CN217947862U - Detachable electrolysis-adsorption coupling reactor and wastewater treatment device - Google Patents
Detachable electrolysis-adsorption coupling reactor and wastewater treatment device Download PDFInfo
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- CN217947862U CN217947862U CN202222236140.1U CN202222236140U CN217947862U CN 217947862 U CN217947862 U CN 217947862U CN 202222236140 U CN202222236140 U CN 202222236140U CN 217947862 U CN217947862 U CN 217947862U
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Abstract
The utility model provides a detachable electrolysis-adsorption coupling reactor, which comprises a vertical flow type reaction cabin, an upper cover and a lower cover, wherein the upper cover and the lower cover are respectively arranged on the upper end surface and the lower end surface of the vertical flow type reaction cabin to seal the upper end surface and the lower end surface of the vertical flow type reaction cabin; a plurality of carbon felt electrodes, porous plate type anodes and conductive metal sheets are arranged in the shell of the vertical flow type reaction cabin; each carbon felt electrode is horizontally arranged in the vertical flow type reaction chamber, a porous plate type anode is horizontally arranged between each two adjacent carbon felt electrodes, each carbon felt electrode is not contacted with the porous plate type anode, and each conductive metal sheet is contacted with the carbon felt but not contacted with the porous plate type anode; the porous plate type porous anodes and the conductive metal sheets are respectively connected with a power supply through leads. Based on the detachable electrolysis-adsorption coupling reactor, the utility model also provides an electrolysis-adsorption coupling wastewater treatment device.
Description
Technical Field
The utility model belongs to the waste water treatment field relates to detachable electrolysis-absorption coupling reactor and effluent treatment plant.
Background
With the development of society, in recent decades, the phenomenon of water resource pollution caused by wastewater discharged from industrial production, agricultural breeding industry, urban construction and the like has become increasingly serious. In particular, hospital wastewater is attracting more and more attention as one of the main urban domestic wastewater. The wastewater of the hospital includes medical wastewater generated by medical departments such as an outpatient department, an operating room, a clinical laboratory, a CT room and the like, and also includes domestic sewage generated by other departments of the hospital. Hospital wastewater discharge is characterized by the complexity and uncertainty of pollutants in the water, and the imbalance of water quality and water quantity.
Antibiotics are a common class of Pharmaceutical and Personal Care Products (PPCPs) contaminants in hospital wastewater, and widespread use of antibiotics poses an increasingly serious water pollution problem. For example, sulfamethoxazole (SMX) is widely used in hospitals as an important sulfonamide antibiotic, and accounts for 5% of the total antibiotic consumption in China. The accumulation of a large amount of SMX in the environment will lead to the development of drug-resistant bacteria and drug-resistant genes in the environment, thereby causing adverse effects on the health and safe life of people.
The existing hospital wastewater treatment method mainly comprises a physical method and a chemical method. Such as ozone treatment techniques, chlorine disinfection techniques, and ultraviolet sterilization techniques. The traditional treatment technology has the problems of complex device, high requirement on operation conditions, high operation cost, low treatment efficiency, easy secondary pollution to water bodies and the like. Therefore, in the face of increasing medical waste water, there is an urgent need for a method and apparatus for treating hospital waste water with low cost, high treatment efficiency and more environmental protection, so as to solve the problems of the current hospital waste water treatment.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to overcome prior art not enough, provide a detachable electrolysis-absorption coupling reactor to and the effluent treatment plant who founds on the basis of this reactor, with improve the degradation effect to waste water, improve the treatment effeciency to waste water.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
a detachable electrolysis-adsorption coupling reactor comprises a vertical flow type reaction cabin, an upper cover and a lower cover,
the shell of the vertical flow type reaction cabin is a cylinder body with the axis vertical to the horizontal plane, the upper cover is provided with a water outlet, the lower cover is provided with a water inlet, and the upper cover and the lower cover are respectively arranged on the upper end surface and the lower end surface of the vertical flow type reaction cabin to seal the upper end surface and the lower end surface of the vertical flow type reaction cabin; the shell, the upper cover and the lower cover of the vertical flow type reaction cabin are not conductive;
a plurality of carbon felt electrodes, porous plate type anodes and conductive metal sheets are arranged in the shell of the vertical flow type reaction cabin, and a power supply is arranged outside the shell of the vertical flow type reaction cabin; each carbon felt electrode is horizontally arranged in the vertical flow type reaction chamber, a porous plate type anode is horizontally arranged between each two adjacent carbon felt electrodes, the carbon felt electrodes are not in contact with the porous plate type anode, the shapes and the sizes of the carbon felt electrodes and the porous plate type anode are matched with the shape and the size of the cross section of the shell of the vertical flow type reaction chamber, and the area between the adjacent carbon felt electrodes and the porous plate type anode is an electrolysis area; each conductive metal sheet is in contact with the carbon felt but not in contact with the porous plate anode; each porous plate type porous anode is connected with the anode of the power supply through an anode power line, and each conductive metal sheet is connected with the cathode of the power supply through a cathode power line.
In the technical scheme of the detachable electrolysis-adsorption coupling reactor, the carbon felt electrode is detachably arranged in the shell of the vertical flow type reaction cabin so as to be convenient for replacing and cleaning the carbon felt electrode.
