유기성폐기물(음식물, 하수슬러지 등)은 2005년부터 육상 직매립이 금지되었고, 2006년에 발효된 런던협약에 따라 2013년 1월부터 해양투기 또한 금지되어 폐기물의 처리 및 재활용이 시급한 실정이다. 따라서, 이러한 유기성 폐기물의 효과적인 자원화 방법 중 하나인 혐기성소화가 각광받고 있는 실정이며, 혐기성소화조에서 발생되는 바이가스는 일반적으로 CH4 50~90%, CO2 10~50%, 소량의 H2S 및 NH4로 알려져 있다. 이러한 바이오가스의 정제방법으로는 탄소흡착법, 막분리법 등이 있으나 높은 운전비용과 공정구성의 어려움, 2차 폐기물 발생 등 많은 문제를 일으키고, CO2의 재활용이 아닌 폐기시키고 있어 자원순환적인 측면에서 바람직하지 못하다. CH4의 전환방법중 하나인 CO2 methanation반응은 1M의 CO2와 4M의 H2가 반응하여 1M의 CH4와 2M의 H2O가 생성되는 반응이다. CO2는 열역학적으로 매우 안정된 물질로, 반응에 필요한 에너지를 공급하기 위해서는 수소 등과 같은 높은 에너지의 환원제를 같이 반응에 참여시켜 주어야 한다. 그러나 열역학적 평형으로 인해 전환이 제한되는 경우가 많아, 적절한 반응속도와 선택도를 달성하기 위해 촉매가 요구되며, CO2 methanation 반응에 사용되는 촉매는 주로 Ni, Fe, Al 등 금속계 촉매가 주를 이루고 있다. 따라서 본 연구에서는 바이오가스의 정제효율을 높이기 위하여 CO2 methanation 촉매를 다양한 조건에 따라 제조하였으며 각각의 촉매별 CO2 전환율을 평가하였다.

This study proposes a selection method of a performance evaluation index of waterproofing and anti corrosion materials used in domestic water treatment facilities for material and construction failures based on different usage and environmental conditions to study the possibility of structural performance maintenance. Different types of waterproofing･anti-corrosion materials have been evaluated based on their respective properties, and have been classified into separate categories based on their case studies of material failures in construction. As a result, 12 different performance evaluation indexes have been produced for the performance evaluation method. Among the 12 performance evaluation index 5 were selected with relatively low importance that produced a low value of 60% importance using AHP analysis method, and conclusively proposed 7 performance evaluation index criteria (wet surface adhesion, fatigue resistance, crack resistance, adhesion performance, joint performance, impact resistance, impermeability)

The efficiencies of Gang-Byeon sewage treatment facilities, which are based on GPS-X modelling, were analysed and used to design recycle water treatment processes. The effluent of an aeration tank contained total kjeldahl nitrogen (TKN) of 1.8 mg/L with both C-1 and C-2 conditions, confirming that most ammonia nitrogen (NH3 +-N) was converted to nitrate nitrogen (NO3 --N). The concentrations of NH3 +-N and NO3 --N were found to be 222.5 and 227.2 mg/L, respectively, with C-1 conditions and 212.2 and 80.4 mg/L with C-2 conditions. Although C-2 conditions with higher organic matter yielded a slightly higher nitrogen removal efficiency, sufficient denitrification was not observed to meet the discharge standards. For the total nitrogen (T-N) removal efficiency, the final effluent concentrations of T-N were 293.8 mg/L with biochemical oxygen demand (BOD) of 2,500 mg/L, being about 1.5 times lower than that (445.3 mg/L) with BOD of 2,000 mg/L. Therefore, an external carbon source to increase the C/N ratio was required to get sufficient denitrification. During the winter period with temperature less than 10 , the denitrification efficiency was dropped rapidly even with a high TKN concentration (1,500 mg/L). This indicates that unit reactors (anoxic/aerobic tanks) for winter need to be installed to increase the hydraulic retention time. Thus, to enhance nitrification and denitrification efficiencies, flexible operations with seasons are recommended for nitrification/anoxic/denitrification tanks.

Recently, Advanced water treatment facilities with Ozone are being introduced domestically. However, waterproofing/corrosion prevention construction method of concrete structure for existing advanced water treatment makes waterproofing/corrosion prevention materials and concrete deteriorated because of strong oxidation of ozone. Therefore, in this study, It was evaluated in ozone resistance and bond strength of metal spraying coating.

