CYCLONE HIGH-SPEED ELECTROLYZER USING HIGH-SPEED TURBULENCE, METHOD FOR RECOVERING VALUABLE METALS USING THE SAME, AND VALUABLE METALS RECOVERED THEREFROM

Abstract

A cyclone high-speed electrolyzer using the high-speed turbulence, a method for recovering a valuable metal using the same, and a valuable metals recovered therefrom are provided, by applying a cyclone high-speed electrolytic recovery method to suppress the increase in concentration polarization caused by the rise in activation polarization and the growth of the diffusion layer, which are issues of conventional electrolytic recovery methods. In the cyclone high-speed electrolytic recovery method, a helical downward vortex is generated along the wall of the cyclone electrolyzer to accelerate the electrolyzer at high speed, forming a high-speed turbulent flow. This high-speed turbulence reduces the diffusion layer, significantly improving electrolytic efficiency and remarkably increasing the recovery rate of valuable metals.

Claims

1. A cyclone high-speed electrolyzer using high-speed turbulence for electrolytic recovery of valuable metal, the electrolyzer comprising: an anode in a shape of a rod; and a cathode including a receiving hole for accommodating the anode to form a reaction space between the anode and the cathode, wherein an area ratio of the anode to the cathode in the reaction space is Anode/Cathode=1100, wherein a diameter ratio of Do (overflow) to Du (underflow) is Do/Du=0.0011, wherein a cross section of the anode is circular, and wherein a cross section of the receiving hole is circular, and the anode is eccentrically positioned in the receiving hole.

2. The electrolyzer of claim 1, wherein a turbulent flow velocity of the cyclone high-speed electrolyzer using high-speed turbulence is 8 to 10 m/s.

3. The electrolyzer of claim 1, wherein a helical downward vortex is generated along a wall of the electrolyzer to accelerate the electrolyzer at high speed, thereby forming a high-speed turbulent flow, and wherein the high-speed turbulent flow reduces a diffusion layer to significantly improve electrolytic efficiency, thereby remarkably increasing a recovery rate of the valuable metal.

4. The electrolyzer of claim 1, wherein a maximum distance between the anode and the cathode in the reaction space is 2 to 100 times a minimum distance.

5. The electrolyzer of claim 1, wherein the reaction space is supplied with an acid leaching agent of hydrochloric acid, sulfuric acid, nitric acid, phosphoric acid, acetic acid, or organic acid.

6. The electrolyzer of claim 1, wherein the cathode is formed with a feed configured to introduce a reactant into the reaction space in a diagonal direction.

7. The electrolyzer of claim 1, wherein the anode is made of stainless steel, graphite, or platinum, wherein the cathode is made of titanium coated with iridium, and wherein the anode includes a plurality of cylindrical grooves.

8. The electrolyzer of claim 1, wherein the valuable metal is gold, platinum, palladium, silver, copper, nickel, cobalt, or manganese.

9. The electrolyzer of claim 1, wherein the valuable metal is leached and recovered simultaneously or separately during a process of the electrolytic recovery, and wherein a recovery rate of the valuable metal is 98 to 99.99 wt %.

10. A method for recovering valuable metal using the cyclone high-speed electrolyzer using high-speed turbulence of claim 1, the method comprising steps of: (a-1) adding a reaction solution containing valuable metal ions to the reaction space of the cyclone high-speed electrolyzer using high-speed turbulence to perform an electrolytic refining reaction; (a-2) observing current density and reduction form of the valuable metal depending on a distance between the anode and the cathode during the electrolytic refining reaction; and (a-3) recovering the valuable metal.

11. The method of claim 10, wherein an area ratio of the anode to the cathode in the reaction space is Anode/Cathode=1100, and wherein a diameter ratio of Do (overflow) to Du (underflow) is Do/Du=0.0011.

12. The method of claim 10, wherein the anode is made of stainless steel, graphite, or platinum, wherein the cathode is made of titanium coated with iridium, and wherein the anode includes a plurality of cylindrical grooves.

13. The method of claim 10, wherein the step (a-1) comprises steps of: obtaining a valuable metal leaching solution as a single solution or a mixed solution depending on a type of the valuable metal from a valuable metal concentrate; and supplying the valuable metal leaching solution to the cyclone high-speed electrolyzer using high-speed turbulence to perform the electrolytic refining reaction of the valuable metal, wherein the step of obtaining the valuable metal leaching solution comprises steps of: preparing a powder of the valuable metal concentrate; and extracting the powder of the valuable metal concentrate using an acid leaching agent.

14. The method of claim 13, wherein the acid leaching agent is hydrochloric acid, sulfuric acid, nitric acid, phosphoric acid, acetic acid, or organic acid, and wherein a concentration of the acid leaching agent is 0.2 M to 5 M.

15. The method of claim 13, wherein in the step of extracting the powder of the valuable metal concentrate using an acid leaching agent, a condition for a process of the extracting is characterized by: a leaching time of 0.5 to 12 hours, a pH of 0.5 to 6.5, a solid-to-liquid ratio of 1/2.5 to 1/4, and a temperature of 20 C. to 90 C.

16. The method of claim 10, wherein in the step (a-1) of adding a reaction solution containing valuable metal ions to the reaction space of the cyclone high-speed electrolyzer using high-speed turbulence to perform an electrolytic refining reaction, an applied voltage during the electrolytic refining reaction is 1.75 V to 25 V, a current is 0.5 to 10 A, and a reaction time is 1 to 720 minutes.

17. The method of claim 10, wherein in the step (a-2) of observing current density and reduction form of the valuable metal depending on a distance between the anode and the cathode during the electrolytic refining reaction, the reduction form of the valuable metal is powder, film, or bulk.

18. The method of claim 10, wherein in the step (a-3) of recovering the valuable metal, the valuable metal is recovered simultaneously or separately, and a recovery rate of the valuable metal is 98 to 99.99 wt %.

19. A valuable metal selected from a group consisting of gold, platinum, palladium, silver, copper, nickel, cobalt, and manganese, wherein the valuable metal is recovered with a recovery rate of 98 to 99.99 wt % through the electrolytic refining of a reaction solution containing valuable metal ions using the cyclone high-speed electrolyzer with high-speed turbulence according to claim 1.

20. A valuable metal selected from a group consisting of gold, platinum, palladium, silver, copper, nickel, cobalt, and manganese, wherein the valuable metal is recovered with a recovery rate of 98 to 99.99 wt % through the electrolytic refining of a reaction solution containing valuable metal ions by the method for recovering valuable metal using the cyclone high-speed electrolyzer using high-speed turbulence according to claim 10.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

[0062] FIG. 1 is a schematic diagram of a cyclone high-speed electrolyzer using high-speed turbulence according to an exemplary embodiment of the present disclosure.

[0063] FIG. 2 is a process flow diagram of a method for recovering a valuable metal using a cyclone high-speed electrolyzer using high-speed turbulence according to an exemplary embodiment of the present disclosure.

[0064] FIG. 3a is a graph showing the measured reduction polarization curve of Au according to an exemplary embodiment of the present disclosure.