Further, in the above technical scheme of the detachable electrolysis-adsorption coupling reactor, the carbon felt electrode comprises a carbon felt electrode body and a sealing strip, the carbon felt electrode body is formed by horizontally overlapping a plurality of layers of carbon felts and is clamped into a whole by a clamping piece, and the sealing strip is located at a position where the clamping piece is in contact with the shell of the vertical flow type reaction cabin. The carbon felt is a commercial product, and according to the thickness requirement of the carbon felt electrode body, a proper amount of commercial carbon felts are overlapped and assembled and clamped together by the clamping piece, so that the carbon felt electrode body can be formed.
Furthermore, in the technical scheme of the detachable electrolysis-adsorption coupling reactor, electrode inserting ports with the same number as that of the carbon felt electrodes are arranged on a shell of the vertical flow type reaction cabin, each carbon felt electrode is inserted into the shell of the vertical flow type reaction cabin through the electrode inserting ports, and after the carbon felt electrodes are inserted in place, sealing strips on the carbon felt electrodes seal the contact part of the clamping piece and the shell of the vertical flow type reaction cabin; the clamping piece wraps one part of the side face of the carbon felt electrode, and after the carbon felt electrode is inserted in place, the part, exposed to the electrode inserting opening, of the carbon felt electrode is sealed by the clamping piece.
In the technical scheme of the detachable electrolysis-adsorption coupling reactor, the shape of the conductive metal sheet is consistent with that of the inner wall of the shell of the vertical flow type reaction cabin, the conductive metal sheet is arranged on the inner wall of the shell of the vertical flow type reaction cabin, and each conductive metal sheet is contacted with the side surface of each carbon felt electrode.
In the technical scheme of the detachable electrolysis-adsorption coupling reactor, the inner wall of a shell of a vertical flow type reaction cabin is provided with an insertion groove, and each carbon felt electrode is inserted into the insertion groove; each porous plate type anode is arranged on the inner wall of the shell of the vertical flow type reaction cabin.
In the technical scheme of the detachable electrolysis-adsorption coupling reactor, the thickness of each conductive carbon felt (specifically, the thickness of each carbon felt electrode body) is 20-30 cm, the porous plate type anode is a BDD electrode net, the BDD electrode net is a boron-doped diamond electrode net, and the BDD electrode net is a commercially available commodity.
In the technical scheme of the detachable electrolysis-adsorption coupling reactor, the number of the carbon felt electrodes is preferably 3-6, and the carbon felt electrodes are arranged at different heights of the vertical flow type reaction cabin. The number of the carbon felt electrodes can be determined according to the water quality condition of the wastewater to be treated.
Furthermore, in the above-mentioned technical solution of the detachable electrolysis-adsorption coupling reactor, in order to ensure the current between the carbon felt electrode and the adjacent porous plate-type anode to be stable, and to ensure the wastewater degradation effect of the document, preferably, the distance between each carbon felt electrode and the adjacent porous plate-type anode is equal.
In the technical scheme of the detachable electrolysis-adsorption coupling reactor, the shell of the vertical flow type reaction cabin is a cylinder with the axis vertical to the horizontal plane, correspondingly, the carbon felt electrode and the porous plate type anode are both circular, and the conductive metal sheet is arc-shaped with the radian consistent with the inner wall of the shell of the vertical flow type reaction cabin.
In the technical scheme of the detachable electrolysis-adsorption coupling reactor, the carbon felt electrode can be used as a cathode and can also play an adsorption role, and when wastewater passes through the carbon felt electrode, the carbon felt electrode can also adsorb large-particle impurities in the wastewater.
Based on above-mentioned detachable electrolysis-absorption coupling reactor, the utility model also provides an electrolysis-absorption coupling effluent treatment plant, the device includes above-mentioned detachable electrolysis-absorption coupling reactor, elementary equalizing basin, secondary equalizing basin and sedimentation tank, elementary equalizing basin is used for throwing to throw and throws catalyst, oxidant and acid, secondary equalizing basin is used for throwing to add alkali, the delivery port of elementary equalizing basin and detachable electrolysis-absorption coupling reactor's water inlet intercommunication, the delivery port of detachable electrolysis-absorption coupling reactor and the water inlet intercommunication of secondary equalizing basin, secondary equalizing basin delivery port and the water inlet intercommunication of sedimentation tank.
Further, the electrolysis-adsorption coupling wastewater treatment device may further include a control system for controlling the addition of the catalyst, the oxidant, the acid and the alkali, the water inlet flow rate, the water outlet flow rate, and the like, and the control system may be a control system commonly used in the prior art, such as a modular management system.
The method for treating the wastewater by adopting the electrolysis-adsorption coupling wastewater treatment device comprises the following steps: introducing the wastewater into a primary regulating tank and feeding the wastewater into a primaryAdding an oxidant (PMS) and a catalyst (Fe) of ferric sulfate (PMS) into a regulating tank 2 (SO 4 ) 3 ) Meanwhile, acid or alkali can be added to adjust the pH value of the wastewater to a proper range, then the wastewater in the primary adjusting tank is introduced into a detachable electrolysis-adsorption coupling reactor, and a power supply is turned on to perform electrocatalytic oxidation treatment on the wastewater. The wastewater after electrocatalytic oxidation treatment enters a secondary regulating reservoir, the pH value of the water body in the secondary regulating reservoir is regulated, and then the water body enters a sedimentation tank, so that iron ions in the water body can be recycled, and the influence of metal ions carried in the effluent on the environment is reduced.
