KR100954274B1 - Electrokinetic removal system of heavy metal - Google Patents

Abstract

PURPOSE: An electrokinetic heavy metal removing device is provided to remove heavy metal stored in deposits by using cathode circulating water as a specific acidity electrolyte solution, and to reduce power consumption. CONSTITUTION: An electrokinetic heavy metal removing device comprises the following: a reactor receiving anode circulation water consisting of an acidity electrolyte solution and anode circulating water consisting of deposit soil and tap water; an anode circulating water supply part(130) supplying the anode circulating water to the reactor; a cathode circulating water supply part(132) supplying cathode circulating water to the reactor; and a power supply part(200) flowing a current to the deposit soil by supplying power to the reactor. The reactor includes an anode(110), a cathode(112), a first separation stand(120), a second separation stand(122), and a deposit receiving part(140) formed between the first separation stand and the second separation stand.

Description

[0001] Electrokinetic removal system of heavy metal [

The present invention relates to a device for removing heavy metals from marine sediments, and more particularly, to an apparatus for removing heavy metals stored in marine sediments by using a copper electrolytic cell and a cathode circulating water as a specific electrolytic solution.

Marine sediments are substances that accumulate on the bottom of the sea, consisting of materials physically separated by weathering and erosion of rocks, or substances derived from organisms or substances formed by chemical reaction of these substances. Thus, the marine sediments formed in this manner serve as a reservoir for storing or accumulating contaminants such as heavy metals discharged from rivers, lakes, and harbors, as well as materials originating from the rocks and organisms. In addition, stored contaminants can be re-leached or resuspended, which can be a new source of pollution.

Such marine pollution affects marine life, and the damage caused by heavy metals is bound to become larger as the food chain becomes higher due to bioconcentration. Accordingly, the removal of heavy metals from marine sediments is an important issue in order to prevent pollution of marine life, which is an important food resource for human beings. For this purpose, it is possible to consider dredging the bottom of the shore by recovering the sediments contaminated with heavy metals, but the dumping of the contaminated sediments after dredging can not be a fundamental solution. In recent years, various purification techniques have been studied in consideration of the method of treating sediments in situ.

However, most of the marine sediments have silt quality soil, so it is difficult to apply the purification technology. Even if the purification technology is applied, organic substances and heavy metals contained in the sediments during the treatment process may cause unexpected reaction mechanism There is a problem that the resistance is increased during operation or operation and the power consumption is large.

Accordingly, a technical problem to be solved by the present invention is to provide a heavy metal removing apparatus using electro dynamics capable of efficiently removing heavy metals stored in a marine sediment, less electric power consumption, .

According to an aspect of the present invention, there is provided an apparatus for removing heavy metals in an electrophoretic medium, comprising: a reactor capable of receiving a negative electrode circulating water made of a positive electrode circulating water and an acidic electrolyte solution made of sediment and tap water; A cathode circulating water supply unit for supplying the cathode circulating water to the reactor, and a power supply unit for supplying electric power to the reactor to supply current to the deposited soil, wherein the reactor is provided at both ends of the reactor The anode and the cathode being spaced apart from each other by a predetermined distance and spaced apart from the anode in the direction of the center of the reactor so as to form a space capable of accommodating the anode circulating water and the sediment can not pass therethrough, A first separator that can pass through the cathode separator, A second separator arranged to be spaced apart from the negative electrode in the direction of the center of the reactor so as to form a space that can be accommodated, the sediment can not pass through but the negative circulating water can pass therethrough, And a sediment receiving portion formed between the sediment receiving portion.

In a preferred embodiment of the present invention, the anode circulating water supply unit and the cathode water circulating water supply unit may further include a circulation pump capable of injecting or discharging the anode circulation water and the cathode circulation water, respectively. The negative electrode circulating water may be an aqueous solution containing any one selected from the group consisting of nitric acid (HNO ₃ ), ethylenediamine tetraacetic acid (EDTA), citric acid and hydrochloric acid (HCl) ) Aqueous solution or citric acid aqueous solution. The concentration of the hydrochloric acid aqueous solution or citric acid aqueous solution may be 0.01 M to 0.5 M.

The electrodynamic heavy metal removal apparatus according to the present invention increases the concentration of heavy metal ions that can be treated in the sediment by making the negative electrode circulating water a specific acidic electrolytic solution, thereby reducing the resistance and keeping the current constant to minimize the power consumption Heavy metals can be treated. In addition, by controlling the pH, it is possible to effectively treat the heavy metals in the sediments by preventing the precipitation that may occur by OH ^- at the cathode.

Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the accompanying drawings. The embodiments described below can be modified in various other forms, and the scope of the present invention is not limited to the embodiments described below. The embodiments of the present invention are provided to enable those skilled in the art to more fully understand the present invention.

Hereinafter, first, the structure of the electrodynamic heavy metal removal apparatus according to the embodiment of the present invention will be described. Then, according to the experimental examples, the removal rate of heavy metal, the intensity of electric current flowing through the soil and the pH The changes will be described by means of tables and graphs, and a preferred embodiment thereof will be presented.

1 is a schematic view showing the structure of an electrodynamic heavy metal removal apparatus 10 according to an embodiment of the present invention.

1, the electrodynamic heavy metal removal apparatus 10 includes a reactor 100, a power supply 200, a cathode circulation water supply unit 500, a cathode circulation water supply unit 510, a first circulation path 400 , A second circulation path (410), a first circulation pump (300), and a second circulation pump (310).

The reactor 100 is a horizontally elongated rectangular parallelepiped container having an open upper end, and has a positive electrode 110 and a negative electrode 112 at both ends thereof. The positive electrode and the negative electrode may be carbon electrodes, and other materials may be applied in some cases. The first separator 120 is disposed at a position spaced apart from the positive electrode 110 by a predetermined distance and the second separator 122 is disposed at a position spaced apart from the negative electrode 112 by a predetermined distance. Accordingly, the inside of the reactor 100 is divided into a sedimentation receiving section 140 having a first separator 120 and a second separator 122 at both ends, a first separator 120 and a reactor 100 And a cathode circulating water receiving portion 132 having a boundary between the other side of the reactor 100 and the anode circulating water receiving portion 130 and the second separating wall 122 with the side surface as a boundary. Accordingly, the positive electrode 110 is disposed in the positive electrode circulating water receiving portion 130, and the negative electrode 112 is disposed in the negative electrode circulating water receiving portion 132.

The first separator 120 and the second separator 122 may include a plurality of small holes formed therein, but not shown. The reason for adding the filter paper is that the anode circulation water and the cathode water circulate through the separators 120 and 122 and the sediment stored in the sediment storage unit 140 can not pass therethrough, Or the cathode circulating water receiving portion 132, as shown in FIG.

The power supply unit 200 is a device for supplying power to the reactor 100. The power supply unit 200 supplies necessary power to maintain a constant voltage and is connected to the positive electrode 110 and the negative electrode 112 to flow a DC current in the reactor 100 do. The positive electrode 110 and the negative electrode 112 may be graphite electrodes.

The material of the reactor 100 is preferably selected to be durable and not corroded by contaminated soil or various electrolyte solutions to be contained therein. Therefore, a durable synthetic resin, a low-corrosive metal or an alloy can be applied. In addition, the size of the reactor 100 can be varied depending on the amount of sediments to be treated and the environment in which it is used. In addition to the rectangular parallelepipeds shown above, the reactor 100 can be manufactured in various shapes such as a cylindrical shape or a polygonal shape, It is possible to block the introduction of external substances or to add a cover for the safety of the user.

 The anode circulating water supply part 500 supplies the anode circulating water to be supplied to the anode circulating water receiving part 130 and corresponds to a storage tank of tap water to be applied as the anode circulating water. The first circulation path 400 may be configured to move the anode circulation water stored in the anode circulation water supply unit 500 to the anode circulation water storage unit 130 or to move the anode circulation water storage unit 130 This is a passage through which the anode circulating water can be discharged to the outside. The first circulation pump 300 may be disposed in the first circulation path 400 that moves from the anode circulation water supply unit 500 to the anode circulation water storage unit 130 to draw tap water. Although not shown, it may be provided in the first circulation path 400 that is moved from the anode circulation water receiving part 130 to the anode circulation water supply part 500 to facilitate the discharge of tap water after the heavy metal treatment.

The cathode circulation water supply unit 510 supplies cathode circulation water to be supplied to the cathode circulation water storage unit 132 and corresponds to a specific acid solution storage tank to be used as the cathode circulation water. The specific acid solution may be any one selected from nitric acid (HNO ₃ ), ethylenediamine tetraacetic acid (EDTA), citric acid and hydrochloric acid (HCl). The second circulation path 410 and the second circulation pump 310 connected to the first circulation path 410 and the second circulation pump 310 have the same structure and principle as those of the first circulation path 400 and the first circulation pump 300 described above, .

