Most wastewater treatment plants are facing odor and sludge disposal problems. In this lab-scale study, odor and sludge from wastewater treatment processes were treated using a combined non-thermal plasma and sludge reactor. The hydrogen sulfide concentration introduced to the reactor was varied at 10, 20, and 50 ppm, and its removal efficiency and system performance were determined. Ozone was produced by the plasma reaction at a concentration of 200 ppm under the given condition. 80% of the hydrogen sulfide was removed regardless of its introduced concentration. In addition, due to the ozone carried over to the sludge reactor, the organic constituents in the waste sludge in terms of TCOD decreased by 30%. The ion concentrations of HS- and SO₄²⁻ in the sludge increased during the four hour experimental period. As a result, the plasma oxidation system can treat waste sludge effectively for the simultaneous reduction of sludge volume and odor.

The continuous transesterification of mixed fat was done on the plug flow reactor packed with the static mixers. The transesterification using 0.5 wt% KOH, 0.8 wt% TMAH and mixed catalyst[40 v/v% KOH(0.5 wt%)+60 v/v% TMAH(0.8 wt%)] was conducted with the changes of molar ratios, weight percentage of beef, flow rates and number of static mixer's elements at 65℃. The overall conversion of mixed fat at 1:8 molar ratio, 50 wt% of beef and 24 of static mixer's elements increased until 0.7mL/min of flow rate. The overall conversion of mixed fat showed 96% at those conditions. So, the optimum operating conditions on tublar reactor were 1:8 molar ratio, 50 wt% of beef, 0.7 mL/min of flow rate and 24 of static mixer' s elements.

the less-reported gaseous studies have primarily dealt with chemical process stream concentrations than indoor air quality (IAQ) concentration levels. Accordingly, the current study was conducted to establish the feasibility of applying visible-light-induced TiO₂ doped with sulfur (S) element to cleanse toluene and ehtyl benzene at IAQ levels. The S-doped TiO₂ was prepared by applying two popular processes and two well-known methods. For both target compounds, the two coating methods exhibited different photocatalytic oxidation (PCO) efficiency. Similarly, the two S-doping processes showed different PCO efficiency. These results indicate that the coating method and doping process are important parameters which can influence PCO efficiency. Meanwhile, it was found that the PCO efficiency of ethyl benzene was higher than that of toluene. In addition, the degradation efficiency of the target compounds increased as the relative humidity (RH) decreased. The PCO efficiency varied from 44% to 74% for toluene and from 68% to 95%, as the RH decreased. Consequently, it is suggested that with appropriate RH conditions, the visible-light-assisted photocatalytic systems can also become an important tool for improving IAQ.

Theoretical total nitrogen removal efficiency and reactor volume ratio in oxic-anoxic-oxic system can be found by influent water quality in this study. The influent water quality items for calculation were ammonia, nitrite, nitrate, alkalinity, and COD which can affect nitrification and denitrification reaction. Total nitrogen removal efficiency depends on influent allocation ratio. The total nitrogen removal follows the equation of 1/(1+b). Optimal reactor volume ratio for maximum TN removal efficiency was expressed by those influent water quality and nitrification/denitrification rate constants. It was possible to expect optimal reactor volume ratio by the calculation with the standard deviation of ±14.2.

Recently, a bioactive foam reactor (BFR) using a surfactant and suspended microorganisms has been suggested as an suitable alternative to conventional packed-bed biofilters. This study was conducted to demonstrate the feasibility of applying the BFR using styrene as a model compound and investigate the effect of the gas residence time on mass transfer and biodegradation rates. At a gas residence time of 40 seconds, the BFR achieved high styrene removal efficiencies greater than 80%, but the biodegradation rate controlled the overall efficiency as the styrene inlet concentration increased. Meanwhile, at a gas residence time of 20 seconds, the change of the styrene removal efficiency was less sensitive to the inlet styrene concentration, indicating the BFR system was operated under the mass transfer limited condition. Therefore, the mass transfer rate needs to balance with the biodegradation rate in the BFR system, and the foam stability had a significant effect on the mass transfer. In the BFR, the maximum elimination capacity was found to be 117 g/㎥/hr, which was higher than those reported in the literature. This finding indicates that the BFR can be an efficient method for the treatment of various VOCs and expand an application range of biological processes.