Compared with the prior art, the technical scheme of the utility model following profitable technological effect has been produced:
1. the utility model provides a detachable electrolysis-absorption coupling reactor, this reactor regard as negative pole and cooperation porous plate formula positive pole with carbon felt electrode, and carbon felt electrode not only plays the effect of negative pole, plays the adsorption effect because of having porous structure moreover, vertically sets up the vertical flow formula reaction cabin simultaneously, and rivers from bottom to top motion can ensure sewage and with the abundant contact of carbon felt electrode to strengthen its absorption and electrolysis. More importantly, the reactor can be matched with an oxidant and a catalyst for use to carry out electrocatalytic oxidation on the wastewater, mainly comprising direct electron transfer and indirect oxidative degradation. The direct electron transfer is an oxidation-reduction reaction of organic pollutants on the surface of an electrode, electrons in pollutant molecules are transferred to the surface of the electrode or the electrons generated on the surface of the electrode directly attack the pollutant molecules, so that the molecular structure of the pollutants is damaged, and the pollutants are degraded. The indirect oxidation is that the anode or cathode surface reacts under the action of an electric field to generate active substances (such as hydroxyl radicals, sulfate radicals and the like) with high oxidizability, and the active substances can perform efficient oxidative degradation on organic pollutants in the wastewater. The comprehensive action of the above various factors ensures that the reactor provided by the utility model has high-efficiency wastewater treatment capacity.
2. Based on the detachable electrolysis-adsorption coupling reactor, the utility model also provides an electrolysis-adsorption coupling wastewater treatment device, which comprises the detachable electrolysis-adsorption coupling reactor, a primary regulating reservoir, a secondary regulating reservoir and a sedimentation tank. The device not only has the efficient wastewater treatment capacity of the detachable electrolysis-adsorption coupling reactor, but also has the advantages of simple structure, small occupied area, strong controllability, energy conservation, environmental protection and the like, and is suitable for wastewater treatment in areas with difficult pipe network building and sewage dispersion, such as rural areas, mountain areas and other areas with inconvenient traffic. Meanwhile, the device is low in noise, free of secondary pollutant outflow and peculiar smell, and can be used for in-situ treatment of domestic sewage and municipal wastewater in cities and towns, so that the risk of environmental pollution in the sewage transportation process can be reduced, and the cost of wastewater transportation can be saved.
3. The utility model discloses an experiment proves, adopts reactor or device carry out waste water treatment, can realize the complete degradation to organic pollutant in 10min, all have efficient degradability to the pollutant including Sulfamethoxazole (SMX), atrazine (ATZ), bisphenol A (BPA), carbamazepine (CBZ), metronidazole (MNZ) and Nitrobenzene (NB) etc.. Meanwhile, when anions with different concentrations coexist with target pollutants, no obvious adverse effect is generated on the degradation of the pollutants, the degradation efficiency of the pollutants in 10min can reach more than 80% and even 100%, the water quality control method has good complex water body adaptability, can be used under various water qualities, and has the advantage of wide application range.
Drawings
FIG. 1 is a schematic structural view of the detachable electrolysis-adsorption coupling reactor of the present invention;
FIG. 2 is an exploded view of the detachable electrolytic-adsorptive coupling reactor of the present invention;
FIG. 3 is a schematic structural diagram of a vertical flow type reaction chamber of a detachable electrolysis-adsorption coupling reactor without a carbon felt electrode;
FIG. 4 is a schematic diagram showing the relative positions of the porous plate anode and the conductive metal plate when they are installed in the vertical flow reactor chamber;
FIG. 5 is a schematic of the structure of a carbon felt electrode;
FIG. 6 is an exploded view of a carbon felt electrode;
FIG. 7 is a schematic view showing the construction of an electrolysis-adsorption coupled wastewater treatment apparatus;
in the figure 1-7, 1-vertical flow type reaction chamber, 1-1-carbon felt electrode, 1-1-1-carbon felt electrode body, 1-1-2-sealing strip, 1-1-3-clamping piece, 1-2-porous plate type anode, 1-3-conductive metal sheet, 2-upper cover, 2-1-water outlet, 3-lower cover, 3-1-water inlet, 4-anode power line, 5-cathode power line, 6-primary regulating tank, 7-secondary regulating tank and 8-sedimentation tank.
Fig. 8 is a scanning electron micrograph of the carbon felt at different magnifications.
FIG. 9 is a graph (a), (b) and (c) showing the degradation efficiency of SMX-simulated wastewater, the concentration of ferrous iron and total iron during operation of the PMS/Fe (III) test group, and the concentration of ferrous iron and total iron during operation of the EC/PMS/Fe (III) test group, respectively, for each test group in example 5.
FIG. 10 shows the efficiency of the device of the present invention in degrading SMX-simulated wastewater in the presence of different types and concentrations of anions.
Figure 11 is the efficiency of the device of the present invention in degrading different target pollutants.
Detailed Description
The chlorinated paraffin purification device in the water environment medium provided by the utility model is further explained by the following embodiments. It is necessary to point out that the following examples are only used for further illustration of the present invention, and should not be construed as limiting the scope of the present invention, and those skilled in the art can make some non-essential improvements and adjustments to the present invention according to the above-mentioned contents of the present invention, and still fall into the scope of the present invention.
Example 1
In this embodiment, a detachable electrolysis-adsorption coupling reactor is provided, and a schematic structural diagram thereof is shown in fig. 1.