The treatment efficiencies of domestic sewage treatment processes were analysed and assessed to suggest and design a suitable technology for coal seam gas (CSG) water treatment. Two sewage treatment plants (S and G in Busan) were selected. The former operates with standard activated sludge and modified Ludzak Ettinger processes while the later uses the combination of A2/O and gravity fiber filtration. For both plants, the concentrations of BOD, CODMn, T-N and T-P were about 5.0, 19.0, 5.0, 11.0 and 1.0 ppm, respectively, which satisfy the discharge standards. Therefore, although sewage treatment processes seems to be applicable for CSG water treatment, additional processes to remove total dissolved solids and ionic compounds (i.e. bicarbonate) need to be introduced to produce fit-for-purpose water resources for beneficial use (in accordance with Water ACT 2013). This, for the CSG treatment process design, it is necessary to align the operating conditions with merging methods of combinable unit technology obtained from sewage treatment processes.

The H water treatment plant has been operating since 1982 and has had no renovation. It is assumed that the filters have been operated for more than 30 years and therefore are deteriorated. Many of the filters show an unequal state of air scouring during backwashing. For this study one filter, which was presumed most deteriorated among eighteen filters, was selected as a model filter for renovation. Some of the effects seen after renovation of the underdrain system were a lower average filtrated turbidity by approximately 0.02 NTU and an equal backwash state throughout the filter bed. Sand wash efficiencies by backwash before renovation of the underdrain system were 28%, 8%, and 5% at the surface, 50 cm depth, and 100 cm depth, respectively, and after renovation of the underdrain system were 94%, 26%, and 15% , respectively. The standard deviation of the effective sand size was 0.025-0.033 mm before renovation of the underdrain system and 0.002-0.011 mm after renovation of the underdrain system, meanings there was equal backwash pressure throughout the filter. Filtration time after renovation was approximately 2 times longer than before renovation.

본 연구에서는 선박에서 발생하는 대기오염물질을 처리하기 위해 사용되는 습식 스크러버를 이용한 배기가스 세정시스템(EGCS: Exhaust Gas Cleaning System)에서 발생되는 폐수를 재이용 할 수 있는 순환시스템을 개발하기 위해 진행되었다. 선박 배기가스 DePM, DeSOx 순환처리장치 (Recycle system)의 세정수의 입자성물질과 분산유를 효과적으로 제거할 수 있는 수 처리 시스템을 개발한 결과 원심 분리형 Purifier만으로는 미세한 분산유의 처리가 어렵다는 결과가 도출되어 원심분리형 Purifier 후처리로 유수분리 경사 분리판을 이용한 유 수분리기의 일종인 Coalescer를 본 시스템에 적용하였다. Coalescer는 2차 분산 상태의 에멀젼화 된 미세 기름입자를 합착시켜 분리하는 기술 이다. 선박 배기가스 DePM, DeSOx 순환처리장치 (Recycle system)에서 배출되는 세정수를 Purifier와 Coalescer를 이용하여 처리한 결과 입자성물질은 55% 분산유는 유입수 대비 99%이상 처리되는 것을 확인하였다. 따라서 선박 대기오염 저감을 위한 습식세정탑 시스템에 본 세 정수 처리시스템을 도입하면 세정수로서 재사용이 가능하다고 판단된다.

To develop various usable water from coal seam gas (CSG) water that needs to be pumped out from coal seams for methane gas production, a feasibility study was carried out, evaluating and analysing a recent report (Coal Seam Gas Water Management Policy 2012) from Queensland State Government in Australia to suggest potential CSG water treatment options for fit-for-purpose usable water production. As CSG water contains intrinsically high salinity-driven total dissolved solid (TDS), bicarbonate, aliphatic carbon, Ca+2, Mg+2 and so on, it was found that appropriate treatment technologies are required to reduce the hardness below 60 mg/L as CaCO3 by setting the reduction rates of Ca+2, Mg+2 and Na+ concentrations, as well as TDS reduction. Also, Along with fiber filtration and membrane separation, an oxidation degradation process was found to be required. Along with salinity reduction, as CSG water contains organic compounds (TOC: 248 mg/L, C6 -C9: <20 mg/L and C10 - C36: <60 mg/L), compounds with relatively high molecular weights (C10 - C36) need to be treated first. Therefore, this study suggests a combined system design with filtration (Reverse osmosis) and oxidation reduction (electrolysis) technologies, offering proper operating conditions to produce fit-for-purpose usable water from CSG water.

