KR100242666B1 - Water purifying plant - Google Patents

Abstract

The present invention relates to a water treatment system capable of purifying industrial wastewater and leachate while supplying ozone and air to a photocatalytic oxidation reaction tank composed of a TiO ₂ catalyst prepared by UV and slipcasting.

The purified water treatment system of the present invention includes a pump for pumping a leachate containing contaminants into a reservoir, a pump for pumping leachate containing contaminants in the reservoir, and a leachate containing contaminants in the storage tank by driving the pump. A reaction tank for purifying the leachate, an air supply means for injecting air into the reaction tank to promote purification during a photocatalytic oxidation reaction, an air pump for pumping air, and air supplied according to the operation of the air pump. The ozone generated by the ozone generator with respect to a drying chamber to receive, the ozone generator for receiving the air dried in the drying chamber to generate ozone to supply ozone to the reaction tank, and the air introduced by the operation of the air pump The ozone concentration calculation / indicator that calculates and displays the concentration at the same time, and controls the overall operation. It is characterized by being a control means.

Description

Water treatment system

The present invention relates to a water purification system for decomposing various organic contaminants present in an aqueous solution. More specifically, the present invention relates to ozone and a photocatalytic oxidation tank composed of an ultraviolet (10) and a TiO ₂ catalyst (20) prepared by a slip casting method. The present invention relates to a water treatment system capable of purifying industrial wastewater and leachate while supplying air.

The purification process of various organic pollutants occurring in nature can be started by the decomposition of organic pollutants by sunlight and proceed to the reaction that ultimately produces carbon dioxide (CO ₂ ) and inorganic substances. In this process, natural sensitizers play a role in accelerating the decomposition of these organic pollutants. In the 1970s, since metal oxide semiconductors proved to accelerate the process of natural purification by sunlight, UV light was applied to semiconductors such as ZnO or TiO ₂ to decompose various organic contaminants in aqueous solutions. The importance of photocatalytic oxidation is emerging.

A band-gap energy model is generally used to explain the mechanism of contaminant oxidation in aqueous solutions using semiconductor catalysts in photocatalytic (TiO ₂ ) oxidation. In semiconductors absorbing light energy above the band-gap energy, holes and electrons are generated by charge separation between the valence band and the conduction band (Equation 1), and two kinds of oxidation reactions proceed. The first oxidation reaction is an electron transfer reaction (Equation 2) of the adsorbent material, the second oxidation reaction formula (3) and (4) the receiving material absorption, such as ^in-the electron transfer reaction of (H ₂ O and HO) . Since most of the substances adsorbed on the surface of the catalyst 10 have high concentrations of H ₂ O and HO ^{− in} the aqueous solution, the second oxidation process of the contaminants plays an important role. In addition, oxygen (O ₂ ), which appears in all oxidation processes, acts as an electron acceptor that causes an electron transfer reaction (Equation 5) from the conduction band.

^{_{TiO 2 → TiO 2 (e -}} + h +) ⑴

^{_{TiO 2 (h +) + RX}} ad → TiO 2 + RX + · ad ⑵

TiO ₂ (h ⁺ ) + H ₂ O _ad → TiO ₂ + HO ^, _ad + H ⁺ ⑶

^{_{TiO 2 (h +) + HO}} - ad → TiO 2 + HO · ad ⑷

^{_{TiO 2 (e -) + O}} 2 → TiO 2 + O 2 - · ⑸

In the oxidation of ozone and H ₂ O ₂ , ozone (O ₃ ) is much more powerful than the oxidizing agent commonly used in water treatment plants, and was first used in France in 1907 for sterilization of purified water in Europe and the United States. It is widely used. Recently, attention has been paid to the treatment of hardly degradable organic pollutants that are not treated by conventional treatment processes. Ozone molecules and additional role is very reactive hydroxyl radicals that contribute to the oxidation reaction (OH˙), superoxide radical ion as a strong oxidizing agent should not cause contamination to the direct reaction present in the aqueous phase (O ₂ ^- ˙) ozone radical not ion to produce a ^{- -} (˙ HO _2), hydrogen peroxide _{(H 2 O 2) (O} 3 ˙), buffer hydroxyl radical not ions. Table 1 shows the decomposition mechanism of ozone.