[0065] FIG. 3b is a graph showing the measured reduction polarization curve of Pt according to an exemplary embodiment of the present disclosure.

[0066] FIG. 3c is a graph showing the measured reduction polarization curve of Pd according to an exemplary embodiment of the present disclosure.

[0067] FIG. 4 is a graph showing the recovery rates of Au, Pt, Pd, Cu, and Ni after cyclone high-speed electrolysis according to an exemplary embodiment of the present disclosure.

[0068] FIG. 5a shows photograph of Pt after cyclone high-speed electrolysis according to an exemplary embodiment of the present disclosure.

[0069] FIG. 5b shows photograph of Pd after cyclone high-speed electrolysis according to an exemplary embodiment of the present disclosure.

[0070] FIG. 5c shows photograph of Cu after cyclone high-speed electrolysis according to an exemplary embodiment of the present disclosure.

[0071] FIG. 5d shows photograph of Ni after cyclone high-speed electrolysis according to an exemplary embodiment of the present disclosure.

[0072] FIG. 6a is a graph showing the electrolytic recovery efficiency based on precious metal concentration according to an exemplary embodiment of the present disclosure.

[0073] FIG. 6b is a graph showing the electrolytic recovery efficiency based on precious metal recovery rate relative to the diameter ratio of Do (overflow) to Du (underflow) (Do/Du) according to an exemplary embodiment of the present disclosure.

[0074] FIG. 7a is a graph showing the electrolytic recovery efficiency based on precious metal concentration according to an exemplary embodiment of the present disclosure.

[0075] FIG. 7b is a graph showing the electrolytic recovery efficiency based on precious metal recovery rate relative to the area ratio of the anode to the cathode (anode/cathode area ratio) according to an exemplary embodiment of the present disclosure.

[0076] FIG. 8a is a graph showing the electrolytic recovery efficiency based on precious metal concentration according to an exemplary embodiment of the present disclosure.

[0077] FIG. 8b is a graph showing the electrolytic recovery efficiency based on precious metal recovery rate relative to the anode material according to an exemplary embodiment of the present disclosure.

[0078] FIG. 9 is a photograph of a solution showing the simultaneous leaching and recovery of Au, Pt, and Pd precious metals according to an exemplary embodiment of the present disclosure.

[0079] FIG. 10a is a graph showing the electrolytic efficiency after simultaneous cyclone electrolytic recovery of the leaching solution following chlorine leaching, based on precious metal concentration according to an exemplary embodiment of the present disclosure.

[0080] FIG. 10b is a graph showing the electrolytic efficiency after simultaneous cyclone electrolytic recovery of the leaching solution following chlorine leaching, based on precious metal recovery rate according to an exemplary embodiment of the present disclosure.

[0081] FIG. 11a is a graph showing the electrolytic efficiency after cyclone electrolytic recovery of the leaching solution following chlorine leaching, based on the metal recovery rate from a single solution according to an exemplary embodiment of the present disclosure.

[0082] FIG. 11b is a graph showing the electrolytic efficiency after cyclone electrolytic recovery of the leaching solution following chlorine leaching, based on the metal recovery rate from a mixed solution according to an exemplary embodiment of the present disclosure.

[0083] FIG. 12a is a graph showing the electrolytic efficiency by concentration after cyclone electrolytic recovery of the leaching solution following chlorine leaching, based on the concentration of gold (Au) according to an exemplary embodiment of the present disclosure.

[0084] FIG. 12b is a graph showing the electrolytic efficiency by concentration after cyclone electrolytic recovery of the leaching solution following chlorine leaching, based on the recovery rate of gold (Au) according to an exemplary embodiment of the present disclosure.

[0085] FIG. 13a is a graph showing the electrolytic efficiency by concentration after cyclone electrolytic recovery of the leaching solution following chlorine leaching, based on the concentration of platinum (Pt) according to an exemplary embodiment of the present disclosure.

[0086] FIG. 13b is a graph showing the electrolytic efficiency by concentration after cyclone electrolytic recovery of the leaching solution following chlorine leaching, based on the recovery rate of platinum (Pt) according to an exemplary embodiment of the present disclosure.

[0087] FIG. 14a is a graph showing the electrolytic efficiency by concentration after cyclone electrolytic recovery of the leaching solution following chlorine leaching, based on the concentration of palladium (Pd) according to an exemplary embodiment of the present disclosure.

[0088] FIG. 14b is a graph showing the electrolytic efficiency by concentration after cyclone electrolytic recovery of the leaching solution following chlorine leaching, based on the recovery rate of palladium (Pd) according to an exemplary embodiment of the present disclosure.

[0089] FIG. 15a is a graph showing the electrolytic efficiency after cyclone electrolytic recovery of the leaching solution following chlorine leaching, based on changes in the applied voltage, with the concentration of gold (Au) according to an exemplary embodiment of the present disclosure.

[0090] FIG. 15b is a graph showing the electrolytic efficiency after cyclone electrolytic recovery of the leaching solution following chlorine leaching, based on changes in the applied voltage, with the recovery rate of gold (Au) according to an exemplary embodiment of the present disclosure.

[0091] FIG. 16a is a graph showing the electrolytic efficiency after cyclone electrolytic recovery of the leaching solution following chlorine leaching, based on changes in the applied voltage, with the concentration of platinum (Pt) according to an exemplary embodiment of the present disclosure.

[0092] FIG. 16b is a graph showing the electrolytic efficiency after cyclone electrolytic recovery of the leaching solution following chlorine leaching, based on changes in the applied voltage, with the recovery rate of platinum (Pt) according to an exemplary embodiment of the present disclosure.

[0093] FIG. 17a is a graph showing the electrolytic efficiency after cyclone electrolytic recovery of the leaching solution following chlorine leaching, based on changes in the applied voltage, with the concentration of palladium (Pd) according to an exemplary embodiment of the present disclosure.

[0094] FIG. 17b is a graph showing the electrolytic efficiency after cyclone electrolytic recovery of the leaching solution following chlorine leaching, based on changes in the applied voltage, with the recovery rate of palladium (Pd) according to an exemplary embodiment of the present disclosure.

DETAILED DESCRIPTION OF THE DISCLOSURE

[0095] Hereinafter, exemplary embodiments of the present disclosure will be described in detail with reference to related drawings.

[0096] The advantages and features of the present disclosure, and methods of accomplishing those advantages and features, will become apparent upon reference to the exemplary embodiments described in detail with reference to the accompanying drawings.

[0097] However, the present disclosure is not limited by the exemplary embodiments disclosed herein, but will be embodied in many and various forms. Therefore, those exemplary embodiments are provided merely to make the present disclosure complete and to give a complete picture of the scope of the present disclosure to one of ordinary skill in the art to which the present disclosure belongs, and the present disclosure shall be defined by the scope of the claims.

[0098] Further, hereinafter, in describing the present disclosure, a detailed description of a configuration determined that may unnecessarily obscure the subject matter of the present disclosure, for example, a detailed description of a known technology including the prior art may be omitted.

[0099] Hereinafter, exemplary embodiments of the present disclosure will be described in detail.

