KR100928972B1 - High efficiency ozone dissolving device and sludge reduction device using micro bubble ozone - Google Patents

Abstract

The present invention relates to a high-efficiency ozone dissolving device and a sludge reduction device using micro-bubble ozone, injecting acid into the excess sludge generated in the sedimentation tank and dissolving ozone in the sludge using an ozone dissolving tank, and finely bubbled in the sludge solubilization tank. A sludge reducing device for reducing sludge by reacting ozone with sludge.

The high-efficiency ozone dissolving device and the sludge reduction device using microbubble ozone of the present invention include: a sludge storage tank into which excess sludge generated in a precipitation tank is mixed with an acid supplied from an acid storage tank; An ozone dissolving tank in which the sludge discharged from the sludge storage tank and the ozone supplied from the ozone generator are pressurized by a sludge circulation pump to be introduced, and an ozone-sludge mixture in which ozone is dissolved in the sludge is formed; A sludge solubilization tank for introducing the ozone-sludge mixed solution discharged from the ozone melting tank to pass through the microbubble generating device and to super-saturate ozone in the form of microbubbles to slowly rise the solubilization of the sludge; And a solubilized sludge storage tank in which the sludge solubilized in the sludge solubilization tank is discharged and stored. Characterized in that it comprises a.

The sludge reduction apparatus according to the present invention has the effect of reducing the amount of ozone injected by injecting acid into the excess sludge and reducing bubbles generated in the sludge solubilization tank by the injection of acid.

In addition, it has the effect of greatly improving the dissolution efficiency of ozone to sludge flowing into the ozone melting tank pressurized by 2.5 ~ 3kgf / cm ² by the sludge circulation pump, and reacting with unreacted ozone and sludge by using micro bubble generator. This prevents the discharge of waste ozone into the atmosphere and increases the efficiency of reducing sludge.

Sludge, Ozone, Microbubbles, Solubilization, Reduction

Description

Sludge Reduce Apparatus Using High Efficiency Ozone Dissolving Tank and Microbubble Ozone}

The present invention relates to a high-efficiency ozone dissolving device and a sludge reduction device using micro-bubble ozone, injecting acid into the excess sludge generated in the sedimentation tank and dissolving ozone in the sludge using an ozone dissolving tank, and finely bubbled in the sludge solubilization tank. A sludge reducing device for reducing sludge by reacting ozone with sludge.

Most developed countries have prevented the discharge of sewage sludge from the sea in preparation for the entry into force of the London Protocol 96 Protocol since the early 1990s. Most countries do not discharge marine water.

Even though most local governments plan to install facilities without sludge treatment, the design, construction and normal operation of the facility took at least three years and faced a situation where it was not possible to apply them in a timely manner. Under these circumstances, the prohibition of direct landfilling on January 1, 2001, has many problems. In the case of deferral, due to the reasonable logic, the government and local governments must defer until the end of June 2003 under the premise of establishing a sludge treatment resource system by reducing sludge generation, supervision and institutional maintenance. It will be implemented from July. In addition, the Ministry of Maritime Affairs and Fisheries established a comprehensive land waste marine dumping plan to reduce land dumping of land waste by 50% as of 2011 as part of measures to improve marine water quality, and to prohibit all dumping of sewage sludge and livestock waste. Regulations on marine discharges are being tightened, such as public announcements, and at this point, it is necessary to establish measures for land treatment.

In activated sludge systems, the treatment and disposal of surplus sludge accounts for 25 ~ 60% of the total operating cost of the sewage treatment plant, which requires enormous costs. For domestic wastewater treatment facilities, more than half of the operating costs are required for sludge treatment and disposal. . Innovative concepts for the production of surplus sludge-free systems in activated sludge systems combined with biomass recycling processes have been developed (Deleris et al., 2000; Huysmans et al., 2001). Yasui et al., 1996), methods such as milling, ultrasonication, heating, alkali treatment and ozone oxidation have been developed for the treatment of waste sludge (Mllller et al., 1998; Scheminski et. al., 2000; Weemaes et al., 2000; Yasui and Shibata, 1994).