Ozone decomposition reaction Initiation stage ^{_{O 3 + OH - → HO 2}} + O 2 - HO 2 ↔O 2 - + H + Delivery stage ^{_{O 3 + O 2 - → O}} 3 - + O 2 O 3 - + H + ↔HO 3 HO 3 → OH + O 2 OH + O 3 → HO 4 HO 4 → HO 2 + O 2 Termination stage HO ₄ + HO ₄ → H ₂ O ₂ + 2O ₃ HO ₄ + HO ₃ → H ₂ O ₂ + O ₃ + O ₂

Common initiators in aqueous solution are OH ^- and H ₂ O ₂ and ultraviolet light (10), which serves to increase OH˙, are called promoters, and react with OH˙ to form other types of substances. Formation is called an inhibitor. In general, substances such as HCO ₃ and CO ₃ ^2- react with OH˙ to inhibit the decomposition of ozone.

Oxidation processes that decompose contaminants in aqueous solutions using photocatalysts, ozone and H ₂ O ₂ can be applied to the following water treatment applications: First, the field of ultrapure water production may be mentioned. Previously, the application of photocatalytic oxidation to water treatment meant the removal of toxic or groundwater contaminants from groundwater. However, it may be applied to a process for producing ultrapure water required in some industrial fields, especially semiconductor manufacturing, pharmaceuticals, and power plants. Second, the field where the photocatalytic oxidation reaction can be easily applied is the domestic water purification field that can produce the amount of 10-20L needed for drinking water at home per day. This method has been considered to be sufficiently economical when compared to activated carbon filtration or reverse osmosis systems, especially for photocatalytic oxidation of trihalomethanes (PCMs), polychlorinated biphenyls (PCBs), pesticides, and herbicides in household water. This will reduce the concentration of these pollutants. Third, although economical processes have been developed to treat industrial wastewater in the industrial wastewater treatment field, it would be sufficient as an alternative process if the existing processes were improved to proceed with faster oxidation without the addition of lower power costs and chemical oxidants.

The reason why TiO ₂ is widely used as a semiconductor material in photocatalytic oxidation that decomposes organic pollutants by irradiating ultraviolet rays to semiconductors is because TiO ₂ is non-toxic and has insolubility. However, some problems may arise if such insoluble semiconductor particles are used directly to remove contaminants in aqueous solutions. In particular, in order to continuously treat the incoming contaminants, additional energy is required for resuspension of the semiconductor particles in the aqueous solution, and a new process for separating semiconductor particles as a subsequent water treatment process is desired.

In addition, in order to make the photocatalytic oxidation practical, when the fixed bed catalyst is compared with the suspended bed catalyst of the same weight, the decomposition efficiency of the material to be treated decreases due to the decrease of the active point at which the photocatalytic oxidation occurs, and the hydroxyl radical (OH˙) The presence of anions or cations known as carriers interferes with photocatalytic oxidation.

In particular, a large amount of metal components in the water is adsorbed on the surface of the photocatalyst serves to block the light. Since most of the wavelength of light as an energy source for photocatalytic oxidation occurs in the region of 300 nm or more, when using sunlight as an energy source, only about 5% of sunlight is available, so an efficient system for generating ultraviolet rays is desired.

Accordingly, the present invention has been made in view of the various problems described above, and in view of the various circumstances described above, and an object of the present invention is to oxidize the photocatalyst 20 by ultraviolet irradiation 10 and the TiO ₂ semiconductor catalyst 20. An object of the present invention is to provide a water treatment system that can easily purify industrial wastewater and leachate.

It is another object of the present invention to provide a water treatment system capable of decomposing hardly degradable contaminants to purify industrial wastewater and leachate.

It is another object of the present invention to provide a water treatment system capable of efficiently purifying industrial wastewater and leachate.

In order to achieve the above object, the water treatment system according to an embodiment of the present invention includes a storage tank 60 into which leachate containing contaminants flow and a pump for pumping leachate containing contaminants in the storage tank 60 ( 50), a reaction tank 30 which receives leachate containing contaminants in the storage tank 60 by the driving of the pump 50 and purifies the leachate, and in the reaction tank to promote purification during the photocatalytic oxidation reaction. An air supply means 96 for injecting air, an air pump 6 for pumping air, a drying chamber 43 for drying the air supplied according to the driving of the air pump 6, and the drying chamber ( 43 is generated in the ozone generator 40 for ozone generator 40 receiving ozone dried in the air and supplying ozone to the reaction tank and air introduced by driving the air pump 6. Old And also it calculates the concentration of the ozone concentration at the same time calculation / display apparatus 100 for displaying, characterized by being a control means 59 that controls the entire operation.