The utility model provides a detachable electrolysis-absorption coupling reactor includes vertical flow formula reaction cabin 1, upper cover 2 and lower cover 3.
The shell of the vertical flow type reaction cabin 1 is a cylinder with an axis vertical to a horizontal plane, flanges are arranged at the upper end and the lower end of the cylinder, the upper cover and the lower cover are hollow round tables, the flanges matched with the flanges at the two ends of the cylinder are arranged at the lower end of the upper cover and the upper end of the lower cover, a water outlet 2-1 is arranged on the upper cover, a water inlet 3-1 is arranged on the lower cover, and the upper cover and the lower cover are respectively arranged on the upper end surface and the lower end surface of the vertical flow type reaction cabin through the flanges and sealing gaskets to seal the upper end surface and the lower end surface of the vertical flow type reaction cabin. A long strip-shaped shell cabin is arranged on the outer wall of a shell of the vertical flow type reaction cabin 1 along the axial direction of the shell, an anode power line 4 and a cathode power line 5 are positioned in the long strip-shaped shell cabin, and the long strip-shaped shell cabin plays a role in protecting the anode power line 4 and the cathode power line 5. The shell, the upper cover and the lower cover of the vertical flow type reaction cabin are all not conductive, and the shell, the upper cover and the lower cover of the vertical flow type reaction cabin are all made of acrylic plates.
As shown in fig. 2, three carbon felt electrodes 1-1, two porous plate anodes 1-2 and three conductive metal sheets 1-3 are arranged in the shell of the vertical flow type reaction chamber 1, and a power supply is arranged outside the shell of the vertical flow type reaction chamber; each carbon felt electrode is horizontally arranged in the vertical flow type reaction chamber, a porous plate type anode is horizontally arranged between each two adjacent carbon felt electrodes, the carbon felt electrodes are not in contact with the porous plate type anode, the shapes and the sizes of the carbon felt electrodes and the porous plate type anode are matched with the shape and the size of the cross section of the shell of the vertical flow type reaction chamber, and the area between the adjacent carbon felt electrodes and the porous plate type anode is an electrolysis area; each conductive metal sheet is in contact with the carbon felt but not with the porous plate anode; each porous plate type porous anode is respectively connected with the anode of a power supply through an anode power line 4, and each conductive metal sheet is respectively connected with the cathode of the power supply through a cathode power line 5.
More specifically, as shown in fig. 3 to 6: three electrode inserting ports are arranged on a shell of the vertical flow type reaction cabin 1, each electrode inserting port is horizontally arranged, the length of each electrode inserting port is half of the circumference of the shell, an inserting groove is formed in the inner wall of the shell of the vertical flow type reaction cabin 1, each carbon felt electrode is inserted into the inserting groove in the inner wall of the vertical flow type reaction cabin through the electrode inserting port, and after the carbon felt electrode is inserted in place, a sealing strip on the carbon felt electrode seals a contact part of the clamping piece and the shell of the vertical flow type reaction cabin. Each carbon felt electrode is similar to a drawer, and the shell is pulled out and pushed in the vertical flow type reaction chamber, so that the carbon felt electrodes can be conveniently replaced and cleaned. Each porous plate type anode 1-2 is arranged on an installation lug arranged on the inner wall of the shell of the vertical flow type reaction cabin 1 through a screw. The carbon felt electrode 1-1 comprises a carbon felt electrode body 1-1-1 and a sealing strip 1-1-2, the carbon felt electrode body is formed by horizontally overlapping a plurality of layers of carbon felts and is clamped into a whole by a clamping piece 1-1-3, the sealing strip is positioned at the part of the clamping piece, which is contacted with a shell of the vertical flow type reaction cabin, the clamping piece is made of an acrylic plate, the clamping piece is non-conductive, the clamping piece is in a semicircular cake shape and is provided with an inner cavity, and the carbon felt electrode is suitable for being attached to and fixing the carbon felt. The scanning electron micrograph of the carbon felt adopted in the embodiment is shown in fig. 8, and it can be seen from fig. 8 that the carbon felt has a large porosity and a large specific surface area, which indicates that the carbon felt has an adsorption capacity. The shape of the conductive metal sheet 1-3 is consistent with that of the inner wall of the shell of the vertical flow type reaction cabin, the conductive metal sheet is arranged on the inner wall of the shell of the vertical flow type reaction cabin, and each conductive metal sheet 1-3 is contacted with the side surface of each carbon felt electrode 1-1. The distance between each carbon felt electrode 1-1 and the porous plate type anode 1-2 adjacent to the carbon felt electrode is equal. The thickness of each conductive carbon felt 1-1 (specifically, the thickness of the carbon felt electrode body of each conductive carbon felt) is 20cm, the porous plate type anode 1-2 is a BDD electrode net, and the conductive metal sheet is a copper sheet.
Example 2
In this embodiment, a detachable electrolysis-adsorption coupling reactor is provided, and the structure diagram is similar to that of fig. 1.
The utility model provides a detachable electrolysis-absorption coupling reactor includes vertical flow formula reaction cabin 1, upper cover 2 and lower cover 3.
