of the front section is also internally provided with an aeration device.
The invention discloses an electrochemical water treatment method for realizing the in-situ generation of strong oxidizing radicals and adsorption flocs in sections by filling catalytic particle electrodes with different compositions and functions in sections in a continuous electrolytic channel. Preferably, the carbon-based supported metal oxide may be SnO2@ C and/or MnO2@ C. The carbon-based supported metal of the preceding stage may be Sb @ C and/or Mn @ C.
Furthermore, the length of the electrolysis channel of the front section of the electrolysis channel accounts for 30-50% of the total length of the electrolysis channel. The anode material may be aluminum or flat plate iron electrode and the cathode material may be porous stainless steel, graphite or titanium electrode.
The method for treating by adopting the electrochemical water treatment device comprises the following steps: adjusting the conductivity and pH value of the wastewater, starting the aeration device and the electrolytic cell, allowing the wastewater to flow through the front-stage electrolytic channel and the rear-stage electrolytic channel of the electrolytic cell in sequence for reaction for 10-60 min, standing and centrifuging.
Furthermore, the reaction time of the invention is preferably 30-50 min. And adjusting the pH value of the wastewater to 5-7 after flowing through the rear-section electrolytic channel. The aeration rate of the aeration device is 0-10L/min.
The working principle is as follows: in the process of treating waste water, the front section of the electrolytic channel generates a large amount of hydroxyl free radicals (OH) and superoxide free radicals (O) with strong oxidizing property2 -) And hydrogen peroxide (H)2O2) And the like, can directly oxidize the pollutants or break the complex long carbon chain structure of the pollutants, and provides favorable conditions for adsorbing and removing the pollutants by the rear-section flocs. The particle electrode at the rear section of the electrolytic channel generates metal cations, and the yield of hydroxide flocs with strong adsorbability is obviously improved. Therefore, when the refractory organic wastewater is treated, pollutants are directly oxidized and removed or changed into micromolecular organic matters with simple structures through front-section deep oxidation, and then the micromolecular organic matters are adsorbed and removed by flocs generated in situ at the rear section, so that the treatment efficiency of the refractory organic wastewater is effectively improved.
Specifically, when iron is used as the anode, the wastewater firstly passes through the front section of the electrolysis channel, and the iron anode electrolyzes the metal cation Fe2+The cathode produces hydrogen peroxide, Fe2+The reaction with hydrogen peroxide generates a large amount of hydroxyl radicals (. OH). Meanwhile, a carbon-based supported metal oxide (SnO)2@C、MnO2@ C) and carbon-based supported metal (Sb @ C, Mn @ C) to produce OH and O2 -And isooxidative free radicals. OH and O formed2 -The isostrong oxidizing free radical can deeply oxidize refractory organic mattersAnd transforming the mixture into non-toxic micromolecular substances or breaking long carbon chain pollutants to change the mixture into micromolecular substances which are easy to be adsorbed by flocs. And then, an acid or alkaline agent is added to adjust the pH value to the optimal value for treating corresponding wastewater by using a segmented dosing method at the rear section of the electrolytic channel, so that the removal efficiency of pollutants is improved more effectively. An Fe @ C, Al @ C particle electrode is filled at the rear section of the electrolytic channel, and in the process of treating wastewater, an iron (aluminum) anode and the Fe @ C (Al @ C) particle electrode are electrolyzed to generate Fe2+Or Fe3+(Al3+) Cathodic electrolysis of H2And a small amount of OH, while a large amount of OH is formed at the particle electrode, and Fe is formed2+Or Fe3+(Al3+) Combined with OH in the waste water to finally form Fe2O3(Al2O3) FeOOH (AlOOH), etc. Addition of particle electrodes allows Fe to be generated2+Or Fe3+(Al3+) And OH is increased, so that the yield of flocs is effectively improved and the wastewater treatment efficiency is accelerated.