1 is a schematic configuration diagram of a water treatment system using a combination process of ozone and H ₂ O ₂ and a photocatalyst (TiO ₂ ) oxidation according to an embodiment of the present invention;

2 is a cross-sectional view of the photocatalytic oxidation tank of FIG.

Figure 3 is a graph showing the TCE residual rate (%) with respect to the elapsed treatment time when the distilled water is treated using the water treatment system of the present invention,

Figure 4 is a graph showing the TCE residual rate (%) with respect to the time elapsed when the raw water per arm using the purified water treatment system of the present invention,

5 is a graph showing the TOC residual rate (%) with respect to the elapse of the treatment time when the raw water per arm using the purified water treatment system of the present invention,

6 is a graph showing absorbance at a wavelength of 254 nm when raw water per arm was treated using the water treatment system of the present invention.

7 is a graph showing the percent TCE retention (%) when the H ₂ O ₂ concentration is 50 mg / L using the water treatment system of the present invention.

8 is a graph showing the percent residual TCE (%) when the H ₂ O ₂ concentration is 100mg / L using the water treatment system of the present invention,

9 is a graph showing the percent TCE retention (%) when the H ₂ O ₂ concentration is 500 mg / L using the water treatment system of the present invention.

* Explanation of symbols for main parts of the drawings

6: air pump 10: UV lamp

20: TiO ₂ catalyst 30: reactor

31: Pyrex 43: drying chamber

40: ozone generator 50: pump

59: control means 60: storage tank

83: KI solution 96: air supply means

100: ozone concentration calculation / indicator

Hereinafter, a water treatment system according to an embodiment of the present invention will be described with reference to the accompanying drawings.

1 is a schematic diagram of a water treatment system using a combination of ozone, H ₂ O _2, and a photocatalyst 20 (TiO ₂ ) oxidation reaction according to an embodiment of the present invention, and FIG. 2 is a photocatalyst of FIG. 1. It is sectional drawing of an oxidation tank.

As shown in Figure 1 and 2, the water treatment system according to an embodiment of the present invention is a storage tank 60 to which leachate containing contaminants flow, and leachate containing contaminants in the storage tank (60) When the pump 50 for pumping, the reaction tank 30 for receiving the leachate containing contaminants in the storage tank 60 by the driving of the pump 50 to purify the leachate, and the photocatalyst 20 during the oxidation reaction An air supply unit 96 for injecting air into the reaction tank to promote purification, an air pump 6 for pumping air, and a drying chamber for drying air supplied in accordance with driving of the air pump 6 43), the ozone generator 40 which receives the air dried in the drying chamber 43 and generates ozone to supply ozone to the reaction tank, and the air introduced by driving the air pump 6 Generated from the ozone generator 40 It is made of the ozone concentration calculation / display apparatus 100, and a control means 59 that controls the entire operation of displaying and simultaneously calculates the concentration of ozone.

In the above description, the reactor 30 is a cylindrical pyrex 31, a plurality of catalysts 20 are installed along the longitudinal direction on the inner circumferential surface of the pyrex 31 to promote the purification of leachate, and the pyrex Ultraviolet lamps (10) provided at the center and the outer side of the (31), respectively, to apply ultraviolet light (10) to the leachate, the ultraviolet lamp (10) provided at the center of the Pyrex (31) and the inner surface of the cylindrical pyrex (31) It consists of a reaction space that is formed by the reaction between the leachate and the leachate while passing through the leachate, and the leachate is purified, the catalyst 20 used in the present invention is using TiO ₂ , the reactor 30 is contaminated and leachate containing substances, ozone, and H ₂ O ₂ and the photocatalyst of claim (20) (TiO ₂₎ is configured to be supplied.

Next, operations and effects of the water purification apparatus according to the embodiment of the present invention configured as described above will be described.

First, the leachate containing contaminants is introduced into the storage tank 60, and the leachate introduced into the storage tank 60 receives the leachate containing contaminants in the storage tank 60 according to the driving of the pump 50. Pump into. Leachate introduced into the reaction vessel 30 supplies air from the air supply means 96 to promote purification during the photocatalyst 10 oxidation reaction.

