Sf6 decomposition system and operating method thereof

Abstract

The sulfur hexafluoride detoxification treatment system according to the present invention comprises: a combustion decomposition unit that combusts sulfur hexafluoride and combustion gas together to generate decomposition gas; a cooling unit that cools and neutralizes the decomposition gas to convert it into exhaust gas and discharges it to the outside; and a circulation unit having a circulating water tank into which an acidic substance among the decomposition gas is introduced, and into which a neutralizing agent is injected together with neutralizing water to generate a neutralizing flame through a neutralization reaction; wherein the neutralizing water in the circulating water tank is discharged and the neutralizing flame is discharged to the bottom of the circulating water tank while continuously circulating through the cooling unit, and the neutralizing water is purified and cooled to supply circulating water to the cooling unit.

Description

Technology Field

[0001] The present invention relates to a sulfur hexafluoride detoxification treatment system, a method of operating the same, and a method of operating the same. More specifically, it relates to a sulfur hexafluoride treatment system that detoxifies and treats sulfur hexafluoride decomposition products, and a method of operating the same. Background Technology

[0003] Sulfur hexafluoride (SF6) is a substance widely used in the electrical and electronic industries, such as semiconductor production and power equipment. It is colorless, odorless, and non-toxic, and possesses flame-retardant properties that prevent it from decomposing easily even at temperatures above 500°C. In particular, due to its inertness, high chemical and thermal stability, and excellent insulation properties, it has been used as an insulator in power distribution and transmission facilities in Korea for over 50 years. Notably, Korea Electric Power Corporation (KEPCO) consumes more than 80% of the domestic SF6 usage.

[0004] However, SF6 is a substance that makes up less than 1% of the Earth's atmosphere; once emitted, it persists for 3,200 years and is a representative greenhouse gas with a global warming potential 23,900 times higher than that of CO2. With the introduction of eco-friendly switchgear, SF6 is generated from discarded GIS, and it is estimated that an average of 66 tons of waste SF6 gas will be generated annually in the future. Ultimately, it is necessary to reduce greenhouse gases by decomposing and processing the SF6 that needs to be disposed of, thereby releasing it into the atmosphere in a harmless form.

[0005] Conventionally, there is a decomposition technology for small amounts of low-concentration SF6 that is used and discarded in semiconductor production etching processes, but a decomposition technology for high-concentration SF6 with a purity of 70% or higher and in large quantities, such as insulators, has not been commercialized, and there is a problem that conventional technology is difficult to apply to high-concentration, large-quantity decomposition.

[0006] Therefore, there is an urgent need to develop a method to more efficiently recover salt generated during the large-scale, high-concentration SF6 decomposition process and to minimize wastewater generation, thereby reducing the operating costs of the SF6 decomposition and detoxification system.

[0007] As background technology to the present invention, Korean Published Patent Application No. 10-2008-0065851 discloses a method for treating sulfur hexafluoride by extracting it with a salt of calcium sulfate or calcium fluoride, but it does not disclose a method for efficiently recovering the salt and reducing the amount of wastewater generated. The problem to be solved

[0009] The objective of the present invention is to provide a system for decomposing and neutralizing large volumes of high-concentration sulfur hexafluoride.

[0010] The present invention provides a sulfur hexafluoride detoxification treatment system that safely and efficiently decomposes and detoxifies salts generated during the decomposition and neutralization processes of sulfur hexafluoride during system operation, and significantly reduces operating costs by minimizing the amount of wastewater generated.

[0011] Another objective of the present invention relates to a method of operating a sulfur hexafluoride detoxification treatment system, and is to provide a method of operating a sulfur hexafluoride detoxification treatment system that can continuously remove salts by continuously operating the sulfur hexafluoride detoxification treatment system and significantly reduce the amount of wastewater generated.

[0012] The above and other objectives of the present invention can all be achieved by the present invention described below. means of solving the problem

[0014] 1. One aspect of the present invention relates to a sulfur hexafluoride detoxification treatment system.

[0015] The sulfur hexafluoride detoxification treatment system includes a combustion decomposition unit that burns sulfur hexafluoride and combustion gas together to generate decomposition gas;

[0016] A cooling unit that cools and neutralizes the above decomposition gas to generate exhaust gas and discharges it to the outside; and

[0017] A circulation unit comprising a circulation tank into which an acidic substance among the above decomposition gases is introduced, and a neutralizing agent is injected together with neutralizing water to generate a neutralizing flame through a neutralization reaction;

[0018] The neutralized water in the above-mentioned circulation tank is discharged and continuously circulates through the above-mentioned cooling unit, while the neutralized flame is discharged to the bottom of the circulation tank, and the neutralized water is purified and cooled to supply circulating water to the above-mentioned cooling unit.

[0019] 2. In the above 1 embodiment, a purification unit may be further included to purify the exhaust gas by being disposed downstream of the cooling unit.

[0020] 3. In the above 1 or 2 embodiments, the purification unit may be equipped with a scrubber or an electrostatic precipitator.

[0021] 4. In any one of the embodiments 1 to 3 above, a heat exchanger may be included that is disposed on one side of the circulation unit and introduces neutralized water into the circulation tank and circulates it to the circulation tank after heat exchange.

[0022] 5. In any one of the embodiments 1 to 4 above, the circulating water tank is provided with a slope at the bottom and can collect and discharge the neutralizing flame to one side by gravity.

[0023] 6. In any one of the embodiments 1 to 5 above, the neutralized water can be discharged from the circulation unit and the suspended solids removed and recovered back into the circulation unit.

[0024] 7. In any one of the embodiments 1 to 6 above, the water level of the circulating water tank can be automatically adjusted according to the electrical conductivity and pH of the neutralized water in the circulating water tank.

[0025] 8. Another aspect of the present invention relates to a sulfur hexafluoride detoxification treatment system that generates and continuously circulates circulating water.

[0026] The above sulfur hexafluoride detoxification treatment system includes a pyrolysis reactor into which sulfur hexafluoride and combustion gas are introduced to burn the sulfur hexafluoride and generate decomposition gas;

[0027] A rapid cooling device provided downstream of the above pyrolysis reactor to rapidly cool the decomposition gas and acidic substance;

[0028] A first circulation tank provided in the downstream of the above-mentioned rapid chiller, into which the decomposition gas is introduced, and a neutralizing agent and water are introduced together, in which an acidic substance in the decomposition gas reacts with the neutralizing agent to form a neutralizing salt and neutralized water, and when the neutralizing salt precipitates, it is continuously discharged;

[0029] A scrubber that receives exhaust gas from the first circulation tank, washes it to settle particulate matter, and cools the exhaust gas;

[0030] An electrostatic precipitator comprising a dust collection tower that receives exhaust gas from the scrubber, collects and treats particulate matter, purifies the exhaust gas, and discharges it to the outside, and a second circulation tank at the bottom of the dust collection tower in which circulating water is collected;

[0031] A hydrocyclone that forms circulating water by introducing neutralized water from the first circulating water tank and removing neutralizing salts within the neutralized water;

[0032] A heat exchanger that cools the circulating water from which neutralizing salt has been removed in the above hydrocyclone through heat exchange;

[0033] A cooler connected to the above heat exchanger to cool the circulating water; and

[0034] It includes a filter tank that introduces neutralized water discharged from the first circulation tank to one side, removes neutralized salts within the neutralized water, and circulates it back to the first circulation tank.

