CN116282400A - Double-pulse piezoelectric flocculation method for treating mine acid wastewater containing heavy metals - Google Patents
Double-pulse piezoelectric flocculation method for treating mine acid wastewater containing heavy metals Download PDFInfo
- Publication number
- CN116282400A CN116282400A CN202310249551.0A CN202310249551A CN116282400A CN 116282400 A CN116282400 A CN 116282400A CN 202310249551 A CN202310249551 A CN 202310249551A CN 116282400 A CN116282400 A CN 116282400A
- Authority
- CN
- China
- Prior art keywords
- flocculation
- pulse
- double
- heavy metals
- water
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 238000005189 flocculation Methods 0.000 title claims abstract description 103
- 230000016615 flocculation Effects 0.000 title claims abstract description 91
- 239000002351 wastewater Substances 0.000 title claims abstract description 44
- 238000000034 method Methods 0.000 title claims abstract description 30
- 229910001385 heavy metal Inorganic materials 0.000 title claims abstract description 28
- 239000002253 acid Substances 0.000 title claims abstract description 24
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims abstract description 70
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 55
- 229910052742 iron Inorganic materials 0.000 claims abstract description 36
- 239000010802 sludge Substances 0.000 claims abstract description 21
- 238000005265 energy consumption Methods 0.000 claims abstract description 19
- 230000033228 biological regulation Effects 0.000 claims abstract description 16
- 230000009467 reduction Effects 0.000 claims abstract description 13
- 238000005273 aeration Methods 0.000 claims abstract description 11
- 238000007885 magnetic separation Methods 0.000 claims abstract description 9
- 238000003860 storage Methods 0.000 claims abstract description 4
- 239000002245 particle Substances 0.000 claims description 16
- 230000000694 effects Effects 0.000 claims description 15
- 238000001556 precipitation Methods 0.000 claims description 12
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims description 11
- 239000003792 electrolyte Substances 0.000 claims description 11
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 8
- -1 aluminum ions Chemical class 0.000 claims description 8
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 7
- 239000001301 oxygen Substances 0.000 claims description 7
- 229910052760 oxygen Inorganic materials 0.000 claims description 7
- 230000002441 reversible effect Effects 0.000 claims description 7
- 238000004062 sedimentation Methods 0.000 claims description 7
- 229910006299 γ-FeOOH Inorganic materials 0.000 claims description 7
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 claims description 6
- VLTRZXGMWDSKGL-UHFFFAOYSA-N perchloric acid Chemical compound OCl(=O)(=O)=O VLTRZXGMWDSKGL-UHFFFAOYSA-N 0.000 claims description 6
- 229910052782 aluminium Inorganic materials 0.000 claims description 5
- 230000015572 biosynthetic process Effects 0.000 claims description 5
- 238000002474 experimental method Methods 0.000 claims description 5
- 229910001448 ferrous ion Inorganic materials 0.000 claims description 5
- 230000005389 magnetism Effects 0.000 claims description 5
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 claims description 4
- 230000008859 change Effects 0.000 claims description 4
- 238000005868 electrolysis reaction Methods 0.000 claims description 4
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 claims description 4
- 239000002244 precipitate Substances 0.000 claims description 4
- 230000001737 promoting effect Effects 0.000 claims description 4
- 239000011780 sodium chloride Substances 0.000 claims description 4
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 3
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 claims description 3
- 239000000460 chlorine Substances 0.000 claims description 3
- 238000000975 co-precipitation Methods 0.000 claims description 3
- 238000000151 deposition Methods 0.000 claims description 3
- 238000013461 design Methods 0.000 claims description 3
- 239000007789 gas Substances 0.000 claims description 3
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 claims description 3
- 238000011835 investigation Methods 0.000 claims description 3
- 239000001103 potassium chloride Substances 0.000 claims description 3
- 230000000630 rising effect Effects 0.000 claims description 3
- 230000002378 acidificating effect Effects 0.000 claims description 2
- 230000027756 respiratory electron transport chain Effects 0.000 claims description 2
- 238000003911 water pollution Methods 0.000 abstract description 2
- 230000007423 decrease Effects 0.000 abstract 1
- 239000011651 chromium Substances 0.000 description 50
- 239000000243 solution Substances 0.000 description 18
- 238000002161 passivation Methods 0.000 description 11
- 238000006243 chemical reaction Methods 0.000 description 8
- 230000008569 process Effects 0.000 description 8
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 6
- 229910052804 chromium Inorganic materials 0.000 description 6
- 238000010586 diagram Methods 0.000 description 6
- 238000001179 sorption measurement Methods 0.000 description 6
- 230000009286 beneficial effect Effects 0.000 description 5
- 150000002500 ions Chemical class 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- 230000007797 corrosion Effects 0.000 description 4
- 238000005260 corrosion Methods 0.000 description 4
- 238000009297 electrocoagulation Methods 0.000 description 4
- 230000007246 mechanism Effects 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 230000001276 controlling effect Effects 0.000 description 3
- 230000010287 polarization Effects 0.000 description 3
- 238000012360 testing method Methods 0.000 description 3
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 238000012271 agricultural production Methods 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 238000009713 electroplating Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 239000003337 fertilizer Substances 0.000 description 2
- 230000036541 health Effects 0.000 description 2
- 238000009776 industrial production Methods 0.000 description 2
- 230000002401 inhibitory effect Effects 0.000 description 2
- SZVJSHCCFOBDDC-UHFFFAOYSA-N iron(II,III) oxide Inorganic materials O=[Fe]O[Fe]O[Fe]=O SZVJSHCCFOBDDC-UHFFFAOYSA-N 0.000 description 2
- 239000010985 leather Substances 0.000 description 2
- 238000005259 measurement Methods 0.000 description 2
- 239000000575 pesticide Substances 0.000 description 2