Has the advantages that: compared with the prior art, the invention has the following remarkable advantages: the device realizes the in-situ generation of strong oxidizing radicals and adsorption flocs in sections by filling catalytic particle electrodes with different compositions and functions in a continuous electrolytic channel in sections, so that the removal rate of refractory organic matters is improved, the filled particle electrodes and the cathode and anode form a three-dimensional electrode system, the effective area of the electrodes is increased while OH is generated, and the current efficiency is also improved; meanwhile, the treatment method is simple, has strong operability, can overcome the problem of anode passivation to a certain degree, and reduces energy consumption.
Drawings
FIG. 1 is a schematic view of the structure of the apparatus of the present invention.
Detailed Description
The technical solution of the present invention is further described in detail with reference to the accompanying drawings and embodiments.
As shown in FIG. 1, the sectional type electrochemical water treatment apparatus of the present invention comprises an electrolytic bath consisting of a cathode 1 and an anode 2, with an electrolytic channel formed therebetween. The anode can be an aluminum or flat plate iron electrode, the cathode can be any one of porous stainless steel, graphite and titanium electrodes, and the distance between the cathode and the anode is 3-30 cm.
The electrolysis channel is divided into a front section A and a rear section B, and the length of the electrolysis channel of the front section A accounts for 30-50% of the total length of the electrolysis channel. The electrolysis channel of the front section A is filled with a mixture of carbon-based loaded metal oxide and corresponding carbon-based loaded metal, the electrolysis channel of the rear section is filled with carbon-based loaded metal and/or iron particles, and an aeration device is further arranged in the electrolysis channel of the front section. Wherein, the carbon-based supported metal oxide SnO2@ C and/or MnO2@ C. The carbon-based supported metal of the former stage is Sb @ C and/or Mn @ C. The carbon-based supported metal at the rear section is Fe @ C and/or Al @ C. The particle electrodes are all columnar particles with the length of 1-8 mm.
The particle electrode is prepared by adopting an immersion method, namely active carbon particles are ultrasonically washed and dried to be used as a matrix for preparing the particle electrode.
Carbon-based supported metal: the pretreated active carbon particles are impregnated with 0.1mol/L Mn (NO)3)2And an aqueous solution of chloride of Fe, Al and Sb for 4 hours. And (3) drying in an oven at 100 ℃, and calcining in a muffle furnace at 400 ℃ for 6h to obtain the corresponding particle electrode.
MnO2@ C: adopting an excess impregnation method to impregnate the pretreated activated carbon particles into 0.2mol/L KMnO4(with NH)3·H2Adjusting pH by O), and dropwise adding 0.3mol/L MnSO4And soaking the solution for 4h, drying the solution in an oven at 105 ℃ for 2h, and calcining the solution in a muffle furnace at 500 ℃ for 5h to obtain the corresponding particle electrode.
SnO2@ C, adopting an excess impregnation method to impregnate the pretreated activated carbon particles into 2g/L SnCl4Adding NaOH solution into the ethylene glycol and the water solution, stirring and dispersing, placing the mixture in an oven, drying for 2 hours at 105 ℃, and then placing the mixture in a muffle furnace, and calcining for 5 hours at 500 ℃ to obtain the corresponding particle electrode.
Example 1
In the embodiment, Methyl Orange (MO) wastewater is treated, and the total concentration of the wastewater is 500 ppm; the treatment method comprises the following specific steps:
(1) adjusting the conductivity of the wastewater to 4000 mus/cm, and adjusting the initial pH value of the wastewater to 3;
(2) the flat iron electrode is used as an anode, the porous stainless steel electrode is used as a cathode, the distance between the polar plates is 3cm, and the particle electrode at the front section of the electrolytic channel is carbon-based loaded metal oxide (MnO)2@ C) and a carbon-based supported metal (Mn @ C); the particle electrode at the rear section of the electrolytic channel is a combination of carbon-based loaded metal (Fe @ C) and scrap iron;
(3) the power supply connected with the electrolytic cell is a direct current power supply, the voltage of the electrolytic reaction is 6V, and the current density is 2mA/cm2Starting an aeration device of the front-section electrolysis channel to ensure that the cathode aeration rate is 1L/min, enabling the wastewater to sequentially flow through the front-section electrolysis channel and the rear-section electrolysis channel of the electrolysis bath to respectively react for 10min, 20min, 30min, 40min, 50min and 60min, and adjusting the pH value of the wastewater to be 5-6 when the wastewater flows through the rear-section electrolysis channel;
(4) and (3) standing the treated wastewater for 15min after the reaction is finished, and centrifuging for 10 min.
