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국내 정수장 정수 수질자료의 특성분석 ( 1994 년 - 1998 년까지 5 년간 자료를 중심으로 )
윤제용(Je Yong Yoon),조순행(Soon Haeng Cho),김해심(Hae Shim Kim) 한국물환경학회 2000 한국물환경학회지 Vol.16 No.4
Water quality data from water treatment plants in Korea during 1994-1998 were investigated to find out the characteristics of their non compliance. The number of plants surveyed were approximately 600 and the number of samples were over 30,000. Ten parameters of water quality selected in this study and their non compliance % (inside parenthesis) were as follows : Heterotrophic plate count (0.14 %), Total coliforms (0.08%), NH₃-N (0.29%), NO₃-N (0.14%), THMs (0.02%), Turbidit(0.11%), Residual chlorine (5.5%), KMnO₄ consumption(0.04%), Hardness(0.03%), pH(0.07%). These levels of non compliance were compared to those obtained from WIDB (Water Industry Database, 1996) of American Water Works Association. This study strongly supported that small water plants ($lt;10,000 tons/day) were more vulnerable in meeting the regulation criteria of many water quality parameters such as Heterotrophic plate count, Total coliforms, NO₃-N, THMs, Turbidity, Residual chlorine, KMnO₄ consumption, Hardness and pH. The NH₃-N concentration was especially high in winter and its violation was frequently found in the specific areas such as the downstream of major rivers. The average THMs concentration was surprisingly low, indicating 13㎍/L which is 43% of US. Accordingly, these characteristics must be reflected in establishing the effective management of water quality policy of drinking water in Korea.
2탑 및 3탑식 Oxygen PSA 장치 운전결과 및 경제성 비교분석
김권일,김종남,조성철,조순행,진명종 ( Kweon Ill Kim,Jong Nam Kim,Sung Chul Cho,Soon Haeng Cho,Myung Jong Jin ) 한국공업화학회 1996 공업화학 Vol.7 No.4
산소 PSA 장치 구성을 위하여, 여러 가지 흡착제에 대한 산소 및 질소의 평형흡착량을 측정하여 유효흡착량을 비교함으로써 산소 PSA에 적절한 흡착제를 선정하였고 Langmuir isotherm parameter를 구하였다. PSA 공정의 단계는 흡착, 탈착, 축압, 세정 및 균압 등으로 구성하고 흡착압력은 2atm을 기준으로 운전하였고 탈착압력은 120∼400torr이며 cycle time은 2탑 80, 3탐 180초로 운전하였다. 2탑식과 3탑식 산소 PSA 장치의 운전특성과 경제성을 비교 분석하기 위하여, 운전조건에 따른 2탑식 및 3탑식 공정의 제품 생산성, 산소농도, 회수율을 비교하였고, 세정 및 축압단계의 영향을 분석하였으며, 대형화 하였을 경우의 투자비와 전력비를 추산하여 2탑식과 3탑식 산소 PSA의 경제성을 비교하여 700Nm³/hr 이하 규모에서는 2탑식이 유리함을 확인하였다. For oxygen PSA process development, adsorbed amount of oxygen and nitrogen on various adsorbents were measured corresponding Langmuir isotherm parameters were measured. A reasonable adsorbent for oxygen process was selected based on the effective adsorbed amount. The PSA process consists of adsorption, desorption, pressurization, purging and pressure equilization steps. Adsorption pressure was about 2 atm and desorption pressure was between 120 torr to 40Dtorr. Cycle time of 2-bed PSA process was 80 seconds and that of 3-bed oxygen PSA process was 180 seconds. In order to compare and analyze operation characteristics and economic feasibilities of 2-bed and 3-bed oxygen PSA processes, productivity, oxygen concentration and recovery were compared and the effect of purge and pressurization steps on the performance of PSA processes were analyzed. For the commercial scale oxygen PSA process, capital and electricity cost were estimated. In the range of O₂production less than 700Nm³/hr, the 2-bed process is conformed more feasible in economic view point.
조순행,서성섭,김종남,신흥수,장동근 한국화학공학회 1999 Korean Chemical Engineering Research(HWAHAK KONGHA Vol.37 No.6
석유화학공장에서 나오는 배가스인 수소, 이산화탄소, 일산화탄소, 메탄의 원료혼합가스로부터 수소를 회수할 수 있는 다탑 PSA공정을 orthogonal collocation법에 의해 전산모사하였다. 고순도 수소를 생산하기 위하여 흡착성능이 다른 두 흡착제를 연속으로 충전시킨 4탑 9단계 공정을 대상으로 하였다. 제올라이트와 활성탄의 충전비율은 제품의 순도 및 회수율에 영향을 미치며 각 흡착제에 대한 최적의 충전길이는 각각 60 ㎝이었다. 주어진 충전비율에 대해서 최적의 흡착 압력과 원료기체 공급 속도가 각각 19 atm 및 11.0 ㎝/s로 결정될 수 있었다. 고압에서 저압으로 떨어지면서 세정기체를 공급하는 항류 감압단계에서 압력 변화의 크기(DP) 즉, 세정 단계로 공급되는 세정기체의 양이 제품의 회수율과 순도에 크게 영향을 미쳤다. DP가 1.3 atm이상에서는 DP가 증가함에 따라 순도가 크게 변하지 않았지만 회수율은 계속 감소하였다. DP가 커질수록 압력균등화 병류감압단계에서의 압력이 낮아지고 세정단계 다음에 이어지는 압력균등화 항류가압단계에서의 균등 압력도 낮아졌으며, 이에 따라 생성물 가압단계에서 압력을 높이는데 필요한 기체 생성물의 양이 증가하였다. Numerical simulation for hydrogen-recovery multibed PSA process was performed by orthogonal collocation method for the feed mixture gas of hydrogen, carbon dioxide, carbon monoxide, and methane in petrochemical plant. A fourbed and nine-step process using a layered-bed which was consecutively packed with two different adsorbents in one bed was employed to produce high-purity hydrogen. The packing ratio of zeolite to activated carbon affected the purity and recovery of the product. The optimum length of zeolite layer and that of activated carbon layer were 60 ㎝ each. The optimum adsorption pressure and feed velocity could be determined to be 19 atm and 11.0 ㎝/s, respectively, for the given packing ratio. The recovery and purity of the product were strongly affected by Difference-Pressure(DP) which was defined as the difference between the initial high pressure and the final low pressure at the cocurrent blowdown step which delivers purge gas to the low pressure bed. When the DP was larger than 1.3atm, the purity did not change much and the recovery was continuously decreased with increasing DP. As DP increased, the pressure at the pressure-equalization cocurrent depressurization step was lowered and the pressure at the pressure-equalization countercurrent pressurization step following purge step was also lowered. Therefore, the amount of the high-pressure product to pressurize the low-pressure column increased.