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- KMUONIBRACKNSN-UHFFFAOYSA-N potassium dichromate Chemical compound [K+].[K+].[O-][Cr](=O)(=O)O[Cr]([O-])(=O)=O KMUONIBRACKNSN-UHFFFAOYSA-N 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 239000011550 stock solution Substances 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- 229910000604 Ferrochrome Inorganic materials 0.000 description 1
- VVQNEPGJFQJSBK-UHFFFAOYSA-N Methyl methacrylate Chemical compound COC(=O)C(C)=C VVQNEPGJFQJSBK-UHFFFAOYSA-N 0.000 description 1
- 229920005372 Plexiglas® Polymers 0.000 description 1
- 238000002835 absorbance Methods 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 239000010405 anode material Substances 0.000 description 1
- 229910001566 austenite Inorganic materials 0.000 description 1
- WURBFLDFSFBTLW-UHFFFAOYSA-N benzil Chemical group C=1C=CC=CC=1C(=O)C(=O)C1=CC=CC=C1 WURBFLDFSFBTLW-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- UPHIPHFJVNKLMR-UHFFFAOYSA-N chromium iron Chemical compound [Cr].[Fe] UPHIPHFJVNKLMR-UHFFFAOYSA-N 0.000 description 1
- VQWFNAGFNGABOH-UHFFFAOYSA-K chromium(iii) hydroxide Chemical compound [OH-].[OH-].[OH-].[Cr+3] VQWFNAGFNGABOH-UHFFFAOYSA-K 0.000 description 1
- 239000000701 coagulant Substances 0.000 description 1
- 238000005345 coagulation Methods 0.000 description 1
- 230000015271 coagulation Effects 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000007865 diluting Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000002848 electrochemical method Methods 0.000 description 1
- 238000003487 electrochemical reaction Methods 0.000 description 1
- 239000008394 flocculating agent Substances 0.000 description 1
- 244000144992 flock Species 0.000 description 1
- 239000013505 freshwater Substances 0.000 description 1
- 239000003673 groundwater Substances 0.000 description 1
- 229910052595 hematite Inorganic materials 0.000 description 1
- 239000011019 hematite Substances 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- LIKBJVNGSGBSGK-UHFFFAOYSA-N iron(3+);oxygen(2-) Chemical compound [O-2].[O-2].[O-2].[Fe+3].[Fe+3] LIKBJVNGSGBSGK-UHFFFAOYSA-N 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000006213 oxygenation reaction Methods 0.000 description 1
- 239000003973 paint Substances 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 238000007747 plating Methods 0.000 description 1
- 229910052697 platinum Inorganic materials 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000011435 rock Substances 0.000 description 1
- 239000013049 sediment Substances 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 238000002798 spectrophotometry method Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000002352 surface water Substances 0.000 description 1
- 230000004083 survival effect Effects 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
- 239000004753 textile Substances 0.000 description 1
- 238000009210 therapy by ultrasound Methods 0.000 description 1
- 238000012876 topography Methods 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 229910021642 ultra pure water Inorganic materials 0.000 description 1
- 239000012498 ultrapure water Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
- 229910000859 α-Fe Inorganic materials 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- 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
- C02F1/463—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrocoagulation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/20—Heavy metals or heavy metal compounds
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Electrochemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Water Treatment By Electricity Or Magnetism (AREA)
Abstract
The invention belongs to the technical field of water pollution treatment, and in particular relates to a double-pulse piezoelectric flocculation method for treating mine acid wastewater containing heavy metals, which comprises the following steps: the raw water quantity and the water quality condition are defined; selecting a vertical folded plate flocculation tank, wherein a plurality of columnar iron anodes and folded plate-shaped iron cathodes are arranged in the vertical folded plate flocculation tank, and the speed gradient or flocculation flow rate gradually decreases from a water inlet to a water storage port in the flocculation process; the electric flocculation Chi Yinyang polar plate is electrified with current to select double-pulse low-voltage current, and wastewater is treated by using an intermittent mode of 'electrifying-de-electrifying' of a pulse power supply; the magnetic separation performance of the flocs is changed by combining the double pulse waveform regulation and control with aeration and air-expelling, and the sludge reduction of water treatment is controlled. The invention uses double pulse current to replace direct current, which can greatly save the energy consumption of treatment and reduce the generation amount of sludge.
Description
Technical Field
The invention belongs to the technical field of water pollution treatment, and particularly relates to a double-pulse piezoelectric flocculation method for treating mine acid wastewater containing heavy metals.
Background
In recent years, chromium has been widely used in plating, chemical, leather and other industries, which causes a large amount of chromium to be discharged into water bodies, resulting in the occurrence of chromium pollution events in recent years. The occurrence of these chromium contamination events poses a serious threat to human survival and health. The sources of Cr (VI) in water are mainly divided into naturally occurring and artificially generated, and the naturally occurring Cr (VI) enters the water mainly by means of the dissolution of rock. However, cr (VI) produced artificially is mainly derived from byproducts produced in industrial and agricultural production activities, for example, in agricultural production activities, chemical fertilizers or pesticides mostly contain chromium, and by applying chemical fertilizers and pesticides to plants, chromium is directly introduced into soil, and is then leached into surface water or groundwater by rainfall. In industrial production activities, a large amount of Cr (VI) containing wastewater is generated in the technological processes of chromite refining, electroplating, leather, ferrochrome, paint, textile and the like. Particularly, a large amount of Cr (VI) containing wastewater is generated in the electroplating industry, and the large-scale Cr (VI) containing wastewater is easy to threaten fresh water resources and human health if the wastewater is discharged or treated improperly.