Ozone treatment of excess sludge has been known to be one of the most economically useful technologies with the highest sludge destruction capacity (M ㆌ ller, 2000; Park et al., 2003). Moreover, it is known that ozonated sludge can be used as an external carbon source that can save a lot of cost in biological nitrogen removal. Ozone depletion of sludge causes sequential flocculation, conversion of particulate matter into dissolved substances and mineralization (Ahn et al., 2002a, b). By generating a large amount of fine solids there is an effect that makes it easy to break down by microorganisms. The biodegradability of ozonated sludge has been confirmed by many researchers (Scheminski et al., 2000; Weemaes et al., 2000; Yeom et al., 2002).

The possibility of activated sludge systems combined with ozone treatment has been demonstrated through full-scale plant operation with no excess sludge emissions (Yasui and Shibata, 1994; Yasui et al., 1996). Minimization of excess sludge can be achieved by recycling the ozonated excess sludge into a bioreactor. Of the many useful parameters for operating such a system, the sludge ozone treatment rate is the most important factor in the field, and according to Yasui and Shibata (1994), the rate of circulating the sludge back to ozone treatment for no discharge of excess sludge is It is known to be at least three times.

On the other hand, it is true that more ozone is injected to generate less excess sludge, but injecting only too much ozone leads to an increase in operating costs, and the remaining ozone adversely affects microorganisms that decompose organic matter. The problem occurs. In addition, when a large amount of ozone is injected, a relatively large amount of waste ozone (unreacted ozone) is generated, and an ozone treatment parameter that is inappropriate for ozone treatment is a factor that impairs system performance with a high operating cost. Works.

Conventional sludge reduction apparatus using ozone has a problem in that the contact efficiency is low and the waste ozone (unreacted ozone) is generated in such a manner that the ozone gas is bubbled using acid stones to contact the ozone gas with the sludge. There is a method of reducing sludge by miniaturizing ozone gas using a high pressure pump, but such a method requires a high pressure, high performance pump and generates a waste ozone that does not react with the sludge no matter how much the ozone gas is refined. . In addition, the method of miniaturizing ozone gas and reacting at atmospheric pressure requires a sufficient residence time, and in this case, the apparatus has to be very large, and there is a problem in that some waste ozone is generated.

The present invention has been made to solve the above problems, an object of the present invention by using an ozone melting tank and a micro bubble generator to increase the contact efficiency of ozone and sludge to reduce the sludge and high-efficiency ozone dissolving device and micro bubbles The present invention provides a sludge reduction device using ozone.

The high-efficiency ozone dissolving device and the sludge reduction device using microbubble ozone of the present invention include: a sludge storage tank into which excess sludge generated in a precipitation tank is mixed with an acid supplied from an acid storage tank; An ozone dissolving tank in which the sludge discharged from the sludge storage tank and the ozone supplied from the ozone generator are pressurized by a sludge circulation pump to be introduced, and an ozone-sludge mixture in which ozone is dissolved in the sludge is formed; A sludge solubilization tank for introducing the ozone-sludge mixed solution discharged from the ozone melting tank to pass through the microbubble generating device and to super-saturate ozone in the form of microbubbles to slowly rise the solubilization of the sludge; And a solubilized sludge storage tank in which the sludge solubilized in the sludge solubilization tank is discharged and stored. Characterized in that it comprises a.

The acid storage tank is characterized in that the sulfuric acid is added to the excess sludge at a rate of 0.010 ~ 0.050 N.

The ozone tank is characterized in that the supply path through which the sludge flows is bent vertically from the inside of the ozone tank to the ground, and the impingement plate is further provided at its end perpendicular to the longitudinal direction of the supply path.

The sludge solubilization tank is characterized in that the inorganic sludge collecting device for collecting and discharging the inorganic sludge further below.