The treated wastewater was subjected to performance testing, and the results obtained are shown in table 1 below.
TABLE 1 parameters of example 1 and performance index of treated wastewater
| Parameters (reaction time) | t＝10min | t＝20min | t＝30min | t＝40min | t＝50min | t＝60min |
| Decolorization ratio/% | 89.37 | 91.55 | 94.55 | 94.72 | 95.05 | 92.48 |
| COD removal Rate/%) | 78.64 | 82.71 | 85.79 | 85.71 | 86.98 | 82.26 |
Comparative example 1
This comparative example is essentially the same as example 1 except that the continuous electrolytic channel is not filled with catalytic particle electrode particles; the specific treatment steps are as follows:
(1) adjusting the conductivity of the wastewater to 4000 mus/cm, and adjusting the initial pH value of the wastewater to 3;
(2) taking an iron electrode as an anode and a porous stainless steel electrode as a cathode, wherein the distance between the polar plates is 3cm, and the cathode aeration rate is 1L/min;
(3) the power supply connected with the electrolytic cell is a direct current power supply, the voltage of the electrolytic reaction is 6V, and the current density is 2mA/cm2The wastewater sequentially flows through a front-stage electrolysis channel and a rear-stage electrolysis channel of the electrolysis bath to react for 10min, 20min, 30min, 40min, 50min and 60min respectively, and when the wastewater flows through the rear-stage electrolysis channel, the pH value of the wastewater is adjusted to be 5-6;
(4) and (3) standing the treated wastewater for 15min after the reaction is finished, and centrifuging for 10 min.
The treated wastewater was subjected to performance testing, and the results obtained are shown in table 2 below.
TABLE 2 parameters of comparative example 1 and performance index of treated wastewater
| Parameters (reaction time) | t＝10min | t＝20min | t＝30min | t＝40min | t＝50min | t＝60min |
| Decolorization ratio/% | 77.92 | 80.37 | 85.43 | 86.94 | 87.61 | 81.40 |
| COD removal Rate/%) | 70.09 | 70.88 | 73.68 | 75.31 | 75.75 | 81.56 |
By combining the table 1 and the table 2, the treatment method for the high-concentration methyl orange wastewater by respectively generating the strong oxidizing radicals and the adsorption flocs in situ in a segmented manner is adopted to treat the high-concentration methyl orange wastewater, so that the decolorization rate and the COD removal rate of the methyl orange are remarkably improved when a direct-current power supply is used compared with those when a particle electrode is not filled, and the treatment effect is optimal when the retention time is 30-50 min.