In Korea, many drinking water treatment plants (DWTPs) have introduced and are going to introduce biological activated carbon (BAC) process to treated dissolved organic matter (DOM) in water which are difficult to control by conventional water treatment processes. Even though more decade have passed since introduced BAC in Korea, most of BAC operating method was followed to the modified sand filter operating manuals. In case of BAC backwashing, many DWTPs set the periods of backwashing about 3∼5 days. In this study, we have collected data to set the proper BAC backwashing periods from both pilot-plant and real DWTPs. We had measured heterotrophic plate count (HPC), turbidity, water temperature, dissolved organic carbon (DOC) and headloss from just after backwashing to the next backwashing time for two years. Considering water quality factors, the BAC run time from backwashing to the next backwashing could extend more 30 days without water quality deterioration if the head loss do not reach the limited level which depends on each BAC facilities’ condition. It means the BAC treated water could be saved in the proportion of extended the backwashing period to the existing backwashing period.

This study carried out continuous column test for estimating the regeneration efficiency with regeneration times and temperatures. More times regenerated granular activated carbon (GAC) has more ash in the GAC and has less apparent density. Two times regenerated GAC (2nd re-GAC) could removed the Trihalomethanes (THMs) in the water for the first two week after starting continuous column test, on the other hand five times regenerated GAC (5th re-GAC) did not have adsorption capacity. The THMs concentration in the effluent was almost equal or higher than that of influent at the first time of continuous column test. 2nd re-GAC showed much more DOC adsorption capacity than 5th re-GAC and the GAC which was regenerated with 700 ℃ had highest DOC removal efficiency among the GACs with 600, 700, 800, 900 ℃ regeneration temperatures. It is anticipated the cost of GAC regeneration could be saved more 100 million won by reducing the furnace temperature of 3rd~4th and 5th~6th about 150 ℃ compared to the current regeneration condition.

본 논고는 고양 정수장과 구미 정수장으로부터 물을 공급받고 있는 5개 도시(고양, 파주, 구미, 김천, 칠곡)를 대상으로 고도정수처리 도입의 경제적 편익을 평가하였다. 지불가능금액(WTP) 추정을 위한 방법으로는 이중경계 양분선택형 CVM을 이용하였다. 특히 평균 WTP 추정값을 도출하기 위한 방법으로 모수 추정법 중 구간 데이터(interval-data) 모델을 이용하였다. 고도정수처리 서비스에 대한 추가 지불 WTP(평균)는 공변량을 포함한 모델을 적용하였을 경우 톤당 231.3원이, 공변량을 포함하지 않은 모델을 적용하였을 경우에는 231.2원인 것으로 추정되었다. 한편 추정된 WTP와 함께 고양 및 구미 정수장으로부터 공급받는 수돗물 공급량(각각 59.675 백만 m3/년, 93.734 백만 m3/년)을 고려하여 정수장별 고도정수처리의 경제적 편익을 도출한 결과 고양정수장은 약 138억 원/년이, 구미 정수장은 16.8억 원/년으로 추정되었다. 그리고 설비의 내구연한을 10년으로 가정할 경우, 비용 대비 편익 비율은 고양정수장이 3.7, 구미정수장이 2.1로 조사되었다. 수도사업 관련 고도정수처리 도입은 공공사업의 한 유형으로, 이는 경제적 편익 및 비용이 동시에 고려되어야 할 정책적 사업이다. 이러한 의미에서 본 연구의 산출물인 고도정수처리의 WTP는 정책결정자의 수질개선 관련 의사결정에 기초 자료가 될 것이다.