The sludge solubilization tank further comprises a solubilization tank recirculation apparatus for injecting the ozone-sludge mixture in the sludge solubilization tank to the upper part of the sludge solubilization tank in order to reduce bubbles generated on the water surface.

The solubilization tank recirculation apparatus is characterized in that it comprises a recycle pump for circulating the ozone-sludge mixture and a nozzle for injecting the ozone-sludge mixture circulated by the recycle pump is provided on the upper part of the sludge solubilization tank.

The microbubble generating device is characterized in that the ozone-sludge mixture supplied from the ozone melting tank passes through the ventry tube and generates microbubbles by shear force.

The sludge reduction apparatus according to the present invention has the effect of reducing the amount of ozone injected by injecting acid into the excess sludge and reducing bubbles generated in the sludge solubilization tank by the injection of acid.

In addition, it has the effect of greatly improving the dissolution efficiency of ozone to sludge flowing into the ozone melting tank pressurized by 2.5 ~ 3kgf / cm ² by the sludge circulation pump. By increasing the contact efficiency of the sludge, there is an effect of preventing the discharge of waste ozone into the atmosphere and reducing the sludge.

Hereinafter, with reference to the accompanying drawings, a high-efficiency ozone dissolving device and a sludge reduction device using micro-bubble ozone of the present invention as described above will be described in detail.

1 is a conceptual view showing a sludge reduction apparatus of the present invention, Figure 2 is a cross-sectional view and a perspective view showing an ozone dissolving tank of the present invention, Figure 3 is a cross-sectional view and a perspective view showing a sludge solubilizing tank of the present invention, Figure 4 5 is a cross-sectional view and a perspective view of the microbubble generator according to the present invention, and FIG. 5 is a table illustrating changes in dissolved oxygen concentrations of the microbubble generator and the acidic stones, and FIG. 7 is a table showing a change in the concentration of COD _Mn according to the ozone contact time, Figure 8 is a table showing a change in the concentration of MLSS according to the ozone injection amount, Figure 9 is a concentration of MLSS according to ozone treatment after acid addition to the sludge 10 is a table showing the change in the amount of waste ozone generation according to the ozone injection concentration, Figure 11 is a BOD ₅ removal by applying the sludge reduction device of the present invention It is a table which shows the change of efficiency, and FIG. 12 is a table which shows the change of nitrogen removal efficiency by applying the sludge reduction apparatus of this invention.

1 to 4, the sludge storage tank 10 is mixed with the acid supplied from the acid storage tank 20, the excess sludge generated in the settling tank (not shown); The sludge discharged from the sludge storage tank 10 and the ozone supplied from the ozone generator 40 are pressurized by the sludge circulation pump 30, and the ozone melting tank in which the ozone-sludge mixed solution in which ozone is dissolved is formed in the sludge. 50; A sludge solubilization tank (60) for introducing the ozone-sludge mixed solution discharged from the ozone dissolution tank (50) to pass through the microbubble generating device (70) to supersaturate ozone and to rise slowly while solubilizing the sludge; And a solubilized sludge storage tank 100 in which the sludge solubilized in the sludge solubilization tank 60 is discharged and stored. It is made, including.

The excess sludge produced in the sedimentation tank through a general wastewater treatment process (such as anaerobic tank, anoxic tank and aeration tank) is mixed with sulfuric acid (H ₂ SO ₄ ) supplied from the acid storage tank 20 and introduced into the sludge storage tank 10. In this case, sulfuric acid is added at a rate of 0.010 to 0.050 N, and the amount of sulfuric acid may be changed according to the concentration of excess sludge, so that the pH-meter (not shown) in the sludge storage tank is adjusted to adjust the amount of acid. When the acid is added to the excess sludge as described above, the amount of ozone consumed by the self-decomposition is reduced, and the foam generated in the sludge solubilization tank 60 is reduced.