[0035] 9. In the above 8 embodiments, the pyrolysis reactor and the quencher may be provided as an integrated unit.

[0036] 10. In the above 8 or 9 embodiments, the first circulating water tank is,

[0037] An upper surface to which the above-mentioned quencher is connected, a pipe into which water and a neutralizing agent are introduced is connected, and the above-mentioned scrubber is connected;

[0038] A side case that receives a neutralizing agent and water, and when the acidic substance is introduced, captures the neutralizing salt and neutralized water generated by the neutralization reaction inside;

[0039] A lower surface formed with a slope to allow the neutralizing flame to gather along the slope to one side by gravity and a salt discharge port formed to continuously discharge the neutralizing flame; and

[0040] It may include a baffle extending from the lower surface to restrict the movement of the neutralizing flame and allowing the upper neutralizing water with low electrical conductivity among the neutralizing waters to overflow and move to the opposite space.

[0041] 11. In any one of the embodiments 8 to 10 above, the salt discharge port is connected to a salt discharge pipe, and a plurality of nitrogen purging ports may be provided in the salt discharge port.

[0042] 12. In the above 11 embodiment, the nitrogen supply tank and the salt discharge pipe connected to the salt discharge port may be equipped with a purging valve to control the amount of nitrogen being purged.

[0043] 13. In the above 10 embodiments, the slope angle of the slope can be determined according to the following Equation 1.

[0044] [Equation 1]

[0045] 10° ≤ 90 - α ≤ 30°

[0046] In Equation 1 above, α is the angle between the slope and the side case.

[0047] 14. In any one of the embodiments of 8 to 13 above, the first circulating water tank may be equipped with a level gauge and a conductivity meter for measuring electrical conductivity, and may be equipped with a pH meter for measuring the pH of the neutralized water generated in the first circulating water tank.

[0048] 15. In any one of the embodiments of 8 to 14 above, the second circulating water tank may be equipped with a pH meter for measuring the pH of the circulating water collected in the second circulating water tank.

[0049] 16. In the above 14 embodiments, a controller may be provided that is electrically connected to the level gauge, conductivity meter, and pH meter and controls the water level in the first circulating water tank according to the electrical conductivity and pH of the neutralized water.

[0050] 17. Another aspect of the present invention relates to a method for detoxifying sulfur hexafluoride decomposition products.

[0051] The above method for detoxifying sulfur hexafluoride decomposition products involves burning sulfur hexafluoride together with combustion gas to generate decomposition gas, removing particulate matter from the decomposition gas and discharging it to the outside, and for acidic substances, introducing a neutralizing agent and water together into a tank to generate a neutralizing flame through a neutralization reaction, and then continuously discharging the neutralizing flame to one side. The pH and electrical conductivity of the generated neutralized water are measured, and the amount of neutralizing agent and the water level of the tank are controlled via feedback so that the neutralized water is continuously circulated.

[0052] 18. Another aspect of the present invention relates to a method for operating a sulfur hexafluoride detoxification treatment system.

[0053] The above method for operating a sulfur hexafluoride detoxification treatment system comprises: (a) a step of introducing sulfur hexafluoride and combustion gas into a pyrolysis reactor and combusting them to generate decomposition gas;

[0054] (b) a step of cleaning the decomposition gas and collecting particulate matter with an electrostatic precipitator to generate purified exhaust gas and discharging it to the outside;

[0055] (c) a step of introducing an acidic substance among the decomposition gases into the first circulation tank, introducing a neutralizing agent and water to generate a neutralizing salt and neutralized water through a neutralization reaction, and collecting along the slope of the lower part of the first circulation tank and continuously discharging through a salt discharge port; and

[0056] (d) a step of recovering the neutralized water, removing residual neutralizing salt from the neutralized water, generating circulating water and delivering it to the electrostatic precipitator, and, when the circulating water is collected in the second circulating water tank at the bottom of the electrostatic precipitator, circulating it back to the first circulating water tank;

[0057] 19. In the above 18 embodiments, the step of adding water to the first circulating water tank in (c) and the step of adding a neutralizing agent to maintain the pH of the neutralized water can be performed in an interlocking manner.

[0058] 20. In the above 18 or 19 embodiments, the step of adding a neutralizing agent to the second circulating water tank in (c) may be further included.

[0059] 21. In any one of the embodiments of 18 to 20 above, the method may include the step of measuring the pH around the salt discharge port of the first circulating water tank in (c), and discharging neutralized salt and neutralized water when the pH is below the target pH.

[0060] 22. In any one of the embodiments of 18 to 21 above, the pH of the circulating water of the second circulating water tank in (d) is measured, and the neutralizing agent may be added as a feedback control to maintain the target pH.

[0061] 23. In any one of the embodiments 18 to 22 above, the water level of the neutralized water can be controlled to 50 to 80% of the volume of the first circulating water tank in (c).

[0062] 24. In any one of the embodiments of 18 to 23 above, the step of removing neutralized salt by purging nitrogen into the salt outlet in (c) above may be included. Effects of the invention

[0064] The sulfur hexafluoride detoxification treatment system according to the present invention can safely separate salts generated during the neutralization process in a high-capacity, high-concentration sulfur hexafluoride (SF6) decomposition treatment process while in operation, and reduce operating costs by minimizing wastewater generation. It is highly environmentally friendly because it prevents process interruption caused by the accumulation of salts generated during the detoxification process in the lower part of the circulating water tank and the pump operating part, thereby not only continuously removing the generated salts but also minimizing wastewater generation by recycling the neutralized water as circulating water. Furthermore, it has the advantage of effectively separating and recovering the generated salts, enabling their utilization as high-value chemical raw materials. Brief explanation of the drawing

[0066] FIG. 1 is a process diagram of a large-capacity high-concentration SF6 decomposition treatment system according to one embodiment of the present invention. FIG. 2 is a process flow diagram of a sulfur hexafluoride detoxification treatment system according to one embodiment of the present invention. FIG. 3 is a process flow diagram of a sulfur hexafluoride detoxification treatment system according to one embodiment of the present invention. FIG. 4 is a schematic diagram of the first circulation tank of a sulfur hexafluoride detoxification treatment system according to one embodiment of the present invention. Figure 5 is a schematic diagram showing the configuration of a salt discharge pipe connected to the lower surface of the first circulation tank of Figure 4. FIG. 6 is a process flowchart of a method for operating a sulfur hexafluoride detoxification treatment system according to another aspect of the present invention. Figure 7 shows the relationship between operating time and electrical conductivity according to the upper and lower pH ranges of the neutralized water during the detoxification process after sulfur hexafluoride decomposition. Figure 8 shows the relationship between operating time and electrical conductivity when pure water is introduced within a certain range of pH and electrical conductivity during the detoxification process after the decomposition of sulfur hexafluoride. FIG. 9 is a graph showing the change in pH of the circulating water over time in a sulfur hexafluoride detoxification treatment system according to one embodiment of the present invention. FIG. 10 is a graph showing the change in electrical conductivity of circulating water over time in a sulfur hexafluoride detoxification treatment system according to one embodiment of the present invention. Specific details for implementing the invention

[0067] The present invention will be described in more detail below with reference to the attached drawings. However, the following drawings are provided merely to aid in understanding the present invention, and the present invention is not limited by the drawings. Furthermore, the shapes, sizes, ratios, angles, numbers, etc. disclosed in the drawings are exemplary, and the present invention is not limited to the depicted details.