The electroflocculation method is an electrochemical technology which is widely applied at present, and mainly relies on the principle of electrochemical reaction to electrolytically reduce heavy metal ions with high valence and strong toxicity into a low valence form, and the heavy metal ions are precipitated under the synergistic effect of a chemical coagulant so as to be removed from water. The reaction mainly comprises the following steps that the anode is subjected to electrolytic reaction and gradually dissolved in a solution to generate a flocculating agent; under the action of the flocculant, the pollutants in the water body are gradually destabilized; the destabilized pollutant is continuously collided with the generated flocculant to form large particles, and then the large particles are deposited and removed. Iron and aluminum are relatively large anode materials used in the electrocoagulation process of water treatment. Taking iron as the anode, at lower current densities, the iron anode gradually oxidizes and begins to dissolve ferrous ions into the water and then reacts with Cr (VI) in the solution. Cr (VI) gets electrons from the cathode and is then reduced to Cr (III), and aluminum ions generated by anodic electrolysis can form aluminum hydroxide precipitates which are co-precipitated with Cr (OH) 3 as a flocculant.
The process for treating Cr (VI) by the electric flocculation method has the advantages of relatively perfect development and good treatment effect, but has the defect of needing improvement. For example, the current intensity needs to be adjusted at all times; the surface of the electrode is easy to be passivated, the anode needs to be replaced at random, an effective product formed after flocculation is unstable, and the electrode is easy to be dissolved by oneself.
Disclosure of Invention
Aiming at the problems of passivation of polar plates, energy consumption, sludge amount and the like of the wastewater containing Cr (VI) by electric flocculation, the invention provides a double-pulse piezoelectric flocculation method for treating mine acidic wastewater containing heavy metals, which can reduce the passivation speed of the polar plates, reduce the energy consumption, reduce the produced sludge amount and treat the wastewater containing Cr (VI) rapidly and efficiently.
In order to achieve the technical purpose and the technical effect, the invention is realized by the following technical scheme:
a double-pulse piezoelectric flocculation method for treating mine acid wastewater containing heavy metals comprises the following steps:
s1, according to investigation data of mine wastewater and related laws and regulations, defining raw water quantity and water quality conditions, and determining design parameters of an electric flocculation tank through experiments and operation experience;
s2, selecting a vertical folded plate flocculation tank from the flocculation tank, wherein a plurality of columnar iron anodes and folded plate-shaped iron cathodes are arranged in the vertical folded plate flocculation tank, and the mine acid wastewater containing heavy metals is repeatedly baffled under the guidance of the folded plate-shaped iron cathodes, so that the speed gradient or the flocculation flow rate in the flocculation process is gradually reduced from a water inlet to a water storage port, and the full and perfect flocculation process is ensured;
s3, the current conducted by the electric flocculation Chi Yinyang polar plate selects double-pulse low-voltage current, and wastewater is treated by using an intermittent mode of 'power-on-power-off-power-on' of a pulse power supply;
s4, changing the magnetic separation performance of the floccules by combining the double pulse waveform regulation and control with aeration and air-expelling, and controlling the sludge reduction of the water treatment.
Further, in step S2, each piece of data of the vertical flap sedimentation tank is:
g=80s relative to the first section of the flap -1 ，t≥240s；
Second section of parallel flap, g=50s -1 ，t≥240s；
Third section of parallel flap, g=25s -1 ，t≥240s。
Further, the included angle of the folded plate is 90-120 degrees, the width of the folded plate is 0.4-0.6 m, and the length of the folded plate is 0.8-1.5 m.
Further, in step S2, the flocculation tank needs to have enough flocculation time, and the flocculation tank should be built in combination with the sedimentation tank as much as possible to avoid using pipe connection, for example, the pipe connection should be controlled to avoid the sudden rise of the flow rate to cause the drop of the water head; to avoid the breaking of formed flocs, the flow rate of the through holes of the water outlet perforated wall of the flocculation tank should be controlled; in order to avoid the flocs depositing in the flocculation basin, corresponding sludge discharge measures are adopted if necessary.
Further, in step S3, after the power is turned on, the iron anode is gradually oxidized and starts to dissolve ferrous ions into water, and then reacts with Cr (VI) in the solution; cr (VI) gets electrons from the cathode and is then reduced to Cr (III), and aluminum ions generated by anodic electrolysis can form aluminum hydroxide precipitates which are used as flocculant and Cr (OH) 3 Co-precipitation; large-particle flocs are removed through precipitation, small-particle flocs are removed through an air floatation effect, and the large-particle flocs are added into a precipitation tank after a water outlet for flocculation precipitation removal.
Further, when energized, the current density was 20Am -2 The peak voltage is 5V, the current frequency is 5000Hz, and the optimal duty cycle is 30%.
Further, when the ratio of the number of positive pulses to the number of negative pulses of the double pulse electric flocculation is larger, the corresponding Cr (VI) removal rate is higher; when the ratio of the positive pulse to the negative pulse is 10, the removal rate is 99.2% at the highest, and the corresponding energy consumption is also the lowest.
Further, factors affecting the removal rate are:
a. when the pH of the mine acid wastewater containing heavy metals is more than 6, the removal rate is less changed along with the rising of the initial pH;
b. the low conductivity of the mine acid wastewater containing heavy metals can lead to the reduction of the removal rate and the increase of the energy consumption, but the excessively high conductivity can limit the voltage, so that the removal rate is reduced;
c. the increase of the plate spacing can increase the removal rate, but the excessive plate spacing can passivate the plates;
d. when the initial concentration of Cr (VI) is too high, the formation of flocs of the anodically dissolved iron ions is insufficient to remove Cr (VI) at high concentrations, which reduces the removal rate.