The sludge stored in the sludge storage tank 10 is introduced into the ozone melting tank 50 by the sludge circulation pump 30, and at this time, the ozone generator 40 connected to the supply path 32 in front of the sludge circulation pump 30 is generated. Ozone is naturally introduced into the ozone melting tank 50 by the pressure difference. As described above, ozone generated in the ozone generator 50 is introduced into the ozone melting tank 50 due to the pressure difference, so that no additional pressure means is required. As shown in FIG. 2, the ozone melting tank 50 is supplied with a sludge circulation pump 30 to increase dissolution efficiency of sludge and ozone introduced into the ozone melting tank 50 along the supply path 32. 32 is bent toward the ground inside the ozone melting tank 50, and a collision plate 52 is formed perpendicularly to the longitudinal direction of the supply passage 32 at a distance from the end of the supply passage 32. . The impingement plate 52 is preferably formed in accordance with the injection area of the sludge and ozone injected from the end of the supply passage 32, and the distance from the end of the supply passage 32 is preferably different depending on the injection pressure. Sludge and ozone injected from the end of the supply path 32 by the sludge circulation pump 30 hit the impingement plate 52 to increase the contact efficiency between the ozone and the sludge, and also inside the ozone melting tank 50 Since the pressure is pressurized by about 2.5 to 3.0 kgf / cm ² by the sludge circulation pump 30, the dissolution efficiency of ozone can be further increased. Due to the ozone dissolution tank 50 of the above structure, ozone is present in the form of a total dissolved in the sludge, and thus the treated ozone-sludge mixture is in a sludge solubilizing tank in a completely liquid form (ozone is supersaturated) (60). ) Will be supplied.

The ozone-sludge mixed liquid formed in the ozone melting tank 60 flows into the sludge solubilization tank 60 through the supply passage 54 and passes through the microbubble generator 70 at the end of the supply passage 54 in the sludge. The supersaturated ozone gas is microbubbled and ejected into the sludge solubilization tank 60. Ozone microbubble through the microbubble generating device 70 is delayed as much as possible to the surface of the water, the unreacted ozone reacts with the sludge. The microbubble generating device 70 is formed of a ventrile tube 72 having a narrow cross-sectional area at its central portion, so that the ozone-sludge mixed liquid supplied from the ozone melting tank 50 passes through the ventrile tube 72 to the shear force. This causes microbubbles. The ozone-sludge mixed liquid supplied from the ozone melting tank 50 passes through the microbubble generating device 70 and the passage is momentarily narrowed due to the ventry tube 72 to increase the flow rate, and the flow rate at the opening 72a is again increased. A negative pressure flow 76 is formed at the front end of the ozone-sludge mixed liquid 74 which is slowed and rapidly progresses as shown in FIG. 4, and as a result, a shear force is generated so that a gas (ozone) supersaturated in the ozone-sludge mixed liquid is a liquid (sludge). It is separated from the fine bubbles are formed. As described above, when the micro bubble generator 70 using the ventry tube 72 is applied, sufficient microbubbles are generated even when the minimum diameter of the ventry tube 72 is increased, thereby reducing clogging caused by foreign substances. There is. As the ozone-sludge mixture is microbubbled by the microbubble generator 70, the contact area of unreacted ozone is expanded to prevent the discharge of waste ozone into the atmosphere, and when the ozone-sludge mixture is microbubbled, Together with this, other unnecessary gases contained in the sludge are degassed. When the gas is dissolved in the deaerated sludge, the solubility of the gas is increased, so that ozone gas may be easily dissolved in the sludge.

The microbubble generator 70 as described above is provided in the lower portion of the sludge solubilization tank 60 to be substantially parallel to the inner wall surface, so that the microbubble mixed liquid ejected from the microbubble generator 70 is sludge as shown in FIG. 3. It is desirable to allow the unreacted ozone to react with the sludge by turning along the inner wall of the solubilization tank and allowing it to float to the surface to delay the injury time to the maximum. Since the microbubble mixed liquid ejected from the microbubble generating device 70 floats and floats along the inner wall surface of the sludge solubilization tank 60, air is not formed in the central part, so that the heavy inorganic matter contained in the sludge moves downward. It is discharged to the outside by the sludge collection device (90).