[0068] Throughout the specification, the same reference numerals refer to the same components. Additionally, in describing the present invention, detailed descriptions of related prior art are omitted if it is determined that such detailed descriptions would unnecessarily obscure the essence of the invention.

[0069] Where terms such as 'includes,' 'have,' and 'consists of' mentioned in this specification are used, other parts may be added unless 'only' is used. Where a component is expressed in the singular, it includes cases where it is expressed in the plural unless specifically stated otherwise.

[0070] In interpreting the components, they are interpreted to include a margin of error even in the absence of a separate explicit statement.

[0071] When the positional relationship between two parts is described using expressions such as 'on', 'on the upper', 'on the lower', or 'next to', one or more other parts may be located between the two parts unless 'immediately' or 'directly' is used.

[0072] Positional relationships such as 'upper,' 'upper surface,' 'lower,' and 'lower surface' are described based solely on the drawing and do not represent absolute positional relationships. In other words, depending on the observation location, the positions of 'upper' and 'lower,' or 'upper surface' and 'lower surface,' may be interchanged.

[0073] In this specification, "a to b" indicating a numerical range is defined as "≥a and ≤b".

[0075] The present invention will be described in detail below with reference to the drawings.

[0076] FIG. 1 is a process diagram of a large-capacity high-concentration SF6 decomposition treatment system according to one embodiment of the present invention.

[0077] Referring to Fig. 1, the SF6 decomposition treatment system is largely composed of a thermal decomposition section and a harmless treatment section for decomposition products.

[0078] In the above pyrolysis section, large-capacity, high-concentration SF6 is introduced into the decomposition furnace along with a heat source using a direct combustion method and undergoes pyrolysis at a high temperature of over 1,000°C to perform a primary neutralization process. Subsequently, the generated decomposition gas is subjected to secondary neutralization through a neutralizer, and finally, clean gas harmless to the atmosphere is discharged through an outlet. This neutralization process is necessary as a detoxification step because highly acidic and toxic atmospheric pollutants such as HF, SO2, and SO3 are generated as products of the pyrolysis of SF6. During the primary and secondary neutralization processes, neutralized water and solid salt (Salt(KF, K2SO4)) are produced; the neutralized water mixed with the solid salt is circulated within the process, and when the batch operation is completed, the solid salt within the process is removed.

[0079] In the harmless treatment section, to minimize the generation of salt during the process, the electrical conductivity is measured and pure water is injected when it is 150 mS / cm or higher. However, when operating manually, a large amount of wastewater is generated, amounting to 20 kg when SF6 1 kg is decomposed, which increases process operating costs. Furthermore, there are factors that hinder stable operation, such as the continuous precipitation of salt in the lower part of the circulation tank and the pump operating part, which causes process stoppages.

[0080] FIG. 2 is a process flow diagram of a sulfur hexafluoride detoxification treatment system according to one embodiment of the present invention.

[0081] Referring to FIG. 2, the sulfur hexafluoride detoxification treatment system includes a combustion decomposition unit (10), a cooling unit (20), and a circulation unit (30).

[0082] The above combustion decomposition unit (10) burns sulfur hexafluoride and combustion gas together to produce decomposition gas.

[0083] In the combustion decomposition unit (10) above, combustion gas is introduced and sulfur hexafluoride is directly combusted to decompose sulfur hexafluoride and form decomposition gas, and the decomposition gas contains an acidic substance.

[0084] In the above combustion decomposition unit (10), sulfur hexafluoride is first decomposed to produce an acidic substance as a decomposition product, and the acidic substance is rendered harmless through a neutralization reaction after the introduction of a neutralizing agent and discharged.

[0085] The above cooling unit (20) cools and neutralizes the decomposition gas to generate exhaust gas and discharges it to the outside.

[0086] The above cooling unit (20) can cool the high-temperature decomposition gas, remove particulate matter from the decomposition gas to purify it, and then discharge it into the atmosphere.

[0087] The above circulation unit (30) is equipped with a circulation tank into which the acidic substance is introduced and a neutralizing agent is introduced together with water to generate a neutralizing salt through a neutralization reaction.

[0088] When an acidic substance is introduced into the above-mentioned circulation tank and a neutralizing agent and water are introduced together from the outside, a neutralization reaction is performed to generate a neutralizing salt and neutralized water. At this time, the neutralizing salt is continuously and automatically discharged to the bottom of the circulation tank, and the neutralized water is purified and cooled to supply circulation water to the cooling unit (20).

[0089] The above circulation unit (30) determines the amount of neutralizing agent added by feedback control according to the electrical conductivity and pH of the neutralizing water, and when the pH of the neutralizing water is adjusted, it can circulate the neutralizing water to supply it as cooling water to the cooling unit (20) and then circulate it back to the circulation tank.

[0090] In one embodiment, a purification unit (40) may be further included to purify the exhaust gas by being positioned downstream of the cooling unit (20).

[0091] The above decomposition gas is first cooled to room temperature in the cooling unit (20) due to high temperature, and then particulate matter contained in the decomposition gas can be removed through the purification unit (40).

[0092] Specifically, the purification unit (40) may be a scrubber or an electrostatic precipitator, and may discharge decomposition gas into the atmosphere through two stages of particulate matter removal.

[0093] In one embodiment, a heat exchanger (50) may be included that is positioned on one side of the circulation unit (30) and introduces neutralized water into the circulation tank and circulates it to the circulation tank after heat exchange.

[0094] The above neutralized water is cooled in a heat exchanger (50) and supplied to the cooler to reduce the temperature of the decomposition gas and acid gas.

[0095] In one embodiment, the circulating water tank is provided with a slope at the bottom and can collect and discharge the neutralizing flame to one side by gravity.

[0096] The circulation tank of the above circulation unit (30) is provided with a slope on its lower surface so that when the neutralizing flame is generated, it gathers to one side of the circulation tank by gravity and the neutralizing flame can be continuously discharged.

[0097] The above neutralized water can be discharged from the circulation unit (30), and suspended solids can be removed and returned to the circulation unit (30). When the above neutralized water is discharged from the circulation unit (30) together with the neutralizing salt, the neutralizing salt is separated, and the neutralized water has a circulation structure in which it passes through the cooling unit (20) and is introduced back into the circulation tank of the circulation unit (30).

[0098] In one embodiment, the water level of the circulating water tank can be automatically controlled according to the electrical conductivity and pH of the neutralized water in the circulating water tank. Specifically, the water level of the circulating water tank is determined by the input of a neutralizing agent and water from the outside, and the amount of the neutralizing agent and water input is controlled by feedback control after measuring the electrical conductivity and pH of the neutralized water in the circulating water tank. For example, when the electrical conductivity of the neutralized water is 140 mS / cm or higher and the pH is 8 or lower, the neutralized water can be discharged and the neutralizing agent and water can be input to maintain the water level of the circulating water tank.