The shell of the vertical flow type reaction cabin 1 is a cylinder with an axis vertical to a horizontal plane, flanges are arranged at the upper end and the lower end of the cylinder, the upper cover and the lower cover are hollow round tables, the flanges matched with the flanges at the two ends of the cylinder are arranged at the lower end of the upper cover and the upper end of the lower cover, a water outlet 2-1 is arranged on the upper cover, a water inlet 3-1 is arranged on the lower cover, and the upper cover and the lower cover are respectively arranged on the upper end surface and the lower end surface of the vertical flow type reaction cabin through the flanges and sealing gaskets to seal the upper end surface and the lower end surface of the vertical flow type reaction cabin. A long strip-shaped shell cabin is arranged on the outer wall of a shell of the vertical flow type reaction cabin 1 along the axial direction of the shell, an anode power line 4 and a cathode power line 5 are positioned in the long strip-shaped shell cabin, and the long strip-shaped shell cabin plays a role in protecting the anode power line 4 and the cathode power line 5. The shell, the upper cover and the lower cover of the vertical flow type reaction cabin are all not conductive, and the shell, the upper cover and the lower cover of the vertical flow type reaction cabin are all made of acrylic plates.
Similar to fig. 2, five carbon felt electrodes 1-1, four porous plate anodes 1-2 and five conductive metal sheets 1-3 are arranged in the shell of the vertical flow type reaction cabin 1, and a power supply is arranged outside the shell of the vertical flow type reaction cabin; each carbon felt electrode is horizontally arranged in the vertical flow type reaction chamber, a porous plate type anode is horizontally arranged between each two adjacent carbon felt electrodes, the carbon felt electrodes are not in contact with the porous plate type anode, the shapes and the sizes of the carbon felt electrodes and the porous plate type anode are matched with the shape and the size of the cross section of the shell of the vertical flow type reaction chamber, and the area between the adjacent carbon felt electrodes and the porous plate type anode is an electrolysis area; each conductive metal sheet is in contact with the carbon felt but not with the porous plate anode; each porous plate type porous anode is respectively connected with the anode of a power supply through an anode power line 4, and each conductive metal sheet is respectively connected with the cathode of the power supply through a cathode power line 5.
More specifically, similar to fig. 3, and as shown in fig. 4-6: five electrode inserting openings are arranged on a shell of the vertical flow type reaction cabin 1, each electrode inserting opening is horizontally arranged, the length of each electrode inserting opening is half of the circumference of the shell, an inserting groove is formed in the inner wall of the shell of the vertical flow type reaction cabin 1, each carbon felt electrode is inserted into the inserting groove in the inner wall of the vertical flow type reaction cabin through the electrode inserting opening, and after the carbon felt electrode is inserted in place, a part, in contact with the shell of the vertical flow type reaction cabin, of the clamping piece is sealed through a sealing strip on the carbon felt electrode. Each carbon felt electrode is similar to a drawer, and the shell is pulled out of and pushed into the vertical flow type reaction chamber, so that the carbon felt electrodes are convenient to replace and clean. Each porous plate type anode 1-2 is arranged on an installation lug arranged on the inner wall of the shell of the vertical flow type reaction cabin 1 through a screw. The carbon felt electrode 1-1 comprises a carbon felt electrode body 1-1-1 and a sealing strip 1-1-2, wherein the carbon felt electrode body is formed by horizontally overlapping a plurality of layers of carbon felts and is clamped into a whole by a clamping piece 1-1-3, the sealing strip is positioned at the part of the clamping piece, which is contacted with a shell of the vertical flow type reaction cabin, the clamping piece is made of an acrylic plate, the clamping piece is non-conductive, the clamping piece is in a semicircular cake shape and is provided with an inner cavity, and the carbon felt electrode is suitable for being attached and fixed with the carbon felt. A scanning electron microscope image of the carbon felt used in this example is shown in fig. 8, and it can be seen from fig. 8 that the carbon felt has a large porosity and a large specific surface area, which indicates that the carbon felt has an adsorption capacity. The shape of the conductive metal sheet 1-3 is consistent with that of the inner wall of the shell of the vertical flow type reaction cabin, the conductive metal sheet is arranged on the inner wall of the shell of the vertical flow type reaction cabin, and each conductive metal sheet 1-3 is contacted with the side surface of each carbon felt electrode 1-1. The distance between each carbon felt electrode 1-1 and the porous plate type anode 1-2 adjacent to the carbon felt electrode is equal. The thickness of each conductive carbon felt 1-1 (specifically, the thickness of the carbon felt electrode body of each conductive carbon felt) is 30cm, the porous plate type anode 1-2 is a BDD electrode net, and the conductive metal sheet is a copper sheet.
Example 3
In this embodiment, an electrolysis-adsorption coupling wastewater treatment apparatus is provided, and a schematic structural diagram of the wastewater treatment apparatus is shown in fig. 7, and includes the detachable electrolysis-adsorption coupling reactor, the primary regulation tank 6, the secondary regulation tank 7, and the sedimentation tank 8 described in embodiment 1, wherein stirring devices are provided in the primary regulation tank 6 and the secondary regulation tank 7, the primary regulation tank is used for adding a catalyst, an oxidant, and an acid, the secondary regulation tank is used for adding an alkali, a water outlet of the primary regulation tank is communicated with a water inlet of the detachable electrolysis-adsorption coupling reactor, a water outlet of the detachable electrolysis-adsorption coupling reactor is communicated with a water inlet of the secondary regulation tank, and a water outlet of the secondary regulation tank is communicated with a water inlet of the sedimentation tank.