Cyclone High-Speed Electrolyzer Using High-Speed Turbulence

[0100] The present disclosure provides a cyclone high-speed electrolyzer using high-speed turbulence for the electrolytic refining and recovery of valuable metals.

[0101] The cyclone high-speed electrolyzer using high-speed turbulence for electrolytic recovery of valuable metal according to the present disclosure may include: [0102] an anode in a shape of a rod; and [0103] a cathode including a receiving hole for accommodating the anode to form a reaction space between the anode and the cathode, [0104] wherein an area ratio of the anode to the cathode in the reaction space is Anode/Cathode=1100, [0105] wherein a diameter ratio of Do (overflow) to Du (underflow) is Do/Du=0.0011, [0106] wherein a cross section of the anode is circular, and [0107] wherein a cross section of the receiving hole is circular, and the anode is eccentrically positioned in the receiving hole.

[0108] According to an exemplary embodiment of the present disclosure, there is provided a a cyclone high-speed electrolyzer using high-speed turbulence by cyclone electrolytic refining for recovering the valuable metal, thereby achieving superior efficiency in the electrolytic refining of valuable metals using the cyclone high-speed electrolyzer with high-speed turbulence.

[0109] In general, the electrolytic recovery method or electrowinning is a process that deposits metals from an electrolyte onto the cathode using an insoluble anode through electrolysis.

[0110] Such electrolytic recovery method has the drawback of a sharp decrease in electrolytic efficiency due to an increase in activation polarization and concentration polarization caused by the growth of the diffusion layer. Consequently, many researchers are conducting studies and developments to overcome the decline in electrolytic efficiency.

[0111] Accordingly, applicants of the present disclosure have applied a cyclone high-speed electrolytic recovery method to suppress the increase in activation polarization and the increase in concentration polarization caused by the growth of the diffusion layer, which are the main issues of electrolytic recovery methods, through extensive efforts and numerous studies over a long period. In the cyclone high-speed electrolytic recovery method, a helical downward vortex is generated along the wall of the cyclone electrolyzer to accelerate the electrolyzer at high speed, forming a high-speed turbulent flow. This high-speed turbulence reduces the diffusion layer, significantly improving electrolytic efficiency and markedly increasing the recovery rate of valuable metals. The present disclosure was thus completed by obtaining the cyclone high-speed electrolyzer using the high-speed turbulence, a method for recovering valuable metals using the same, and the valuable metals recovered therefrom.

[0112] The cyclone high-speed electrolyzer using high-speed turbulence according to an exemplary embodiment of the present disclosure may include an anode in a shape of a rod; and a cathode including a receiving hole for accommodating the anode to form a reaction space between the anode and the cathode.

[0113] Furthermore, in the cyclone high-speed electrolyzer using high-speed turbulence, a helical downward vortex may be generated along a wall of the electrolyzer to accelerate the electrolyzer at high speed, thereby forming a high-speed turbulent flow, and the high-speed turbulent flow may reduce a diffusion layer to significantly improve electrolytic efficiency, thereby remarkably increasing a recovery rate of the valuable metal.

[0114] According to an exemplary embodiment of the present disclosure, an area ratio of the anode to the cathode in the reaction space may be Anode/Cathode=1100.

[0115] Here, when the area ratio of the anode to the cathode in the reaction space falls within the above range, the electrolytic efficiency of the cyclone high-speed electrolyzer using high-speed turbulence can be significantly enhanced.

[0116] Furthermore, the area ratio of the anode to the cathode in the reaction space may be preferably anode/cathode=1 to 98, and more preferably anode/cathode=1 to 95.

[0117] According to an exemplary embodiment of the present disclosure, a diameter ratio of Do (overflow) to Du (underflow) is Do/Du=0.0011.

[0118] Here, when the diameter ratio of Do (overflow) to Du (underflow) falls within the above range, a high-speed turbulent flow can be induced, significantly enhancing the electrolytic efficiency of the cyclone high-speed electrolyzer using high-speed turbulence for valuable metals.

[0119] Furthermore, the diameter ratio of Do (overflow) to Du (underflow) may be preferably Do/Du=0.003 to 1, and more preferably Do/Du=0.005 to 1.

[0120] According to an exemplary embodiment of the present disclosure, a cross section of the anode is circular.

[0121] According to an exemplary embodiment of the present disclosure, a cross section of the receiving hole may be circular, and the anode may be eccentrically positioned in the receiving hole.

[0122] According to an exemplary embodiment of the present disclosure, a turbulent flow velocity of the cyclone high-speed electrolyzer using high-speed turbulence may be 8 to 10 m/s.

[0123] Here, when the turbulent flow velocity of the cyclone high-speed electrolyzer using high-speed turbulence falls within the specified range, the electrolytic efficiency of the cyclone high-speed electrolyzer for valuable metals can be significantly enhanced.

[0124] Furthermore, the turbulent flow velocity of the cyclone high-speed electrolyzer using high-speed turbulence may be preferably 8.1 to 10 m/s, and more preferably 8.3 to 10 m/s.

[0125] In addition, a maximum distance between the anode and the cathode in the reaction space may be 2 to 100 times a minimum distance.

[0126] In other words, the maximum distance between the anode and the cathode in the reaction space may be 2 to 100 times the minimum distance between the anode and the cathode in the reaction space.

[0127] Here, when the maximum distance between the anode and the cathode in the reaction space falls within the specified range, the electrolytic efficiency of the cyclone high-speed electrolyzer using high-speed turbulence for valuable metals can be significantly enhanced.

[0128] Furthermore, the maximum distance between the anode and the cathode in the reaction space may be preferably 2 to 98 times the minimum distance, and more preferably 2 to 95 times the minimum distance.

[0129] In addition, the reaction space may be supplied with an acid leaching agent of hydrochloric acid, sulfuric acid, nitric acid, phosphoric acid, acetic acid, or organic acid.

[0130] In other words, the reaction space may be supplied with at least one acid leaching agent selected from a group consisting of hydrochloric acid, sulfuric acid, nitric acid, phosphoric acid, acetic acid, and organic acid.

[0131] According to an exemplary embodiment of the present disclosure, the cathode may be formed with a feed configured to introduce a reactant into the reaction space in a diagonal direction.

[0132] According to an exemplary embodiment of the present disclosure, the anode may be made of stainless steel, graphite, or platinum.

[0133] According to an exemplary embodiment of the present disclosure, the cathode may be made of titanium coated with iridium.

[0134] According to an exemplary embodiment of the present disclosure, the anode may include a plurality of cylindrical grooves.

[0135] In addition, the valuable metal may be gold, platinum, palladium, silver, copper, nickel, cobalt, or manganese.

[0136] In other words, the valuable metal may be at least one selected from a group consisting of gold, platinum, palladium, silver, copper, nickel, cobalt, and manganese.

[0137] According to an exemplary embodiment of the present disclosure, the valuable metal may be leached and recovered simultaneously or separately during a process of the electrolytic recovery.

[0138] According to an exemplary embodiment of the present disclosure, a recovery rate of the valuable metal may be 98 to 99.99 wt %.

[0139] Here, when the valuable metals coexist with the reactant in the electrolytic recovery process, the valuable metals can be simultaneously leached and recovered.