[0099] Accordingly, a sulfur hexafluoride detoxification treatment system according to one embodiment of the present invention decomposes a large amount of high-concentration sulfur hexafluoride by high-temperature combustion to form decomposition products, cools and purifies the decomposition gas, which is the decomposition product, and discharges it into the atmosphere, and injects a neutralizing agent and water into an acidic substance to generate a neutralizing salt through a neutralization reaction, and continuously discharges the generated neutralizing salt according to the structure of a circulating water tank, and adjusts the water level of the circulating water tank according to the electrical conductivity and pH of the neutralized water to purify the discharged neutralized water and supply it to a cooling unit (20) as circulating water, and continuously circulates it from the cooling unit (20) to the circulating unit (30), thereby eliminating the need to treat the neutralized water as wastewater, effectively recovering the discharged neutralizing salt, and significantly reducing process operating costs.

[0100] Another aspect of the present invention relates to a sulfur hexafluoride detoxification treatment system that generates and continuously circulates circulating water.

[0101] FIG. 3 is a process flow diagram of a sulfur hexafluoride detoxification treatment system according to one embodiment of the present invention, FIG. 4 is a schematic diagram of a first circulation tank of a sulfur hexafluoride detoxification treatment system according to one embodiment of the present invention, and FIG. 5 is a schematic diagram showing the configuration of a salt discharge pipe connected to the lower surface of the first circulation tank of FIG. 4.

[0102] Referring to FIGS. 3 to 5, the sulfur hexafluoride (SF6) detoxification treatment system comprises a pyrolysis reactor (100), a quencher (200), a first circulation tank (300), a scrubber (400), an electrostatic precipitator (500), a hydrocyclone (600), a heat exchanger (800), a cooler (900), and a filter tank (700).

[0103] The above pyrolysis reactor (100) can form decomposition products by directly burning a high concentration and a large amount of sulfur hexafluoride.

[0104] For example, sulfur hexafluoride can be decomposed by the combustion reaction of the following chemical formula 1 and the decomposition reaction of 2.

[0105] [Chemical Formula 1]

[0106] C3H8+ 5O2+ 18.8N2→ CO2+ 4H2O + 18.8N2

[0107] [Chemical Formula 2]

[0108] SF6+ 3H2O → SO2+ 6HF + 0.5O2

[0109] The above pyrolysis reactor (100) is operated at a high temperature of 900°C to 1000°C, and a high concentration of sulfur hexafluoride is directly combusted to form combustion products, namely decomposition gas (CO2, H2O, N2) and acidic substances (SO2, HF).

[0110] According to the above chemical formula 2, a strong acidic substance is generated, resulting in highly toxic atmospheric pollutants; therefore, a process to detoxify this substance is required.

[0111] The above quencher (200; Quencher) is provided after the pyrolysis reactor (100) to rapidly cool the decomposition gas.

[0112] The above pyrolysis reactor (100) is combusted at a high temperature of 900°C or higher, and the decomposition gas is in a high-temperature state, and the decomposition gas passes through the rapid cooling unit (200) and is rapidly cooled. Specifically, while the decomposition gas flows downstream, circulating water recovered to the rapid cooling unit (200) is sprayed to cool it down to 70°C or lower, thereby neutralizing it.

[0113] In one embodiment, the pyrolysis reactor (100) and the quencher (200) may be provided as a single unit.

[0114] It is preferable that the above pyrolysis reactor (100) and the rapid cooling unit (200) are provided as a single unit, so that the combustion reaction decomposition gas can be cooled sequentially according to the travel distance.

[0115] The first circulation tank (300) is provided after the rapid cooling unit (200), and the decomposition gas is introduced into it, along with a neutralizing agent and water. Acidic substances in the decomposition gas react with the neutralizing agent to form neutralizing salt and neutralized water, and when the neutralizing salt settles, it is discharged continuously.

[0116] The first circulating water tank (300) above provides a space in which an acidic substance in the decomposition gas is neutralized by a neutralization reaction with a neutralizing agent to produce a neutralizing salt. Specifically, the acidic substance contained in the decomposition gas is introduced together with a neutralizing agent and water to be controlled to a constant water level in the first circulating water tank (300), and the acidic substance generated according to the above chemical formula 2 can be neutralized by a neutralization reaction according to the following chemical formula 3 to produce a halogen salt and neutralized water.

[0117] [Chemical Formula 3]

[0118] HF + KOH → KF + H2O

[0119] SO3 + 2KOH → K2SO4 + H2O

[0120] In the above chemical formula 3, the acidic substance is converted into a harmless halogen salt through a neutralization reaction with a neutralizing agent, and the halogen salt can be recovered and utilized as fluorine, and K2SO4 is utilized as a raw material for chemical fertilizers, thus having high added value.

[0121] The halogen salt generated in the first circulating water tank (300) may be one or more of NaF, KF, NaSO4, and K2SO4 depending on the added neutralizing agent, and the NaSO4 generated by the neutralization reaction can be used as a raw material for glass, detergent, dye, dye, etc.

[0122] The scrubber (400) receives decomposition gas from the first circulation tank (300), cleans it to settle particulate matter, and cools the exhaust gas.

[0123] The scrubber (400) may be provided in the downstream of the first circulation tank (300), and the decomposition gas introduced into the first circulation tank (300) may pass through the scrubber (400) to remove particulate matter and purify it.

[0124] In one embodiment, the first circulation tank (300) includes an upper surface (301), a side case (302), a lower surface (303), and a baffle (310).

[0125] The first circulation tank (300) above may specifically be a hexagonal body having a rectangular lower surface (303), and provides a space in which the decomposition gas is introduced together with a neutralizing agent and water to generate neutralizing flame and neutralized water.

[0126] The upper surface (301) is connected to the quencher (200; Quencher), a pipe through which water and a neutralizing agent are introduced is connected, and the scrubber (400) is connected.

[0127] The upper surface (301) is connected to the rapid cooling unit (200) on one side and to the scrubber (400) on the other side.

[0128] The above side case (302) can have a neutralizing agent and water introduced into it, and when the acidic substance is introduced, it can capture the neutralizing salt and neutralized water generated by the neutralization reaction inside.

[0129] The lower surface (303) is provided with a slope so that the neutralizing flame gathers along the slope to one side by gravity, and a salt discharge port (330) is formed to continuously discharge the neutralizing flame.

[0130] The first circulation tank (300) is provided with an upper surface (301), a side case (302), and a lower surface (303) to provide a space where a neutralization reaction is performed, and can collect the generated neutralizing flame and neutralized water inside, and can allow the decomposition gas introduced from the downstream of the rapid cooler (200) to move toward the scrubber (400) on the other side.

[0131] When the lower surface (303) is provided as a slope, the generated neutralizing flame moves along the lower surface and accumulates on one side of the lower surface (303).

[0132] In one embodiment, the angle of inclination of the inclined slope can be determined according to the following Equation 1.

[0133] [Equation 1]

[0134] 10° ≤ 90 - α ≤ 30°

[0135] In the above equation 1, α is the angle between the slope and the side case (302).

[0136] If α is determined within the above range, the neutralizing flame may accumulate along the above slope, and if it falls short of the above range, the movement speed of the neutralizing flame is too slow, resulting in a low neutralizing flame discharge efficiency, and if it exceeds the range, the neutralizing flame may accumulate on the lower surface (303) and potentially block the salt discharge port (330) and the salt discharge pipe (332).

