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The blend (wax M) of crude by-product polyolefin wax (wax K) and a fractionated commercial paraffin wax (wax J) was suggested to replace the wax J as a coating agent for wax-coated papers. The rheological properties of waxes J, K, and M were examined and compared. The correlation between viscosity and shear rate applied on these waxes maintained at 90 oC and 130 oC was identified. In particular, this paper, for the first time, presented non-Newtonian shear thinning behavior of not only wax K but also its blend of wax M in terms of their viscosity affected by shear rate at an operating temperature below their melting temperature of higher-melting-temperature DSC endothermic peaks (HMTEPs). They showed non-Newtonian behavior, so-called shear thinning behavior, at 90 oC in the light of characteristics of both suspension systems and polymer systems. In addition, the profiles of viscosity at 130 oC of all the waxes versus the shear rate exhibited Newtonian fluid behavior. Wax J also showed the behavior of a dilatant fluid. Then, the physical properties including water vapor transmission rates (WVTR), surface roughness, and coated weights, of thin papers coated with waxes J (WJP), K (WKP), and M (WMP) were evaluated, characterized, and compared. As a result, WMP had an equivalent value to that of WJP or the lowest value among wax-coated papers in terms of WVTR. The surface roughness and the barrier property of WVTR were minimized and enhanced, respectively, by blending waxes J and K. The additional physical properties, including dynamic contact angles, surface tension, wet and dry tensile strength, optical examination of the wax-coated fiber structure, and antimicrobial properties of the wax-coated papers, were evaluated. The excellent antimicrobial properties of clinoptilolite added to wax J or wax M appeared.

Curcumin was incorporated into oil/water (o/w) emulsion by dissolving it in soybean oil to cover the surface of the oil droplets with a pH-sensitive polyelectrolyte complex (PEC) composed of chitosan and fucoidan molecules. This curcumin-loading efficiency of the suspension system was investigated. The size and zeta potential distributions of novel curcumin-loaded chitosan nanoparticles self-assembled with fucoidan (CFNPLC) were assessed at various pH and fucoidan-to-chitosan mass ratio (FCMR). The release behavior of curcumin from CFNPLC was confirmed quantitatively by the superimposition of relevant release behavior. The release of curcumin from CFNPLC prepared with a chitosan solution of pH 6 for one to two days was slower than that from CFNPLC prepared with a chitosan solution of pH 3.7 for five to 10 hrs. This was attributed to the higher affinity of a chitosan molecule to curcumin molecules at a higher pH. The centrifugation of release medium accelerated the release of curcumin droplet from the surface of CFNPLC into the release medium much faster than a conventional curcumin release. Not to mention a high stability of curcumin blended with soybean oil, encapsulated in CFNPLC, the advantage of the CFNPLC is addressed in such a way that curcumin releasing period of a conventional curcumin delivery using CFNPLC, is supposed to be extended for much longer time than one to two days of the curcumin release period in this study. Thus, CFNPLC can bring about an enhanced effect of curcumin bioavailability resulting from the high curcumin stability and its extended release because it was dissolved in soybean oil and CFNPLC sustained slow curcumin-release for more than days in the oral drug (curcumin) delivery system. Therefore, CFNPLC can be treated mainly as a food-functional additive or healthy dietary product for tumor patients.

구미공단 대규모합성섬유제조업체들의 총괄 점오염원 및 개별 점오염원에 의한 각각의 트리메틸아민 관련 기여도 평가예측을 위하여 CALPUFF 모델링을 수행하였다. 또한 개별 점오염원의 총괄 점오염원에 대한 트리메틸 관련 상대적 기여도를 산출하였다. T사 배출설비 개선 후 총괄 점오염원의 트리메틸아민 배출에 의한 본 연구 CALPUFF 모델링 결과로서 2011년 겨울(1월), 봄(4월)에는 주로 구미 3공단에서, 여름(7월), 가을(10월)에는 주로 구미 1공단에서 트리메틸아민 농도의 최대값이 도출되었다. 한편 T사 배출설비 개선 후에는 구미 1공단의 경우에 트리메틸아민 예측 최대값 범위가 매우 개선되었음이 확인되었다. 반면에 구미3공단의 경우는 T사 배출설비 개선 후에 오히려 트리메틸아민 예측 최대값의 상한치가 더욱 커졌으나 그 상한치를 제외하였을 때는 T사 배출설비 개선 전의 트리메틸아민 측정치의 상한치와 비슷하였다. 이와 같이 T사 배출설비 개선이 공단별 트리메틸아민 농도에 미치는 영향이 구미 1공단에서는 컸으나 구미 3공단에서는 미미한 수준이었다. 한편 본 연구 CALPUFF 모델링 결과로서 트리메틸아민 농도 예측치는 트리메틸아민 농도의 측정치 범주와 거의 일치하므로 본 연구의 총괄 점오염원에 의한 트리메틸아민 기여도 평가에 대한 유효성을 보여주었다.