Example 4
In this embodiment, an electrolysis-adsorption coupling wastewater treatment apparatus is provided, which has a structure schematic diagram similar to that of fig. 7, and includes the detachable electrolysis-adsorption coupling reactor, the primary regulation tank 6, the secondary regulation tank 7, and the sedimentation tank 8 described in embodiment 2, and further includes a control system, where the control system is used to control the feeding of the catalyst, the oxidant, the acid, and the alkali, and the water inlet flow rate and the water outlet flow rate, and the control system is specifically a common modular management system in the prior art. Stirring devices are arranged in the primary regulating tank 6 and the secondary regulating tank 7, the primary regulating tank is used for adding a catalyst, an oxidant and an acid, the secondary regulating tank is used for adding alkali, a water outlet of the primary regulating tank is communicated with a water inlet of the detachable electrolysis-adsorption coupling reactor, a water outlet of the detachable electrolysis-adsorption coupling reactor is communicated with a water inlet of the secondary regulating tank, and a water outlet of the secondary regulating tank is communicated with a water inlet of the sedimentation tank.
Example 5
In this example, common antibiotic Sulfamethoxazole (SMX) was used as a target pollutant to prepare SMX-simulated wastewater with an SMX concentration of 2mg/L, and the simulated wastewater was treated by using the electrolysis-adsorption coupled wastewater treatment apparatus provided in example 3.
In this example, 8 experimental groups were set, and different experimental conditions were used in each experimental group to compare the treatment effects of the SMX-simulated wastewater under various experimental conditions:
adsorption (adsorption) experimental group: introducing SMX simulation wastewater into a detachable electrolysis-adsorption coupling reactor, adsorbing the SMX simulation wastewater by using a carbon felt electrode without turning on a power supply, sampling from the reactor every 2-5 min for water quality detection, and respectively calculating the SMX concentration (C) and the SMX initial concentration (C) after processing for corresponding time 0 ) As shown by the curve adsorption in the graph (a) of fig. 9, it is understood that the carbon felt electrode has a certain adsorption capacity for SMX, and can adsorb and remove about 20% of SMX in the SMX-simulated wastewater.
EC experimental group: introducing SMX simulation wastewater into a detachable electrolysis-adsorption coupling reactor, turning on a power supply, and controlling the current density to be 11.1mA/cm 2 Sampling from the reactor once every 2-5 min for water quality detection, and respectively calculating the SMX concentration (C) and the SMX initial concentration (C) after the treatment for corresponding time 0 ) As shown by the curve EC in the graph (a) of fig. 9, it is understood that the SMX degradation is enhanced by turning on the power supply based on the adsorption of the carbon felt electrode to the SMX.
PMS experimental group: introducing SMX simulated wastewater into a primary regulating reservoir, and feeding into the primary regulating reservoirAdding an oxidant Peroxymonosulfate (PMS) to ensure that the concentration of the oxidant in the SMX simulation wastewater is 0.05mmol/L, then introducing the wastewater into a detachable electrolysis-adsorption coupling reactor, sampling from the reactor once every 2-5 min without turning on a power supply to perform water quality detection, and respectively calculating the SMX concentration (C) and the SMX initial concentration (C) after the treatment for corresponding time 0 ) The results are shown in the graph (a) of fig. 9 as curve PMS, and it is understood from the graph that the effect of treating wastewater by the PMS test group and the adsorption test group is substantially the same.
EC/PMS experimental group: on the basis of a PMS experimental group, a power supply is started, and the current density is controlled to be 11.1mA/cm 2 As shown by the curve EC/PMS in the graph (a) of fig. 9, it is clear that the degradation effects of the EC/PMS test group and the EC test group on SMX are close to each other, indicating that the effect of only adding an oxidizing agent on the degradation ability is insignificant on the basis of energization.
PMS/Fe (III) experimental group: introducing SMX simulated wastewater into a primary regulating tank, and adding an oxidant Peroxymonosulfate (PMS) and a catalyst ferric sulfate (Fe) into the primary regulating tank 2 (SO 4 ) 3 ) Making the concentrations of an oxidant and a catalyst in SMX simulation wastewater be 0.05mmol/L, then introducing the wastewater into a detachable electrolysis-adsorption coupling reactor, sampling from the reactor every 2-5 min without turning on a power supply for water quality detection, and respectively calculating the concentration (C) of SMX and the initial concentration (C) of SMX after the corresponding time of treatment 0 ) The results are shown in the graph (a) of FIG. 9 as curve PMS/Fe (III), and it is clear from the graph that the effect of treating wastewater by the PMS/Fe (III) test group and the adsorption (adsorption) test group is almost the same.
PMS/Fe (II) experimental group: the catalyst in the PMS/Fe (III) experimental group is replaced by ferrous sulfate (FeSO) 4 ) As shown by the curve PMS/Fe (II) in the graph (a) of FIG. 9, it can be seen that the experimental group PMS/Fe (II) can degrade and remove about 60% of SMX, and the removal rate of SMX is basically unchanged after 2min of reaction, which indicates that the concentration of ferrous iron in the system is high at the beginning, and the rapid activation reaction of PMS generates highly oxidative active substances to perform oxidative degradation on pollutants. As the reaction proceeds, ferrous iron is gradually converted toThe stable ferric iron and the system do not have the reducing capability, so that the ferric iron is accumulated, the ferrous iron disappears, the PMS activation reaction is stopped, and the active substances cannot be continuously produced.