The operation principle of the electrodynamic heavy metal removal apparatus 10 having the above structure will be described. First, sediments contaminated with a heavy metal are filled in the sediment receiving portion 140 of the reactor 100. The anode circulating water receiving portion 130 receives and replenishes the tap water serving as the anode circulating water from the anode circulating water supplying portion 500 and the cathode circulating water receiving portion 132 receives the anode circulating water from the cathode circulating water supplying portion 510, Acid solution is supplied and filled. Then, the power supply unit 200 is connected to the positive electrode 110 and the negative electrode 112, and a constant voltage is applied to flow a direct current to the contaminated sediment. Here, the principle of removing heavy metals is by electro-osmosis, electromigration, and eletrophoresis.

Electro-osmosis is a phenomenon in which a liquid in a medium moves in a specific direction when a voltage is applied to a porous medium such as soil. In general, soil particles come into contact with water to form a negative charge, a liquid having a high positive charge density is collected between the soil particles, and the liquid flows in the direction of the cathode when a current flows. Electrophoresis is a phenomenon in which metals or ions move to the opposite electrode, and electrophoresis means that colloid or charged particles move to the opposite electrode. The embodiment of the present invention uses a principle of removing heavy metals contained in sediments by supplying electrolytic solution to the sediments using the above-mentioned phenomena and flowing electric current.

In order to examine the efficient application of the electrodynamic heavy metal removal apparatus 10 described above, experiments were conducted to investigate the removal rate of heavy metals, the current change of sediment soil, and the pH change of sediments while varying the types of negative electrode circulating water and application period of constant voltage Give examples.

The electrophysiological heavy metal removal apparatus 10 applied to the experiment was made to have a predetermined size for the convenience of experiment. The reactor 100 was made of acrylic material and had a size of 30 cm in length, 4 cm in width, And the length of the anode circulation water supply part 130 and the length of the cathode water circulation water supply part 132 are 5 cm respectively and the opened top is sealed. In addition, the separators 120 and 122 were made of an acrylic plate having a plurality of holes so that the electrolytic solution and the tap water can flow, and the filtration paper was attached to prevent the loss of sediment. The cathode circulating water and the cathode circulating water supplying part 500 were made of a measuring flask.

Sediments used as experimental materials were collected from harbors located in Pusan. The collected samples were used without any pretreatment after removing the contaminants. The initial state of the sample and the heavy metal content are as shown in <Table 1>.

Category (unit) shame Hydrogen ion concentration (pH) 7.7 Organic matter content (%) 13.3 Water content (%) 50.2 Heavy metal concentration (mg / kg) Ni 20.4 Cu 193 Zn 219 CD 2.2 Pb 79

In the following Experimental Example, the collected sediments were poured into the sedimented soil receiving portion 140, and 1 liter of tap water was continuously supplied to the anode circulating water receiving portion 130 by the first circulating pump 300 as the anode electrolyte solution . As a negative electrode electrolyte solution, 0.1 M of EDTA, citric acid, nitric acid and hydrochloric acid were continuously supplied by a circulation pump to the negative electrode circulating water receiving portion by 1 L each. In addition, in order to examine the action of the acidic solution as the negative electrode electrolyte solution, a distilled water (H ₂ O) was used as a negative electrode circulating water as a comparative example. The place where the reactor 100 was installed was kept horizontal to minimize the influence of the water level difference. The conditions of each experiment are shown in Table 2 below.

Experiment number Voltage gradient (V / cm) Anode circulation water Cathode circulation water Experiment period (days) Example 1 One tap water nitric acid 5 Example 2 One tap water nitric acid 10 Example 3 One tap water nitric acid 15 Example 4 One tap water EDTA 5 Example 5 One tap water EDTA 10 Example 6 One tap water EDTA 15 Seventh Experimental Example One tap water Hydrochloric acid 15 Example 8 One tap water Citric acid 15 Comparative Example One tap water Distilled water 15

After conducting the experiment under the above conditions, the sediment was separated from the reactor and divided into 10 equal parts from the anode to the cathode. By measuring the heavy metal concentration at that point, the mobility of ions was analyzed and the removal rate of heavy metals was confirmed.