In the drying chamber 43, the air introduced by the operation of the air pump 6 is dried, supplied to the ozone generator 40, the ozone is generated and supplied into the reaction tank 30, and the air pump 6 is driven. To the ozone concentration calculation / indicator 100.

The ozone concentration calculation / indicator 100 receives ozone generated from the ozone generator 40 and compares it with the air supplied by the driving of the air pump 6 to calculate and display the ozone concentration.

The driving of the pump 50, the air pump 6, the ozone concentration calculation / indicator 100 and the ozone generator 40 is controlled by the control means 59 which controls the overall operation of the system. 2 is a cross-sectional view schematically showing the reaction tank 30 used for the photocatalyst 20 oxidation reaction used in the present invention, in which the TiO ₂ catalyst 20 is mounted vertically. Leachate introduced into the reaction tank 30 receives the air introduced from the air supply means 96 and the ultraviolet ray 10 and TiO ₂ irradiated from the ultraviolet ray lamp 10 by receiving ozone from the ozone generator 40. The leachate is purified by oxidation of the photocatalyst 20 together with the catalyst 20 agent.

3 is a time when the catalyst was applied 0.98mL / cm ² and containing 1mg O ₃ / L to flow the air in the ozone concentration in the air in a 1L / min, the catalyst in distilled water (TiO ₂₎ with ozone and ultraviolet radiation TCE (trichloroethylene, hereinafter referred to as TCE) according to the residual rate (curve a), when ozone is added to distilled water only, the residual TCE (curve b) with time, reaction with ultraviolet (TiO ₂ ) The TCE residual ratio (curve c) when it is made and the TCE residual ratio (curve d) when not controlled are shown. 4 shows that the catalyst (10) contained 0.98 mL / cm ² and flowed at a rate of 1 L / min of air at an ozone concentration of 1 mg O ₃ / L air, and the catalyst (TiO ₂ ), ozone, and ultraviolet light were added to the raw water. TCE residual ratio (curve a) over time, TCE residual ratio (curve b) over time when ozone was added only to Paldang, and TCE residue when reacted with ultraviolet rays and catalyst (TiO ₂ ) The rate (curve c) is shown.

FIG. 5 shows that the catalyst 10 contains 0.98 mL / cm ² and the catalyst (TiO ₂ ), ozone and ultraviolet rays were added to Paldang water by flowing air at a rate of 1 L / min at an ozone concentration of 1 mg O ₃ / L air. In the case of TOC (Total Organic Carbon, hereinafter TOC), the residual ratio (curve a), the TOC residual ratio (curve b) over time if only ozone is added to Paldang, and the UV and catalyst When reacted with TiO ₂ ), the TOC residual rate (curve c) is shown.

6 is a catalyst, if applied and 0.98mL / cm ² and containing 1mg O ₃ / L in an ozone concentration in the air flow the air into a 1L / min to the catalyst in raw water Paldang (TiO ₂₎ with ozone and ultraviolet radiation 6.254nm Absorption (curve a) over time, 6.254 nm when ozone was added only to Paldang, and absorbance (curve b) over time, when reacted with ultraviolet light and catalyst (TiO ₂ ) at Paldang The absorbance (curve c) with progress is shown.

7 is pre-fed for 10 minutes and air to the H ₂ O ₂ when the concentration of H ₂ O ₂ was used to 50mg / L, and while the catalyst containing 0.98mL / cm ² H ₂ O ₂ and UV light and residual catalyst TCE The ratio (curve a), TCE residual ratio (curve b) for H ₂ O ₂ when only ultraviolet light is used, and TCE residual ratio (curve c) for H ₂ O ₂ when ultraviolet light and catalyst are used are shown.

8 is previously supplied air for 10 minutes and the concentration of H ₂ O ₂ 100mg / L and TOC Residual H ₂ O ₂ for containing the catalyst, while when 0.98mL / cm ² using H ₂ O ₂ and UV light and catalyst rate (curve a), UV and H ₂ O when using ₂ TOC residual rate of the H ₂ O ₂ (curve b), when using an ultraviolet and catalyst TOC residual rate of the H ₂ O ₂ (curve c) Indicates.

FIG. 9 shows TCE residual for H ₂ O ₂ when H ₂ O ₂ and UV and a catalyst were used while supplying air for 10 minutes in advance, the concentration of H ₂ O ₂ was 500 mg / L, and the catalyst contained 0.98 mL / cm ² . rate (curve a), UV and H ₂ O when using ₂ TCE residual ratio of the H ₂ O ₂ (curve b), when using an ultraviolet and catalyst TCE residual ratio of the H ₂ O ₂ (curve c) Indicates.