본 연구에서는 CALPUFF 모델링을 수행하여 구미국가산업단지 공단지역에 악취로 인한 주민의 민원이 빈번한 지역과 아세트알데히드 배출 주요 점오염원인 구미국가산업단지 공단지역 합성섬유제조업체 악취배출시설과의 상관관계를 정립하고자 하였다. 본 연구의 CALPUFF 모델링 결과로서 T사 배출설비 개선 후에 구미공단의 아세트알데히드 농도의 최대값이 T사 배출설비 개선 전보다 O (10-5 g/m3)에서 O (10-6 g/m3)으로 저감되고 겨울(1월)과 봄(4월)에 구미 1공단의 아세트알데히드 농도가 개선되어서 구미 3공단에서 자주 아세트알데히드 농도의 구미공단 내 최대값이 도출되었다. 또한 T사 배출설비 개선 후에 도출된 아세트알데히드 농도의 구미공단 내 최대값 예측범위는 T사 배출설비 개선 전의 구미공단 내 최대값 예측범위보다 개선되었다. 이와 같은 총괄 점오염원의 아세트알데히드 기여도 평가 예측을 위한 CALPUFF 모델링 최대값은 ‘구미대구지역 HAPs 조사연구’의 측정 최대값 결과와 비교하였을 때에 상호비교할 수 있는 비슷한 값을 보였고 민원추세와도 잘 일치하였다. 따라서 본 연구에서 총괄 점오염원의 아세트알데히드 기여도 평가 예측에 대한 유효성을 보여주었다. 한편 총괄 점오염원에서의 아세트알데히드 배출에 의하여 확산된아세트알데히드 농도에 대한 T사 점오염원의 상대적 기여도가 T사 배출설비 개선 후에 개선 전보다 대부분 배 이상낮아짐이 예측되었다. 반면에 이에 대한 W사 점오염원의 상대적 기여도는 T사 배출설비 개선 후가 T사 배출설비 개선 전보다 배 이상 증가하였다. 이것은 T사 배출설비 개선에 의하여 상대적으로 W사 점오염원의 아세트알데히드 기여도가 커졌음을 의미하였다.

The stoichiometric distributions of both positive amino groups and negative sulfate ions loaded in chitosan-fucoidan nanoparticles (CFNs) were predicted quantitatively by correlating the separate yields of loaded chitosan and fucoidan, and a proposed relative charge density model (case 1). In addition, those distributions of both positive amino groups and negative sulfate ions loaded in CFNs were obtained by deriving the expression of their loaded concentrations directly from the experimental data (case 2). Both the model-prediction and experimental derivations were remarkably consistent with each other except at pH 2. The discrepancy between cases 1 and 2 at pH 2 was explained by an increase in the sulfate group loading because of the most intensive electrostatic (specific ion) interactions at pH 2. The ratio of the CFN-free net charge density shielded by counter-ions in the solution entrapped in CFNs to their counter-ion-crosslinking charge density was suggested to be a quantitative criterion for determining the size distribution of CFNs. The formation of CFNs ranked according to size was predicted well and explained reasonably by the suggested criterion, considering both the ionic strength of the entrapped solution in CFNs and the nonspecific binding (interaction) of the positive amino groups among the chitosan molecules. Furthermore, the fraction of nonspecifically-bound positive amino groups causing hysteresis was quantified from the positive net charged amino groups per unit-mass CFN. Thus, its magnitude was predicted to have a strong correlation with the CFN-preparation conditions, such as pH and fucoidan to chitosan mass ratio.