Example 2
The embodiment treats Malachite Green (MG) wastewater, and the total concentration of the wastewater is 50 ppm; the treatment method comprises the following specific steps:
(1) adjusting the conductivity of the wastewater to be 500 mu s/cm, and adjusting the initial pH values of the wastewater to be 2, 3 and 4 respectively;
(2) an aluminum electrode is used as an anode, a porous graphite electrode is used as a cathode, the distance between polar plates is 10cm, and a particle electrode at the front section of an electrolysis channel is a carbon-based supported metal oxide (SnO)2@ C) and a carbon-based supported metal (Sb @ C); the particle electrode at the rear section of the electrolytic channel is a combination of carbon-based supported metal (Al @ C) and iron particles;
(3) the power supply connected with the electrolytic cell is an intermittent pulse power supply, and the current output density is controlled to be 4mA/cm2The duty ratio is 0.4, the frequency is 1kHz, the power-on period is 0.5ms, and the power-off period is 0.4 ms; starting an aeration device of the front-section electrolysis channel to ensure that the cathode aeration rate is 4L/min, reacting the wastewater flowing through the front-section electrolysis channel and the rear-section electrolysis channel of the electrolysis bath for 30min in sequence, and adjusting the pH value of the wastewater to be 6-7 when the wastewater flows through the rear-section electrolysis channel;
(4) and (3) standing the treated wastewater for 20min after the reaction is finished, and centrifuging for 5 min.
The treated wastewater was subjected to performance tests, and the results obtained are shown in table 3 below.
TABLE 3 parameters of example 2 and performance index of treated wastewater
Comparative example 2
This comparative example is essentially the same as example 2, except that the continuous electrolytic channel is not filled with catalytic particle electrode particles; the treatment method comprises the following specific steps:
(1) adjusting the conductivity of the wastewater to be 500 mu s/cm, and adjusting the initial pH value of the wastewater to be 2, 3 and 4;
(2) taking an aluminum electrode as an anode and a porous graphite electrode as a cathode, wherein the distance between polar plates is 10 cm;
(3) the power supply connected with the electrolytic cell is an intermittent pulse power supply, and the current output density is controlled to be 4mA/cm2The duty ratio is 0.4, the frequency is 1kHz, the power-on period is 0.5ms, and the power-off period is 0.4 ms; starting an aeration device of the front-section electrolysis channel to ensure that the cathode aeration rate is 4L/min, reacting the wastewater flowing through the front-section electrolysis channel and the rear-section electrolysis channel of the electrolysis bath for 30min in sequence, and adjusting the pH value of the wastewater to be 6-7 when the wastewater flows through the rear-section electrolysis channel;
(4) after the reaction is finished, the treated wastewater is statically precipitated for 20min and centrifuged for 5 min.
The treated wastewater was subjected to performance tests, and the results obtained are shown in table 4 below.
TABLE 4 parameters of comparative example 2 and performance index of treated wastewater
| Parameters (initial pH) | 2 | 3 | 4 |
| Decolorization ratio/% | 84.47 | 88.65 | 85.13 |
| COD removal Rate/%) | 76.64 | 80.32 | 78.25 |
It can be known from tables 3 and 4 that, when the treatment method of the present invention is used to treat malachite green wastewater, which generates strong oxidizing radicals and adsorbed flocs in situ in stages, the malachite green decolorization rate and the COD removal rate are both effectively improved compared with those when no particle electrode is filled, and the treatment effect is the best when the initial pH is 3.
Example 3
This example treats reactive blue 19(RB19) wastewater with a total concentration of 100 ppm; the treatment method comprises the following specific steps:
(1) adjusting the conductivity of the wastewater to 8000 mus/cm and the initial pH value of the wastewater to 3;
(2) taking an iron electrode as an anode and a porous titanium electrode as a cathode, wherein the distance between the polar plates is 30cm, and the particle electrode at the front section of the electrolytic channel is a carbon-based supported metal oxide (SnO)2@C、MnO2@ C) and a carbon-based supported metal (Sb @ C, Mn @ C); the particle electrode at the rear section of the electrolytic channel is a combination of carbon-based supported metal (Fe @ C), iron particles and scrap iron;
(3) the power supply connected with the electrolytic cell is a direct current power supply, the voltage of the electrolytic reaction is 25V, and the current density is 6mA/cm2Starting an aeration device of the front-section electrolysis channel to ensure that the cathode aeration rate is 10L/min, enabling the wastewater to sequentially flow through the front-section electrolysis channel and the rear-section electrolysis channel of the electrolysis bath for reaction for 40min, and adjusting the pH value of the wastewater to be 5-7 when the wastewater flows through the rear-section electrolysis channel;
(4) and (3) standing the treated wastewater for 25min after the reaction is finished, and centrifuging for 6 min.