Further, in the step S4, the magnetic separation performance of the floccule is changed by combining aeration/gas-expelling and easily-obtained chlorine ion-containing electrolyte through reversible reverse waveform regulation and control of double pulses, and the sludge reduction of water treatment is controlled; the gamma-FeOOH is generated by promoting electron transfer through the combination of double pulse waveform regulation and aeration, and when the gas is purged, the dissolved oxygen is reduced, and the Cl is electrolyzed by the iron and the electrolyte containing chloride ions under the double pulse regulation and control - Is converted into green rust, thereby changing the magnetism of the floc.
Further, the electrolyte containing chloride ions is at least one of NaCl, KCl, HCl and perchloric acid.
The beneficial effects of the invention are as follows:
1. compared with direct current flocculation, the double-pulse electric flocculation can greatly save the energy consumption of treatment and reduce the generation amount of sludge. The positive ions dissolved by the anode are beneficial to diffusing into the solution during the outage period of the current in one period, which is beneficial to inhibiting the concentration polarization phenomenon, and the purposes of saving energy consumption and reducing the passivation of the polar plate are achieved. Compared with traditional direct current flocculation, the double-pulse electric flocculation has more stable treatment process.
2. The invention researches the influence of different positive and negative pulse numbers on the electric flocculation effect and the electric energy consumption. The ratio of positive pulse to negative pulse with the highest removal rate is obtained.
3. The invention confirms that the pulse double electric flocculation has good stability in the field of treating Cr (VI) wastewater by exploring the change of the floc magnetism in the electric flocculation process.
4. The invention obtains the optimal operation condition by exploring the influence of different water quality conditions and operation parameters on the electric flocculation and the double-pulse electric flocculation to remove Cr (VI) in the wastewater and comparing the different electric flocculation process performances.
5. The invention reduces the consumption and replacement frequency of the anode plate by using the columnar anode, has large contact area between sewage and the electrode, and improves mass transfer effect between substances.
6. The invention uses the folded plate-shaped cathode plate, which not only generates electrolytic reaction but also plays a role in guiding water flow. The passivation phenomenon of the polar plate can be eliminated, and the flocculation effect is improved.
7. The invention combines the double pulse waveform regulation and control with aeration/gas expelling and the easily obtained chloride ion electrolyte to change the magnetic separation performance of the floccule, thereby controlling the sludge reduction of the water treatment.
Of course, it is not necessary for any one product to practice the invention to achieve all of the advantages set forth above at the same time.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings that are needed for the description of the embodiments will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic diagram of a vertical flap flocculation basin;
1-double pulse power supply, 2-positive electrode, 3-negative electrode, 4-columnar anode, 5-folded plate-shaped cathode, 6-water inlet, 7-water outlet, 8-sedimentation tank and 9-flocculation tank;
FIG. 2 is a schematic diagram of the experimental apparatus in example 2;
10-magnetic stirrer, 11-electric flocculation reactor, 12-iron anode, 13-direct current and pulse power supply;
FIG. 3 is a schematic waveform diagram of a pulse current;
wherein, (a) a single pulse current, (b) a double pulse current waveform;
FIG. 4 is a microscopic topography of the flocs (400 x magnification);
wherein, (a) direct current flocs, (b) single pulse flocs, (C) double pulse flocs, (d-f) standing the flocs for 1h, and (d) attracting the direct current flocs, (e) single pulse flocs and (f) double pulse flocs by an external magnetic field;
FIG. 5 is a schematic diagram of the mechanism of forming iron flocs and removing Cr (VI) by direct current and pulse electric flocculation;
wherein DC is DC flocculation, DO is aeration oxygenation, PC is pulse electric flocculation, DO abscent+CI - Is oxygen-scavenging and combines chloride ions.
Detailed Description
The following description of the embodiments of the present invention will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
The related embodiments of the invention are:
example 1
The embodiment provides a double-pulse piezoelectric flocculation method for treating mine acid wastewater containing heavy metals, which comprises the following steps:
s1, according to investigation data of mine wastewater and related laws and regulations, the raw water quantity and water quality condition are defined, the effluent quality requirement is determined, and the design parameters of the electric flocculation tank are determined through experiments and operation experience.
S2, selecting a vertical folded plate flocculation tank from the flocculation tank, wherein a plurality of columnar iron anodes and folded plate-shaped iron cathodes are arranged in the vertical folded plate flocculation tank, and the mine acid wastewater containing heavy metals is repeatedly baffled under the guidance of the folded plate-shaped iron cathodes, so that the speed gradient or the flocculation flow rate in the flocculation process is gradually reduced from a water inlet to a water storage port, and the full and perfect flocculation process is ensured; data of each section of vertical folded plate sedimentation tank:
g=80s relative to the first section of the flap -1 ，t≥240s；
Second section of parallel flap, g=50s -1 ，t≥240s；
Third section of parallel flap, g=25s -1 ，t≥240s。
The included angle of the folded plate is 90-120 degrees, the width of the folded plate is 0.4-0.6 m, and the length of the folded plate is 0.8-1.5 m.
The flocculation tank needs to have enough flocculation time, the flocculation tank should be built together with the sedimentation tank as much as possible, and the connection with a pipe is avoided, if the connection with the pipe is needed, the flow rate should be controlled, and the drop of a water head caused by the sudden rise of the flow rate is avoided; to avoid the breaking of formed flocs, the flow rate of the through holes of the water outlet perforated wall of the flocculation tank should be controlled; in order to avoid the flocs depositing in the flocculation basin, corresponding sludge discharge measures are adopted if necessary.