[0140] Moreover, the valuable metals can be individually leached and recovered, when the valuable metals coexist with the reactant in the electrolytic recovery process or when a single type of valuable metal is present.

[0141] FIG. 1 is a schematic diagram of a cyclone high-speed electrolyzer using high-speed turbulence according to an exemplary embodiment of the present disclosure.

[0142] Referring to FIG. 1, the reactant may be introduced through the feed into the reaction space, which is the internal space between the anode located at the center of the cyclone high-speed electrolyzer using high-speed turbulence and the cathode surrounding the anode.

[0143] Subsequently, by varying the diameter of the overflow (Do) at the top of the anode and the diameter of the underflow (Du) at the bottom of the cyclone high-speed electrolyzer using high-speed turbulence, strong turbulence may be formed, and a voltage may be applied to efficiently perform electrolytic refining of the reactant in the reaction space.

[0144] In addition, referring to the enlarged view of FIG. 1, the bulk valuable metal ions in the solution between the cathode and the cyclone high-speed electrolyzer using high-speed turbulence may be reduced at the cathode, allowing the valuable metals to be recovered.

A Method for Recovering Valuable Metal by Using a Cyclone High-Speed Electrolyzer Using High-Speed Turbulence

[0145] The present disclosure provides a method for recovering valuable metals using the cyclone high-speed electrolyzer using the high-speed turbulence.

[0146] The method for recovering valuable metal using the cyclone high-speed electrolyzer using high-speed turbulence according to an exemplary embodiment of the present disclosure may include: [0147] (a-1) adding a reaction solution containing valuable metal ions to the reaction space of the cyclone high-speed electrolyzer using high-speed turbulence to perform an electrolytic refining reaction; [0148] (a-2) observing current density and reduction form of the valuable metal depending on a distance between the anode and the cathode during the electrolytic refining reaction; and [0149] (a-3) recovering the valuable metal.

[0150] According to an exemplary embodiment of the present disclosure, an area ratio of the anode to the cathode in the reaction space may be Anode/Cathode=1100.

[0151] According to an exemplary embodiment of the present disclosure, a diameter ratio of Do (overflow) to Du (underflow) may be Do/Du=0.0011.

[0152] Here, when the area ratio of the anode to the cathode in the reaction space falls within the above range, the electrolytic efficiency of the cyclone high-speed electrolyzer using high-speed turbulence can be significantly enhanced.

[0153] Furthermore, the area ratio of the anode to the cathode in the reaction space may be preferably anode/cathode=1 to 98, and more preferably anode/cathode=1 to 95.

[0154] Here, when the diameter ratio of Do (overflow) to Du (underflow) falls within the above range, a high-speed turbulent flow can be induced, significantly enhancing the electrolytic efficiency of the cyclone high-speed electrolyzer using high-speed turbulence for valuable metals.

[0155] Furthermore, the diameter ratio of Do (overflow) to Du (underflow) may be preferably Do/Du=0.003 to 1, and more preferably Do/Du=0.005 to 1.

[0156] According to an exemplary embodiment of the present disclosure, the anode may be made of stainless steel, graphite, or platinum.

[0157] According to an exemplary embodiment of the present disclosure, the cathode may be made of titanium coated with iridium.

[0158] According to an exemplary embodiment of the present disclosure, the anode may include a plurality of cylindrical grooves.

[0159] According to an exemplary embodiment of the present disclosure, the step (a-1) may include steps of: [0160] obtaining a valuable metal leaching solution as a single solution or a mixed solution depending on a type of the valuable metal from a valuable metal concentrate; and [0161] supplying the valuable metal leaching solution to the cyclone high-speed electrolyzer using high-speed turbulence to perform the electrolytic refining reaction of the valuable metal.

[0162] According to an exemplary embodiment of the present disclosure, the step of obtaining the valuable metal leaching solution may include steps of: [0163] preparing a powder of the valuable metal concentrate; and [0164] extracting the powder of the valuable metal concentrate using an acid leaching agent.

[0165] In addition, the acid leaching agent may be hydrochloric acid, sulfuric acid, nitric acid, phosphoric acid, acetic acid, or organic acid, and a concentration of the acid leaching agent may be 0.2 M to 5 M.

[0166] In other words, the acid leaching agent may be at least one selected from a group consisting of hydrochloric acid, sulfuric acid, nitric acid, phosphoric acid, acetic acid, or organic acid.

[0167] According to an exemplary embodiment of the present disclosure, a concentration of the acid leaching agent may be 0.2 M to 5 M.

[0168] Here, when the concentration of the acid leaching agent falls within the above range, the valuable metal leaching solution can be obtained at a high concentration.

[0169] Furthermore, the concentration of the acid leaching agent may be preferably 0.2 M to 4.8 M, and more preferably 0.2 M to 4.5 M.

[0170] According to an exemplary embodiment of the present disclosure, in the step of extracting the powder of the valuable metal concentrate using an acid leaching agent, a condition for a process of the extracting may be characterized by: [0171] a leaching time of 0.5 to 12 hours, [0172] a pH of 0.5 to 6.5, [0173] a solid-to-liquid ratio of 1/2.5 to 1/4, and [0174] a temperature of 20 C. to 90 C.

[0175] Here, when the leaching time falls within the above range, the powder of the valuable metal concentrate can be extracted at a high concentration.

[0176] Furthermore, the leaching time may be preferably 0.5 to 11.5 hours, and more preferably 0.5 to 11 hours.

[0177] In addition, when the pH falls within the above range, the powder of the valuable metal concentrate can be extracted at a high concentration.

[0178] Furthermore, the pH may be preferably 0.5 to 6.4, and more preferably 0.5 to 6.3.

[0179] In addition, when the solid-to-liquid ratio falls within the above range, the powder of the valuable metal concentrate can be extracted at a high concentration.

[0180] Furthermore, the solid-to-liquid ratio may be preferably 1/2.5 to 1/3.9, and more preferably 1/2.5 to 1/3.8.

[0181] In addition, when the temperature falls within the above range, the powder of the valuable metal concentrate can be extracted at a high concentration.

[0182] Furthermore, the temperature may be preferably 20 C. to 88 C., and more preferably 20 C. to 85 C.

[0183] According to an exemplary embodiment of the present disclosure, in the step (a-1) of adding a reaction solution containing valuable metal ions to the reaction space of the cyclone high-speed electrolyzer using high-speed turbulence to perform an electrolytic refining reaction, [0184] an applied voltage during the electrolytic refining reaction may be 1.75 V to 25 V, [0185] a current may be 0.5 to 10 A, and [0186] a reaction time may be 1 to 720 minutes.

[0187] Here, when the applied voltage falls within the specified range, the valuable metals can be recovered with high efficiency.

[0188] Furthermore, the applied voltage may be preferably 1.75 V to 24 V, and more preferably 1.75 V to 23 V.

[0189] In addition, when the current falls within the specified range, the valuable metals can be recovered with high efficiency.

[0190] Furthermore, the current may be preferably 0.5 to 9.9 A, and more preferably 0.5 to 9.8 A.