The treated wastewater was subjected to performance tests, and the results obtained are shown in table 5 below.
TABLE 5 parameters of example 3 and performance index of treated wastewater
| Performance of | Decolorization ratio/% | COD removal Rate/%) |
| Parameter(s) | 91.34 | 85.23 |
Example 4
This comparative example is substantially the same as example 3 except that the power source was changed from a direct current power source to an intermittent pulse power source.
The comparative example treats the wastewater of the active blue 19(RB19), and the total concentration of the wastewater is 100 ppm; the treatment method comprises the following specific steps:
(1) adjusting the conductivity of the wastewater to 8000 mus/cm and the initial pH value of the wastewater to 3;
(2) taking an iron electrode as an anode and a porous titanium electrode as a cathode, wherein the distance between the polar plates is 30cm, and the particle electrode at the front section of the electrolytic channel is a carbon-based supported metal oxide (SnO)2@C、MnO2@ C) and a carbon-based supported metal (Sb @ C, Mn @ C); the particle electrode at the rear section of the electrolytic channel is a combination of carbon-based supported metal (Fe @ C), iron particles and scrap iron;
(3) the power supply connected with the electrolytic bath is an intermittent pulse power supply,controlling the current output density to be 6mA/cm2The duty ratio is 0.5, the frequency is 1kHz, the power-on period is 0.9ms, and the power-off period is 0.8 ms; starting an aeration device of the front-section electrolysis channel to ensure that the cathode aeration rate is 10L/min, enabling the wastewater to sequentially flow through the front-section electrolysis channel and the rear-section electrolysis channel of the electrolysis bath for reaction for 40min, and adjusting the pH value of the wastewater to be 5-7 when the wastewater flows through the rear-section electrolysis channel;
(4) and (3) standing the treated wastewater for 25min after the reaction is finished, and centrifuging for 6 min.
The treated wastewater was subjected to performance tests, and the results obtained are shown in table 6 below.
TABLE 6 parameters of example 4 and performance index of treated wastewater
| Performance of | Decolorization ratio/% | COD removal Rate/%) |
| Parameter(s) | 92.06 | 85.85 |
Example 5
This comparative example is substantially the same as example 3 except that the particle electrodes filled in the front and rear stages are all single particles.
The comparative example treats the wastewater of the active blue 19(RB19), and the total concentration of the wastewater is 100 ppm; the treatment method comprises the following specific steps:
(1) adjusting the conductivity of the wastewater to 8000 mus/cm and the initial pH value of the wastewater to 3;
(2) taking an iron electrode as an anode and a porous titanium electrode as a cathodeThe distance between the cathode and the polar plate is 30cm, and the particle electrode at the front section is carbon-based supported metal oxide (SnO)2@ C); the particle electrode at the rear section is carbon-based supported metal (Fe @ C);
(3) the power supply connected with the electrolytic cell is a direct current power supply, the voltage of the electrolytic reaction is 25V, and the current density is 6mA/cm2Starting an aeration device of the front-section electrolysis channel to ensure that the cathode aeration rate is 7L/min, enabling the wastewater to sequentially flow through the front-section electrolysis channel and the rear-section electrolysis channel of the electrolysis bath for reaction for 40min, and adjusting the pH value of the wastewater to be 5-7 when the wastewater flows through the rear-section electrolysis channel;
(4) and (3) standing the treated wastewater for 25min after the reaction is finished, and centrifuging for 6 min.
The treated wastewater was subjected to performance tests, and the results obtained are shown in table 7 below.