[ 250℃의 고온에서 수증기 선택 투과 특성을 가지는 silica 막을 메탄을 탈수에 의한 dimethyl ether (DME) 합성 반응에 분리막 반응기로 적용하였다. Silica 전구체로서 tetraethoxysilane (TEOS)을 이용하여 초음파 분무 열분해 및 기상화학 증착법(CVD)법 등에 의해 다공성 스테인레스 스틸(SUS)에 silica 막을 합성하였다. CVD법에 의해 합성한 silica막의 수증기 투과도 및 메탄올에 대한 분리계수 상관관계 trade-off 선이 열분해 silica 막보다 높이 존재하였다. 수증기 투과도가 1.2×10-7;mol;·;m-2;·;S-1;·;Pa-1 이상이고, 메탄올에 대한 분리계수가 10 이상의 성능을 가지는 분리막 반응기에 대해서 기존 반응기 대비 20% 이상 메탄을 전환율이 향상되었다. 고온 수증기 선택성 silica 막이 메탄을 탈수 반응에 의해 생성되는 수증기를 제거함으로서 촉매 활성 저하를 억제하여 반응 전환율을 개선시키는 막 반응기로서의 효과를 확인할 수 있었다.

유기물과 질소를 동시에 제거하기 위하여 연속회분식으로 운전한 MBR (membrane bioreactor)시스템에서 미생물농도와 슬러지 부하량이 막오염과 미생물 활성에 미치는 영향을 살펴보았다. 막오염은 MLSS (mixed liquor suspended solid) 농도 증가에 따라 조금씩 증가하는 경향을 보였고, 그 효과는 비포기 조건보다 포기 조건에는 좀더 두드러지게 나타났다. MLSS 농도는 막오염에 직접적인 커다란 영향을 주지는 않으나, 지나치게 높은 MLSS에서 유도되는 낮은 슬러지 부하에서는 막오염이 크게 증가하는 현상이 발견되었고, 이러한 조건에서는 포기에 의한 막 세척 효과도 크게 줄어들었다. 미생물의 개별 활성도는 슬러지 부하가 감소할수록 지속적으로 감소하는 경향을 나타내었다 반응조 전체 활성도 또한 17,000 mg/L 이상의 높은 MLSS로부터 유도되는 낮은 슬러지 부하율에서는 높은 미생물 농도에도 불구하고 오히려 감소했는데 이는 기질 부족으로 인한 경쟁으로 활성도가 떨어지고, 용액의 점성 증가로 인해 산소 전달율이 저하되었기 때문이다.

Synthesis gas is a high valued compound as a basic chemicals at various chemical processes. Synthesis gas is mainly produced commercially by a steam reforming process. However, the process is highly endothermic so that the process is very energy-consuming process. Thus, this study was carried out to produce synthesis gas by the partial oxidation of methane to decrease the energy cost. The effects of reaction temperature and flow rate of reactants on the methane conversion, product selectivity, product ratio, and carbon deposition were investigated with 13wt% Ni/MgO catalyst in a fluidized bed reactor. With the fluidized bed reactor, CH4 conversion was 91%, and Hz and CO selectivities were both 98% at 850℃ and total flow rate of 100 mL/min. These values were higher than those of fixed bed reactor. From this result, we found that with the use of the fluidized bed reactor it was possible to avoid the disadvantage of fixed bed reactor (explosion) and increase the productivity of synthesis gas.

Phytopathogenic fungi들에 대해 매우 공격적인 Trichoderma hurzianum은 다른 곰팡이들의 세포벽 주성분인 chitin을 분해하는 extracellualr chitinase를 분비하기 때문에 매우 효율적인 biocontrol agent로 사용할 수 있다. Trichoderma harzianum의 생물학적 제어 기능을 이용하기 위하여 extracellualr chitinase의 생산성을 높일 수 있는 batch모드에서의 적정

The effects of reaction temperature and flow rate of reactants on the methane conversion, product selectivity, product ratio, and carbon deposition were investigated with 13wt% Ni/MgO catalyst. Reaction temperatures were changed from 600 to 850℃, and reactants flow rates were changed from 100 to 200 mL/mim. There were no significant changes in the methane conversion observed in the range of temperatures used. It is possibly stemmed from the nearly total exhaustion of oxygen introduced. The selectiveties of hydrogen and carbon monoxide did not largely depend on the reaction temperature. The selectivities of hydrogen and carbon monoxide were 96 and 90%, respectively. Carbon deposition observed was the smallest at 750℃ and the largest at 850℃. It is found that the proper reaction temperature is 750℃. The best reactant flow rate was 150 ml/min.

Copolymerization of α-Methylstyrene(AMS) with Acrylonitrile(AN) was carried out with benzoylperoxide(BPO) as an initiator in toluene at 80℃ in a continuous stirred tank reactor. Reaction volume and residence time were 0.6 liters and 3 hours, respectively. The monomer reactivity ratios, rAMS and rAN determined by both the Kelen-Tüdös method and the Fineman-Ross method were rAMS=0.16(0.14), rAN=0.04(0.06). The cross-termination factor Φ of the copolymer over the entire AMS composition ranged from 0.75 to 0.92. The Φ factors of poly(AMS-co-AN) were increased with increasing AMS content. The simulated conversions and copolymerization rates were compared with the experimental results. It was observed that the average time to reach dynamic steady-state was three times the residence time.

