에너지 소비량 증가 및 국제 유가 상승으로 인해 대체에너지 개발의 중요성이 더욱 증가하고 있으며 염색슬러지의 경우 육상 매립 금지 및 해양배출 규제 정책의 강화로 인해 새로운 처리방안이 요구되고 있으므로 이에 대한 해결책으로 가스화 기술 등을 적용할 수 있다. 해양투기가 금지되는 연간 50 만톤 가량 발생되는 염색슬러지를 가스화 원료로 활용할 경우 처리비 약 240억 원을 절약할 수 있고 연간 약 6만 TOE의 화석연료 대체 효과가 있다. 가스화 기술은 유기성 슬러지에 포함된 유기물질을 CO와 H₂가 주성분인 합성가스로 변환시키고 가스화를 통해 생성된 청정 합성가스는 고온고압화가 가능하기 때문에 폐압 터빈을 적용함으로써 수요처의 특성에 따라 전기 및 스팀을 생산 할 수 있다. 또한 염색슬러지의 경우 폐수처리 과정에서 응집제의 사용으로 인해 산화철 성분을 포함하고 있으므로 처리대상물질 자체가 함유하고 있는 촉매성 물질인 고농도 산화철을 회수하여 타르 개질 촉매로 활용함으로써 타르의 생성량을 저감시킬 수 있고 고가의 촉매를 대체함으로써 경제성을 확보할 수 있으며 합성가스 생산 품질에 영향을 미치는 중요 인자인 오염물질을 제거함으로써 가스화율을 증가시킬 수 있을 것으로 판단된다. 본 연구에서는 염색슬러지와 왕겨 혼합물을 대상 시료로 하여 2톤/일급 가스화 설비를 이용하여 1단 버블유동층(BFBG)방식을 적용하여 가스화 실험을 수행하였으며 발생되는 합성가스 농도 측정 및 오염물질 분석을 통해 합성가스 생산 특성 및 오염물질 배출 특성을 파악하였다. 실험 결과 합성가스 조성별 평균 가스 농도는 H₂ 7.8%, O₂ 0.4%, N₂ 59.5%, CH₄ 2.1%, CO 11.4%, CO₂ 14.8%, C₂∼C₄ 2.1%로 나타났으며 평균 탄소전환율과 냉가스효율은 각각 72.6%와 49.8%로 나타났다. 또한 오염물질 제거 특성을 파악한 결과 타르 제거효율은 95.9%, 분진 제거효율은 99.7%로서 안정적인 연속운전이 가능하였다.

세계적으로 에너지 수요량의 증가하고, 화석연료 고갈 및 지구온난화 대응 등 문제로 바이오매스 가스화를 통한 에너지 자원 개발이 이슈화 되고 있다. 일반적으로 바이오매스 가스화 공정에서 발생하는 타르는 가스화기 후단 설비 혹은 배관에 부착되어 배관 폐쇄에 따른 운전 정지와 가스화 전체 시스템 효율 저하의 주요 원인이 되고 있다. 이와 같은 타르 부착문제를 해결하기 위한 타르 개질용 촉매 대부분은 귀금속계로 고가일 뿐만 아니라, 탄소 침적에 의한 불활성 문제가 있으나, 산화철은 가격이 저렴하고 탄소 석출량이 적으며 열화가 잘 일어나지 않는 유기물 분해 촉매로 주목받고 있다. 육상직매립 및 해양투기가 금지된 염색슬러지 회재 중 약 70%는 산화철 성분이여서 타르개질 촉매로 충분히 활용 가능한 것으로 알려져 있다. 본 연구에서는 염색슬러지 혼합 유기자원 저온가스화 공정특성을 파악하고자 가스화 및 염색슬러지 내 철 촉매를 이용한 타르개질 공정 모사 모델을 구축하여 혼합 유기자원의 종류 및 운전조건 변화에 따른 합성가스 생산 특성을 고찰하였다. 왕겨, 타르 및 폐플라스틱을 염색슬러지와 각각 혼합한 시료의 가스화 공정 모사 결과 폐플라스틱을 혼합한 경우의 합성가스 발열량이 가장 높은 것으로 나타났다.

Microwave pyrolysis of SF6 on alumina-based catalyst doped with cerium sulfate was investigated. Silicon Carbide (SiC) used as a microwave susceptor. The catalysts were characterized by X-ray diffraction (XRD) and the destruction and removal efficiency (DRE) of SF6 was evaluated by GC-TCD. We found that the optimal cerium content was 20wt% at microwave pyrolysis of SF6. The catalysts modified by cerium showed higher DRE at lower reaction temperature compared with original catalysts. The highest DRE of SF6 on CeA (20) was 80% at 600oC reaction temperature and the DRE was up to 95% when the reaction temperature over 700oC. It showed the alumina-based with cerium promotes the removal efficiency of SF6 at a mild reaction temperature. From XRD results, modified catalysts could be higher stability because of no transformation of the crystal phase after reaction.