2A to 2E are graphs showing removal ratios of heavy metals in the first to third experimental examples using nitric acid (HNO ₃ ) as the negative electrode circulating water. Here, the removal rate of heavy metals is the value of the amount of heavy metals removed after the experiment in each heavy metal contained in the sediments (the amount of each heavy metal contained in the sediment before the experiment - the amount of each heavy metal remaining after the experiment) The amount of each heavy metal contained in the former sediment soil × 100 (%)).

FIG. 2A shows nickel, FIG. 2B shows copper, FIG. 2C shows zinc, FIG. 2D shows cadmium, and FIG. In this case, the vertical axis represents the concentration (mg / kg) of each heavy metal, and the horizontal axis represents the position of the uniformly divided section, expressed as the distance from the anode. At this time, the dotted line represents the concentration of the heavy metal in each section before the heavy metal removal apparatus is operated. Here, .smallcircle. Is the first experimental example, .largecircle. Is the second experimental example, and? Is the concentration of each heavy metal in the third experimental example. Therefore, by comparing the concentration of each heavy metal before the experiment with the concentration of each heavy metal after the experiment, it is possible to know the removal rate of the heavy metal by the section, and furthermore, the average removal rate can be confirmed.

Figs. 3A to 3E are graphs showing the removal ratios of heavy metals in the fourth to sixth experimental examples. Fig. FIG. 3A shows nickel, FIG. 3B shows copper, FIG. 3C shows zinc, FIG. 3D shows cadmium, and FIG. The graphs were analyzed in the same manner as in FIGS. 2A to 2E, wherein .largecircle. Is the fourth experimental example, .largecircle. Is the fifth experimental example, and V: is the concentration of each heavy metal in the sixth experimental example.

4A to 4E are graphs showing removal rates of heavy metals in the seventh and eighth experimental examples and comparative examples. FIG. 4A shows nickel, FIG. 4B shows copper, FIG. 4C shows zinc, FIG. 4D shows cadmium, and FIG. Here, .smallcircle. Represents the seventh experimental example, .largecircle. Represents the eighth experimental example, and? Represents the concentration of each heavy metal in the comparative example.

As a method of analyzing the concentration of heavy metals in sediments, each sediments after the end of the experiment were dried at 105 ° C for 4 hours according to the soil pollution process test method. Then, the sediment was sieved with a standard (100 mesh) And then used as a sample. To 1 g of this sample, a mixture of 7 ml of hydrochloric acid and 2.3 ml of nitric acid was added, and the mixture was allowed to stand at 75 ° C for 1 hour. Then, the mixture was filtered through 5B filter paper, and the heavy metal concentration was measured with the filtrate. ICP-MASS 7500CX (Agilent, USA) was used for the concentration measurement.

The average heavy metal removal ratios in the first to eighth experimental examples and the comparative examples, which were calculated based on the above measured values, were as shown in Table 3 below. The removal rate of - has a value due to the pretreatment method for the analysis. In order to analyze the heavy metals in sediments, it is subjected to an extraction step. Most of the analytical methods can not extract 100% of the heavy metals. It is known that the extraction method used in the present invention extracts 50-80% of the total heavy metal content by aqua regia extraction method. Thus - the removal rate means that the heavy metals which were not extracted by the water extraction before the treatment were extracted by the water extraction after the treatment.

Experiment number Average removal rate of heavy metals (%) Ni Cu Zn CD Pb Example 1 20.1 15.5 7.7 -5.9 -12.12 Example 2 -30.6 8.4 9.3 100 31.16 Example 3 49.9 15.7 -2.8 100 0.85 Example 4 23.4 3 -5 -11 -16 Example 5 42 26.8 6.4 100 19.5 Example 6 25.1 12.3 -21 100 -5.7 Seventh Experimental Example 71.5 68.6 62.4 100 65.3 Example 8 56.3 71.3 60.3 -28.6 54 Comparative Example 25.8 40.9 3.2 -39.7 13.9

According to FIGS. 2A to 4E and 3, the removal rate of heavy metals was the highest in the seventh experiment using hydrochloric acid as the cathode circulating water. However, in the first to third experimental examples using nitric acid, the removal rate of heavy metals was remarkably decreased despite application of a strong acid electrolyte solution. The reason for this is that the chloride ion (Cl ^- ) of hydrochloric acid can exist in the form of an ion in association with metal, but the nitrate ion (NO ₃ ^- ) has no reaction mechanism capable of binding to the metal and the ligand bond itself does not occur do.

