Slag and coal ash were selected to evaluate the recyclability of waste generated during the heat treatment processes. A list of waste types and recyclable types of the two wastes were identified. A recycling environmental hazardous assessment was reviewed step by step. In addition, the hazardous properties of slag and coal ash were investigated, and the chemical components, leaching, and content of harmful substances in the waste were analyzed. The two selected wastes were classified as general wastes. As a result of chemical analysis with XRF, the two wastes did not produce toxic gases in contact with water and show leaching toxicity from the analysis of harmful substances. In addition, waste is often brought into contact with the soil when recycled, so the content of slag and coal ash is analyzed and compared with the 2 region standard of soil; two samples were within the standard. Therefore, the surveyed wastes can be recycled in non-matrix contact types and the recycling purpose and method permitted by the new law is excluded from the recycling environmental hazardous assessment. However, to recycle wastes for new uses, the recycling environmental hazardous assessment is required.

Aeration with low energy micro-bubble generation and UV/H2O2 processes was introduced to verify the possibility of oxidation treatment for acid mine drainage. During 10 hours of aeration with micro-bubbles, Fe and As concentrations were decreased to 18.1 and 61.8%, respectively, while Cu, Cd, Al were kept at influent concentrations. Other heavy metals such as Mn, Cr, Pb, Zn, and Ni concentrations fluctuated due to the repetition of oxidation and release. Twenty days of aeration indicated the oxidation possibility for Cu, Cd, and Al. With the employment of UV/H2O2 processes, more than 77% of Cu and Fe removed, whereas slightly more than 30% of Cd and Al removed.

Recently, production of sewage and wastewater sludge have increased sharply with the population density and related industrial activity. As a result, studies of sludge treatment and reduction have been conducted and a pre-treatment method that uses thermal hydrolysis has emerged as a solution to this problem. To address problems with the thermal hydrolysis pre-treatment process, the deaeration and nitrogen recovery processes have been set up together, thus generating factors that inhibit dewaterability. In this study, the effect of pre-treatment, deaerated sludge on dewaterability-inhibiting factors (pH, temperature, aeration rate) was evaluated and alternative solutions were prepared. First, the dewaterability improvement effect increased rapidly at 190°C or higher when thermal hydrolysis pre-treatment was applied. Then, 1 L of thermal hydrolysis pre-treatment reactants at 190°C were injected into 1, 5, and 10 L/min air flows at 50°C, but no significant difference in capillary suction time (CST) or time to filter (TTF) was found. The dewaterability improved when the temperatures of the pre-treatment reactants varied between 30, 50, and 70°C under aeration at 5 L/min. However, when the pH was increased to 7, 9, or 11 at 5 L/min and 50°C, the dewaterability worsened by at least 10 times relative to the hydrolysis pre-treatment reactants. The zeta potential decreased from -30 mV to -50 mV as the pH increased. Thus, the stabilities and dispersities of the reactants increased due to the repulsive force of the particles. This was confirmed to be the cause of poor dewaterability. A coagulant can be used to solve to this problem, or the deaeration process can be placed after solid-liquid separation and the heat of thermal hydrolysis can be extracted via heat exchanger.

This study was conducted to evaluate the effects of physical characteristics. Twelve specific odorous compounds and various sources of bacteria were tested via treatment of food waste using an ultra-thermophilic aerobic composting process. Food waste was mixed with seed material and operated for 47 days. During composting, the temperature was maintained at 80-90°C. The variations in O2, CO2 and NH3 production suggested typical microorganism-driven organic decomposition patterns. After composting, the concentrations of 12 specific odorous compounds other than ammonia did not exceed the allowable exhaust limits for odor. After composting, thermophiles represented 50% of all bacteria. After composting, the percentage of thermophile bacterial increased by 15%. Therefore, both stable composting operation and economic benefit can be expected when an ultra-thermophilic composting process is applied to food waste.

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.