[0137] The above baffle (310) extends from the lower surface (303) to restrict the movement of the neutralizing flame and allow the upper neutralizing water, which has low electrical conductivity among the neutralizing waters, to overflow and move to the opposite space.

[0138] When a baffle (310) is provided within the first circulating water tank (300), the first circulating water tank (300) can be partitioned. When a neutralizing flame is generated through a neutralization reaction between an acidic substance and a neutralizing agent in one partition, the upper neutralizing water, which has a relatively reduced electrical conductivity, passes over the baffle (310) and reaches the other partition. The neutralizing water that reaches the other partition contains less neutralizing flame, and can be recycled as circulating water by more effectively removing suspended matter and neutralizing flame in the hydrocyclone (600) located in the following section.

[0139] When the above decomposition gas is neutralized, the pump and pipe transporting the neutralized water become clogged due to the precipitation of neutralizing salt, causing the process to stop. However, the solution with low electrical conductivity, i.e., the neutralized water containing less neutralizing salt, can be recycled from the first circulation tank (300), thereby significantly reducing the amount of wastewater generated and increasing process efficiency, as well as being very environmentally friendly.

[0140] In one embodiment, the salt discharge port (330) is connected to a salt discharge pipe (332), and a plurality of nitrogen purging ports (322) may be provided in the salt discharge port (330).

[0141] The salt discharge port (330) is connected to a salt discharge pipe (332), and the salt discharge port (330) is equipped with a plurality of nitrogen purging ports (322). Specifically, a plurality of nitrogen purging ports (322) are arranged at regular intervals along the outer edge of the salt discharge port (330) to purge nitrogen during operation and remove neutralized salt, thereby preventing blockage of the salt discharge pipe (332) and the salt discharge port (330).

[0142] In one embodiment, the nitrogen supply tank (320) and the salt discharge pipe (332) connected to the salt discharge port (330) are equipped with purging valves (323a, 323b, 324a, 324b) to control the amount of nitrogen being purged. For example, when the purging valve (323a) of the nitrogen purging line (321) leading to the salt discharge port (330) is opened and the purging valve (324a) inside the salt discharge pipe (332) is opened, nitrogen is injected to remove the neutralizing flame attached to the salt discharge port (330), and then the second purging valve (324b) is opened to effectively remove the neutralizing flame attached to the salt discharge port (330) and the salt discharge pipe (332).

[0143] In one embodiment, the filter tank (700) introduces the neutralized water discharged from the first circulation tank (300) to one side along the neutralized water inflow line (S2) to remove neutralized salts in the neutralized water and then circulates it back to the first circulation tank (300) along the neutralized water discharge line (S3).

[0144] Neutralized water containing neutralizing salt is introduced into the filter tank (700) along the salt discharge pipe (332) to remove the neutralizing salt, and the neutralized water from which the neutralizing salt has been removed is recovered to the first circulation tank (300) to reduce the amount of wastewater generated and to control the water level in the first circulation tank (300).

[0145] The above hydrocyclone (600) introduces neutralized water from the first circulation tank (300) to remove residual neutralizing salt in the neutralized water and forms circulating water.

[0146] The above hydrocyclone (600) can introduce neutralized water containing residual neutralized salt and suspended matter, in which a large amount of neutralized salt has been removed from the first circulation tank, along the inlet line (S4), and purify it to form circulating water (S5).

[0147] The heat exchanger (800) cools the circulating water from which the neutralizing salt has been removed in the hydrocyclone (600) by heat exchange.

[0148] The above cooler (900) is connected to the above heat exchanger (800) to cool the circulating water.

[0149] Specifically, the heat exchanger (800) is introduced with a circulating water flow (S5), and is cooled by heat exchange with the circulating water (S6) cooled in the cooler (900) to produce low-temperature circulating water (S7).

[0150] The above circulating water (S7) is introduced into the electrostatic precipitator (500), and another circulating water (S10) can be introduced as cooling water to one side of the scrubber (400) and the rapid cooler (200) to be used to cool the decomposition gas.

[0151] By removing the above neutralizing salt to generate circulating water and circulating it to be used as cooling water for the electrostatic precipitator (500), scrubber (400), and rapid cooler (200), not only can the amount of wastewater generated be reduced, but effective cooling can also be achieved in the electrostatic precipitator (500), scrubber (400), and rapid cooler (200) by utilizing the latent heat of the circulating water.

[0152] The above electrostatic precipitator (500) is equipped with a dust collection tower that receives exhaust gas from the scrubber (400), collects and processes particulate matter, purifies the exhaust gas, and discharges it to the outside, and a second circulation tank (510) in which circulating water is collected at the bottom of the dust collection tower.

[0153] The above electrostatic precipitator (500) can remove fine particulate matter again by electrostatic precipitating it after particulate matter is first removed in the scrubber (400) and discharge exhaust gas to the outside. Since the decomposition gas passes through the scrubber (400) and the electrostatic precipitator (500) to remove particulate matter, it is environmentally friendly as it removes pollutants from the decomposition gas.

[0154] The circulating water introduced into the above electrostatic precipitator (500) is stored in the second circulating water tank (510) at the bottom, and the circulating water stored in the second circulating water tank (510) is introduced back into the first circulating water tank (300) to form a circulation structure of the neutralized water in the sulfur hexafluoride detoxification treatment system.

[0155] In one embodiment, the first circulating water tank (300) may be equipped with a level gauge (340) and a conductivity meter (350) for measuring electrical conductivity, and may be equipped with a pH meter (360) for measuring the pH of the neutralized water generated in the first circulating water tank (300).

[0156] In one embodiment, the first circulating water tank (300) is equipped with a level gauge (340) and a conductivity meter (350) for measuring electrical conductivity, and is equipped with a pH meter (360) to measure the water level, the electrical conductivity of the neutralized water, and the pH within the first circulating water tank (300).

[0157] In one embodiment, a controller (370) may be provided that is electrically connected to the level gauge (340), conductivity meter (350), and pH meter (360) and controls the water level in the first circulating water tank (300) according to the electrical conductivity and pH of the neutralized water.

[0158] The above controller (370) measures the electrical conductivity and pH of the neutralized water and determines the amount of neutralizing agent and water to be supplied in the neutralizing water discharge and neutralizing agent supply unit (1000) and water supply unit (1100), thereby adjusting the water level of the first circulating water tank (300) to 50 to 80% of the total internal volume, so as to improve the operating efficiency of the sulfur hexafluoride detoxification treatment system.

[0159] At this time, the water level of the first circulation tank (300) can be fed back according to the electrical conductivity and pH, and the amount of neutralizing agent and water to be supplied can be determined. For example, the water level of the first circulation tank (300) can be determined to be 50% to 80%, and the electrical conductivity of the neutralizing water can be maintained at 150 mS / cm or less to generate circulating water. At this time, neutralizing water with an electrical conductivity of 140 mS / cm or more and a pH of 8 or less is discharged, and the neutralizing agent and water are supplied again according to the measurement of the level gauge (340) to maintain the water level of the first circulation tank (300) constant, thereby generating circulating water with a target electrical conductivity and reducing the generation of neutralizing salt during circulation, so that circulating water can be generated and circulated.