[0191] In addition, when the reaction time falls within the above range, the valuable metals can be recovered with high efficiency.

[0192] Furthermore, the reaction time may be preferably 1 to 710 minutes, and more preferably 1 to 700 minutes.

[0193] According to an exemplary embodiment of the present disclosure, in the step (a-2) of observing current density and reduction form of the valuable metal depending on a distance between the anode and the cathode during the electrolytic refining reaction, [0194] the reduction form of the valuable metal may be powder, film, or bulk.

[0195] According to an exemplary embodiment of the present disclosure, in the step (a-3) of recovering the valuable metal, [0196] the valuable metal may be recovered simultaneously or separately, and [0197] a recovery rate of the valuable metal may be 98 to 99.99 wt %.

[0198] Here, when the valuable metals coexist with the reactant in the electrolytic recovery process, the valuable metals can be simultaneously leached and recovered.

[0199] Moreover, the valuable metals can be individually leached and recovered, when the valuable metals coexist with the reactant in the electrolytic recovery process or when a single type of valuable metal is present.

[0200] FIG. 2 is a process flow diagram of a method for recovering a valuable metal using a cyclone high-speed electrolyzer using high-speed turbulence according to an exemplary embodiment of the present disclosure.

[0201] Referring to FIG. 2, at first, an electrolytic refining reaction may be performed by adding a reaction solution containing valuable metal ions to the reaction space of the cyclone high-speed electrolyzer using high-speed turbulence (S210).

[0202] Next, the current density and the reduction form of the valuable metal may be observed depending on the distance between the anode and the cathode during the electrolytic refining reaction (S220).

[0203] Then, the valuable metal may be recovered (S230).

Valuable Metal Recovered by Using the Cyclone High-Speed Electrolyzer Using High-Speed Turbulence

[0204] The present disclosure provides a valuable metal recovered by using the cyclone high-speed electrolyzer using high-speed turbulence.

[0205] The valuable metal recovered by using the cyclone high-speed electrolyzer using high-speed turbulence according to an exemplary embodiment of the present disclosure may provide a valuable metal selected from a group consisting of gold, platinum, palladium, silver, copper, nickel, cobalt, and manganese, wherein the valuable metal may be recovered with a recovery rate of 98 to 99.99 wt % through the electrolytic refining of a reaction solution containing valuable metal ions.

[0206] According to an exemplary embodiment of the present disclosure, there is provided a valuable metal recovered by using the cyclone high-speed electrolyzer using high-speed turbulence, achieving remarkably high recovery rates and enabling their use in various applications.

Valuable Metal Recovered by the Method for Recovering Valuable Metal Using the Cyclone High-Speed Electrolyzer Using High-Speed Turbulence

[0207] The present disclosure provides a valuable metal recovered by the method for recovering valuable metal using the cyclone high-speed electrolyzer using high-speed turbulence.

[0208] The valuable metal recovered by the method for recovering valuable metal using the cyclone high-speed electrolyzer using high-speed turbulence according to an exemplary embodiment of the present disclosure may provide a valuable metal selected from a group consisting of gold, platinum, palladium, silver, copper, nickel, cobalt, and manganese, wherein the valuable metal may be recovered with a recovery rate of 98 to 99.99 wt % through the electrolytic refining of a reaction solution containing valuable metal ions.

[0209] According to an exemplary embodiment of the present disclosure, there is provided a valuable metal recovered by the method for recovering valuable metals using a cyclone high-speed electrolyzer with high-speed turbulence, achieving significantly high recovery rates and enabling their use in various applications.

[0210] Hereinafter, the present disclosure will be described in more detail through exemplary embodiments. However, the following exemplary embodiments are provided to further illustrate the present disclosure, and the scope of the present disclosure is not limited to these exemplary embodiments. The following exemplary embodiments may be appropriately modified or altered by those skilled in the art within the scope of the present disclosure.

EXEMPLARY EMBODIMENTS

<Exemplary Embodiment 1 to Exemplary Embodiment 3> High-Speed Turbulence Cyclone Electrolytic Refining Using a Hydrochloric Acid Leaching Agent

[0211] A valuable metal leaching solution with an initial concentration of valuable metal ions of 50 to 100 ppm, obtained using a hydrochloric acid leaching agent, was introduced into the reaction space of the cyclone high-speed electrolyzer with high-speed turbulence meeting the specifications in Table 1, and electrolytic refining was performed under the conditions listed in Table 1.

<Exemplary Embodiment 4 to Exemplary Embodiment 6> High-Speed Turbulence Cyclone Electrolytic Refining Using a Sulfuric Acid Leaching Agent

[0212] A valuable metal leaching solution with an initial concentration of valuable metal ions of 50 to 100 ppm, obtained using a sulfuric acid leaching agent, was introduced into the reaction space of a cyclone high-speed electrolyzer with high-speed turbulence meeting the specifications in Table 1, and electrolytic refining was performed under the conditions listed in Table 1.

TABLE-US-00001 TABLE 1 Exemplary Exemplary Exemplary Exemplary Exemplary Exemplary embodiment 1 embodiment 2 embodiment 3 embodiment 4 embodiment 5 embodiment 6 Anode/cathode 1 1.02 1.5 1 1.02 1.5 area ratio Do/Du 0.5 0.7 1.0 0.5 0.7 1.0 diameter ratio Anode material stainless graphite platinum stainless graphite platinum steel steel Cathode titanium titanium titanium titanium titanium titanium material Acid leaching hydrochloric hydrochloric hydrochloric sulfuric sulfuric sulfuric agent acid acid acid acid acid acid Acid leaching 0.2 2 5 0.2 2 5 agent concentration (M) Leaching time 12 8 0.5 12 8 0.5 (hr) pH 6.5 2 0.5 6 1 0.3 Solid-to-liquid 1/2.5 1/3 1/4 1/2.5 1/3 1/4 ratio Temperature 90 40 20 20 90 40 ( C.) Applied voltage 1.75 7.5 25 25 10 1.75 (V) Current (A) 0.5 3.9 10 5 10 0.5 Reaction time 10 480 720 1 480 240 (min) Valuable metal 98 >99.84 99.99 99 99.5 99.9 recovery rate (wt %)

[0213] Referring to Table 1, the recovery rates of valuable metals in Exemplary embodiment 1 to Exemplary embodiment 3 were 98 to 99.99 wt %, and the recovery rates of valuable metals in Exemplary embodiment 4 to Exemplary embodiment 6 were 99 to 99.9 wt %.

EXPERIMENTAL EMBODIMENT

<Experimental Embodiment 1> Measurement of Reduction Polarization Curves for Au/Pt/Pd

[0214] The reduction polarization curves for Au/Pt/Pd were measured under the following conditions: 100 ppm concentration, 2% HCl, working electrode (WE): carbon, counter electrode (CE): Pt mesh, reference electrode (RE): AgCl/KCl new electrode, and without agitation.

[0215] For Au, measurements were conducted at 0.5 V/s from 1.0 to 0.5 vs. Ref.

[0216] For Pt, measurements were conducted at 1.0 V/s from 1.0 to 1.0 vs. Ref.