EC/PMS/Fe (III) experimental group: on the basis of PMS/Fe (III) experimental group, the power supply is turned on, and the current density is controlled to be 11.1mA/cm 2 The results are shown by the curves EC/PMS/Fe (III) in the graph (a) of FIG. 9.
EC/PMS/Fe (II) experimental group: on the basis of PMS/Fe (II) experimental group, the power supply is turned on, and the current density is controlled to be 11.1mA/cm 2 The results are shown by the curves EC/PMS/Fe (II) in the graph (a) of FIG. 9.
EC/PMS/Fe (III) experimental group and EC/PMS/Fe (II) experimental group can reach 100% degradation effect to the pollutant in 6min, explain to adopt the utility model discloses a device is switched on the basis of adding catalyst and oxidant, is favorable to improving the circulation efficiency of catalyst, improves PMS's activation efficiency, and the reinforcing system is to the getting rid of the pollutant. It can also be seen from the degradation curves that the degradation rates of SMX were very fast for both experimental groups, indicating that both had very high contaminant removal efficiency.
The catalyst for realizing the catalytic activation effect is mainly Fe (II), and the divalent iron is mainly from the reduction of trivalent iron on the surface of the cathode, so the regeneration rate of the divalent iron also reflects the running performance of the device provided by the utility model. Fig. 9 (b) (c) is the ferrous iron and total iron concentration conditions of the PMS/Fe (III) experimental group and the EC/PMS/Fe (III) experimental group during the operation process, respectively, and it can be known from fig. 9 (c) that the device provided by the present invention can achieve about 40% efficiency for the regeneration of ferrous iron, and under the condition of PMS, the generation of ferrous iron is not detected in the first 6min of the system reaction, which indicates that the regenerated ferrous iron can be efficiently utilized by PMS.
Example 6
In this example, different anions (Cl) were examined - 、H 2 PO 4 - 、HCO 3 - 、NO 3 - ) Effect on the performance of the device of example 3.
The actual waste water system is complex and is stored thereinIn the presence of various types of anions which may adversely affect certain aspects of the wastewater treatment process, the present example explored various anions (Cl) - 、H 2 PO 4 - 、HCO 3 - 、NO 3 - ) The influence on the running efficiency of the device under the common anion concentration condition in the actual wastewater. Common antibiotic Sulfamethoxazole (SMX) is used as a target pollutant to prepare an SMX solution, anions with different concentrations are added into the SMX solution, and simulated wastewater containing the anions with different concentrations and the SMX concentration of 2mg/L is prepared.
Introducing SMX simulated wastewater into a primary regulating tank, and adding an oxidant Peroxymonosulfate (PMS) and a catalyst ferric sulfate (Fe) into the primary regulating tank 2 (SO 4 ) 3 ) Making the concentration of oxidant and catalyst in SMX simulation wastewater be 0.05mmol/L, introducing the wastewater into a detachable electrolysis-adsorption coupling reactor, turning on a power supply, and controlling current density to be 11.1mA/cm 2 Sampling from the reactor once every 1-2 min for water quality detection, and respectively calculating the SMX concentration (C) and the SMX initial concentration (C) after the treatment for corresponding time 0 ) The results are shown in FIG. 10.
As shown in FIG. 10 (a), in Cl - Has an accelerating effect on the SMX degradation efficiency in the coexistence of the conditions, which are caused by active substances such as · OH and SO 4 ·- Can react with Cl - The reaction produces other active chlorine species which are also capable of oxidatively degrading organic contaminants. As shown in FIG. 10 (b), at H 2 PO 4 - Under the coexistence condition, with H 2 PO 4 - The degradation efficiency of SMX is inhibited to a certain extent by increasing the concentration. This may be H 2 PO 4 - Can react with active substances generated in the reaction process to generate quenching effect on the active substances, thereby reducing the content of active substances · OH and SO 4 ·- The reaction rate with contaminants, but the efficiency of SMX degradation still reached near 100% with the reaction time extended to 10 min. As shown in the figure10 (c) of (c), HCO 3 - The addition of (a) has substantially no adverse effect on the degradation of SMX. As shown in (d) of FIG. 10, in NO 3 - In the coexistence of NO 3 - The degradation efficiency of SMX is also inhibited to some extent by increasing the concentration, which is probably NO 3 - And reacting with active substances generated in the reaction process. But the degradation efficiency of the SMX reaches about 80 to 100 percent along with the prolonging of the reaction time to 8 to 10 min.
In summary, the coexistence of above four kinds of common anions in the concentration range of actual water, the adverse effect that produces the pollutant degradation is all not obvious, explains the utility model provides a device has good complicated water adaptability, can demonstrate stable organic pollutant degradation ability under multiple different quality of water.
Example 7
In this example, the ability of the device of example 3 to degrade different contaminants was examined.
The target pollutants are degradation of several organic pollutants commonly found in the environment, and specifically include Atrazine (ATZ), bisphenol A (BPA), carbamazepine (CBZ), metronidazole (MNZ) and Nitrobenzene (NB). Dissolving each target pollutant in water, and respectively preparing simulated wastewater with the target pollutant concentration of 2 mu mol/L.