불용성 농축어육단백질(fish protein concentration, FPC)의 기능성을 개선하기 위한 목적으로 한외여과막 반응기 (MWCO 5,000)를 사용하여 효소적 가수분해를 시도하였다. 막반응기에서 불용성인 FPC의 막힌현상(fooling)을 완화시키기 위하여 회분식에서 pepsin으로 1차 가수분해하였으며, 그 가수분해물을 한외여과막 반응기에서 pronase E를 사용하여 2차 가수분해하였다. 회분식에서 FPC의 최적가수분해 조건은 45℃, pH 2.0, 기질 대 효소비 150 (w/w)였으며, 이때의 가수분해도는 약 89%였다. 회분식에서 반응속도 상수 Km 및 Vmax는 각각 1.25%, 0.89 mg/mℓ/min이었으며, 기질농도 1.5% 이상에서 기질저해가 있었다. 한외여과막 반응기는 순환속도 474 mℓ/min, 투과압력 15 psi로 작동하였으며, 온도에 따른 투과유속은 증가하였으나 pH에 대해서는 거의 일정하였다. 막반응기에서 기질과 2차 가수분해효소 pronase E의 비 (S/E)는 200 (w/w)이 가장 효율적이었으며, 이때의 가수분해물의 생산량은 효소 mg당 702 mg으로 회분식 51 mg에 비해 13배 이상 높았다. FPC 가수분해물의 분자량은 1차 가수분해물의 경우 2,500~20,000 Da 영역에 분포하였으며, 2차 가수분해물은 700~10,000 Da 이었다.

가용성 전분으로부터 CGTase 효소에 의한 Cyclodextrin(CD) 동족체의 생산 실험을 dead-end형 막모듈을 설치한 막-효소 반응기에서 수행하였다. 회분 반응기에서의 CD 동족체 생산시 생산물 저해작용 및 생산된 CD의 다른 환원당으로의 분해에 의해 반응시간에 따른 전분의 CD 동족체로의 총 전환율이 최대 45%를 나타내었다가 급격히 감소하였다. 반면 분획분자량 10,000 달톤의 분리막이 설치된 막-효소 반응기에서의 CD 동족체 생산시 CD 동족체를 생산 즉시 반응기로부터 막을 통해 연속 분리할 수 있어 총 전환율이 35%로 일정하게 유지되었다. 10% 전분용액 및 2 atm 조작압력하에서 막-효소 반응기를 24시간 운전하였을 때 CD 동족체의 누적 생산량은 약 3.7 kg/m2이었다.

한외여과막 반응기에서 gelatin 및 bovine serum albumin(BSA) 용액을 한외여과막(MWCO 5,000)으로 여과시 작동시간, pH, 온도, 농도 및 단백질 가수분해 효소의 첨가가 투과유속에 미치는 영향에 대하여 검토하였다. 한외여과막 반응기의 작동시간에 따른 gelatin 용액의 투과유속은 작동시간 20분까지 약간 감소하다가 그 이후에는 18.9l/m2· hr로 거의 일정하게 유지되었으며, BSA 용액은 작동시간 40분까지 완만하게 감소하다가 그후 6.4l/m2· hr로 초기유속의 66%가 감소하였다. 온도에 따른 gelatin 용액의 투과유속은 온도가 올라감에 따라 비례적으로 증가하였다. BSA 용액은 60℃에서 투과유속이 가장 높았으며, 30~50℃ 범위에서는 온도의 영향을 받지 않았다. pH 변화에 따른 gelatin 및 BSA 용액의 투과유속은 10psi 이상에서 각각의 등전점 영역인 pH 5.0에서 가장 낮았다. 투과압력 30psi에서 1% 및 6%(w/v) gelatin용액의 투과유속은 각각 43.0l/m2· hr 및 13.5l/m2· hr 였으며, BSA 용액의 경우는 1% 및 4%에서 33.0l/m2· hr 및 14.0l/m2· hr로 농도가 증가됨에 따라 각각 68.6% 및 57.6% 감소하였다. Gelatin 및 BSA 용액에 단백질 가수분해효소의 첨가에 의한 투과유속은 gelatin 및 BSA의 저분자화에 의한 점도의 감소로 효소를 첨가하지 않은 것보다 30% 향상되었다.