[0217] For Pd, measurements were conducted at 1.0 V/s from 0 to 1.5 vs. Ref.

[0218] FIG. 3 is a graph showing the measured reduction polarization curves of (a) Au, (b) Pt, and (c) Pd according to an exemplary embodiment of the present disclosure.

[0219] Referring to FIG. 3a, the reduction potential of gold was approximately 0.5 V.

[0220] Referring to FIG. 3b, the reduction potential of platinum was approximately 0.05 V.

[0221] Referring to FIG. 3c, the reduction potential of palladium was approximately 0.4 V.

<Experimental Embodiment 2> Cyclone High-Speed Electrolysis Behavior and Related Photographs of Au/Pt/Pd/Cu/Ni

[0222] The high-speed turbulence cyclone electrolytic refining behavior of Au, Pt, Pd, Cu, and Ni, respectively, using the hydrochloric acid leaching agent from Exemplary embodiment 2 is sequentially shown in Tables 2 to 6, and the recovery rates of the valuable metals after cyclone high-speed electrolysis are shown in FIG. 4.

[0223] In addition, FIG. 5a to FIG. 5d shows photographs of Pt, Pd, Cu, and Ni after electrolytic refining.

[0224] FIG. 4 is a graph showing the recovery rates of Au, Pt, Pd, Cu, and Ni after cyclone high-speed electrolysis according to Exemplary embodiment 2 of the present disclosure as specified above.

TABLE-US-00002 TABLE 2 Residual Time concentration Voltage Recovery (min.) of Au (V) rate (%) 0 98.9 8.0 0.00 30 81.8 8.0 17.29 60 68.7 8.0 30.54 120 44.1 8.0 55.41 240 21.1 8.0 78.67 480 0.24 8.0 99.76

[0225] Referring to Table 2 and FIG. 4, the recovery rate of gold after 480 minutes of high-speed turbulence cyclone electrolytic refining was 99.76 wt %.

TABLE-US-00003 TABLE 3 Residual Time concentration Voltage Recovery (min.) of Pt (V) rate (%) 0 57.5 7.0 0 30 45.3 7.3 21.22 60 19.5 7.0 66.09 120 1.0 7.3 98.26 240 <0.1 7.5 >99.83 480 <0.1 7.9 >99.83

[0226] Referring to Table 3 and FIG. 4, the recovery rate of platinum after 480 minutes of high-speed turbulence cyclone electrolytic refining was at least 99.83 wt %.

TABLE-US-00004 TABLE 4 Residual Time concentration Voltage Recovery (min.) of Pd (V) rate (%) 0 64.1 7.3 0 30 29.9 7.0 53.35 60 5.8 7.0 90.95 120 0.17 7.2 99.73 240 0.13 7.4 99.80 480 <0.1 7.5 >99.84

[0227] Referring to Table 4 and FIG. 4, the recovery rate of palladium after 480 minutes of high-speed turbulence cyclone electrolytic refining was at least 99.84 wt %.

TABLE-US-00005 TABLE 5 Residual Time concentration Voltage Recovery (min.) of Cu (V) rate (%) 0 117 8.6 0 30 85.1 8.8 27.26 60 56.5 8.6 51.71 120 30.2 7.4 74.19 240 5.5 8.7 95.30 480 1.3 10.6 98.89

[0228] Referring to Table 5 and FIG. 4, the recovery rate of copper after 480 minutes of high-speed turbulence cyclone electrolytic refining was 98.89 wt %.

TABLE-US-00006 TABLE 6 Residual Time concentration Voltage Recovery (min.) of Ni (V) rate (%) 0 148 16.7 0 30 145 16.2 2.03 60 145 16.1 2.03 120 142 17.0 4.05 240 94.6 18.6 36.08 480 39.5 21.5 73.31

[0229] Referring to Table 6 and FIG. 4, the recovery rate of nickel after 480 minutes of high-speed turbulence cyclone electrolytic refining was 73.31 wt %.

[0230] FIG. 5a shows photograph of Pt after cyclone high-speed electrolysis according to Exemplary embodiment 2 of the present disclosure as specified above.

[0231] FIG. 5b shows photograph of Pd after cyclone high-speed electrolysis according to Exemplary embodiment 2 of the present disclosure as specified above.

[0232] FIG. 5c shows photograph of Cu after cyclone high-speed electrolysis according to Exemplary embodiment 2 of the present disclosure as specified above.

[0233] FIG. 5d shows photograph of Ni after cyclone high-speed electrolysis according to Exemplary embodiment 2 of the present disclosure as specified above.

[0234] Referring to FIGS. 5a to 5d, all of Pt, Pd, Cu, and Ni remained in a powder form after cyclone high-speed electrolysis.

<Experimental Embodiment 3> Measurement of Electrolytic Recovery Efficiency Based on the Diameter Ratio of do (Overflow) to Du (Underflow) (do/Du)

[0235] In the high-speed turbulence cyclone electrolytic refining behavior of Au using the hydrochloric acid leaching agent from Exemplary embodiment 2, FIG. 6a and FIG. 6b show the electrolytic recovery efficiency based on the diameter ratio of Do (overflow) to Du (underflow) (Do/Du) during the continuous input of waste solution containing precious metals into the cyclone high-speed electrolyzer with high-speed turbulence.

[0236] FIG. 6a is a graph showing the electrolytic recovery efficiency based on precious metal concentration according to Exemplary embodiment 2 of the present disclosure as specified above.

[0237] FIG. 6b is a graph showing the electrolytic recovery efficiency based on precious metal recovery rate relative to the diameter ratio of Do (overflow) to Du (underflow) (Do/Du) according to Exemplary embodiment 2 of the present disclosure as specified above.

[0238] Referring to FIG. 6a, when the diameter ratio of Do (overflow) to Du (underflow) (Do/Du) was 1 or less, the concentration of gold was recovered at a higher level compared to when Do/Du exceeded 1.

[0239] In addition, referring to FIG. 6b, when the diameter ratio of Do (overflow) to Du (underflow) (Do/Du) was 1 or less, the recovery rate of gold increased by 10 wt % or more compared to when Do/Du was greater than 1.

<Experimental Embodiment 4> Measurement of Electrolytic Recovery Efficiency Based on the Diameter Ratio of do (Overflow) to Du (Underflow) (do/Du)

[0240] FIG. 7a and FIG. 7b illustrate the electrolytic recovery efficiency based on the anode/cathode area ratio of the cyclone high-speed electrolyzer with high-speed turbulence during the continuous input of waste solution containing precious metals in the high-speed turbulence cyclone electrolytic refining behavior of Au using the hydrochloric acid leaching agent from Exemplary embodiment 2.

[0241] FIG. 7a is a graph showing the electrolytic recovery efficiency based on precious metal concentration according to Exemplary embodiment 2 of the present disclosure as specified above.

[0242] FIG. 7b is a graph showing the electrolytic recovery efficiency based on precious metal recovery rate relative to the area ratio of the anode to the cathode (anode/cathode area ratio) according to Exemplary embodiment 2 of the present disclosure as specified above.

[0243] Referring to FIG. 7a, when the anode/cathode area ratio was 1 or more, the concentration of gold was recovered at a higher level compared to when the anode/cathode area ratio was less than 1.