D염색공단의 폴리에스테르 알카리 감량폐수가 혼합된 실제 혼합염색폐수를 처리하기 위하여 Pseudomonas sp. 및 Bacillus cereus/thuringiensis를 고정한 폐타이어담체를 충전한 유동상 바이오필터를 운전하였다. 또한 유동상 바이오필터와 450 W의 UV/광촉매반응기를 결합한 하이브리드 재순환시스템을 구축하여 stage I에서는 UV/광촉매반응기를 바이패스하고 유동상 바이오필터만을, stage II-i, ii, iii에서는 하이브리드 재순환시스템을 각각 운전하였다. 유동상 바이오필터만을 사용하였을 경우에 $COD_{Cr}$ 및 색도 제거효율은 각각 75~80% 및 67%를 나타내었다. 한편 하이브리드 재순환시스템 운전에서 stage I에서 stage II-i로 전환되었을 때에 UV/광촉매산화공정의 $COD_{Cr}$ 제거율이 20~30%에 달하여 총 $COD_{Cr}$ 제거율은 75%로부터 80~85%까지 제고되었다. 한편 stage I에서 stage II-i로 전환되었을 때에 UV/광촉매산화공정의 색도제거율은 0~5%에 불과하였으나 총 색도제거율은 45~65%로부터 65~70%까지 제고되었다. 색도 제거에서는 $COD_{Cr}$ 제거와 다르게 UV/광촉매산화공정에 의하여 유동상 바이오필터의 효율이 제고되어서 하이브리드 재순환시스템의 시너지효과가 나타났다. 또한 색도제거에서는 $COD_{Cr}$ 제거와 다르게 반송비 증가에 따른 광촉매 비활성화가 관찰되지 않았고, $COD_{Cr}$ 제거에서 반송비 증가에 따른 광촉매 비활성화는 비가역적으로 관찰되었다. 【A fluidized biofilter was filled with Pseudomonas sp. and Bacillus cereus/thuringiensis-fixed waste-tire crumb media and was run to treat authentic textile-dyeing wastewater mixed with alkaline polyester-weight-reducing wastewater. As a result, its removal efficiency of $COD_{Cr}$ and color were 75~80% and 67%, respectively. In addition, upon constructing hybrid-recirculating system composed of the fluidized biofilter and a 450 W-UV/photocatalytic reactor, only fluidized biofilter was run bypassing UV/photocatalytic reactor at stage I. Subsequently, the hybrid system was continuously run at stage II-i, ii and iii. At stage II-i, the total removal efficiency of $COD_{Cr}$ was enhanced to be 80~85%, compared to 75% at stage I, owing to 20~30% removal efficiency of the UV/photocatalytic reactor. However, at stage II-i, the total removal efficiency of color was enhanced to be 65~70%, compared to 45~65% at stage I, even though the removal efficiency of the UV/photocatalytic reactor was tantamount to merely 0~5%. As far as the removal efficiency of fluidized biofilter of the hybrid-recirculating system is concerned, its removal efficiency of color was enhanced by the synergy effect of the hybrid-recirculating system unlike $COD_{Cr}$ . Besides, despite of the increase of hybrid-recirculating system-recycle ratio, the deactivation of photo-catalytic activity was scarcely observed to eliminate the color while its irreversible deactivation was observed to eliminate $COD_{Cr}$ .】

Paclitaxel (PTX)-loaded gelatin nanoparticles (NPs) were prepared, for the first time, by novel O/W/O emulsion with a single-step emulsion process accompanying solvent diffusion, in contrast to the conventional double-step emulsion processes. Linoleic acid was chosen among the natural fatty acids as the exterior medium for the single-step emulsion process accompanying solvent diffusion. The size mean and zeta potential of the PTX-loaded gelatin NPs in their suspension were 164.95 nm (±6.43 nm) distributed with a polydispersity of 0.074 (±0.046) and −23.85 mV (±12.66 mV), respectively. The size of the PTX-loaded gelatin NPs prepared in this study was the smallest among the reported sizes of PTX-loaded gelatin NPs, which would contribute to the enhanced permeability and retention (EPR). In addition, TEM showed that the loaded PTX was located mostly inside the gelatin NPs unlike previous investigations. Accordingly, the conceptual model of the designed PTX-loaded gelatin nanoparticle was introduced. Sustaining a slow PTX release on a day-time scale without an initial burst release into a release medium was observed along with a delay of more than 2 days (i.e., 50 h) before a bursting PTX release from 50 to 70 h despite the addition of a protein degrading enzyme. The observed PTX-loading efficiency was 54.5%. This loading efficiency was greater than that of previous study using gelatin of bloom 75–100 of Lu et al. to prepare PTX-loaded gelatin NPs using a desolvation method.