[0160] In one embodiment, the second circulation tank (510) may be equipped with a pH meter (360) for measuring the pH of the circulating water collected in the second circulation tank (510).

[0161] Since the pH of the neutralizing water near the salt discharge port (330) of the first circulation tank (300) is the lowest and the pH of the circulating water in the second circulation tank (510) is the highest, so that the atomization treatment of sulfur hexafluoride is performed continuously, it is advantageous for the continuous circulation of the circulating water to be directly injected into the second circulation tank (510), and at this time, the amount of neutralizing agent injected can be determined according to the feedback of the pH meter (360) provided in the second circulation tank (510).

[0162] Accordingly, the sulfur hexafluoride detoxification treatment system according to one embodiment of the present invention reduces the amount of wastewater generated by circulating neutralized water during the detoxification process of neutralizing sulfur hexafluoride, and has very high operational efficiency by continuously discharging neutralized salt, thereby preventing the neutralization salt from clogging pumps and pipes and causing operation to stop.

[0163] Another aspect of the present invention relates to a method for detoxifying sulfur hexafluoride decomposition products.

[0164] The above method for detoxifying sulfur hexafluoride decomposition products involves burning sulfur hexafluoride together with combustion gas to generate decomposition gas, removing particulate matter from the decomposition gas and discharging it to the outside, and for acidic substances, introducing a neutralizing agent and water together into a tank to generate a neutralizing flame through a neutralization reaction, and then continuously discharging the neutralizing flame to one side. The pH and electrical conductivity of the generated neutralized water are measured, and the amount of neutralizing agent and the water level of the tank are controlled via feedback so that the neutralized water is continuously circulated.

[0165] The above method for detoxifying sulfur hexafluoride decomposition products reduces the amount of wastewater generated by continuously circulating neutralized water and can continuously detoxify high-volume, high-concentration sulfur hexafluoride.

[0166] Another aspect of the present invention relates to a method for operating a sulfur hexafluoride detoxification treatment system.

[0167] FIG. 6 is a process flowchart of a method for operating a sulfur hexafluoride detoxification treatment system according to another aspect of the present invention.

[0168] Referring to FIG. 6, the method of operating the sulfur hexafluoride detoxification treatment system comprises: (a) introducing sulfur hexafluoride and combustion gas into a pyrolysis reactor and combusting them to generate decomposition gas; (b) washing the decomposition gas and collecting particulate matter with an electrostatic precipitator to generate purified exhaust gas and discharge it to the outside; (c) introducing acidic substances among the decomposition gas into a first circulation tank, introducing a neutralizing agent and water to generate neutralizing salt and neutralized water through a neutralization reaction, and collecting along the slope of the lower part of the first circulation tank and continuously discharging it through a salt discharge port; and (d) recovering the neutralized water, removing residual neutralizing salt from the neutralized water, generating circulating water and delivering it to the electrostatic precipitator, and when the circulating water is collected in the second circulation tank at the bottom of the electrostatic precipitator, circulating it back to the first circulation tank.

[0169] First, sulfur hexafluoride and combustion gas are introduced into a pyrolysis reactor and combusted to produce decomposition gas (S100).

[0170] A large amount of high-concentration sulfur hexafluoride is burned using the above pyrolysis reactor to generate decomposition gas.

[0171] The above decomposition gas can be cleaned, and particulate matter can be collected by an electrostatic precipitator to generate purified exhaust gas, which can then be discharged to the outside.

[0172] The above decomposition gas can be cleaned to remove fine particulate matter from the decomposition gas and discharged into the atmosphere.

[0173] Acidic substances among the decomposition gases are introduced into the first circulation tank, and a neutralizing agent and water are introduced to generate a neutralizing flame through a neutralization reaction, which is collected along the slope of the lower part of the first circulation tank and continuously discharged through the salt discharge port (S300).

[0174] A neutralizing agent and water are introduced into the first circulation tank, and when a neutralizing flame is generated through a neutralization reaction by introducing the neutralizing agent into an acidic substance in the decomposition gas, the neutralizing flame can be collected and discharged through the slopes of the first circulation tank.

[0175] In one embodiment, the method may include the step of removing the neutralized salt by purging nitrogen into the salt outlet.

[0176] By purging the above salt outlet with nitrogen, the salt outlet or salt outlet pipe can be prevented from becoming clogged due to the accumulation of neutralized salt.

[0177] In one embodiment, the steps of introducing water into the first circulation tank in the above S300 and introducing a neutralizing agent to maintain the pH of the neutralized water can be performed in an interlocking manner.

[0178] The step of adding a neutralizing agent to maintain the pH of the first circulation tank at a constant standard and the step of supplying water to maintain a constant water level are performed in an interlocking manner, making it very easy to maintain a constant water level of the first circulation tank and to maintain the neutralized water at a constant pH through the neutralization reaction.

[0179] In one embodiment, the pH is measured around the salt discharge port of the first circulating water tank in the S300, and if the pH is below the target pH, neutralized salt and neutralized water can be discharged.

[0180] Specifically, the discharge amount of neutralized water and the amount of water supplied can be determined by measuring the electrical conductivity and pH of the neutralized water in the first circulating water tank. In cases where the amount of neutralizing agent used is reduced by managing the electrical conductivity to 150 mS / cm or less, it is determined that the electrical conductivity satisfies the discharge standard when the electrical conductivity is 140 mS / cm or higher, and neutralized water with a pH of 8 or less is discharged, and if the electrical conductivity exceeds 150 mS / cm, neutralized water can be discharged regardless of the pH measurement value.

[0181] In the neutralization water discharge process, if the neutralization water conditions of 140 mS / cm or more and a pH of 8 or less are not satisfied, additional neutralizing agent may be supplied, and if the neutralization reaction proceeds and the pH drops to 8 or less, the neutralization water may be discharged.

[0182] Afterwards, the water level of the first circulation tank can be controlled by supplying water and a neutralizing agent again.

[0183] In one embodiment, the step of adding a neutralizing agent to the second circulating water tank in the above S300 may be further included.

[0184] The neutralization reaction can be performed in the first circulation tank and the second circulation tank. Since it is desirable for the pH around the salt outlet of the first circulation tank to be the lowest, if a neutralizing agent is added in the second circulation tank so that the neutralization reaction occurs first in the second circulation tank, and subsequently the neutralization reaction occurs in the circulating water around the salt outlet of the first circulation tank, it is very easy to control the pH of the discharged neutralized water.

[0185] In the above S300, the pH of the circulating water in the second circulating water tank is measured, and the neutralizing agent may be added via feedback control to maintain the target pH. Specifically, it is preferable that the amount of neutralizing agent added via feedback control is added to maintain the pH around the salt discharge port of the first circulating water tank according to the target standard.

[0186] In the above S300, the water level of the neutralization water can be controlled to 50 to 80% of the volume of the first circulation tank. The water level of the first circulation tank is determined, and the amount of neutralizing agent and water supply is determined according to the water level, while the water level of the first circulation tank is controlled including the flow rate of the circulating water to enable continuous detoxification treatment.