Respectively introducing the simulated wastewater into a primary regulating tank, and adding an oxidant Peroxymonosulfate (PMS) and a catalyst ferric sulfate (Fe) into the primary regulating tank 2 (SO 4 ) 3 ) Leading the concentrations of an oxidant and a catalyst in the simulated wastewater to be 0.05mmol/L, then leading the wastewater into a detachable electrolysis-adsorption coupling reactor, starting a power supply, and controlling the current density to be 11.1mA/cm 2 Sampling from the reactor once every 1-2 min for water quality detection, and respectively calculating the target concentration (C) and the initial concentration (C) of the target pollutant after the treatment for corresponding time 0 ) The results are shown in FIG. 11. As can be seen from FIG. 11, the degradation efficiency of the device provided by the present invention can reach 100% for all target pollutants within 10min of reaction time.
Claims (10)
1. A detachable electrolysis-adsorption coupling reactor is characterized in that the reactor comprises a vertical flow type reaction cabin (1), an upper cover (2) and a lower cover (3),
the shell of the vertical flow type reaction cabin (1) is a cylinder body with the axis vertical to the horizontal plane, the upper cover is provided with a water outlet (2-1), the lower cover is provided with a water inlet (3-1), and the upper cover and the lower cover are respectively arranged on the upper end surface and the lower end surface of the vertical flow type reaction cabin to seal the upper end surface and the lower end surface of the vertical flow type reaction cabin; the shell, the upper cover and the lower cover of the vertical flow type reaction cabin are not conductive;
a plurality of carbon felt electrodes (1-1), porous plate anodes (1-2) and conductive metal sheets (1-3) are arranged in a shell of the vertical flow type reaction cabin (1), and a power supply is arranged outside the shell of the vertical flow type reaction cabin; each carbon felt electrode is horizontally arranged in the vertical flow type reaction chamber, a porous plate type anode is horizontally arranged between each two adjacent carbon felt electrodes, the carbon felt electrodes are not in contact with the porous plate type anode, the shapes and the sizes of the carbon felt electrodes and the porous plate type anode are matched with the shape and the size of the cross section of the shell of the vertical flow type reaction chamber, and the area between the adjacent carbon felt electrodes and the porous plate type anode is an electrolysis area; each conductive metal sheet is in contact with the carbon felt but not in contact with the porous plate anode; each porous plate type porous anode is connected with the anode of the power supply through an anode power line (4), and each conductive metal sheet is connected with the cathode of the power supply through a cathode power line (5).
2. The detachable electrolytic-adsorptive coupling reactor according to claim 1, wherein said carbon felt electrode is detachably mounted in the housing of said vertical flow reaction chamber (1).
3. The detachable electrolysis-adsorption coupling reactor according to claim 2, wherein the carbon felt electrode (1-1) comprises a carbon felt electrode body (1-1-1) and a sealing strip (1-1-2), the carbon felt electrode body is horizontally overlapped by a plurality of layers of carbon felts and is clamped into a whole by a clamping piece (1-1-3), and the sealing strip is positioned at the part where the clamping piece is contacted with the shell of the vertical flow type reaction cabin.
4. The detachable electrolysis-adsorption coupling reactor according to claim 3, wherein the shell of the vertical flow type reaction chamber (1) is provided with electrode insertion ports with the same number as that of the carbon felt electrodes (1-1), each carbon felt electrode is inserted into the shell of the vertical flow type reaction chamber through the electrode insertion port, and after the carbon felt electrodes are inserted in place, the sealing strips on the carbon felt electrodes seal the contact part of the clamping piece and the shell of the vertical flow type reaction chamber.
5. The detachable electrolytic-adsorptive coupling reactor according to any one of claims 1 to 4, wherein said conductive metal sheets (1-3) are formed in a shape corresponding to the shape of the inner wall of the shell of said vertical flow reactor chamber, said conductive metal sheets are mounted on the inner wall of said shell of said vertical flow reactor chamber, and each of said conductive metal sheets (1-3) is in contact with the side of each of said carbon felt electrodes (1-1).
6. The detachable electrolytic-adsorptive coupling reactor according to any one of claims 1 to 4, wherein the inner wall of the shell of the vertical flow type reaction cabin (1) is provided with a slot, and each carbon felt electrode is inserted into the slot; each porous plate type anode (1-2) is arranged on the inner wall of the shell of the vertical flow type reaction cabin (1).
7. The detachable electrolytic-adsorptive coupling reactor according to any one of claims 1 to 4, wherein each carbon felt electrode (1-1) has a thickness of 20 to 30cm, and the porous plate anode (1-2) is a BDD electrode mesh.
8. The detachable electrolysis-adsorption coupling reactor according to any claim 1 to 4, wherein the number of the carbon felt electrodes (1-1) is 3-6, and the carbon felt electrodes are arranged at different heights of the vertical flow type reaction cabin (1).
9. The detachable electrolytic-adsorptive coupling reactor according to any one of claims 1 to 4, wherein each carbon felt electrode (1-1) is equally spaced from the adjacent porous plate-type anode (1-2).
10. An electrolysis-adsorption coupling wastewater treatment device, which is characterized by comprising the detachable electrolysis-adsorption coupling reactor, a primary regulating tank (6), a secondary regulating tank (7) and a sedimentation tank (8) according to any one of claims 1 to 9, wherein the primary regulating tank is used for adding a catalyst, an oxidant and an acid, the secondary regulating tank is used for adding alkali, a water outlet of the primary regulating tank is communicated with a water inlet of the detachable electrolysis-adsorption coupling reactor, a water outlet of the detachable electrolysis-adsorption coupling reactor is communicated with a water inlet of the secondary regulating tank, and a water outlet of the secondary regulating tank is communicated with a water inlet of the sedimentation tank.
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