현재 국내에서 발생하는 음폐수의 해양투기 금지와 음식물류 폐기물의 에너지화 정책에 따라 유기성 폐기물의 혐기소화를 통한 바이오가스화 시설이 지속적으로 설치 및 운영되고 있다. 그동안 많은 연구와 운영 경험을 통해 유기성 폐기물의 바이오가스화 공정은 점차적으로 안정화되어 가고 있는 가운데, 해당 시설에서 발생하는 혐기소화여액에 대한 적정 처리가 전체 시설의 경제성에 큰 영향을 미치고 있다. 해외, 특히 유럽에서는 유기성 폐기물의 혐기소화여액을 대부분 퇴비 또는 비료로 활용하고 있으나 국내에서는 경작 면적 및 시비 시기 등에 대한 제약으로 인해 해외의 경우처럼 혐기소화여액을 퇴비 및 비료로 활용하는데 한계를 가지고 있다. 이에 대다수의 국내 음식물류 폐기물 바이오가스화 시설에서는 혐기소화여액을 별도의 폐수처리 후 하수처리장에 연계 처리하고 있으며, 고형물인 탈수케익은 일부 퇴비원료로 생산하고 있으나 이에 대한 수요 및 구매 매력도가 떨어져 무상공급 또는 유상처리하고 있는 실정이다. 이에 따라 탈수케익을 퇴비원료로 생산하는 대신 매립 또는 소각 처리로 전환하는 시설도 늘어나고 있다. 또한, 음식물류 폐기물의 혐기소화여액은 높은 질소 농도로 인해 하수처리장 연계수질에 따라 단순 응집침전부터 다단 고도처리까지 적용하여 처리하고 있어, 본 과제에서는 국내 음식물류 폐기물 바이오가스화 시설을 직접 방문 조사하여 각 시설의 폐수처리공정 성능 및 애로사항 파악을 통해 주요 연계수질 기준에 따른 최적 폐수처리공정 선정 Guideline을 도출하고자 하였다.

산업혁명 이후 대기 중의 온실가스 중 하나인 이산화탄소가 증가하면서 전세계적으로 지구온난화가 화두되고 있다. 이산화탄소 저감기술인 CCS(Carbon Capture and Storage) 기술은 이산화탄소를 포집 후 저장하는 기술로 저장의 한계에 따라 CCU(Carbon Capture and Utilization) 기술이 각광받고 있다. CCU는 이산화탄소를 이온화 하여 무기 혹은 유기재료로 전환이 가능하다. 폐기물의 금속이온을 이용하여 화학적으로 무기탄산화가 가능하며, 폐기물과 이산화탄소를 동시에 처리할 수 있다는 이점이 있다. 본 연구에서는 최종산물을 탄산칼슘을 생성하는 것이며, 탄산칼슘의 수율을 증대시키기 위해서는 폐기물 내의 칼슘 이온의 추출효율을 올리는 것이 중요하다. 하지만 용매를 이용할 경우 칼슘이온 외에 다른 이온들도 같이 추출되면서 탄산칼슘의 순도를 떨어뜨린다. 이에 최종생성물의 순도를 높이기 위하여 칼슘이온만 선택적으로 추출하기 위해 실험을 진행하였다. 실험에 사용된 폐기물은 탈황석고와 폐시멘트를 이용하였으며, 칼슘이온을 선택적으로 추출한 샘플을 이용하여 탄산화반응을 통하여 탄산칼슘을 생성하였다. 생성된 탄산칼슘은 XRD (X-ray diffraction analyzer(Ultima Ⅳ))와 FE-SEM(Field emission scanning electron microscope, JEOL-7800)를 통하여 결정구조를 분석하였다.

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.

In this paper, tin-waste resources were pulverized and separated by cut-mill and multi cyclone separator, respectively. After the cut-mill process, more than 98% of the Pb-Sn and Sn-Ag-Cu scraps were recovered, and the by-products consisting of metal and oxide could be reused as solder. The separation of pulverized powders was performed using the minimum fluidization velocity depending on the density of the materials. When the flow rate was 21 L/min (70% blower output), it had the highest separation efficiency.