[0187] Afterwards, the neutralized water is recovered and residual neutralizing salt in the neutralized water is removed, and then circulating water is generated and delivered to the electrostatic precipitator, and when the circulating water is collected in the second circulating water tank at the bottom of the electrostatic precipitator, it is circulated back to the first circulating water tank (S400).

[0188] When the above-mentioned circulating water is generated and the amount of neutralizing agent added and the amount of water supplied are adjusted according to the electrical conductivity and pH of the first water circulation tank, the amount of circulating water flow is increased to maintain the water level of the first circulating tank at a constant level, significantly reducing the amount of wastewater generated and enabling the sulfur hexafluoride detoxification treatment system to be operated efficiently.

[0190] Hereinafter, preferred embodiments are presented to aid in understanding the present invention; however, the following embodiments are merely illustrative of the invention and the scope of the invention is not limited to the following embodiments.

[0192] Examples

[0193] Sulfur hexafluoride was introduced into the pyrolysis reactor of the sulfur hexafluoride detoxification treatment system and burned at 1000°C to generate decomposition gas, which was then cooled in a rapid cooling tank and introduced into the first circulating water tank to perform a neutralization reaction to produce neutralized flame and neutralized water.

[0194] A neutralizing agent and water were supplied to control the water level of the first circulation tank to 60%, and a KOH:water ratio of 25:75 (w / w) was supplied to maintain the pH of the neutralized water discharged from the first circulation tank at 8 or higher in order to form the circulating water. At this time, the supply of water and the neutralizing agent to control the water level so that a sufficient neutralization reaction could proceed was carried out in an interlocking manner.

[0195] Neutralized water was discharged to produce and cool circulating water, collected in the second circulation tank of an electrostatic precipitator, and then recovered back into the first circulation tank so that the neutralized water could be continuously circulated to reduce the amount of wastewater generated and operate a harmless treatment system.

[0197] Experimental Example 1

[0198] We aimed to verify the harmlessness of sulfur hexafluoride and the operation method of the treatment system based on the control of electrical conductivity and pH of the neutralized water.

[0199] Figure 7 shows the relationship between operating time and electrical conductivity according to the upper and lower pH ranges of the neutralized water during the detoxification process after sulfur hexafluoride decomposition.

[0200] Referring to Fig. 7, if the neutralization process after the decomposition of sulfur hexafluoride is operated by controlling only the upper and lower pH limits of the neutralization water, there is a problem in that the concentration of salt in the process neutralization water increases with increasing operating time, resulting in the precipitation of a large amount of salt. In addition, a large amount of wastewater is generated, which can significantly increase process operating costs.

[0201] Figure 8 shows the relationship between operating time and electrical conductivity when pure water is introduced within a certain range of pH and electrical conductivity during the detoxification process after the decomposition of sulfur hexafluoride.

[0202] Referring to Fig. 8, when the electrical conductivity and pH values ​​reach the target range, pure water is introduced to lower the electrical conductivity. As the neutralization reaction continues, the electrical conductivity gradually increases from a high range due to the influence of the neutralizing salt dissolved in the neutralized water, reaching an upper limit. After continuing operation until the pH reaches a lower limit, the control logic for lowering the electrical conductivity through wastewater treatment and process water supply can operate normally.

[0203] Therefore, it was confirmed that controlling electrical conductivity and pH during the process and circulating neutralized water to continuously remove neutralizing salts can not only reduce the amount of wastewater generated but also enable stable detoxification treatment operation.

[0205] Experimental Example 2

[0206] The correlation between the amount of sulfur hexafluoride supplied and the water level of the first circulation tank according to the pH change during the operation period was confirmed in the pH meter of the sulfur hexafluoride detoxification treatment system according to Example 1.

[0207] FIG. 9 is a graph showing the change in pH of the circulating water over time in a sulfur hexafluoride detoxification treatment system according to one embodiment of the present invention.

[0208] Referring to Figure 9, it was confirmed that when a trend line is calculated based on the SF6 supply amount and the liquid level of the neutralization sedimentation tank in the section where the pH changes constantly, a consistent pattern of change appears as shown in the figure below, and on average, it can be expressed as 1.7160E-5 pH / (SF6· Tank Level).

[0209] FIG. 10 is a graph showing the change in electrical conductivity of circulating water over time in a sulfur hexafluoride detoxification treatment system according to one embodiment of the present invention.

[0210] Referring to Fig. 10, the change in electrical conductivity was analyzed for a section where the water level of the first circulating tank was constant. As a result, the electrical conductivity changed by 76.21–77.49 mS / cm, and by dividing this by the injection amount of sulfur hexafluoride and the water level of the first circulating tank, a change of 2.8695E-5 mS / cm · SF6) was confirmed. Similar changes were observed in other sections as well, which means that there is almost no change in electrical conductivity due to ions generated by the reaction between HF and KOH.

[0211] Therefore, it was confirmed that sulfur hexafluoride can be continuously detoxified by circulating the water while maintaining a constant water level in the first circulating water tank, which uses pH as a standard and adds electrical conductivity as a neutralized water discharge standard.

[0213] The present invention has been described above with reference to embodiments. Those skilled in the art will understand that the present invention may be embodied in modified forms without departing from the essential characteristics of the invention. Therefore, the disclosed embodiments should be considered in an illustrative rather than a restrictive sense. The scope of the invention is defined by the claims, not by the foregoing description, and all variations within the scope of equivalents should be interpreted as being included in the invention. Explanation of the symbols

[0215] 10: Combustion decomposition section 20: Cooling section 30 : Circulation Section 40 : Purification Section 50 : Heat exchanger (H / E) 100 : Pyrolysis reactor 200 : Quick chiller 300 : 1st Circulation Tank 301 : Upper Surface 302: Side case 303: Bottom surface 310 : Baffle 320 : Nitrogen supply tank 321: Nitrogen purging line 323a, 323b, 324a, 324b: Purge valves 330: Salt discharge port 322: Nitrogen purging port 332: Salt discharge pipe 340: Level gauge 350: Conductivity meter 360: pH meter 370 : Controller 400 : Scrubber 500: Electrostatic precipitator 510: Second circulation tank 600 : Hydrocyclone 700 : Filter tank 800 : Heat exchanger 900 : Cooler 1000 : Neutralizing agent supply unit 1100 : Water supply unit