Next, the change of the current flowing in the sedimentation soil in each experimental example was measured with the passage of time.

FIG. 5A is a graph showing the change in the intensity of the current over time in the first to third experimental examples in which nitric acid is applied as the negative electrode circulating water. FIG. In this case, the abscissa represents the elapsed time and the unit represents hour, and the ordinate represents the intensity of the current flowing in the sedimentation soil, and the unit is mA. The symbol &amp;thetas; represents the first experimental example, the symbol O represents the second experimental example, and the symbol V represents the results for the third experimental example.

FIG. 5B is a graph showing changes in the intensity of the current over time in the fourth to sixth experimental examples in which EDTA is applied as the negative electrode circulating water. FIG. In this case, the horizontal axis and the vertical axis are the same as those in FIG. 5A,? Represents the fourth example,? Represents the fifth example, and? Represents the sixth example.

FIG. 5C is a graph showing changes in intensity of electric current with passage of time in the seventh and eighth experimental examples and the comparative example. The symbol represents the seventh example, the symbol represents the eighth example, and the symbol represents the comparative example to which distilled water is applied.

According to Figs. 5A to 5C, the seventh and eighth experimental examples show that the current intensity is constant or increases even if the circulating water is changed during the experiment period. Here, the increase in electric current means that there are many heavy metal ions that can be removed from the sediments. Therefore, when hydrochloric acid or citric acid is used as a negative electrode circulating water, it means that many heavy metals are present as ions, which means that the removal of heavy metals is efficient.

However, in the case of using an electrolyte solution other than hydrochloric acid or citric acid, the intensity of the total current is decreased, and the heavy metal ions which can be removed by increasing the resistance have eluted but the ion migration has not occurred. At this time, the eluted heavy metal ions accumulated in the vicinity of the cathode and the vicinity of the anode, impeding the flow of the electric current, and the removal rate of the heavy metal was remarkably decreased. Therefore, it was found that it is effective to operate the heavy metal removal apparatus for about 15 days by using hydrochloric acid or citric acid.

Table 4 below shows the power consumption in each experimental example.

Experiment number Power consumption (KWh / ton) Example 1 61.88 Example 2 265.75 Example 3 308.96 Example 4 99.68 Example 5 105.56 Example 6 218.01 Seventh Experimental Example 305.7 Example 8 50.11 Comparative Example 115.47

According to Table 4, the power consumption is the lowest in the eighth experimental example. Therefore, it can be seen that it is economically more effective to use citric acid as the cathode circulating water when considering the power consumption.

6A to 6C are graphs showing changes in the pH of sediments according to the experimental period in the first to eighth experimental examples and the comparative examples, respectively.

6A shows the pH values in the first experimental example, O in the second experimental example, and V in the third experimental example. In Fig. 6B,? Represents the fourth experimental example,? Represents the fifth experimental example, and? Represents the pH value in the sixth experimental example. Further, in Fig. 6C,? Represents the seventh experimental example,? Represents the eighth experimental example, and? Represents the pH value in the comparative example.

6A to 6C, a current flows in the sediments, and as a result of the reaction at the electrode, the concentration of H ⁺ ions becomes high in the positive electrode and becomes acidic, and the concentration of OH ^- ions in the negative electrode becomes basic. At this time, the pH can be adjusted by using an acidic solution as a circulating water in order to prevent precipitation by OH ^- ion around the cathode. On the other hand, as the heavy metal removal treatment progresses, the rate of H ⁺ ions is fast, and the whole is acidified. When nitric acid was used as the cathode circulating water, the anode showed strong acidity with time, but EDTA showed no significant effect on the pH control due to the buffering capacity of the sediments in comparison with the control experiment using distilled water appear. In addition, when citric acid or hydrochloric acid was used, it was acidic around the anode, and especially when hydrochloric acid was used, it showed strong acidity.

In view of the above results, the electrodynamic heavy metal removal apparatus according to the embodiment of the present invention can apply various acid solutions as negative electrode circulating water. Specifically, the experimental results obtained after 15 days of experiment with the acid solution proposed by the present invention, and the results of the experiment conducted for 10 days using EDTA as the cathode circulating water, It can be confirmed that the heavy metal removal rate of the present invention is higher than that of the distilled water which is out of the scope of the invention.