The TiO ₂ catalyst 20 used in the water treatment system of the present invention used a catalyst 20 prepared by the TiO ₂ slipcasting method having a composition as shown in Table 2, wherein the TiO ₂ catalyst 20 TiO ₂ sol was coated to increase the surface area. In order to obtain a suitable strength, porosity, and microstructure as the TiO ₂ photocatalyst 20, the TiO ₂ slip formed was dried at room temperature for 24 hours, and then heated at a rate of 1 ° C./min up to 500 ° C., and 2 ° C./min up to 1000 ° C. After heating up at a rate of presintered for 2 hours. The apparent porosity of the prepared TiO ₂ catalyst 20 was 42.3% and the specific surface area was 79 m ² / g. In addition, after the TiO ₂ sol is titanium isopropoxide _{[Ti (OC 3 H 7)} ] was added to the secondary distilled water and nitric 1080㎖ 7㎖ the 90㎖ adjusted to pH 1 using the surface coating of TiO ₂ slip them Prepared by stirring for 3 days. In order to obtain a suitable pH for the coating ammonia water was added to the final pH of the sol was 1.45.

Main composition of TiO ₂ slip Item Starting material TiO ₂ Powder water Davan-c PVA Composition (wt%) 49.8 49.8 0.24 0.16 Source YAKURI Chem. Co. (Yakuri Chemical Co., Ltd., high purity product) Particle diameter: 0.2㎛ Distilled water R.T. Banderbit company (R.T.VanderbitCo.) Wako Pure Chemical Co., Ltd. (WAKOPure Chem.Co.)

In addition, this study conducted the experiment by selecting ozone and H ₂ O ₂ to efficiently use photocatalyst (20) oxidation reaction for the treatment of hardly degradable pollutants. The photocatalyst (20) oxidation reaction and ozone combined process experiment was largely carried out using distilled water and Paldang raw water as solvents, and by injecting TCE into this, oxidation reaction by ozone, photochemical reaction using photocatalyst (20) and both In the case of using a combination of the TCE decomposition efficiency was compared. In addition, the degree decomposition at the time when the combined process experiment with H ₂ O ₂ by varying the concentration of H ₂ O ₂ to 50, 100, 500 ㎎ / L equipped with a degradation degree and the photocatalyst 20 of TCE in accordance with the respective concentrations Was compared.

Hereinafter, the configuration and operation of the present invention will be described in detail by way of examples.

Example 1 Combined Process of Photocatalyst 10 and Ozone

This experiment was divided into experiments in which TCE was injected into distilled water and experiments injected in Paldang raw water. . At this time, the characteristics of the number of eight members are shown in Table 3.

The statue Total Organic Carbon (mg / L) pH Turbidity (NTU) 254 nm ultraviolet (abs./cm) 4.9 6.6 8.1 0.18

In the experiment in which TCE was injected into distilled water and ozone and photocatalyst 20 were combined as shown in FIG. As a result, the result of the experiment was 10-20% higher than the sum. This is a small amount of oxygen in the air that enters with ozone injection, but oxygen and H ₂ O ₂ generated during the decomposition of ozone act in combination to prevent recombination of electrons and holes generated by the photocatalytic oxidation reaction. Presumably because it promoted the generation of. The results are shown in Table 4 below.

Residual TCE in Distilled Water (%) Item TCE Uptime (min) 0 5 10 15 20 25 30 Uncontrolled Concentration (mg / L) 5.417 5.321 5.308 5.285 5.249 5.213 5.184 Residual rate,% 100.0 98.2 98.0 97.6 96.9 96.2 95.7 O ₃ Concentration (mg / L) 5.899 4.958 2.900 2.568 1.734 1.304 0.669 Residual rate,% 100.0 84.0 49.2 43.5 29.4 17.5 12.3 UV + TiO ₂ Concentration (mg / L) 6.072 5.817 5.601 5.319 4.920 4.572 4.571 Residual rate,% 100.0 95.8 92.2 87.6 81.0 75.3 75.3 O ₃ + UV + TiO ₂ Concentration (mg / L) 5.989 3.092 1.574 0.826 0.356 0.142 0.030 Residual rate,% 100.0 51.7 26.3 13.8 5.9 2.4 0.5

As shown in FIG. 4, the decomposition efficiency was slightly lowered even in the experiment using raw sugar, but similar results to the above experiment were obtained. However, in the photocatalyst 20 oxidation experiment, the efficiency decrease of about 8% is due to the turbidity of the raw water, which reduces the effect of ultraviolet light 10 on the catalyst 20 and the foreign matter in the raw water is adsorbed on the catalyst 20. It is assumed that it prevented decomposition of. The results are shown in Table 5 below.