Tetrafluoromethane(CF4) have been widely used as etching and chemical vapor deposition gases for semiconductor manufacturing processes. CF4 decomposition efficiency using microwave system was carried out as a function of the microwave power, the reaction temperature, and the quantity of Al2O3 addition. High reaction temperature and addition of Al2O3 increased the CF4 removal efficiencies and the CO2/CF4 ratio. When the SA30 (SiC+30wt%Al2O3) and SA50 (SiC+50wt%Al2O3) were used, complete CF4 removal was achieved at 1000℃. The CF4 was reacted with Al2O3 and by-products such as CO2 and AlF3 were produced. Significant amount of by-product such as AlF3 was identified by X-ray powder diffraction analysis. It also showed that the γ-Al2O3 was transformed to α-Al2O3 after microwave thermal reaction.

Sulfur hexa-fluoride has been used as a etching gas in semiconductor industry. From the globally environmental issues, it is urgent to control the emissions of this significant greenhouse gas. The main objective of this experimental investigation was to find the effective catalyst for SF6 decomposition. The precursor catalyst of hexa-aluminate was prepared to investigate the catalytic activity and stability. The precursor catalyst of hexa-aluminate was modified with Ni to enhance the catalytic activities and stability. The catalytic activity for SF6 decomposition increased by the addition of Ni and maximized at 6wt% addition of Ni. The addition of 6wt% Ni in precursor catalyst of hexa-aluminate improved the resistant to the HF and reduced the crystallization and phase transition of catalyst.

Electrochemical degradation of phenol was evaluated at DSA (dimensionally stable anode), JP202 (Ru, 25%; Ir, 25%; other, 50%) electrode for being a treatment method in non-biodegradable organic compounds such as phenol. Experiments were conducted to examine the effects of applied current (1.0~4.0 A), electrolyte type (NaCl, KCl, Na2SO4, H2SO4) and concentration (0.5~3.0 g/L), initial phenol concentration (12.5~100.0 mg/L) on phenol degradation and UV254 absorbance as indirect indicator of by-product degraded phenol. It was found that phenol concentration decreased from around 50 mg/L to zero after 10 min of electrolysis with 2.5 g/L NaCl as supporting electrolyte at the current of 3.5 A. Although phenol could be completely electrochemical degraded by JP202 anode, the degradation of phenol COD was required oxidation time over 60 min due to the generation of by-products. UV254 absorbance can see the impact of as an indirect indicator of the creation and destruction of by-product. The initial removal rate of phenol is 5.63 times faster than the initial COD removal rate.

Alumina-supported catalysts containing different transition metals such as Cu, Cr, Mn, Zn, Co, W were investigated for their activity in the selective oxidation of toluene. Catalytic oxidation of toluene was investigated at atmospheric pressure in a fixed bed flow reactor system over transition metals with Al2O3 catalyst. The result showed the order of catalytic activities for the complete oxidation of toluene was Mn > Cu> Cr> Co> W> Zn for 5wt.% transition metals/Al2O3. Mn/Al2O3 catalysts containing different amount of Mn were characterized by X-ray diffraction spectroscopy for decision of loading amount of metal to alumina. 5 wt.%Mn/Al2O3 catalyst exhibits the highest catalytic activity, over which the toluene conversion was up to 90% at a temperature of 289℃.

In this study, the thermo-catalytic hydrogenation using corn stark and wasted palm kernel shell was carried out for the production of hydrocarbon compounds in direct biomass liquefaction. The conversion of biomass in direct biomass liquefaction over Mo-based catalyst increased with increasing the reaction temperature and the content of the volatile matter contained in biomass and the corn starch was more available than the wasted palm kernel shell. And then, the conversion was about 97.9% using corn starch and was about 92.4% using wasted palm kernel shell at 400oC. It was confirmed that the liquefied products obtained after the thermo-catalytic reaction were C6, C7, C8-typed hydrocarbon compounds.

Acid hydrolysis of cellulose using hydrothermal reaction was conducted to maximize reducing sugar concentration and the response surface methodology (RSM) was applied to study the effects of independent variables, such as reaction temperature (116 ~ 184oC), reaction time (12 ~ 28 min) and hydrochloric acid concentration (HCl, 0.0159 ~ 0.1841 N) on reducing sugar concentration and production yield from the cellulose. With the optimum conditions of the acid-catalyzed hydrothermal hydrolysis, the reducing sugar (RS) was obtained as 369.14 mg-RS/g-cellulose in 172.77oC of the reaction temperature, 28.41 min of the reaction time and 0.067 N of the hydrochloric acid concentration. The glucose (Glu) was obtained as 281.94 mg-Glu/g-cellulose in 154.70oC of the reaction temperature, 11.59 min of the reaction time and 0.184 N of the hydrochloric acid concentration.

The present work has been devoted to the catalytic reduction of N2O by H2 with Pt/SiO2 catalysts at very low temperatures, such as 110oC, and their nanoparticle sizes have been determined by using H2-N2O titration, X-ray diffraction(XRD) and high-resolution transmission electron microscopy(HRTEM) measurements. A sample of 1.72% Pt/SiO2, which had been prepared by an ion exchange method, consisted of almost atomic levels of Pt nanoparticles with 1.16 nm that are very consistent with the HRTEM measurements, while a Pt/SiO2 catalyst possessing the same Pt amount via an incipient wetness technique did 13.5 nm particles as determined by the XRD measurements. These two catalysts showed a noticeable difference in the on-stream deN2O activity maintenance profiles at 110℃. This discrepancy was associated with the nanoparticle sizes, i.e., the Pt/SiO2 catalyst with the smaller particle size was much more active for the N2O reduction. When repeated measurements of the N2O reduction with the 1.16 nm Pt catalyst at 110oC were allowed, the catalyst deactivation occurred, depending somewhat on regeneration excursions.

Simulated waste-derived synthesis gas has been tested for hydrogen production through water gas shift (WGS) reaction in the temperature range of 240oC ~ 400oC over supported Pt catalysts prepared by an incipient wetness impregnation method. MG30, MgO, ZrO2, Al2O3 and CeO2 were employed as supports for WGS reaction in this study. 1 wt.% Pt/ CeO2 catalyst exhibited the highest CO conversion as well as 100% CO2 selectivity. This is due to easier reducibility of Pt/CeO2 and high oxygen mobility and oxygen storage capacitiy of CeO2. Pt/CeO2 catalyst can be a promising catalyst for WGS reaction from waste-derived synthesis gas.

In this study, we devised a regeneration process for deactivated catalyst which used in SCR denitrification facility using sulfuric acid. Catalyst regeneration process using sulfuric acid showed the recovery of the activity of waste catalyst over 80% comparison with new catalyst, and we optimized operating condition through control sulfuric acid concentration and regeneration time. The activity recovery ratio of waste catalyst was revealed at 0.5 M sulfuric acid in regeneration solution, but for the case of higher than 2.5 M of H2SO4 concentration, activity recovery high hest ratio was decreased owing to the elution of active compounds from the catalyst surface. The eluted active compounds were increased for the case of longer regeneration time and higher sulfuric acid concentration. Sulfuric acid concentration and regeneration time were main operating factors in regeneration of waste catalyst. But, the conditions of waste catalyst are affected by the boiler and SCR operating conditions and preliminary tests are needed to check the waste catalyst and decide the regeneration method and process.

The purpose of this study is to synthesize transition metal doped mesoporous silica catalyst and to characterize its surface in an attempt to decomposition of N2O. Transition metal used to surface modification were Ru, Pd, Cu and Fe concentration was adjusted to 0.05 M. The prepared mesoporous silica catalysts were characterized by X-ray diffraction, BET surface area, BJH pore size, Scanning Electron Microscopy and X-ray fluorescence. The results of XRD for mesoporous silica catalysts showed typical the hexagonal pore system. BET results showed the mesoporous silica catalysts to have a surface area of 537 ∼973 m2/g and pore size of 2∼4 nm. The well-dispersed particle of mesoporous silica catalysts were observed by SEM, the presence and quantity of transition metal loading to mesoporous surface were detected by XRF. The N2O decomposition efficiency on mesoporous silica catalysts were as follow: Ru>Pd>Cu>Fe. The results suggest that transition metal doped mesoporous silica is effective catalyst for decomposition of N2O.

In this study, Ibuprofen (IBP) degradation by the photo catalytic process was investigated under various parameters, such as UV intensity, optimum dosage of TiO2, alkalinity, temperature and pH of bulk solution. The pseudo-first order degradation rate constants were in the order of 10-1 to 10-4 min-1 depending on each condition. The Photocatalytic IBP degradation rate increased with an increase in the applied UV power. At high UV intensity a high rate of tri-iodide (I3 -) ion formation was also observed. Moreover, in order to avoid the use of an excess catalyst, the optimum dosage of catalyst under the various UV intensities (30 and 40 W/L) was examined and ranged from approximately 0.1 gL-1. The photo catalytic IBP degradation rate was changed depending on the alkalinity and temperature and pH in the aqueous solution. This study demonstrated the potential of photo catalytic IBP degradation under different conditions.

A unit emission reduction of nitrous oxide (N2O) from anthropogenic sources is equivalent to a 310-unit CO2 emission reduction because the N2O has the global warming potential (GWP) of 310. This greatly promoted very active development and commercialization of catalysts to control N2O emissions from large-scale stationary sources, representatively nitric acid production plants, and numerous catalytic systems have been proposed for the N2O reduction to date and here designated to Options A to C with respect to in-duct-application scenarios. Whether or not these Options are suitable for N2O emissions control in nitric acid industries is primarily determined by positions of them being operated in nitric acid plants, which is mainly due to the difference in gas temperatures, compositions and pressures. The Option A being installed in the NH3 oxidation reactor requires catalysts that have very strong thermal stability and high selectivity, while the Option B technologies are operated between the NO2 absorption column and the gas expander and catalysts with medium thermal stability, good water tolerance and strong hydrothermal stability are applicable for this option. Catalysts for the Option C, that is positioned after the gas expander thereby having the lowest gas temperatures and pressure, should possess high deN2O performance and excellent water tolerance under such conditions. Consequently, each deN2O technology has different opportunities in nitric acid production plants and the best solution needs to be chosen considering the process requirements.

Ti-SBA-15 catalysts doped with samarium ion were synthesized using conventional hydrothermal method. The physical properties of Sm/Ti-SBA-15 catalysts have been characterized by XRD, FT-IR, DRS and PL. In addition, we have also examined the activity of these materials on the photocatalytic decomposition of methylene blue. The Sm/ Ti-SBA-15 was shown to have the mesoporous structure regardless of Sm ion doping. With doping amount of 1% lanthanide ion, the pore size and pore volume of Sm(Er, Cs)/Ti-SBA-15 decreased and the surface area increased. For the purpose of vibration characteristics on the Ti-SBA-15 and Sm/Ti-SBA-15 photocatalysts, the IR absorption at 960 cm-1 commonly accepted the characteristic vibration of Ti-O-Si bond. 1% of Sm/Ti-SBA-15 had the highest photocatalytic activity on the decomposition of methylene blue but the catalysts doped with Er ions had lower activity in comparison with pure Ti-SBA-15 catalyst.

TiO2- and SiO2-supported Co3O4, Pt and Co3O4-Pt catalysts have been studied for CO and C3H8 oxidations at temperatures less than 250℃ which is a lower limit of light-off temperatures to oxidize them during emission test cycles of gasoline-fueled automotives with TWCs (three-way catalytic converters) consisting mainly of Pt, Pd and Rh. All the catalysts after appropriate activation such as calcination at 350℃ and reduction at 400℃ exhibited significant dependence on both their preparation techniques and supports upon CO oxidation at chosen temperatures. A Pt/TiO2 catalyst prepared by using an ion-exchange method (IE) has much better activity for such CO oxidation because of smaller Pt nanoparticles, compared to a supported Pt obtained via an incipient wetness (IW). Supported Co3O4-only catalysts are very active for CO oxidation even at 100℃, but the use of TiO2 as a support and the IW technique give the best performances. These effects on supports and preparation methods were indicated for Co3O4-Pt catalysts. Based on activity profiles of CO oxidation at 100℃ over a physical mixture of supported Pt and Co3O4 after activation under different conditions, and typical light-off temperatures of CO and unburned hydrocarbons in common TWCs as tested for C3H8 oxidation at 250℃ with a Pt-exchanged SiO2 catalyst, this study may offer an useful approach to substitute Co3O4 for a part of platinum group metals, particularly Pt, thereby lowering the usage of the precious metals.

In this study, reaction model and reactions rate accelerated by o-iodosobenzoate ion(IB⊖) on hydrolysis reaction of p-nitrophenyl valate(NPV) using ethyl tri-octyl ammonium mesylate(ETAMs) for quaternary ammonium salts, the phase transfer catalysis(PTC) reagent, were investigated. The effect of IB⊖ on hydrolysis reaction rate constant of NPV was weak without ETAMs solutions. Otherwise, in ETAMs solutions, the hydrolysis reactions exhibit higher first order kinetics with respect to the nucleophile, IB⊖, and ETAMs, suggesting that reactions are occurring in small aggregates of the three species including the substrate(NPV), whereas the reaction of NPV with OH⊖ is not catalyzed by ETAMs. Different concentrations of NPV were tested to measure the change of rate constants to investigate the effect of NPV as substrate and the results showed that the effect was weak. This means the reaction would be the first order kinetics with respect to the nucleophile. This behavior for the drastic rate-enhancement of the hydrolysis is referred as 'Aggregation complex model' for reaction of hydrophobic organic ester with o-iodosobenzoate ion(IB⊖) in hydrophobic quarternary ammonium salt(ETAMs) solutions.