The purpose of this study was to evaluate the applicability of the microbial fuel cell for the combined treatment of food waste water and landfill leachate. Contents of the study was to develop a carbon-containing electrode material radially to maximize microbial attachment. Also to evaluate the electric energy production efficiency by combining the electrode surface coating technology. By using a microbial fuel cell organic matter and nitrogen removal efficiency is evaluated for the food waste water and landfill leachate. BET to evaluate the surface characteristics of the developing electrode (Brunauer Emmett Teller) To evaluate the coating adhesion through measurement and to evaluate the adhesion characteristics micro-organism Weighing. Excellent electrical conductivity in the development electrode platinum, cobalt, by coating a catalyst such as palladium and to evaluate the electric energy generation efficiency. Lab. scale reactor capacity is a 5 L, and to configure the cross-section and the oxidizing electrode as cathode sequentially added.

Three hundred thousand tons per year of water works sludge are produced in Korea. End disposal of the sludge is mainly based on recycle such as supplementary material for cement kiln, raw material for construction materials and fill material. The dry clarifier sludge organic content is about 30% and the major elements determined are aluminum(about 14%), iron(about 4%), potassium(1.8%), and manganese(0.5%). The recovery of coagulant has high economic advantage and recommended as a suitable treatment option for the disposal of water works sludge. Chemically, coagulant(aluminum) recovery from the water works sludge is a simple process. This process is however, somewhat complicated by pH control in the mixture of dewatered clarifier sludge and sulfuric acid solution. Also, the thickened water works sludge(TWS), which is withdrawn from the bottom of the thickener in water works plant, is difficult to dewater. In addition coagulation is used to remove total phosphorus(T-P) from municipal wastewater in oder to strengthening discharge water quality standard for T-P in municipal wastewater treatment plant(MWTP). Nevertheless it has the drawback of producing a large amount of sludge which together with the coagulants such as alum and polyaluminum chloride used to treat T-P in municipal wastewater increases the operating cost. Reject water originates from the dewatering of digested sludge in the MWTP. It contains heavy metals and large amounts of nutrients such as phosphorus and nitrogen. Traditionally, reject water is recycled back to the main flow line on of the MWTP. Although this method seems to be simple, it also has its drawbacks. First of which is the increase in the load of the MWTP as the reject water characteristics is very much different from the normal municipal wastewater. The objective of this study is to investigate the effectiveness of thickened water works sludge as an adsorbent of phosphorus from the reject water. In this study, batches of experiments were conducted to investigate the effect of dosage of TWS for reject water on its phosphorus adsorption properties. Increasing the TWS dosage to 30%(vol/vol), T-P and COD of reject water decreased to 55% and 20% respectively. Experimental results show that the potential of the TWS as coagulant in phosphorus and organic matter immobilization, thus converting they from rejector water to a useful material in pollutant control.

A comprehensive fractionation technique was applied to a set of water samples obtained along drinking water treatment process with ozonation and biological activated carbon (BAC) process to obtain detailed profiles of dissolved organic matter (DOM) and to evaluate the haloacetic acid (HAA) formation potentials of these DOM fractions. The results indicated that coagulation-sedimentation-sand filtration treatment showed limited ability to remove hydrophilic fraction (28%), while removal of hydrophobic and transphilic fraction were 57% and 40%, respectively. And ozonation and BAC treatment showed limited ability to remove hydrophobic fractions (6%), while removal of hydrophilic and transphilic fractions were 25% and 18%. The haloacetic acid formation potential (HAAFP)/dissolved organic carbon (DOC) of hydrophilic fraction was the highest along the treatment train and HAAFP/DOC of hydrophilic fraction was higher than hydrophobic and transphilic fraction as 23% 30%, because of better removal for hydrophobic fraction both in concentration and reactivity.

This study aimed for evaluating the applicability of the two stage dual media filtration system in field water treatment plant. The field plant of two stage and dual media filtration system was operated for 2 months. Average iron concentrations of the settled water, existing filtered water and second stage filtered water was 0.041 mg/L, 0.007 mg/L and 0.005 mg/L, respectively. Removal efficiency of iron concentration in the second stage is appropriately 35% more than in existing filtered water. Also removal efficiency of residual chlorine in the dual media filtration system is relatively 42.3% more than in existing filtered water due to adsorption of activated carbon, but the removal of ammonia nitrogen by adsorption is insufficient. Average concentrations of THM and chloroform in the settled water are 0.033 mg/L, 0.026 mg/L, respectively and in existing filtered water are 0.023 mg/L and 0.023 mg/L. Average concentrations of THM and chloroform in the dual media filtration system are 0.008 mg/L and 0.013 mg/L. Therefore removal efficiency of THM concentration in second stage is more than 66.4% in existing filtrated water. Also removal efficiency of chloroform in the dual media filtration system is more than 50.0% in existing filtered water because of the adsorption of activated carbon. In this case backwashing period in dual stage system is 4～5 days, but in existing filtration system is 1～2 days.