On the other hand, it is desirable to apply hydrochloric acid or citric acid in various acidic solutions in consideration of the efficiency of removing heavy metals. Particularly, it is more preferable to apply citric acid in consideration of the efficiency of heavy metal removal and the power consumption as an economic aspect. The concentration of hydrochloric acid or citric acid is preferably in the range of about 0.01 M to 0.5 M (about 0.1 M). If the concentration of the acidic solution is less than 0.01 M, the pH adjustment of the sediments having a large buffering ability against pH If the concentration is greater than 0.5M, the pH of sediments can be controlled, but the price competitiveness is lowered due to the use of citric acid, which is relatively expensive, and it is difficult to treat wastewater after treatment due to the combination of citric acid and heavy metals.

While the present invention has been particularly shown and described with reference to exemplary embodiments thereof, it is to be understood that the invention is not limited to the disclosed exemplary embodiments, but variations and modifications may be made without departing from the scope of the present invention. It is possible. For example, the size, shape or material of the reactor may be varied depending on the case, and the apparatus for supplying the circulating water may be modified within the scope of the present invention. The power supplied and the concentration of the acid solution can also be set as needed.

1 is a schematic diagram of an electro-mechanical heavy metal removal apparatus according to an embodiment of the present invention.

FIGS. 2A to 2E are graphs showing nickel removal rate, copper removal rate, zinc removal rate, cadmium removal rate, and lead removal rate according to the first through third experimental examples of the present invention, respectively.

3A to 3E are graphs showing nickel removal rate, copper removal rate, zinc removal rate, cadmium removal rate, and lead removal rate according to the fourth through sixth experimental examples of the present invention, respectively.

4A to 4E are graphs showing nickel removal rate, copper removal rate, zinc removal rate, cadmium removal rate, and lead removal rate according to the seventh and eighth experimental examples and comparative examples of the present invention, respectively.

FIG. 5A is a graph showing changes in current intensity with time according to the first through third experimental examples of the present invention, respectively.

FIG. 5B is a graph showing changes in current intensity with time according to the fourth to sixth experimental examples of the present invention. FIG.

FIG. 5C is a graph showing changes in current intensity with time according to the seventh, eighth and comparative examples of the present invention. FIG.

6A is a graph showing pH values according to the first to third experimental examples of the present invention.

6B is a graph showing pH values according to the second through sixth experimental examples of the present invention.

6C is a graph showing pH values according to the seventh and eighth experimental examples and comparative examples of the present invention.

Description of the Related Art [0002]

10: Electrodynamic heavy metal removal device

100: Reactor 110: Positive electrode

112: negative electrode 120: first separator

122: second separator 130: anode circulating water receiving portion

132: cathode circulating water receiving portion 140: deposited deposit receiving portion

200: power supply unit 300: first circulation pump

310: second circulation pump 400: first circulation path

410: second circulation path 500: anode circulation water supply part

510: cathode circulation water supply part

Claims (5)

A reactor capable of receiving cathode circulating water composed of anode circulating water and acidic electrolyte solution made of sediment and tap water; A cathode circulating water supply unit for supplying the anode circulating water to the reactor; A cathode circulating water supply unit for supplying the cathode circulating water to the reactor; And And a power supply unit for supplying electric power to the reactor to cause a current to flow in the deposit, The reactor A positive electrode and a negative electrode disposed at both ends of the reactor and spaced apart from each other by a predetermined distance; A first separator arranged so as to be spaced apart from the positive electrode in a direction toward the center of the reactor so as to form a space for accommodating the positive electrode circulating water, the sediment can not pass through but the positive electrode circulating water can pass; A second separator arranged to be spaced apart from the negative electrode in the direction of the center of the reactor so as to form a space for receiving the negative circulating water, the sediment can not pass through but the negative circulating water can pass; And And a sediment receiving portion formed between the first separating block and the second separating block, Wherein the anode circulating water is an aqueous solution of hydrochloric acid (HCl) or an aqueous solution of citric acid. The apparatus of claim 1, wherein the anode circulation water supply unit and the cathode water circulation water supply unit further include a circulation pump capable of injecting or discharging the anode circulation water and the cathode circulation water, respectively. delete delete The electrophysiological heavy metal removal apparatus according to claim 1, wherein the concentration of the hydrochloric acid aqueous solution or citric acid aqueous solution is 0.01M to 0.5M.

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