A semi-pilot biofilter inoculated with the microbes consortium of Bacillus cereus DAH-1056 and Arthrobacter sp. KDE-0311 was operated under various operating conditions in order to treat malodorous waste air containing both hydrogen sulfide and ammonia. When both hydrogen sulfide and ammonia contained in malodorous waste air were treated simultaneously by semi-pilot biofilter inoculated with Thiobacillus sp. IW and return-sludge, the removal efficiencies of hydrogen sulfide and ammonia were ca. 80% and ca. 50%, respectively. On the other hand, in this study, the removal efficiencies of hydrogen sulfide and ammonia were ca. 90% and ca. 60%, respectively. Therefore, the removal efficiencies of hydrogen sulfide and ammonia were enhanced by ca. 13% and 20%, respectively, compared to the semipilot biofilter inoculated with Thiobacillus sp. IW and return-sludge. In addition, in this study, the maximum elimination capacities of hydrogen sulfide and ammonia were enhanced by ca. 15% () and 10~17% (), respectively. In this study, it was observed either that in case of even a same inlet load of hydrogen sulfide, a higher concentration of hydrogen sulfide causes more difficulties in treating ammonia containing in waste air than a lower one, or that in case of even a same inlet load of ammonia, a lower concentration of ammonia results in higher removal efficienciy and elimination capacity than a higher one. Even though hydrogen sulfide and ammonia were treated simultaneously by a biofilter in this study, the maximum elimination capacity of hydrogen sulfide in this study exceeded or was similar to that in previous study of biofilter treating only hydrogen sulfide. In addition, this study showed the higher maximum elimination capacity of ammonia than other previous investigation of biofilter treating hydrogen sulfide and ammonia simultaneously.

A semi-pilot hybrid system composed of a photocatalytic reactor and a biofilter was operated under various operating conditions in order to treat malodorous waste air containing both hydrogen sulfide and ammonia which are major air pollutants emitted from composting factories and many publicly owned treatment works (POTW). When both hydrogen sulfide and ammonia contained in malodorous waste air were treated simultaneously by a biofilter system, its performance of ammonia removal was much more poor than that by a biofilter system treating waste air containing only ammonia, unlike its performance of hydrogen sulfide removal. For semi-pilot hybrid system, the removal efficiencies of hydrogen sulfide and ammonia turned out to be ca. 83 and 65%, respectively. Therefore, for semi-pilot hybrid system, the removal efficiencies of hydrogen sulfide and ammonia was increased by ca. 4 and 30%, respectively, compared to those of semi-pilot biofilter system (control). In addition, the maximum elimination capacities of hydrogen sulfide and ammonia for semi-pilot hybrid system turned out to be ca. 60 and , respectively. These maximum elimination capacities of hydrogen sulfide and ammonia were estimated to be ca. 9.1% and ca. 23.3% greater than those for semi-pilot biofilter system (control), respectively. Therefore, the semi-pilot hybrid system contributed the enhancement of removal efficiency and the maximum elimination capacity of ammonia in a higher degree than that of hydrogen sulfide, compared to the semi-pilot biofilter system.

The preparation conditions for both a high yield without aggregation and a small mean-size of chitosanfucoidan nanoparticles were sought by a screening method, i.e., discarding the ones satisfying neither of both to prepare them by polyelectrolyte complexation with chitosan and fucoidan. The effect of the pH level of chitosan solution and the chitosan-fucoidan mass ratio was investigated on the following aspects: the turbidity and aggregation pattern of suspension, the yield of dried mass, electrostatic interaction, fucoidan loading efficiency, the particle size distribution and the morphology of the polyelectrolyte complex prepared by polyelectrolyte complexation between chitosan and fucoidan. The mean size of prepared nanoparticle ranges between 365-900 nm. The nanoparticles tended to grow as the pH of chitosan was increased up to 3.69, after which they became smaller. This pattern of growth is prominent as the mass ratio of chitosan and fucoidan decrease. The conditions of pH 5 and 1: 1 chitosan-fucoidan mass ratio were suggested as ad hoc optimum conditions by the screening method to prepare chitosan-fucoidan nanoparticles for high yield, small size and good suspension stability. They were almost consistent with the optimum conditions for the maximum value of chitosan-fucoidan nanoparticles prepared per unit input mass, which were analyzed by response surface methodology (RSM).