In addition, the sludge solubilization tank 60 is provided with a solubilization tank recirculation device 80 for removing bubbles generated on the water surface. The solubilization tank recirculation apparatus 80 is provided on the recirculation pump 82 for circulating the ozone-sludge mixed liquid in the sludge solubilization tank 60 and the sludge solubilization tank 60 and supplied by the recirculation pump 82. And a nozzle 84 for radially spraying the ozone-sludge mixture. Since the ozone-sludge mixture is sprayed radially toward the bubbles generated on the water surface through the nozzles 84, bubbles are prevented from being formed.

The solubilized sludge is discharged from the sludge solubilization tank 60 through the above process is made to flow into the solubilized sludge storage tank 100 and the cycle is completed.

As described above, when ozone is used in the sludge reduction apparatus, it is impossible to confirm accurate dissolution efficiency due to the self-decomposition of ozone and ozone reacted by organic substances in water. Therefore, the results of dissolution efficiency experiment using oxygen are described as follows. FIG. 5 shows changes over time of DO (dissolved oxygen) concentrations when a certain amount of air is supplied to water using an acid stone (AS: air stone) and a microbubble moudle (MB). In the case of acidite, DO of about 0.73 mg / L was increased in the first 10 minutes at 10 mL / min air flow. On the other hand, in the case of the microbubble generating device, the DO increased by 1.97 mg / L for the first 10 minutes at 10 mL / min of air flow rate, indicating a DO increase of about 2.7 times higher than that of acid stone. In the case of increasing the air flow rate to 100 mL / min, it can be seen that the DO increase amount was increased by 3.7 times to 1.95 mg / L in the mountain stone and 7.29 mg / L in the microbubble generator.

Figure 6 shows the results of measuring the amount of waste ozone generated after injecting ozone using tap water to the reactor to determine the degree of ozone dissolution when using the acid stone and micro bubble generator. Experimental results using an acid stone, a microbubble generator (70), a microbubble generator (70), and an ozone melting tank (50) were compared with the injected gaseous ozone concentration of 161g O ₃ / m ³ . In case of using acid stone, the occurrence of waste ozone occurred at 15.4 mg / L 2 minutes after the start of ozone injection, and it increased sharply thereafter to 55.7 mg / L 11 minutes after the injection. In the case of using the microbubble generator 70, the waste ozone generation amount was 1.7 mg / L after 2 minutes of ozone injection, and the concentration of waste ozone was increased to 43.2 mg / L after 11 minutes. When the microbubble generator and ozone lysis tank were used at the same time, waste ozone was generated at a concentration of 1.5 mg / L after 2 minutes of ozone injection, and the amount of waste ozone was rapidly increased from 6 minutes after the start of the experiment. As such, when the microbubble generator is used, the amount of waste ozone can be rapidly reduced, and it can be seen that most of the injected ozone can be used for oxidizing organic substances. In addition, when the concentration of organic matter in the water it can be seen that the use of a micro bubble generator than the case of using a general acid stone is a way to increase the absorption efficiency of ozone.

Figure 7 shows the change of TCOD _Mn and SCOD _Mn with ozone contact time for the gas phase ozone injection concentration 150g O ₃ / m ³ . As the amount of ozone is increased, it can be seen that the SCOD (soluble COD) increases with the decrease of TCOD (total COD). In general, the amount of soluble COD may vary depending on the amount of ozone injected, and SCOD increases up to 20-30% of total COD removal, but SCOD _Mn increases by about 60% based on 1 hour of reaction time in the present invention. I could confirm that. It is believed that this result is because the present invention simultaneously causes physical decomposition by microbubbles together with chemical reaction by ozone. Since the increased SCOD is mostly removed by microorganisms when it enters the bioreactor, it can be expected that the effect will be even greater when the ozone treatment device is combined with biotreatment.