TABLE 7 parameters of example 5 and performance index of treated wastewater
| Performance of | Decolorization ratio/% | COD removal Rate/%) |
| Parameter(s) | 90.45 | 84.73 |
As can be seen from table 5, table 6 and table 7, under the same conditions, the decoloring rate and the COD removal rate of the wastewater containing active blue 19 by connecting the dc power supply and the intermittent pulse power supply are nearly the same; the decolorization rate and the COD removal rate of the active blue 19 wastewater by filling the mixed particle electrode and filling the single particle electrode are also approximately consistent. Therefore, the treatment method of connecting any power supply, filling single or mixed particle electrodes and respectively generating strong oxidizing free radicals and adsorbing flocs in situ can improve the decolorization rate and the COD removal rate of the dye wastewater.
Example 6
In the embodiment, the rhodamine B (RhB) wastewater is treated, and the total concentration of the wastewater is 100 ppm; the treatment method comprises the following specific steps:
(1) adjusting the conductivity of the wastewater to 2000 mus/cm and the initial pH value of the wastewater to 3;
(2) an aluminum electrode is used as an anode, a porous stainless steel electrode is used as a cathode, the distance between polar plates is 20cm, and a particle electrode at the front section of an electrolysis channel is a carbon-based supported metal oxide (SnO)2@ C) and a carbon-based supported metal (Sb @ C); the particle electrode at the rear section of the electrolytic channel is carbon-based loaded metal (Al @ C);
(3) the power supply connected with the electrolytic cell is a direct current power supply, the voltage of the electrolytic reaction is 20V, and the current density is 5mA/cm2Starting an aeration device of the front-section electrolysis channel to ensure that the cathode aeration rate is 6L/min, reacting the wastewater flowing through the front-section electrolysis channel and the rear-section electrolysis channel of the electrolysis bath for 50min in sequence, and adjusting the pH value of the wastewater to be 5-7 when the wastewater flows through the rear-section electrolysis channel;
(4) and (3) standing the treated wastewater for 15min after the reaction is finished, and centrifuging for 8 min.
The treated wastewater was subjected to performance tests, and the results obtained are shown in table 8 below.
TABLE 8 parameters and performance index of treated wastewater of example 6
| Performance of | Decolorization ratio/% | COD removal Rate/%) |
| Parameter(s) | 95.67 | 89.36 |
Comparative example 3
The comparative example is basically the same as the example 6, except that the electrode which is not filled with particles at the front section of the electrolytic channel is changed into a flat catalytic electrode; the treatment method comprises the following specific steps:
(1) adjusting the conductivity of the wastewater to 2000 mus/cm and the initial pH value of the wastewater to 3;
(2) the anode of the electrolysis channel section is Ti/SnO2Bi, wherein the anode at the rear section of the electrolytic channel is an aluminum electrode, the cathode is a porous stainless steel electrode, and the distance between polar plates is 20 cm; the particle electrode at the rear section of the electrolytic channel is carbon-based loaded metal (Al @ C);
(3) the power supply connected with the electrolytic cell is a direct current power supply, the voltage of the electrolytic reaction is 20V, and the current density is 5mA/cm2Starting an aeration device of the front-section electrolysis channel to ensure that the cathode aeration rate is 6L/min, reacting the wastewater flowing through the front-section electrolysis channel and the rear-section electrolysis channel of the electrolysis bath for 50min in sequence, and adjusting the pH value of the wastewater to be 5-7 when the wastewater flows through the rear-section electrolysis channel;
(4) and (3) standing the treated wastewater for 15min after the reaction is finished, and centrifuging for 8 min.
The treated wastewater was subjected to performance tests, and the results obtained are shown in table 9 below.
TABLE 9 parameters of comparative example 3 and performance index of treated wastewater
| Performance of | Decolorization ratio/% | COD removal Rate/%) |
| Parameter(s) | 93.52 | 86.29 |
It can be known from tables 8 and 9 that, under the same other conditions, the decoloring rates of the rhodamine B wastewater by filling catalytic particle electrode particles or adding a flat catalytic electrode are nearly the same, so that the decoloring rate and the COD removal rate of the dye wastewater can be improved by any treatment method of respectively generating strong oxidizing radicals and adsorbing flocs in situ in a segmented manner.