S3, the current conducted by the electric flocculation Chi Yinyang polar plate selects double-pulse low-voltage current, and wastewater is treated by using an intermittent mode of 'power-on-power-off-power-on' of a pulse power supply; after being electrified, the iron anode is gradually oxidized, starts to dissolve ferrous ions into water, and then reacts with Cr (VI) in the solution; cr (VI) gets electrons from the cathode and is then reduced to Cr (III), and aluminum ions generated by anodic electrolysis can form aluminum hydroxide precipitates which are used as flocculant and Cr (OH) 3 Co-precipitation; large-particle flocs are removed through precipitation, small-particle flocs are removed through an air floatation effect, and the large-particle flocs are added into a precipitation tank after a water outlet for flocculation precipitation removal.
S4, changing the magnetic separation performance of the floccules by combining the double pulse waveform regulation and control with aeration and air-expelling, and controlling the sludge reduction of the water treatment. The magnetic separation performance of the floccules is changed by combining aeration/gas-expelling and easily available chlorine ion-containing electrolyte through the reversible reverse waveform regulation and control of double pulses, so as to control the sludge reduction of water treatment; and when the air is expelled, the dissolved oxygen is reduced, and the Cl-electrolyzed by the iron and the electrolyte containing chlorine ions is converted into the green rust under the double pulse regulation, so that the magnetism of the floccule is changed. The electrolyte containing chloride ions is at least one of NaCl, KCl, HCl and perchloric acid.
Factors influencing the removal rate are:
a. when the pH of the mine acid wastewater containing heavy metals is more than 6, the removal rate is less changed along with the rising of the initial pH;
b. the low conductivity of the mine acid wastewater containing heavy metals can lead to the reduction of the removal rate and the increase of the energy consumption, but the excessively high conductivity can limit the voltage, so that the removal rate is reduced;
c. the increase of the plate spacing can increase the removal rate, but the excessive plate spacing can passivate the plates;
d. when the initial concentration of Cr (VI) is too high, the formation of flocs of the anodically dissolved iron ions is insufficient to remove Cr (VI) at high concentrations, which reduces the removal rate.
The electrochemical behavior of the iron electrode is explored by using Tafel curves in the double-pulse electric flocculation process. And measuring the forward current of the iron electrode, obtaining the corrosion voltage of iron through a Tafel curve of Cr (VI), and calculating the corrosion current through a Tafel equation after the current direction is converted. The corrosion current is continuously reduced with the increase of the energization time because a dense oxide film is gradually formed on the surface of the electrode during energization, resulting in passivation of the electrode surface. This demonstrates that applying a reverse current can slow the rate of passivation film formation on the ferroelectric. Therefore, the periodic overturning of the cathode and the anode can be realized by applying double pulse current, the generation of a passivation film can be reduced, and the purpose of reducing energy consumption is realized.
The embodiment is researched aiming at the influence of different positive and negative pulse numbers on the electric flocculation effect and the electric energy consumption. When the number of positive pulses is the same as that of negative pulses, the removal rate of Cr (VI) in the solution is 7.23%, and the corresponding energy consumption is highest. The higher the ratio of positive pulses to negative pulses, the higher the corresponding Cr (VI) removal rate. When the number ratio of positive pulses to negative pulses is 10, the removal rate is 99.2% at the highest, and the corresponding energy consumption is also the lowest. In addition, the current density is continuously increased along with the increase of the number of the pulses, and the increase of the number of the positive and negative pulses is found to be equivalent to the increase of the duty ratio of one current period through the waveform schematic diagrams of the combination of different positive pulse currents and negative pulse currents. When the peak voltage is unchanged, the average voltage over the total pulse period increases with increasing duty cycle.
Three different electric flocculation are respectively compared from the aspects of removal rate, energy consumption, sludge quantity and the like, and the double-pulse electric flocculation relatively requires longer treatment time to achieve the removal rate similar to that of direct current electric flocculation. But compared with direct current flocculation, the double-pulse electric flocculation can greatly save the energy consumption of treatment and reduce the generation amount of sludge. The method is characterized in that due to the characteristic of double pulse current, positive ions dissolved by the anode are beneficial to diffusing into the solution during the outage period of the current in one period, which is beneficial to inhibiting concentration polarization, so that the energy consumption in the reaction process is reduced, and sludge reduction is realized.
This example gives a change in the magnetic properties of the flocs, which are more magnetic than the flocs produced by double pulse electroflocculation, possibly due to the conversion of the flocs into hematite and magnetite. The composition of the iron flocks during electroflocculation is very complex and is susceptible to the external environment, in particular the presence of Dissolved Oxygen (DO) and Cl-. When sufficient DO is present in the solution, the ferrous floc component produced during the electrocoagulation process can rapidly oxidize to ferric components. The mixed iron phase then continues to convert to gamma-FeOOH in the presence of dissolved oxygen. However, when DO is scarce, the mixed-valence iron phase will be converted to green rust (GRCl) in the presence of Cl-, which is a generic term for various green crystalline compounds. Due to the different current characteristics, during water treatment, direct current flocculation takes longer than double pulse electroflocculation, resulting in the formation of a large amount of oxygen on the electrodes. In this case, gamma-FeOOH is produced due to the presence of sufficient DO during the electrocoagulation process, and GRCl is produced due to the absence of sufficient DO and the presence of Cl-during the double pulse electrocoagulation process.