Claims

Claim 1 A sulfur hexafluoride detoxification treatment system comprising: a combustion decomposition unit that combusts sulfur hexafluoride and combustion gas together to generate decomposition gas; a cooling unit that cools and neutralizes the decomposition gas to convert it into exhaust gas and discharges it to the outside; and a circulation unit having a circulating water tank into which an acidic substance among the decomposition gas is introduced, and a neutralizing agent is introduced together with neutralizing water to generate a neutralizing flame through a neutralization reaction; wherein the neutralizing water in the circulating water tank is discharged and the neutralizing flame is discharged to the bottom of the circulating water tank while continuously circulating the cooling unit, and the neutralizing water is purified and cooled to supply circulating water to the cooling unit, and a heat exchanger disposed on one side of the circulating unit that introduces the neutralizing water in the circulating water tank and circulates it to the circulating water tank after heat exchange. Claim 2 A sulfur hexafluoride detoxification treatment system according to claim 1, further comprising a purification unit disposed downstream of the cooling unit to purify the exhaust gas. Claim 3 A sulfur hexafluoride detoxification treatment system according to paragraph 2, wherein the purification unit is equipped with a scrubber or an electrostatic precipitator. Claim 4 delete Claim 5 A sulfur hexafluoride detoxification treatment system according to claim 1, wherein the circulating water tank is provided with a slanted surface at the bottom and collects and discharges the neutralizing flame to one side by gravity. Claim 6 A sulfur hexafluoride detoxification treatment system according to claim 1, wherein the neutralized water is discharged from a circulation unit and suspended solids are removed and recovered back into the circulation unit. Claim 7 A sulfur hexafluoride detoxification treatment system according to claim 1, wherein the water level of the circulating water tank is automatically controlled according to the electrical conductivity and pH of the neutralized water in the circulating water tank. Claim 8 A pyrolysis reactor into which sulfur hexafluoride and combustion gas are introduced to burn sulfur hexafluoride and generate decomposition gas; a quencher provided downstream of the pyrolysis reactor to rapidly cool the decomposition gas; a first circulation tank provided downstream of the quencher, into which the decomposition gas flows, along with a neutralizing agent and water, in which acidic substances in the decomposition gas react with the neutralizing agent to form neutralizing salt and neutralized water, and which continuously discharges the neutralizing salt once it precipitates; a scrubber that receives the decomposition gas from the first circulation tank, washes it to precipitate particulate matter, and cools the exhaust gas; an electrostatic precipitator equipped with a dust collection tower that receives the exhaust gas from the scrubber, collects and treats particulate matter, purifies the exhaust gas, and discharges it to the outside, and a second circulation tank at the bottom of the dust collection tower in which circulating water is collected; and a hydrocyclone that introduces the neutralized water from the first circulation tank to remove the neutralizing salt within the neutralized water to form circulating water. A sulfur hexafluoride detoxification treatment system comprising: a heat exchanger for cooling the circulating water from which neutralizing salts have been removed in the above hydrocyclone through heat exchange; a cooler connected to the heat exchanger for cooling the circulating water; and a filter tank for introducing the neutralized water discharged from the first circulating water tank to one side to remove neutralizing salts within the neutralized water and circulating it back to the first circulating water tank. Claim 9 A sulfur hexafluoride detoxification treatment system according to claim 8, wherein the pyrolysis reactor and the quencher are provided as an integrated unit. Claim 10 In claim 8, the sulfur hexafluoride detoxification treatment system comprises: an upper surface to which the rapid cooling unit is connected, a pipe to which water and a neutralizing agent are introduced is connected, and to which the scrubber is connected; a side case into which the neutralizing agent and water are introduced, and which collects the neutralizing salt and neutralized water generated by the neutralization reaction when the acidic substance is introduced; a lower surface provided with a slope to cause the neutralizing salt to gather to one side along the slope by gravity and a salt discharge port formed to continuously discharge the neutralizing salt; and a baffle extending from the lower surface to restrict the movement of the neutralizing salt and to cause the upper neutralizing water, which has low electrical conductivity among the neutralizing water, to overflow and move to the opposite space. Claim 11 A sulfur hexafluoride detoxification treatment system according to claim 10, wherein the salt discharge port is connected to a salt discharge pipe and the salt discharge port is equipped with a plurality of nitrogen purge ports. Claim 12 A sulfur hexafluoride detoxification treatment system according to claim 11, wherein the nitrogen supply tank and salt discharge pipe connected to the salt discharge port are equipped with a purging valve to control the amount of nitrogen purged. Claim 13 In claim 10, the above slope is a sulfur hexafluoride detoxification treatment system in which the slope angle is determined according to the following Equation 1: [Equation 1] 10° ≤ 90 - α ≤ 30° In the above Equation 1, α is the angle between the slope and the side case. Claim 14 A sulfur hexafluoride detoxification treatment system according to claim 8, wherein the first circulating water tank is equipped with a level gauge and a conductivity meter for measuring electrical conductivity, and a pH meter for measuring the pH of the neutralized water generated in the first circulating water tank. Claim 15 In claim 8, the sulfur hexafluoride detoxification treatment system is equipped with a pH meter that measures the pH of the circulating water collected in the second circulating water tank. Claim 16 A sulfur hexafluoride detoxification treatment system according to claim 14, equipped with a controller that is electrically connected to the level gauge, conductivity meter, and pH meter and controls the water level in the first circulating water tank according to the electrical conductivity and pH of the neutralized water. Claim 17 A method for detoxifying sulfur hexafluoride decomposition products, wherein sulfur hexafluoride and combustion gas are combusted together to generate decomposition gas, the decomposition gas is discharged to the outside after removing particulate matter, and acidic substances are neutralized by introducing a neutralizing agent and water together into a circulating water tank to generate a neutralizing flame through a neutralization reaction, and the neutralizing flame is continuously discharged to one side, wherein the pH and electrical conductivity of the generated neutralizing water are measured to continuously circulate the neutralizing water by feedback controlling the amount of the neutralizing agent and the water level of the circulating water tank, and the neutralizing water flows into a heat exchanger to exchange heat with the circulating water, and the circulating water cools the decomposition gas. Claim 18 (a) a step of introducing sulfur hexafluoride and combustion gas into a pyrolysis reactor and combusting them to generate decomposition gas; (b) a step of cleaning the decomposition gas and collecting particulate matter with an electrostatic precipitator to generate purified exhaust gas and discharging it to the outside; (c) a step of introducing acidic substances among the decomposition gas into a first circulation tank, introducing a neutralizing agent and water to generate neutralizing salt and neutralized water through a neutralization reaction, and collecting along the slope of the lower part of the first circulation tank and continuously discharging through a salt discharge port; and (d) a step of recovering the neutralized water, removing residual neutralizing salt from the neutralized water, generating circulating water and delivering it to the electrostatic precipitator, and when the circulating water is collected in a second circulation tank at the lower part of the electrostatic precipitator, circulating it back to the first circulation tank; comprising a method for operating a sulfur hexafluoride detoxification treatment system. Claim 19 A method for operating a sulfur hexafluoride detoxification treatment system according to claim 18, wherein the step of introducing water into the first circulating water tank and the step of introducing a neutralizing agent to maintain the pH of the neutralized water in (c) above are performed in an interlocking manner. Claim 20 A method for operating a sulfur hexafluoride detoxification treatment system, wherein, in claim 18, the step of adding a neutralizing agent to the second circulating water tank in (c) above is further included. Claim 21 A method for operating a sulfur hexafluoride detoxification treatment system according to claim 18, wherein in (c) above, the pH is measured around the salt discharge port of the first circulating water tank, and if the pH is below the target pH, the neutralizing salt and neutralizing water are discharged. Claim 22 A method of operating a sulfur hexafluoride detoxification treatment system according to claim 18, wherein the pH of the circulating water of the second circulating water tank is measured in (c) above, and the neutralizing agent is added by feedback control to maintain the target pH. Claim 23 A method for operating a sulfur hexafluoride detoxification treatment system according to claim 18, wherein the water level of the neutralization water in (c) above is controlled to 50 to 80% of the volume of the first circulating water tank. Claim 24 A method for operating a sulfur hexafluoride detoxification treatment system according to claim 18, comprising the step of removing neutralized salt by purging nitrogen into the salt discharge port in (c) above.

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