퇴비공장 또는 공공시설에서 발생되는 악취폐가스의 대표적인 제거대상 오염원인 황화수소와 암모니아를 포함한 악취폐가스를 처리하기 위하여 여러 운전 조건 하에서의 Thiobacillus sp. IW 및 반송슬러지를 고정한 담체를 충전한 semi-pilot 바이오필터 시스템을 운전하였다. Semi-pilot 바이오필터 운전 초반 및 중반에서는 황화수소 제거효율은 암모니아 부하와 무관하였으나, 암모니아 제거효율은 황화수소 부하가 커짐에 따라서 감소하였다. 그럼에도 불구하고 semi-pilot 바이오필터 운전 후반에서는 황화수소 부하가 커짐에도 불구하고 암모니아 제거효율이 영향을 받지 않았다. 이것은 semi-pilot 바이오필터 운전 후반의 buffer solution의 지속적 투입으로 인하여 semi-pilot 바이오필터담체의 산성화가 크지 않음에 기인한다고 간주된다. Semi-pilot 바이오필터시스템으로 황화수소와 암모니아의 동시제거를 할 때에 황화수소와 암모니아의 최대 elimination capacity 값은 각각 약 58 및 30 g/m3/h이었다. 이와 같이 semi-pilot 바이오필터 운전에 의하여 황화수소와 암모니아를 동시 제거한 경우에는 실험실규모 바이오필터의 유사한 운전조건 하에서 둘중의 하나만을 함유한 경우보다 제거용량이 각각 약 39와 46% 만큼 감소하여서, 황화수소와 암모니아를 동시 제거한 경우에 암모니아 최대제거용량이 황화수소 최대제거용량보다 7% 만큼 더 감소하였다.

퇴비공장 또는 공공시설에서 발생되는 악취폐가스의 대표적인 제거대상 오염원인 암모니아를 포함한 악취폐가스를 처리하기 위하여 여러 운전 조건 하에서의 광촉매반응기와 바이오필터로 구성된 하이브리드시스템을 운전하였다. 암모니아 총 제거효율은 하이브리드시스템의 운전부하가 운전 단계별로 커졌음에도 불구하고 약 80%로 유지되었다. 광촉매반응기에서의 암모니아 제거효율은 광촉매반응기로의 암모니아 유입부하량이 증가함에 따라서 광촉매반응기의 암모니아 제거효율은 65%에서 약 22%로 감소하였다. 같은 암모니아 유입부하량일지라도 암모니아농도가 클 때보다 적은 경우에 광촉매반응기의 암모니아 제거효율이 상대적으로 높았다. 반면에 바이오필터의 경우는 운전 전반부에는 암모니아 처리효율이 현저하게 억제되었으나 광촉매반응기의 경우와 반대로 시간이 경과하면서 암모니아 유입부하량이 증가함에도 불구하고 바이오필터의 암모니아 제거효율은 지속적으로 약 78%까지 증가하여서 Lee 등의 연구결과에서의 암모니아 제거효율과 비슷하게 도달하였다. 광촉매반응기에 의한 최대 암모니아 제거용량( $EC_{PR}$ )은 약 16 g-N/ $m^3$ /h 이었고, 바이오필터에 의한 암모니아 제거용량( $EC_{BF}$ )은 운전 초기에 암모니아 총 부하가 작은 경우에는 암모니아 총 부하증가에 따른 $EC_{BF}$ 의 증가추세가 미약하였으나 운전 후반부에 암모니아 총 부하가 큰 경우에는 암모니아 총 부하증가에 따른 $EC_{BF}$ 의 증가추세가 급격하게 커졌다. 하이브리드시스템 운전 6단계에서 암모니아 총 부하가 약 80 g-N/ $m^3$ /h일 때에 광촉매반응기에서의 $EC_{PR}$ 은 약 16 g-N/ $m^3$ /h이었고, 2차 공정이고 주공정인 바이오필터에 걸리는 암모니아 부하는 나머지인 약 64 g-N/ $m^3$ /h이고 주공정인 바이오필터의 $EC_{BF}$ 은 약 48 g-N/ $m^3$ /h로 산출되었다. 이러한 바이오필터의 암모니아 제거용량은 Kim 등의 연구결과로서 최대 암모니아 제거용량인 1,200 g-N/ $m^3$ /day와 거의 비슷하였다. 【The hybrid system composed of a photocatalytic reactor and a biofilter was operated under various operating conditions in order to treat malodorous waste air containing ammonia which is a major air pollutant emitted from composting factories and many publicly owned treatment works. Total ammonia removal efficiency of the hybrid system was maintained to be ca. 80% even though its inlet loads were increased at a higher operating stage according to an operating schedule of the hybrid system. The ammonia removal efficiency of photocatalytic reactor was decreased from 65% to 22% as ammonia inlet loads to photocatalytic reactor were increased. In spite of same inlet loads of ammonia to the photocatalytic reactor, the ammonia removal efficiency of photocatalytic reactor with lower ammonia concentration of fed-waste air was higher than that with higher ammonia concentration of fed-waste air. To the contrary, during the first half of the hybrid system operation the ammonia removal efficiency of a biofilter was quite suppressed while, despite of increased ammonia inlet loads, the ammonia removal efficiency of the biofilter was continuously increased to 78% and reached the ammonia removal efficiency similar to what Lee et al. attained. The maximum ammonia elimination capacity of the photocatalytic reactor was observed to be ca. 16 g-N/ $m^3$ /h. In an incipient stage of hybrid system run, the ammonia elimination capacity of the biofilter showed little sensitivity against ammonia inlet loads to the hybrid system. However, in the 2nd half of its run, the ammonia elimination capacity of the biofilter was increased abruptly in case of high ammonia inlet loads to the hybrid system. In 6th stage of hybrid system run, total ammonia inlet load attained at ca. 80 g-N/ $m^3$ /h corresponding to 16 g-N/ $m^3$ /h of ammonia elimination capacity of the photocatalytic reactor. Then, the remaining ammonia inlet load to the 2nd and main process of the biofilter and its elimination capacity was expected and shown to be ca 64 g-N/ $m^3$ /h and ca 48 g-N/ $m^3$ /h, respectively. The ammonia elimination capacity of the biofilter was close to 1,200 g-N/ $m^3$ /day of the maximum elimination capacity of the investigation performed by Kim et al.】