[0244] Additionally, referring to FIG. 7b, when the anode/cathode area ratio was 1 or more, the recovery rate of gold increased by 15 wt % or more compared to when the anode/cathode area ratio was less than 1.

<Experimental Embodiment 5> Measurement of Electrolytic Recovery Efficiency Based on Anode Material

[0245] In the high-speed turbulence cyclone electrolytic refining behavior of Au using the hydrochloric acid leaching agent from Exemplary embodiment 2, FIG. 8a and FIG. 8b illustrate the electrolytic recovery efficiency based on the anode material of the cyclone high-speed electrolyzer with high-speed turbulence during the continuous input of waste solution containing precious metals.

[0246] FIG. 8a is a graph showing the electrolytic recovery efficiency based on precious metal concentration according to Exemplary embodiment 2 of the present disclosure as specified above.

[0247] FIG. 8b is a graph showing the electrolytic recovery efficiency based on precious metal recovery rate relative to the anode material according to Exemplary embodiment 2 of the present disclosure as specified above.

[0248] Referring to FIG. 8a, the concentration of gold showed no significant variation based on the anode material, and the concentration of gold was recovered at a high level regardless of the anode material used.

[0249] In addition, referring to FIG. 8b, the recovery rate of gold showed no significant variation based on the anode material, and the recovery rate of gold increased by up to nearly 100 wt % regardless of the anode material used.

<Experimental Embodiment 6> Photograph of Solutions Showing the Simultaneous Leaching And Recovery of Au, Pt, and Pd Precious Metals in a Mixed Leaching Solution

[0250] FIG. 9 shows a photograph of solutions illustrating the simultaneous leaching and recovery of Au, Pt, and Pd precious metals in a mixed leaching solution during the high-speed turbulence cyclone electrolytic refining behavior using the hydrochloric acid leaching agent from Exemplary embodiment 2.

[0251] FIG. 9 is a photograph of a solution showing the simultaneous leaching and recovery of Au, Pt, and Pd precious metals according to Exemplary embodiment 2 of the present disclosure as specified above.

[0252] Referring to FIG. 9, during the high-speed turbulence cyclone electrolytic refining behavior of the mixed leaching solution using the hydrochloric acid leaching agent, the Au, Pt, and Pd precious metals transformed into a transparent solution after 1 hour, and the Au, Pt, and Pd precious metals were reduced and recovered.

<Experimental Embodiment 7> Measurement of Electrolytic Recovery Efficiency Showing the Simultaneous Leaching and Recovery of Au, Pt, and Pd Precious Metals During the High-Speed Turbulence Cyclone Electrolytic Refining Behavior of the Mixed Leaching Solution

[0253] FIG. 10a and FIG. 10b show the electrolytic recovery efficiency demonstrating the simultaneous leaching and recovery of Au, Pt, and Pd precious metals during the high-speed turbulence cyclone electrolytic refining behavior of the mixed leaching solution using the hydrochloric acid leaching agent from Exemplary embodiment 2.

[0254] FIG. 10a is a graph showing the electrolytic efficiency after simultaneous cyclone electrolytic recovery of the leaching solution following chlorine leaching, based on precious metal concentration according to Exemplary embodiment 2 of the present disclosure as specified above.

[0255] FIG. 10b is a graph showing the electrolytic efficiency after simultaneous cyclone electrolytic recovery of the leaching solution following chlorine leaching, based on precious metal recovery rate according to Exemplary embodiment 2 of the present disclosure as specified above.

[0256] Referring to FIG. 10a, during the high-speed turbulence cyclone electrolytic refining behavior of the mixed leaching solution using the hydrochloric acid leaching agent, Au, Pt, and Pd precious metals were simultaneously recovered at high concentrations after approximately 2 hours of electrolytic refining.

[0257] In addition, referring to FIG. 10b, during the high-speed turbulence cyclone electrolytic refining behavior of the mixed leaching solution using the hydrochloric acid leaching agent, Au, Pt, and Pd precious metals were simultaneously recovered with high efficiency of over 99 wt % after approximately 2 hours of electrolytic refining.

<Experimental Embodiment 8> Measurement of Electrolytic Recovery Efficiency of Au, Pt. and Pd Precious Metals During the High-Speed Turbulence Cyclone Electrolytic Refining Behavior in Single and Mixed Solutions

[0258] FIG. 11a and FIG. 11b illustrate the electrolytic recovery efficiency of Au, Pt, and Pd precious metals during the high-speed turbulence cyclone electrolytic refining behavior of single and mixed solutions with an initial concentration of 50 to 100 ppm, using the hydrochloric acid leaching agent from Exemplary embodiment 2.

[0259] FIG. 11a is a graph showing the electrolytic efficiency after cyclone electrolytic recovery of the leaching solution following chlorine leaching, based on the metal recovery rate from a single solution according to Exemplary embodiment 2 of the present disclosure as specified above.

[0260] FIG. 11b is a graph showing the electrolytic efficiency after cyclone electrolytic recovery of the leaching solution following chlorine leaching, based on the metal recovery rate from a mixed solution according to Exemplary embodiment 2 of the present disclosure as specified above.

[0261] Referring to FIGS. 11a and 11b, in both of single and mixed solutions, Au, Pt, and Pd precious metals were recovered with high efficiency of over 99 wt % after 3 hours.

<Experimental Embodiment 9> Measurement of Electrolytic Recovery Efficiency by Concentration for Au Precious Metal During High-Speed Turbulence Cyclone Electrolytic Refining Behavior

[0262] FIG. 12a and FIG. 12b show the electrolytic recovery efficiency by concentration for Au precious metal during the high-speed turbulence cyclone electrolytic refining behavior using the hydrochloric acid leaching agent from Exemplary embodiment 2.

[0263] FIG. 12a is a graph showing the electrolytic efficiency by concentration after cyclone electrolytic recovery of the leaching solution following chlorine leaching, based on the concentration of gold (Au) according to Exemplary embodiment 2 of the present disclosure as specified above.

[0264] FIG. 12b is a graph showing the electrolytic efficiency by concentration after cyclone electrolytic recovery of the leaching solution following chlorine leaching, based on the recovery rate of gold (Au) according to Exemplary embodiment 2 of the present disclosure as specified above.

[0265] Referring to FIG. 12a, at low concentrations, residual ions were present near 0 ppm within a reaction time of 1 hour, while at high concentrations, residual ions were present near 0 ppm within a reaction time of 4 hours.

[0266] In addition, referring to FIG. 12b, at low concentrations, approximately 100 wt % of the Au was electrolytically recovered within 1 hour of reaction time, while at high concentrations, approximately 100 wt % of the Au was electrolytically recovered within 4 hours of reaction time.

<Experimental Embodiment 10> Measurement of Electrolytic Recovery Efficiency by Concentration for Pt Precious Metal During High-Speed Turbulence Cyclone Electrolytic Refining Behavior

[0267] FIG. 13a and FIG. 13b illustrate the electrolytic recovery efficiency by concentration for Pt precious metal during the high-speed turbulence cyclone electrolytic refining behavior using the hydrochloric acid leaching agent from Exemplary embodiment 2.