In this study, we have investigated to find optimal pre-treatment flocculation condition by analyzing the floc growth rate with mixing conditions and the membrane permeation flux for pre-treatment step of the membrane process. The higher mixing intensity showed a constant floc size index (FSI) values, and lower mixing intensity increased the degree of dispersion of the FSI values. Results of comparing the distribution characteristics of the FSI value and the permeation flux were more effective in increasing flux when the FSI values were 0.2 or higher. The degree of dispersion of FSI was relatively large in 40 rpm mixing condition compared to 120 rpm. In 40 rpm mixing condition, it decreased the permeation flux compared to 120 rpm because various sizes of flocs were distributed. Coagulation-UF membrane process enhanced 30%∼40% of the flux rate compare to UF alone process, and the coagulation-MF process increased up to 5% of the flux rate compare to MF alone process. Pre-treatment, that is, coagulation process, has been found to be less effects on relatively larger pore size for MF membrane. For UF membrane, the flux was a little bit same when applying only the rapid mixing process or rapid mixing with slow mixing processes together. In case of MF membrane, the flux was improved when rapid mixing process applied with slow mixing process together.

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.

본 연구에서는 선박에서 발생하는 오․폐수의 처리를 위하여 SBR공정에 유효미생물을 주입하는 변법을 이용하여 Lab scale 실험을 수행하였다. 유해물질 유입에 따른 생물학적 처리 장치의 효율 저하 문제를 해결하기 위하여 SBR공정에 유효미생물을 주입하는 변법은 크루 즈선이라는 특수 환경과의 접목성과 생물학적 처리 시 야기될 수 있는 문제를 대비하기 위한 대안으로 선박환경에 매우 적합한 공정으로 평가 되었다. 슬러지 관찰 결과 기존의 활성슬러지에 유효미생물의 주입함으로써 슬러지의 안정성을 확보할 수 있었으며, 슬러지의 EPS 함량도 40% 이상 높아진 것을 확인할 수 있었다. 또한 슬러지의 미생물 분석 결과 유효미생물 주입으로 인해 수처리에 유리한 미생물종이 다수 출현 하여 휘발성 유기화합물과 같은 유기 유해물질이 생분해되어 안전한 물질로 전환되는 것을 확인할 수 있었으며. 중금속과 같은 무기 유해물질 도 중금속의 종류와 유입농도에 영향을 받지 않고 70% 이상의 안정적인 처리 효율도 확보할 수 있는 것으로 확인되었다.

Greenhouse gas (GHG) emissions from dye wastewater treatment processes were estimated by analysing their mass and energy balances, which were then used as baseline information for environmental assessment. The total GHG emissions from dye wastewater treatment plants were divided into direct emissions from the treatment processes and indirect ones from electricity usage. The amounts of CO2, CH4 and N2O emissions were calculated according to the Intergovernmental Panel on Clime Change (IPCC) guideline for the GHG target management system. For 3 years between 2011 and 2013, direct and indirect emissions were on average 8,742.7 and 7,892.0 Ton.CO2eq/year, respectively, with the former exhibiting 52.6 %. Also, compared to 2012, in 2013, the eco-efficiency indicator by the GHG emissions was found to be more than 1, suggesting that environmental quality was effectively improved.

본 연구에서는 유입수의 변동이 심하고 전문가가 부재한 환경인 선박에서 발생하는 오수의 효과적인 처리를 위하여 RCM공법을 선박오수처리장치에 적용하는 실험실 규모의 실험을 수행하였다. 질소·인의 고도처리 효율과 선박이라는 특수환경과의 접목성을 검토한 결과 RCM공정에 유효미생물을 주입하는 방법은 선박환경에 적합한 것으로 평가되었다. 또한 RCM공정은 활성슬러지 공정에서 배출되는 슬러지 는 배출시키지 않고 슬러지액화분해조(SDC)에서 재분해하여 순환함으로써, 최근 해양투기가 금지됨으로 인해 문제가 되고 있는 슬러지의 발 생량을 최소한으로 하여 친환경적인 수처리가 가능하다. 복합미생물제제 주입 후 미생물 관찰결과 고도처리에 유리한 미생물종의 출현을 확 인하였으며 이들의 상호기작으로 질소·인의 처리에 도움을 주어 처리효율이 높은것이라 판단된다. 유기물 제거효율 실험결과 BOD5, CODcr T-N, T-P의 처리효율이 각각 96, 97, 78, 81.68 %로 나타나 Membrane이나 Filter없이도 강화되어가는 해양오염기준을 충족시킬 수 있는 공 정으로 판단된다.