In addition, the chloride ions accelerate the settling of the floccules, and increase the particle size of the floccules. Compared with GRCl, the gamma-FeOOH has not very strong adsorption capacity to Cr (VI), so that the double-pulse electroflocculation has higher Cr (VI) removal rate than the direct-current electroflocculation. As the reaction proceeds, DO is gradually consumed and gamma-FeOOH generated during dc flocculation begins to convert to magnetite (Fe 3 O 4 ). This results in the final release of Cr (VI) that was originally adsorbed by the flocsAnd back into solution, so that the final removal rate is reduced. The removal mechanism of the double-pulse electroflocculation Cr (VI) is realized by the adsorption of GRCl with effective adsorption sites, and the Cr (VI) can be adsorbed on the adsorption sites of the GRCl to be removed. Another mechanism is the substitution of Cr (VI) for Fe in GRCl 2+ The binding of Cr (VI) to the flocs is made tighter, which makes it difficult for the GRCl-adsorbed Cr (VI) to be returned from the flocs to the solution. In addition, in the presence of DO, a small amount of GRCl is converted into gamma-FeOOH, so that the double-pulse electroflocculation has good stability in the field of Cr (VI) wastewater treatment.
Example 2
In this example, potassium dichromate (K) was prepared at a concentration of 200mg/L 2 Cr 2 O 7 ) The solution is used as a simulated water sample stock solution, and other concentrations required in the experiment are all prepared by diluting the stock solution. The simulated water sample adopts sodium chloride (NaCI) as electrolyte, the conductivity of the solution is regulated to be 2mS/cm, and the pH value of the solution is regulated to be 7.5-8.0 by adopting 1M sodium hydroxide solution and dilute sulfuric acid. A500 mL plexiglass reactor (100 mm. Times.100 mm. Times.50 mm) was used as the reactor device, and two pure iron plates were connected as electrodes to the cathode and anode of the pulsed power supply. The waveform of the current (dc and pulse) can be achieved by adjusting the duty cycle of the power supply. The effective area of the iron electrode immersed in the solution is 50cm 2 (50 mm. Times.100 mm. Times.1 mm), the electrode was subjected to sanding and then to ultrasonic treatment in an ultrasonic machine for 10 minutes before use to remove the oxide layer on the surface, and the electrode was sufficiently cleaned with ultrapure water. The spacing of the electrode plates can be adjusted from 5mm to 25 mm. All experiments were performed at room temperature (25.+ -. 2 ℃ C.) with stirring at 300rpm/min for enhanced mass transfer.
According to national standard GB7467-87, a dibenzoyl dihydrazide spectrophotometry is adopted, solutions required by corresponding standard curves are prepared according to the steps shown in the standard, the respective absorbance is measured at 540nm wavelength, the corresponding standard curve is made, then wastewater at different moments of electric flocculation treatment is filtered by an inorganic filter head of 0.45um, a test sample is measured by adopting the same measuring method as the standard curve, and the concentration of the test sample is estimated according to the formula of the standard curve.
Electrochemical characterization is carried out by adopting an electrochemical workstation, a testing system (Ag/AgCI is used as a reference electrode, a platinum sheet is used as an auxiliary electrode, iron is used as a working electrode) is formed by using three electrodes, forward scanning is followed by reverse scanning, and a double-pulse current electrifying mode is simulated to realize tafel curve measurement of the iron anode so as to judge the passivation degree of the iron anode in the reaction process.
The particle size of the flocs generated in the electric flocculation process is measured by adopting a laser particle sizer, the flocs are stirred for 3 minutes before measurement, so that a longer growth period is obtained, and the coagulation condition of the flocs generated under different current conditions is measured.
Example 3
Based on the device shown in figure 1, wastewater is introduced into an electric flocculation tank, columnar anodic oxidation is carried out after the wastewater is electrified, anode ions are dissolved into water for hydrolysis, cr (VI) is reduced into Cr (III) through a folded plate-shaped cathode, then flocculation is carried out to form flocs, the flocs with strong adsorption capacity can adsorb Cr (III) to form chromium hydroxide and chromium-iron co-sediments, large-particle flocs are removed through precipitation, small-particle flocs are removed through air floatation, and the flocs are added into a precipitation tank for precipitation after a water outlet. The cathode is designed into a folded plate shape, so that not only does the electrolytic reaction occur, but also the diversion effect of water flow is achieved. The method can eliminate the passivation phenomenon of the polar plate and improve the flocculation effect. During the flocculation treatment of direct current, a large amount of oxygen is generated to oxidize the flocs into alpha-Fe 2O3 and gamma-Fe 2O3, so that Cr (VI) which is originally adsorbed by the flocs is finally released and returned to the solution, and the final removal rate is reduced. The removing mechanism of the pulse electric flocculation to Cr (VI) is based on the adsorption of GRCl, so that the stability of the pulse electric flocculation treatment process is better. The electrode corrosion current can be increased by the current commutation in the double-pulse electric flocculation process, and the effect of alleviating the passivation of the polar plate is achieved. The optimal current density of the fed double-pulse low-voltage current is 20Am -2 The peak voltage is 5V, the current frequency is 5000hz, and a duty cycle of 30% is most suitable. When the ratio of the number of positive pulses to the number of negative pulses of the double pulse electroflocculation is larger, the corresponding Cr (VI) removal rate is higher. When the ratio of the positive pulse to the negative pulse is 10, the removal rate is 99.2% at the maximum, and corresponds toIs also the lowest. In addition, the current density is continuously increased along with the increase of the number of the pulses, and the increase of the number of the positive and negative pulses is found to be equivalent to the increase of the duty ratio of one current period through the waveform schematic diagrams of the combination of different positive pulse currents and negative pulse currents. When the peak voltage is unchanged, the average voltage over the total pulse period increases with increasing duty cycle.
The invention innovatively introduces an improved electric flocculation technology of replacing direct current by double pulse current, and the pulse power supply can effectively solve the problem of concentration polarization, thereby saving energy consumption, relieving passivation of polar plates, adjusting magnetism of water treatment sludge, promoting magnetic separation performance, effectively promoting sludge reduction and reducing sludge disposal cost generated after water treatment.