[0268] FIG. 13a is a graph showing the electrolytic efficiency by concentration after cyclone electrolytic recovery of the leaching solution following chlorine leaching, based on the concentration of platinum (Pt) according to Exemplary embodiment 2 of the present disclosure as specified above.

[0269] FIG. 13b is a graph showing the electrolytic efficiency by concentration after cyclone electrolytic recovery of the leaching solution following chlorine leaching, based on the recovery rate of platinum (Pt) according to Exemplary embodiment 2 of the present disclosure as specified above.

[0270] Referring to FIG. 13a, at low concentrations, residual ions were present near 0 ppm within 1 hour of reaction time, while at high concentrations, residual ions were present near 0 ppm within 2 hours of reaction time.

[0271] In addition, referring to FIG. 13b, at low concentrations, approximately 100 wt % of the Pt was electrolytically recovered within 1 hour of reaction time, while at high concentrations, approximately 100 wt % of the Pt was electrolytically recovered within 2 hours of reaction time.

<Experimental Embodiment 11> Measurement of Electrolytic Recovery Efficiency by Concentration for Pd Precious Metal During High-Speed Turbulence Cyclone Electrolytic Refining Behavior

[0272] FIG. 14a and FIG. 14b illustrate the electrolytic recovery efficiency by concentration for Pd precious metal during the high-speed turbulence cyclone electrolytic refining behavior using the hydrochloric acid leaching agent from Exemplary embodiment 2.

[0273] FIG. 14a is a graph showing the electrolytic efficiency by concentration after cyclone electrolytic recovery of the leaching solution following chlorine leaching, based on the concentration of palladium (Pd) according to Exemplary embodiment 2 of the present disclosure as specified above.

[0274] FIG. 14b is a graph showing the electrolytic efficiency by concentration after cyclone electrolytic recovery of the leaching solution following chlorine leaching, based on the recovery rate of palladium (Pd) according to Exemplary embodiment 2 of the present disclosure as specified above.

[0275] Referring to FIG. 14a, at low concentrations, residual ions were present near 0 ppm within 1 hour of reaction time, while at high concentrations, residual ions were present near 0 ppm within 2 hours of reaction time.

[0276] In addition, referring to FIG. 14b, at low concentrations, approximately 100 wt % of the Pd was electrolytically recovered within 1 hour of reaction time, while at high concentrations, approximately 100 wt % of the Pd was electrolytically recovered within 2 hours of reaction time.

<Experimental Embodiment 12> Measurement of Electrolytic Recovery Efficiency by Concentration for Au Precious Metal During High-Speed Turbulence Cyclone Electrolytic Refining Behavior

[0277] FIG. 15a and FIG. 15b illustrate the electrolytic recovery efficiency by concentration for Au precious metal during the high-speed turbulence cyclone electrolytic refining behavior using the hydrochloric acid leaching agent from Exemplary embodiment 2.

[0278] FIG. 15a is a graph showing the electrolytic efficiency after cyclone electrolytic recovery of the leaching solution following chlorine leaching, based on changes in the applied voltage, with the concentration of gold (Au) according to Exemplary embodiment 2 of the present disclosure as specified above.

[0279] FIG. 15b is a graph showing the electrolytic efficiency after cyclone electrolytic recovery of the leaching solution following chlorine leaching, based on changes in the applied voltage, with the recovery rate of gold (Au) according to Exemplary embodiment 2 of the present disclosure as specified above.

[0280] Referring to FIG. 15a, at both of high and low voltages, residual ions were present near 0 ppm within 1 hour of reaction time.

[0281] In addition, referring to FIG. 15b, at both of high and low voltages, approximately 100 wt % of the Pd was electrolytically recovered within 1 hour of reaction time.

<Experimental Embodiment 13> Measurement of Electrolytic Recovery Efficiency by Applied Voltage for Pt Precious Metal During High-Speed Turbulence Cyclone Electrolytic Refining Behavior

[0282] FIG. 16a and FIG. 16b illustrate the electrolytic recovery efficiency by applied voltage for Pt precious metal during the high-speed turbulence cyclone electrolytic refining behavior using the hydrochloric acid leaching agent from Exemplary embodiment 2.

[0283] FIG. 16a is a graph showing the electrolytic efficiency after cyclone electrolytic recovery of the leaching solution following chlorine leaching, based on changes in the applied voltage, with the concentration of platinum (Pt) according to Exemplary embodiment 2 of the present disclosure as specified above.

[0284] FIG. 16b is a graph showing the electrolytic efficiency after cyclone electrolytic recovery of the leaching solution following chlorine leaching, based on changes in the applied voltage, with the recovery rate of platinum (Pt) according to Exemplary embodiment 2 of the present disclosure as specified above.

[0285] Referring to FIG. 16a, at the applied voltage, residual ions were present near 0 ppm within 1 hour of reaction time.

[0286] In addition, referring to FIG. 16b, at the applied voltage, approximately 100 wt % of Pt was electrolytically recovered within 1 hour of reaction time.

<Experimental Embodiment 14> Measurement of Electrolytic Recovery Efficiency by Applied Voltage for Pd Precious Metal During High-Speed Turbulence Cyclone Electrolytic Refining Behavior

[0287] FIG. 17a and FIG. 17b illustrate the electrolytic recovery efficiency by applied voltage for Pd precious metal during the high-speed turbulence cyclone electrolytic refining behavior using the hydrochloric acid leaching agent from Exemplary embodiment 2.

[0288] FIG. 17a is a graph showing the electrolytic efficiency after cyclone electrolytic recovery of the leaching solution following chlorine leaching, based on changes in the applied voltage, with the concentration of palladium (Pd) according to Exemplary embodiment 2 of the present disclosure as specified above.

[0289] FIG. 17b is a graph showing the electrolytic efficiency after cyclone electrolytic recovery of the leaching solution following chlorine leaching, based on changes in the applied voltage, with the recovery rate of palladium (Pd) according to Exemplary embodiment 2 of the present disclosure as specified above.

[0290] Referring to FIG. 17a, at the applied voltage, residual ions were present near 0 ppm within 0.5 hour of reaction time.

[0291] In addition, referring to FIG. 17b, at the applied voltage, approximately 100 wt % of Pd was electrolytically recovered within 0.5 hour of reaction time.

[0292] In the above, exemplary embodiments of a cyclone high-speed electrolyzer using high-speed turbulence, a method for recovering valuable metals using the same, and the valuable metals recovered therefrom according to the present disclosure have been described. Moreover, it will be appreciated that various modifications to these exemplary embodiments are possible without departing from the scope of the present disclosure.

[0293] The scope of the present disclosure should therefore not be limited to those exemplary embodiments described above, but should be defined by the following claims and their equivalents.

[0294] In other words, the foregoing exemplary embodiments are to be understood as illustrative rather than restrictive in all respects, and the scope of the present disclosure is indicated by the following claims rather than the detailed description. All modifications or variations derived from the meaning, scope, and equivalent concepts of the claims should be interpreted as being included within the scope of the present disclosure.