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.

The effect of temperature on the removal process of Cr(VI) ion contained in wastewater by a precipitation method has been investigated for the improvement of its design and operation. The distribution diagram of chromium ion was constructed by employing the MINTEQ program and the quantitative feature of Cr(VI) depending on pH was investigated. As the temperature increases, the relative amount of H2CrO4 was examined to be raised and the pH range in which H2CrO4 exists as a stable form was also investigated to be extended according to the temperature. Cr(VI) ion was shown to be changed from HCrO4 − to Cr2O7 2− as the concentration of Cr(VI) ion is increased in the neutral pH condition and the concentration of Cr(VI) ion which is necessary for the ionic transformation was observed to rise in the acidic and alkaline conditions. The major reactant which involved in the reduction reaction for the removal of Cr(VI) ion was examined to be HCrO4 − and the reduction of Cr(VI) ion to Cr(III) ion was investigated to be influenced much by the temperature change at higher pH conditions. The reduction reaction of Cr(VI) ion for its removal as a precipitate was examined to be promoted as the temperature decreases and pH is lowered. In addition, the stable region of Cr(OH)3 was shown to be enlarged with temperature based on the thermodynamic estimation and it was thought to be necessary to design and control the precipitating process of Cr(VI) ion by considering the thermal characteristics of reduction and precipitation stage.

This paper presents the results of the electrochemical treatment of chemical oxygen demand(COD) and total nitrogen(T-N) compounds in the wastewater generated from flue gas desulfurization process by using a lab-scale electrolyzer. With the increase in the applied current from 0.6 Ah/L to 1.2 Ah/L, the COD removal efficiency rapidly increases from 74.5% to 96%, and the T-N removal efficiency slightly increases from 37.2% to 44.9%. Therefore, it is expected that an electrochemical treatment technique will be able to decrease the amount of chemicals used for reducing the COD and T-N in wastewater of the desulfurization process compared to the conventional chemical treatment technique.

The principle of treatment of type 2, 3 odontoid process fracture is controversial. The debate is in regard to which is effective between conservative treatment and surgery. We enrolled 41 patients with type 2, 3 odontoid process fracture from January 2007 to December 2011 at Chosun University Hospital. Patients in Group I (GI) received a halo vest and those in Group II (GII) underwent surgery by ant. screw fixation. The bone fusion was classified according to stable bone union, fibrous union, and unstable non-union. Patients in GI received halo vest for a mean period of 4.9 months and those in GII received a neck collar for a mean period of 3.8 months. Tweleve patients in GI and 17 patients in GII had stable bone union. Three patients in GI and two patients in GII had fibrous union. Five patients in GI and two patients in GII had non-union. The halo vest was a good conservative treatment for type 2, 3 odontoid process fracture : however, low bone fusion rate is a problem in particularly old age. However, ant. screw fixation is a better treatment in regard to short surgical time, short fusion time, and high bone fusion rate.

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.

본 연구에서는 크루즈선에서 발생하는 오 폐수의 고도처리를 위하여 SBR공정에 유효미생물을 주입하는 변법을 이용하여 실험실 규모의 실험을 수행하였다. 질소 인의 고도 처리 효율과 크루즈선이라는 특수 환경과의 접목성을 검토한 결과 SBR공정에 유효미생물을 주입하는 변법은 선박환경에 매우 적합한 것으로 평가되었다. 또한 기존의 활성슬러지에 유효미생물의 주입함으로써 슬러지 팽화 등의 문제를 해결할 수 있어 슬러지의 안정성을 확보할 수 있었으며, 미생물 관찰 결과 고도처리에 유리한 미생물종의 출현으로 질소 인의 처리 효율이 높아지는 것을 확인할 수 있었다. 이로 인해 총질소와 인의 제거 효율은 74%, 75%로 나타났으며 이러한 결과로 미루어 강화되어가는 해양오염기준을 충만족시킬 수 있을 공정으로 판단된다.