This study investigated phosphorus removal from secondary treated effluent using coagulation-membrane separation hybrid treatment to satisfy strict regulation in wastewater treatment. The membrane separation process was used to remove suspended phosphorus particles after coagulation/settlement. Membrane separation with 0.2 μm pore size of micro filtration membrane could reduce phosphorus concentration to 0.02 mg P/L after coagulation with 1 mg Al/L dose of polyaluminum chloride (PACl). Regardless of coagulant, the residual concentration of phosphorus decreased as the dose increased from 1.5 to 3.5 mg Al/L, while the target concentration of 0.05 mg P/L or less was achieved at 2.5 mg Al/L for the aluminum sulfate (Alum) and 3.5 mg Al/L for PACl. Moreover, alum showed better membrane flux as make bigger particles than PACl. Alum showed a 40% of flux decrease at 2.5 mg Al/L dose, while PACl indicated a 50% decrease of membrane flux even with a higher dose of 3.5 mg Al/L. Thus, alum was more effective coagulant than PACl considering phosphorus removal and membrane flux as well as its dose. Consequently, the coagulation-membrane separation hybrid treatment could be mitigate regulation on phosphorus removal as unsettleable phosphorus particles were effectively removed by membrane after coagulation.

Modified coagulants were investigated for the removal of phosphorus from secondary effluent of wastewater treatment. The modified coagulants were prepared by mixing alkali earth metal ions such as calcium and magnesium. The basicity of a coagulant influenced on the removal of phosphorus, and coagulants with basicity of 5.9% showed a better removal of total phosphorus than that of 38.5%. Also, coagulants with alkali earth metals enhanced the performance of coagulation by 10% and resulted in 67.1% for total phosphorus removal. Moreover, the removal of suspended solids and chemical oxygen demand was improved using coagulants with low basicity and earth metal ions. Results of this study demonstrated that the use of coagulants with low basicity, and calcium and magnesium ions is recommended to improve wastewater effluent quality.

원자력시설에서 방사성요오드 제거용으로 사용되는 TEDA 첨착활성탄의 고온공정에서치 메틸요오드의 제거성능을 은이온제올라이트(AgX)와 상호 비교하였다. 3-40 온도범위에서 온도에 따른 메틸요오드의 흡착량 및 탈착후 잔존량을 측정한 결과, 비첨착활성탄의 흡착성능은 온도가 증가함에 따라 급격히 감소하지만 TEDA 첨착활성탄의 흡착성능은 10 부근에서도 AgX-10과 거의 유사한 값을 나타내었고, 탈착후 잔존량은 25 까지도 비첨착활성탄에 비하여 매우 높은 값을 유지하였다. 또한 10 이상의 고온공정에서 AgX 및 TEDA 첨착활성탄을 충전한 고정층 파과특성을 상호 비교한 결과 10 이상에서 AgX-10의 메틸요오드 흡착량 및 잔존량은 TEDA 첨착활성탄에 비하여 평균 30%정도 높은 값을 나타내어 고온에서 더 흡착성능이 우수함을 보여주고 있다. 흡착반응 후 생성된 기체의 성분을 분석한 결과를 토대로 AgX-10 흡착제를 충전한 고정층에서 메틸요오드 제거 메카니즘을 제안하였다.

SF6 (sulfur hexafluoride) gas has an extremely high global warming potential (GWP) because of strong absorption of infrared radiation and long atmospheric lifetime which cause the global warming effect. The objective of this study is to identify the effects of destruction and removal efficiency (DRE) of SF6 by the addition of oxygen, water vapor and hydrogen. The applied dose of ionization energy was 1,028 kGy(5 mA). The initial concentrations of SF6, O2, H2O and H2 gases were 1,000 ppm, 1,000 ppm, 3,000 ppm, 3,000 ppm, respectively. The DRE was increased about 2 times with O2 gas injection. The SF6 was completely removed with H2O and H2 gas injection. By-products formed by SF6 destruction were mainly HF and F2 gases. In addition, SF2, NF3, N2O, SO2, SO2F2, and NOx gases were produced.

The purpose of this study was to investigate the characteristics of removal efficiency for aromatic hydrocarbons using a high-temperature fiber filter on a laboratory scale. The main elemental compositions of a high-temperature fiber filter are aluminium and silica, which can act as the catalysts. Benzene, toluene and o-xylene among aromatic hydrocarbons were used in this experiment. For 3㎝ thickness of fiber filter, these compounds were removed more than 90% at the face velocities of 3㎝/sec and 5㎝/sec above 450℃. For 4㎝ thickness of it, the removal efficiencies of these compounds were almost 90% from 400℃ at the same face velocities, suggesting that it may be due to increasing the contact time between the fiber filter and aromatic hydrocarbons. The pressure drop ranged from 22 to 48㎜H2O for 3㎝ thickness of fiber filter. However, for 4㎝ thickness of it, it was about two times(41-89㎜H2O) higher than that for 3㎝ fiber thickness.