Residual TCE in Raw Sugar (%) Item TCE, TOC wavelength is 254nm UV Uptime (min) 0 5 10 15 20 25 30 O ₃ TCE concentration (mg / L) 6.833 5.311 3.979 2.712 2.132 1.515 0.886 Residual rate,% 100.0 77.7 58.2 39.7 31.2 22.2 13.0 TOC concentration (mg / L) 8.448 8.015 7.417 6.830 6.360 5.443 4.405 Residual rate,% 100.0 95.0 87.8 80.8 75.3 64.4 52.1 UV, absorbance / cm 0.177 0.173 0.170 0.165 0.161 0.158 0.158 UV + TiO ₂ TCE concentration (mg / L) 6.157 5.917 5.535 5.030 4.550 4.452 4.839 Residual rate,% 100.0 96.1 89.9 82.7 81.9 79.3 78.6 TOC concentration (mg / L) 6.947 6.831 6.710 6.694 6.700 6.519 6.460 Residual rate,% 100.0 98.3 96.6 96.3 96.1 96.4 93.0 UV, absorbance / cm 0.160 0.156 0.154 0.154 0.153 0.152 0.151 O ₃ + UV + TiO ₂ TCE concentration (mg / L) 6.778 3.525 2.342 1.415 0.818 0.429 0.206 Residual rate,% 100.0 42.0 34.6 20.9 12.1 6.3 3.0 TOC concentration (mg / L) 7.753 6.632 6.198 4.984 4.266 3.766 2.980 Residual rate,% 100.0 85.5 79.9 64.3 55.0 48.6 38.3 UV, absorbance / cm 0.150 0.134 0.134 0.127 0.118 0.113 0.110

In addition, as shown in FIG. 5, TOC (total organic carbon) decomposition efficiency also showed a slight synergistic effect in a separate experiment of ozone and photocatalyst 20 oxidation reactions as well as TCE decomposition efficiency, and decomposition efficiency increased with time. It can be seen indirectly that the production of other by-products is suppressed. However, due to the turbidity of the raw water, the decomposition efficiency in the photocatalyst 20 oxidation experiment was estimated to be about 7%. As shown in FIG. 6, the UV spectrophotometer having a wavelength of 254 nm was analyzed to indirectly determine the removal of the hardly decomposable organic substances in the raw water. In addition, the combined effect of ozone and photocatalyst (20) oxidation reaction showed a synergistic effect of about 8% and the synergistic effect gradually increased over time.

This indicates that the problem of by-products from the removal of organic pollutants from the actual treatment plant is reduced in combination treatment than with ozone or photocatalyst 20 alone. The combination of ozone and photocatalyst (20) oxidation reaction is considered to be an effective alternative.

Example ₂ Process of Merging Photocatalyst 10 with H ₂ O ₂

H ₂ O ₂ is a more efficient electron acceptor than oxygen molecules, and by removing the electrons on the surface of the catalyst 20, the recombination rate of electrons and holes is lowered to increase the hole utilization efficiency. That is, the holes combine with hydroxide ions (OH ⁻ ) to generate OH ′, which promotes the oxidation of the photocatalyst 20, and may be directly photodecomposed to generate OH ′. In addition, when the oxygen is consumed or the oxygen transfer is slow, the oxygen of the reaction solution may be depleted, and the addition of H ₂ O ₂ increases the reaction rate when the oxygen supply is sufficient. Therefore, the addition of H ₂ O ₂ can increase the decomposition efficiency of the target material. Table 6 H ₂ O ₂ + TCE remaining amount on the H ₂ O ₂ in UV + TiO ₂ (%) and Table 7 is H ₂ O ₂ + in the UV to indicate TCE remaining amount on the H ₂ O ₂ H ₂ O ₂ + UV + TiO ₂ showed higher decomposition efficiency than H ₂ O ₂ + UV. That is, the decomposition efficiency when comparing the UV + H ₂ O ₂ + O ₂ , UV + TiO ₂ , UV + H ₂ O ₂ + O ₂ + TiO ₂ system as shown in Figure 7, 8, 9 UV + H ₂ O ₂ + O ₂ + TiO ₂ was the highest when the photocatalyst 10 and H ₂ O ₂ were combined.