The preferred embodiments of the invention disclosed above are intended only to assist in the explanation of the invention. The preferred embodiments are not exhaustive or to limit the invention to the precise form disclosed. Obviously, many modifications and variations are possible in light of the above teaching. The embodiments were chosen and described in order to best explain the principles of the invention and the practical application, to thereby enable others skilled in the art to best understand and utilize the invention. The invention is limited only by the claims and the full scope and equivalents thereof.
Claims (10)
1. A double-pulse piezoelectric flocculation method for treating mine acid wastewater containing heavy metals is characterized by comprising the following steps:
s1, according to investigation data of mine wastewater and related laws and regulations, defining raw water quantity and water quality conditions, and determining design parameters of an electric flocculation tank through experiments and operation experience;
s2, selecting a vertical folded plate flocculation tank from the flocculation tank, wherein a plurality of columnar iron anodes and folded plate-shaped iron cathodes are arranged in the vertical folded plate flocculation tank, the mine acid wastewater containing heavy metals is repeatedly baffled under the guidance of the folded plate-shaped iron cathodes, and the speed gradient or the flocculation flow rate in the flocculation process gradually becomes smaller from a water inlet to a water storage port;
s3, the current conducted by the electric flocculation Chi Yinyang polar plate selects double-pulse low-voltage current, and wastewater is treated by using an intermittent mode of 'power-on-power-off-power-on' of a pulse power supply;
s4, changing the magnetic separation performance of the floccules by combining the double pulse waveform regulation and control with aeration and air-expelling, and controlling the sludge reduction of the water treatment.
2. The double-pulse piezoelectric flocculation method for treating mine acid wastewater containing heavy metals according to claim 1, wherein in step S2, each section of data of the vertical folded plate sedimentation tank is as follows:
g=80s relative to the first section of the flap -1 ，t≥240s；
Second section of parallel flap, g=50s -1 ，t≥240s；
Third section of parallel flap, g=25s -1 ，t≥240s。
3. The double-pulse piezoelectric flocculation method for treating mine acid wastewater containing heavy metals according to claim 2, wherein the included angle of the folded plate is 90-120 degrees, the width of the folded plate is 0.4-0.6 m, and the length of the folded plate is 0.8-1.5 m.
4. The double-pulse piezoelectric flocculation method for treating mine acid wastewater containing heavy metals according to claim 1, wherein in the step S2, the flocculation tank needs to have enough flocculation time, the flocculation tank should be built as much as possible together with the sedimentation tank, and the connection with a pipe canal is avoided, if the connection with the pipe canal needs to be controlled, the flow rate should be controlled, and the sudden rise of the flow rate is avoided, so that the water head is dropped; to avoid the breaking of formed flocs, the flow rate of the through holes of the water outlet perforated wall of the flocculation tank should be controlled; in order to avoid the flocs depositing in the flocculation basin, corresponding sludge discharge measures are adopted if necessary.
5. The double pulse piezoelectric flocculation method for treating mine acid wastewater containing heavy metal according to claim 1, wherein in step S3, the iron anode is gradually oxidized after being electrified and ferrous ions begin to dissolve into water, and then the ferrous ions are mixed with the solutionCr (VI) reacts; cr (VI) gets electrons from the cathode and is then reduced to Cr (III), and aluminum ions generated by anodic electrolysis can form aluminum hydroxide precipitates which are used as flocculant and Cr (OH) 3 Co-precipitation; large-particle flocs are removed through precipitation, small-particle flocs are removed through an air floatation effect, and the large-particle flocs are added into a precipitation tank after a water outlet for flocculation precipitation removal.
6. The double-pulse piezoelectric flocculation method for treating mine acid wastewater containing heavy metals according to claim 5, which is characterized in that: when energized, the current density was 20Am -2 The peak voltage is 5V, the current frequency is 5000Hz, and the optimal duty cycle is 30%.
7. The double-pulse piezoelectric flocculation method for treating mine acid wastewater containing heavy metals according to claim 5, which is characterized in that: when the ratio of the number of positive pulses to the number of negative pulses of the double-pulse electroflocculation is larger, the corresponding Cr (VI) removal rate is higher; when the ratio of the positive pulse to the negative pulse is 10, the removal rate is 99.2% at the highest, and the corresponding energy consumption is also the lowest.
8. The double-pulse piezoelectric flocculation method for treating mine acid wastewater containing heavy metals according to claim 5, wherein factors influencing the removal rate are as follows:
a. when the pH of the mine acid wastewater containing heavy metals is more than 6, the removal rate is less changed along with the rising of the initial pH;
b. the low conductivity of the mine acid wastewater containing heavy metals can lead to the reduction of the removal rate and the increase of the energy consumption, but the excessively high conductivity can limit the voltage, so that the removal rate is reduced;
c. the increase of the plate spacing can increase the removal rate, but the excessive plate spacing can passivate the plates;
d. when the initial concentration of Cr (VI) is too high, the formation of flocs of the anodically dissolved iron ions is insufficient to remove Cr (VI) at high concentrations, which reduces the removal rate.
9. According to claimThe double-pulse piezoelectric flocculation method for treating mine acid wastewater containing heavy metals is characterized in that in the step S4, aeration/gas-expelling and easily-obtained chlorine ion-containing electrolyte are combined through double-pulse reversible waveform regulation and control to change the magnetic separation performance of flocs, so that the reduction of water treatment sludge is controlled; the gamma-FeOOH is generated by promoting electron transfer through the combination of double pulse waveform regulation and aeration, and when the gas is purged, the dissolved oxygen is reduced, and the Cl is electrolyzed by the iron and the electrolyte containing chloride ions under the double pulse regulation and control - Is converted into green rust, thereby changing the magnetism of the floc.