Figure 8 shows the concentration change of SS (Suspended Solids) according to the ozone injection rate. Assuming that the ozone dose for the mixed liquor suspended solids (MLSS) is the same and that all the injected ozone is consumed for sludge oxidation, the initial MLSS concentration of 6,447 mg / L is 4,658 mg at 0.1 g O ₃ / g MLSS. The decrease in / L resulted in a decrease of 1,789 mg / L, whereas the initial MLSS concentration decreased to 3,180 mg / L to 2,075 mg / L, resulting in a decrease of 1,105 mg / L. In the case of the lower initial concentration of 515 mg / L is expected to be about 371 mg / L at 0.1 g O ₃ / g MLSS ozone injection rate, the difference can be seen that only a decrease of 144 mg / L. From the above results, it can be seen that as the initial concentration of MLSS increases, the concentration change range increases much.

Figure 9 shows the change in the concentration of MLSS when not pretreated with acid and when sulfuric acid was injected and pretreated with sulfuric acid concentrations of 0.010 N, 0.025 N and 0.050 N, followed by ozone treatment. Comparing the case of pretreatment with acid and the case of no pretreatment, it can be seen that the treatment efficiency of MLSS is significantly higher when the pretreatment with acid is carried out. It can be seen that the removal rate is slightly high, and in the case of 0.025 N and 0.050 N, there is almost no difference or rather 0.025 N has a high treatment efficiency. Therefore, the concentration of sulfuric acid was determined to be less effective in improving the removal rate of MLSS compared to the concentration of acid injected at 0.025 N or more. In the present invention, the concentration of sulfuric acid was determined to be 0.025 N.

Next, as an experimental result of the waste ozone generation amount, Figure 10 is the result of the change in the waste ozone generation amount according to the ozone injection concentration in the sludge with the MLSS concentration of about 5,000 mg / L. Waste ozone was hardly generated in this experiment, and it was partially generated at the end of the experiment, but the amount was less than 0.1% of the injected ozone amount. As such, when ozone is injected using microbubbles during ozone oxidation, it can be seen that ozone contact efficiency can be maximized while minimizing waste ozone generation.

The following shows the demonstration plant operation result of combining the sludge reduction apparatus of the present invention with the biological treatment process. The biotreatment process (not shown) consisted of anaerobic tank, anaerobic tank, and aerobic tank on a scale of 15 m ³ / day, and the sludge reduction apparatus was configured with the sludge reduction apparatus of the present invention described above. The biotreatment process was 150% for internal circulation and 50% for external circulation. Soluble amount of sludge, that is, solubilization of excess sludge, was solubilized about 3 times the actual amount generated, and the solubilized sludge was recycled to an oxygen-free tank. In order to examine the effect of the biological treatment process due to recycling of the solubilized sludge, the biotreatment was operated alone for four months after the start of operation. The single operation of the biotreatment process was operated from May 1 to August 31, 2007. Since September 1, 2007, the excess sludge is reduced and solubilized by using microbubble ozone and recycled to an anoxic tank. It was operated with a surplus sludge discharge device that did not draw out.

Figure 11 shows the change in the removal efficiency of BOD5, the average BOD ₅ concentration of the influent was 97.6 mg / L in the case of the effluent showed 2.4 to 14.9 mg / L, 7.2 mg / L, the average removal rate of 92.5%. . Even when the biotreatment was operated alone for four months from May to August 2007, the treatment was stable compared to the large fluctuations in the influent. From September to December, when ozone treatment began to discharge the sludge, From the results, it was confirmed that the BOD ₅ concentration of the treated water was stable. Therefore, it is believed that BOD ₅ can be treated stably in the biological treatment process even in long-term operation without sludge discharge through solubilization of excess sludge by ozone.