Claims (3)
1. A sectional type electrochemical water treatment device is characterized in that: the electrolytic cell comprises an electrolytic cell consisting of a cathode and an anode, wherein an electrolytic channel is formed between the cathode and the anode and is divided into a front section and a rear section, wherein the electrolytic channel of the front section is filled with carbon-based loaded metal oxide and/or corresponding carbon-based loaded metal, the electrolytic channel of the rear section is filled with carbon-based loaded metal and/or iron particles, and an aeration device is also arranged in the electrolytic channel of the front section; the anode material is an aluminum or flat plate iron electrode, and the cathode material is a porous stainless steel, graphite or titanium electrode; the length of the front-section electrolysis channel accounts for 30-50% of the total length of the electrolysis channel; the front-section carbon-based supported metal oxide is SnO2@ C and/or MnO2@ C; the carbon-based supported metal of the front section is Sb @ C and/or Mn @ C; the carbon-based supported metal at the rear section is Fe @ C and/or Al @ C.
2. A method of treatment using the electrochemical water treatment device of claim 1, comprising the steps of: adjusting the conductivity and pH value of the wastewater, starting the aeration device and the electrolytic bath, sequentially flowing through a front-section electrolytic channel and a rear-section electrolytic channel of the electrolytic bath, reacting for 10-60 min, wherein the aeration rate of the aeration device is 1-10L/min, adjusting the pH value of the wastewater to 5-7 after flowing through the rear-section electrolytic channel, standing and centrifuging.
3. The processing method according to claim 2, characterized in that: and reacting for 30-50 min.
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101955280A (en) * | 2010-08-13 | 2011-01-26 | 南京赛佳环保实业有限公司 | Technology for processing high-concentration organic wastewater in composite electrochemical method |
| CN103539296A (en) * | 2013-10-31 | 2014-01-29 | 四川凯沃环保科技有限公司 | Method and device for treating high-concentration nonbiodegradable organic wastewater |
| CN108706693A (en) * | 2018-05-24 | 2018-10-26 | 天津大学 | Handle suspended matter and changeable three electrode reactors of persistent organic pollutants |
| CN109694119A (en) * | 2018-04-26 | 2019-04-30 | 中电华创电力技术研究有限公司 | A method of desulfurization wastewater is handled using modified activated carbon granule electrode |
| GB201913584D0 (en) * | 2019-06-26 | 2019-11-06 | Univ Central South | Method and device for sewage treatment |
-
2019
- 2019-11-08 CN CN201911085910.3A patent/CN110845055B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101955280A (en) * | 2010-08-13 | 2011-01-26 | 南京赛佳环保实业有限公司 | Technology for processing high-concentration organic wastewater in composite electrochemical method |
| CN103539296A (en) * | 2013-10-31 | 2014-01-29 | 四川凯沃环保科技有限公司 | Method and device for treating high-concentration nonbiodegradable organic wastewater |
| CN109694119A (en) * | 2018-04-26 | 2019-04-30 | 中电华创电力技术研究有限公司 | A method of desulfurization wastewater is handled using modified activated carbon granule electrode |
| CN108706693A (en) * | 2018-05-24 | 2018-10-26 | 天津大学 | Handle suspended matter and changeable three electrode reactors of persistent organic pollutants |
| GB201913584D0 (en) * | 2019-06-26 | 2019-11-06 | Univ Central South | Method and device for sewage treatment |
Non-Patent Citations (1)
| Title |
|---|
| 活性炭负载多组元金属氧化物复合材料制备及其电催化氧化水中污染物的性能;赵鑫;《中国优秀博硕士学位论文全文数据库（硕士） 工程科技I辑》;20180415;第14-16、18页 * |
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