10. The double pulse piezoelectric flocculation method for treating mine heavy metal-containing acidic wastewater according to claim 9, wherein the electrolyte containing chloride ions is at least one of NaCl, KCl, HCl and perchloric acid.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310249551.0A CN116282400A (en) | 2023-03-15 | 2023-03-15 | Double-pulse piezoelectric flocculation method for treating mine acid wastewater containing heavy metals |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310249551.0A CN116282400A (en) | 2023-03-15 | 2023-03-15 | Double-pulse piezoelectric flocculation method for treating mine acid wastewater containing heavy metals |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN116282400A true CN116282400A (en) | 2023-06-23 |
Family
ID=86793777
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202310249551.0A Pending CN116282400A (en) | 2023-03-15 | 2023-03-15 | Double-pulse piezoelectric flocculation method for treating mine acid wastewater containing heavy metals |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN116282400A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117303510A (en) * | 2023-09-07 | 2023-12-29 | 兰州理工大学 | Self-adaptive control method for waveform characteristic analysis of wastewater treatment power supply |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN203159296U (en) * | 2013-03-12 | 2013-08-28 | 贵州威德环境科技有限公司 | Electro-coagulation wastewater treatment equipment |
| US20180215635A1 (en) * | 2017-01-27 | 2018-08-02 | Uti Limited Partnership | Electrocoagulation using oscillating electrodes |
| CN210394033U (en) * | 2019-08-13 | 2020-04-24 | 河北天泓环保科技有限公司 | A processing system for containing chromium waste water |
| CN113582412A (en) * | 2021-08-17 | 2021-11-02 | 华北理工大学 | Advanced sewage treatment device |
| CN114790056A (en) * | 2022-05-05 | 2022-07-26 | 中创宏远（北京）环保科技有限公司 | Electric flocculation sewage treatment system and method |
-
2023
- 2023-03-15 CN CN202310249551.0A patent/CN116282400A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN203159296U (en) * | 2013-03-12 | 2013-08-28 | 贵州威德环境科技有限公司 | Electro-coagulation wastewater treatment equipment |
| US20180215635A1 (en) * | 2017-01-27 | 2018-08-02 | Uti Limited Partnership | Electrocoagulation using oscillating electrodes |
| CN210394033U (en) * | 2019-08-13 | 2020-04-24 | 河北天泓环保科技有限公司 | A processing system for containing chromium waste water |
| CN113582412A (en) * | 2021-08-17 | 2021-11-02 | 华北理工大学 | Advanced sewage treatment device |
| CN114790056A (en) * | 2022-05-05 | 2022-07-26 | 中创宏远（北京）环保科技有限公司 | Electric flocculation sewage treatment system and method |
Non-Patent Citations (1)
| Title |
|---|
| 刘方圆等: "脉冲电絮凝处理含Cr(VI)废水的调控机制", 《中国优秀硕士学位论文全文数据库 工程科技I辑》, 15 January 2022 (2022-01-15), pages 8 - 9 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117303510A (en) * | 2023-09-07 | 2023-12-29 | 兰州理工大学 | Self-adaptive control method for waveform characteristic analysis of wastewater treatment power supply |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| Xu et al. | Optimization and assessment of Fe–electrocoagulation for the removal of potentially toxic metals from real smelting wastewater | |
| Meas et al. | Industrial wastewaters treated by electrocoagulation | |
| Liu et al. | Electrocoagulation in water treatment | |
| Kobya et al. | Treatment of rinse water from zinc phosphate coating by batch and continuous electrocoagulation processes | |
| US6878268B2 (en) | Apparatus for purification of water | |
| CN107337301B (en) | A kind of method of the electric Fenton processing waste water of additional hydrogen peroxide | |
| AU2010265836A1 (en) | Water treatment method and system | |
| EP2158163A1 (en) | Electrolytic process for removing fluorides and other contaminants from water | |
| CN109354134B (en) | Method for removing chroma of anodic oxidation dyeing wastewater through electric flocculation | |
| El-Ashtoukhy et al. | Removal of heavy metal ions from aqueous solution by electrocoagulation using a horizontal expanded Al anode | |
| Shaker et al. | Nickel and chromium removal by electrocoagulation using copper electrodes | |
| CN106242129A (en) | A kind of municipal sewage plant discharge water is put forward mark method by one-level B to one-level A | |
| CN116282400A (en) | Double-pulse piezoelectric flocculation method for treating mine acid wastewater containing heavy metals | |
| Liu et al. | Factors influencing the removal of phosphorus and the purity of recycling struvite in wastewater by the electrochemical sacrificial magnesium anode method | |
| Yilmaz et al. | Removal of cadmium by electrocoagulation and a cost evaluation | |
| KR100372849B1 (en) | Advanced apparatus for treating wastewater using the electrolysis and coagulation | |
| Cho et al. | Continuous clarification and thickening of activated sludge by electrolytic bubbles under control of scale deposition | |
| CN109422332A (en) | Treating Electroplate Wastewater Containing Nickel processing method | |
| CN106430744A (en) | Device for improving standards of discharged water of municipal sewage treatment plant to first-level A from first-level B | |
| Idhayachander et al. | Electrolytic recovery of nickel from spent electroless nickel bath solution | |
| CN210855619U (en) | Contain salt organic waste water electrocatalytic oxidation coupling preprocessing device | |
| RU2031855C1 (en) | Method and device for purification of industrial drainage water | |
| Liu et al. | Experimental study on the treatment of chromium containing wastewater by electric flocculation | |
| KR0170360B1 (en) | Apparatus for removing kernel and organic substance by electrochemical condensation method | |
| DE2406574C2 (en) |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |