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강석환,이영우,강용,한근희,이창근,진경태,손재익,박영성,Kang, Suk-Hwan,Rhee, Young-Woo,Kang, Yong,Han, Keun-Hee,Yi, Chang-Keun,Jin, Gyoung-Tae,Son, Jae-Ek,Park, Yeong-Seong 한국에너지학회 1996 에너지공학 Vol.5 No.2
석탄가스화 복합발전 시스템의 주요 단위 공정인 고온건식 탈황공정에 사용되는 탈황제의 개발을 위한 연구의 일환으로 국내산 철광석과 호주산 철광석에 대해 환원, 황화 및 재생 반응을 수행하였다. 실험 장치로는 TGA와 시료 제조용 고정층 반응기를 이용하였고, BET 표면적, SEM, 탈황/재생 cycle 실험, 반응 온도 변화 및 탈황제의 질량변화곡선 등을 이용하여 세가지 철계 탈황제에 대한 기초반응 특성을 규명하였다. 500-$700^{\circ}C$ 구간에서 반응온도 증가에 따라 탈황반응의 H$_2$S 제거율과 재생반응의 재생율이 증가하였다. Reduction, sulfidation, and regeneration reactions were performed using domestic and Australian iron ore in order to develop a desulfurizing sorbent for the high temperature desulfurization process that is one of major processes in the integrated coal gasification combined cycle (IGCC) system. A TGA (Thermogravimetric Analysis) reactor and a fixed-bed reactor were used. Some basic kinetic information was obtained from BET surface area measurements, SEM photos, cyclic reactions, reaction temperature changes and TGA curves of the sorbents. The rates of both desulfurization and regeneration increased with increasing reaction temperature in the range of 500-700$^{\circ}C$.
이영우,손재익,박영옥 忠南大學校 産業技術硏究所 1997 산업기술연구논문집 Vol.12 No.1
A neutralized fabric filter was characterized in terms of pressure drop, penetration and figure of merit in a pilot scale test unit for two kinds of ash dust generated from coke manufacturing process of steel industries (coke ash) and clinker calcination process of cement industries (clinker ash). Effects of filtration velocity, cleaning method, pulse jet cleaning pressure, and bag cage type on the characterizing items were investigated. In order to perform an effective cleaning operation and continuous dust collection for both of dust filtrations, the filtration velocity and poulse jet cleaning pressure should be kept above 1.0m/min and 4.0kg/㎠ respectively. The suitable cleaning interval and dust loading for the coke dust filtration were 4 minutes and 120-200g/㎡, and under these conditions the pressure drop and dust penetration could be maintained below 30mmH₂O and 0.5%, respectively. Also, the suitable cleaning interval for the clinker dust filtration was 1 hour, and under this condition the pressure drop and dust penetration could be maintained below 90mmH₂O and 0.5%, respectively. A visual analysis for dust penetration phenomena suggested that a reinforcement be needed for the bag filter in the region of 70cm below the top of the bag cage, especially below the venturi.