Figure 12 shows the change in the removal efficiency of TN, the average TN concentration of the influent was 31.4 mg / L TN concentration of the treated water was up to 12.6 mg / L, minimum 5.4 mg / L, average 8.6 mg / L The removal rate was 71.7% on average. In the case of T-N, the average removal rate of T-N was 69.2% in the biotreatment alone, but the removal rate of T-N increased to 75.1% after solubilizing excess sludge by ozone treatment and using it as a carbon source for denitrification.

1 is a conceptual diagram showing a sludge reduction apparatus of the present invention.

Figure 2 is a sectional view and a perspective view of the ozone melting tank of the present invention.

Figure 3 is a sectional view and a perspective view showing a sludge solubilization tank of the present invention.

Figure 4 is a sectional view and a perspective view showing a microbubble generating device of the present invention.

Figure 5 is a table showing the dissolved oxygen concentration change of the micro bubble generator and acid stone.

Figure 6 is a table showing the ozone absorption efficiency change of the micro bubble generator and acid stone.

7 is a table showing a change in CODmn according to the ozone contact time.

8 is a table showing a change in concentration of MLSS according to the ozone injection amount.

9 is a table showing a change in the concentration of MLSS according to ozone treatment after sulfuric acid in the sludge.

10 is a table showing the change in the amount of waste ozone generated according to the ozone injection concentration.

11 is a table showing a change in BOD5 removal efficiency by applying the sludge reduction apparatus of the present invention.

12 is a table showing a change in nitrogen removal efficiency by applying the sludge reduction apparatus of the present invention.

** Description of the symbols for the main parts of the drawings **

10: sludge storage tank 20: acid storage tank

30: sludge circulation pump 40: ozone generator

50: ozone melting tank 52: collision plate

60: sludge solubilization tank 70: fine bubble generator

80: solubilization tank recirculation device 82: recirculation pump

84: nozzle 90: inorganic sludge collector

100: solubilized sludge reservoir

Claims (7)

Sludge storage tank 10, the excess sludge generated in the settling tank is mixed with the acid supplied from the acid storage tank 20 to be introduced; The sludge discharged from the sludge storage tank 10 and the ozone supplied from the ozone generator 40 are pressurized by the sludge circulation pump 30, and the ozone dissolving tank in which the ozone-sludge mixed liquid in which ozone is dissolved is formed in the sludge ( 50); A sludge solubilization tank (60) for introducing the ozone-sludge mixed solution discharged from the ozone dissolution tank (50) to pass through the microbubble generating device (70) to supersaturate ozone and to rise slowly while solubilizing the sludge; And Solubilized sludge storage tank 100 in which the solubilized sludge is discharged and stored in the sludge solubilization tank 60; The ozone melting tank 50 has a supply path 32 through which the sludge flows is bent vertically in the ozone melting tank 50 toward the ground, and at the end thereof, a collision plate is perpendicular to the longitudinal direction of the supply path 32. 52 is further provided, The sludge solubilization tank 60 is further provided with an inorganic sludge collection device 90 for collecting and discharging inorganic sludge in the lower portion and an ozone-sludge mixed liquid recirculation pump 82 to reduce bubbles generated on the water surface. The microbubble generating device 70 is formed of a ventry tube 72 having a narrow cross-sectional area at the center thereof, and has a lower portion inside the sludge solubilization tank 60 in order to delay the floating time to the maximum so that unreacted ozone reacts with the sludge. A high-efficiency ozone dissolving apparatus and micro-bubbles, which are provided on the inner wall side so that the micro-bubble mixture liquid ejected from the micro-bubble generating device 70 rotates along the inner wall of the sludge solubilization tank 60 and floats on the water surface. Sludge reduction device using ozone. The method of claim 1, The acid storage tank 20 is a high-efficiency ozone dissolving apparatus and a sludge reduction apparatus using micro-bubble ozone, characterized in that the sulfuric acid is added to the excess sludge at a rate of 0.010 ~ 0.050 N. delete delete delete delete delete

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