본 연구에서는 악취 및 휘발성 유기화합물(VOC)를 함유하는 폐가스 처리에 있어서 개선된 바이오필터시스템의 악취 및 VOC의 제거거동 및 제거효율 등을 관찰하고, 전통적 바이오필터의 경우의 악취 및 VOC의 제거거동 및 제거효율 등과 비교하였다. 개선된 바이오필터시스템 운전 1~7단계에서 바이오필터 유효높이 차이에도 불구하고 미생물 population 분포 차이로 인하여, 정해진 시간에 각 단에서 에탄올 농도 순서가 바뀌었다. 반면에 운전 8단계에서 폐가스의 개선된 바이오필터시스템으로의 공급방향들이 바뀌었을 때에 에탄올 농도가 높은 순서는 운전 1~7단계와 다르게 바이오필터의 유효높이가 낮은 순서와 일치하였다. 황화수소 경우도 마찬가지였으나 에탄올 경우와 비교하였을 때에 농도순서가 바뀐 단의 황화수소 농도의 차이는 매우 적었다. 바이오필터 운전 8단계에서 개선된 바이오필터시스템의 에탄올 제거효율은 약 96%로서 전통적 바이오필터반응기의 에탄올 제거효율인 94%보다 약 2% 증가하였다. 개선된 바이오필터시스템 처리가스의 황화수소 농도의 거동은 전통적 바이오필터반응기와 비슷하였으나 황화수소 처리농도가 더 낮았다. 운전 8단계의 개선된 바이오필터시스템의 황화수소제거효율은 전통적 바이오필터반응기의 황화수소 제거효율보다 약 2% 가량 높았다. 따라서 개선된 바이오필터시스템의 제거효율은 에탄올과 황화수소 경우에 전통적 바이오필터반응기보다 각각 2% 제고되었음이 관찰되었다. 【In this study, both transient behaviors of a biofilter system with improved design and a conventional biofilter were observed to perform the treatment of waste air containing malodor and volatile organic compound (VOC). Their behaviors of removal efficiency and treated concentration of malodor and VOC were compared each other. During 1st~7th stages of improved biofilter system operation it was observed that the order of treated ethanol concentration at each sampling port was switched due to the difference of microbe-population-distribution in spite of the difference of biofilter effective height. However, at 8th stage of its operation, the order of treated ethanol concentration at each sampling port was consistent to the order of biofilter effective height at each sampling port. The same was applied to the case of hydrogen sulfide, even though the difference of switched treated-hydrogen sulfide-concentrations was less than that of switched treated-ethanol-concentrations. The ethanol-removal efficiency of the biofilter system with improved design was ca. 96%, which was greater by 2% than that of the conventional biofilter. The transient behavior of treated hydrogen sulfide concentration of both biofilters were similar to each other. However, the concentration of hydrogen sulfide treated by the biofilter system with improved design was observed lower than that by the conventional biofilter. The hydrogen sulfide-removal efficiency of the biofilter system with improved design was higher by ca. 2% than that of the conventional biofilter. Therefore, the hydrogen sulfide-removal efficiency of the biofilter system with improved design was observed to be enhanced by the same as its ethanol-removal efficiency.】