We compared the applicability and economical efficiency of peroxone process with those of ozone process in the existing water treatment plant on downstream of Nakdong River. After comparing the peroxone process for removing geosmin with the ozone process in lab scale test, peroxone process showed much higher removal efficiency than the ozone process at the same ozone dosage. Proper range of H2O2/O3 ratio were 0.5~1.0 and the half-life of geosmin was about 5.5~6.8 min when the H2O2/O3 ratio was set to 0.5 during 1~2 mg/L of ozone dosage. Peroxone process could reduce the ozone dosage about 50 to maximum 30% for the same geosmin removal efficiency compared to the ozone process in the pilot scale test. In case of 1,4-dioxane treatment, peroxone process could have 3~4 times higher efficiency than ozone process at the same ozone dosage. The results of estimating the economical efficiency of ozone and peroxone process for treating geosmin and 1,4-dioxane by using pilot scale test, in case of the removal target was set to 85% for these two materials, the cost of peroxane process could be reduced about 1.5 times compared to ozone process, and in the same production cost peroxone process could have 2~3 times higher removal efficiency than ozone process. The removal efficiency by peroxone process showed a large difference depending on the physicochemical characteristics of target materials and raw water, therefore detailed examination should be carried out before appling peroxone process.

Dielectric discharges are an emerging technique in environmental pollutant degradation, which that are characterized by the production of hydroxyl radicals as the primary degradation species. For practical application of the plasma reactor, reactor that can handle large amounts of water are needed. Plasma research to date has focused on small-scale water treatment. This study was carried out basic study for scale-up of a single DBD (dielectric barrier discharge) plasma reactor. The degradation of N, N-Dimethyl-4-nitrosoaniline (RNO, indicator of the generation of OH radical) was used as a performance indicator of multi-plasma reactor. The experiments is divided into two parts: design parameters [effect of distance of single plasma module (1~14 cm), arrangement of ground electrode (single and multi), rector number (1~5) and power number (1~5)]; operation parameter [effect of applied voltage (60~220 V), air flow rate (1~5 L/min), electric conductivity of solution (1.4 μS/cm, deionized water)~18.8 mS/cm (addition of NaCl 10 g/L) and pH (5~9)]. Considering the electric stability of the plasma reactor, optimum spacing between the single plasma module was 2 cm. Multi discharge electrodes - single ground electrode array was selected. Combination of power 3-plasma module 5 was the optimal combination for maximum RNO degradation. The optimum 1st voltage and air flow rate for RNO degradation were 180 V and 4 L/min, respectively. The pH and conductivity of the solution was not influencing the RNO degradation.

This study, changes in raw water quality is to indicate on the efficiency of ozone treatment of each pollutant as compared to derive the appropriate operating measures. The appropriate selection for injection rate of pre-ozone and did not inject pre-ozone assess changes in the water. When good water quality, you not injected of pre-ozone to evaluate the economic efficiency of electricity and put the most cost-effective ozone concentration were evaluated. Evaluation remove organic matter and chlorophyll-a concentration level in experiments with each factor of the water DOC> 2.5 ㎎ / L, THMFP> 70 ㎍ / L, Chl-a> 30 ㎎/ ㎥or less constant process, if you do not need to put pre-ozone showed little impact. It also does not put you in pre-ozone appropriate produce enough power rate savings was calculated as approximately 90 million won. Ability to remove organic materials and the ability to produce disinfection byproducts, and cost-effective decisions by considering the concentration of injection if pre-ozone 1 mg/L was investigated by the appropriate concentration of ozone injection.

This study utilized atomic force microscopy (AFM) and nanoindentation methods to evaluate epoxy water-resistance and anti-corrosiveness. This study considered two different epoxy formulations to assess typical degradation characteristics of epoxy surfaces with regard to water-resistance and anti-corrosiveness. As a result, this study was able to clearly confirm changes in physical characteristics and performance tendencies regarding ozone oxidizing reactions.