Residual TCE% by H ₂ O ₂ (H ₂ O ₂ + UV + TiO ₂ ) H ₂ O ₂ (mg / L) TCE Uptime (min) 0 30 60 90 120 0 TCE concentration (mg / L) 2.001 1.120 0.817 0.670 0.485 Residual rate,% 100.0 56.0 40.8 33.5 24.2 50 TCE concentration (mg / L) 3.70 1.839 1.014 0.507 0.152 Residual rate,% 100.0 49.7 27.4 13.7 4.1 100 TCE concentration (mg / L) 3.860 1.633 0.969 0.378 0.065 Residual rate,% 100.0 42.3 25.1 9.8 1.7 500 TCE concentration. (Mg / L) 2.200 0.854 0.528 0.154 0.026 Residual rate,% 100.0 38.8 24.0 7.0 1.2

Residual TCE% by H ₂ O ₂ (H ₂ O ₂ + UV) H ₂ O ₂ (mg / L) TCE Uptime (minutes) 0 30 60 90 120 50 TCE concentration (mg / L) 5.20 3.39 2.39 1.40 0.50 Residual rate,% 100.0 65.2 46.0 26.9 9.6 100 TCE concentration (mg / L) 4.91 3.401 2.213 1.00 0.49 Residual rate,% 100.0 69.2 45.1 20.4 10.0 500 TCE concentration (mg / L) 3.73 1.28 0.93 0.76 0.39 Residual rate,% 100.0 34.4 25.0 20.4 10.5

As described above, according to the purified water treatment system of the present invention, the pump 50 for pumping the leachate containing the contaminant in the storage tank 60, the leachate containing the contaminant, and the contaminant in the reservoir 60, A reaction tank 30 which receives leachate containing contaminants in the storage tank 60 by the pump 50 and purifies the leachate, and promotes purification during oxidation of the photocatalyst 20. An air supply means 96 for injecting air, an air pump 6 for pumping air, a drying chamber 43 for drying the air supplied according to the driving of the air pump 6, and the drying chamber ( 43 is generated in the ozone generator 40 for ozone generator 40 receiving ozone dried in the air and supplying ozone to the reaction tank and air introduced by driving the air pump 6. The concentration of ozone To the ozone for displaying at the same time as chulham concentration calculation / display apparatus 100, since the control means 59 that controls the entire operation, ultraviolet ray 10 is irradiated with TiO ₂ photocatalyst oxidation reaction by the catalyst 20, the By this, the industrial wastewater and leachate can be easily purified, and the industrial wastewater and leachate can be efficiently purified by decomposing hardly degradable contaminants.

Claims (3)

A storage tank 60 into which leachate containing contaminants flows, a pump 50 for pumping leachate containing contaminants in the reservoir 60, and a leachate containing contaminants in the storage tank 60. A reaction tank 30 for purifying the leachate by driving the pump 50 and air supply means 96 for injecting air into the reaction tank 30 to promote purification during oxidation of the photocatalyst 20. ), An air pump 6 for pumping air, a drying chamber 43 for drying the air supplied according to the driving of the air pump 6, and air dried in the drying chamber 43 The concentration of ozone generated by the ozone generator 40 with respect to air introduced by the ozone generator 40 and ozone generator 40 to supply ozone to the reactor 30 and the air pump 6 is driven. Calculating and displaying ozone concentration calculation / indicator (100), Being a control means 59 for controlling the operation body water treatment system according to claim. 2. The reactor according to claim 1, wherein the reaction tank is formed of a cylindrical pyrex (31), a plurality of catalysts (20) provided along the longitudinal direction of the pyrex (31) along the longitudinal direction to promote the purification of leachate, 31 is provided in the center and the outside of the ultraviolet 10 lamp for applying the ultraviolet light 10 to the leachate, between the ultraviolet 10 lamp installed in the center of the Pyrex 31 and the cylindrical Pyrex 31 inner peripheral surface And a reaction space formed by the reaction chamber and allowing the catalyst to react while passing the leachate to purify the leachate. The water treatment system according to claim 1, wherein the catalyst (20) is TiO ₂ .

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