본 연구에서는 광촉매담지 실리카담체 카트리지를 장착한 광촉매반응기시스템을 활용하여 악취 가스인 황화수소 및휘발성유기화합물(VOC)인 에탄올 및 톨루엔이 함유된 폐가스처리를 수행하고, 그 연구결과를 상용 광촉매담지 부직포필터 카트리지를 장착한 광촉매반응기시스템을 활용한 연구결과와 비교 및 평가하였다. 광촉매담지 실리카담체 카트리지를 장착한 광촉매반응기시스템의 경우는 1단계 운전에서 에탄올 및 톨루엔의 제거율은 각각 80% 및 20% 값을계속 유지하였으나, 에탄올의 제거율은 톨루엔과 다르게 점점 떨어져서 1단계 끝에는 제거율 40% 값을 보였다. 한편황화수소의 제거율은 100%에서 90%로 감소하였다. 에탄올의 제거율은 2단계 운전에서 10% 값을 보여서 더욱 감소하였으나, 황화수소 및 톨루엔 제거효율은 처리대상 폐가스의 톨루엔 부하가 4배로 급격히 증가하였음에도 불구하고제거효율이 각각 90% 및 20% 값을 그대로 유지하였다. 3단계 운전은 알루미늄 코팅된 반사막필름을 광촉매반응기에사용한 결과로서, 에탄올 및 톨루엔의 제거율은 각각 약 5%가 증가한 15% 및 25%의 제거율을 보였다. 한편 광촉매담지 부직포필터 카트리지를 장착한 광촉매반응기시스템의 에탄올, 황화수소 및 톨루엔 제거율은 1단계 운전에서 각각 10%, 97% 및 100% 값을 유지하였다. 그러나 2단계 운전에서 에탄올, 황화수소 및 톨루엔 제거율은 각각 5%, 95%및 2~3% 미만의 제거율을 보여서 에탄올과 황화수소는 제거율이 약간 저하되었으나 톨루엔의 경우에는 완전 제거에서 급락하였다. 또한 에탄올, 황화수소 및 톨루엔 모든 경우에서 반사막필름의 효과를 전혀 보지 못하였다. 따라서 상용 광촉매담지 부직포필터 카트리지를 장착한 광촉매반응기시스템에서 에탄올, 황화수소 및 톨루엔 제거는 부직포필터의 혐수성 VOC에 대한 흡착능에 주로 기인하였고, 광촉매 활성에 의한 제거는 광촉매담지 실리카담체 카트리지를장착한 광촉매반응기시스템보다 훨씬 미미하였다.Abstact

본 연구에서는 개선된 바이오필터설계를 가지는 새로운 바이오필터의 압력강하 및 미생물 population 분포 등을 관찰하고, 같은 유효부피를 갖고 unidirectional flow (UF)를 갖는 전통적 바이오필터의 경우와 비교하였다. 개선된 바이오필터는 운전 초기 또는 정상상태의 장기운전에서 전통적 바이오필터 압력강하의 약 40~80% 이상을 감소시켰다. 미생물 population 분포는 바이오필터 담체인 폐타이어담체와 입상 활성탄의 두 경우 모두 바이오필터 top 단에서 가장 낮았고 바이오필터 밑으로 내려갈수록 미생물 population이 커졌다. 한편 폐타이어담체는 입상활성탄 담체보다 월등히 큰 미생물 population을 나타내는 미생물 콜로니 개체수(CFU counts)를 보였다. 개선된 바이오필터에서 악취가스가 $bottom{\rightarrow}up$ 으로 공급되는 경우에 악취가스가 $top{\rightarrow}down$ 으로 공급되는 경우보다 미생물 population 성장이 더욱 컸으며, 입상활성탄 담체보다 폐타이어담체에서 이 현상이 더욱 두드러졌다. 전통적 바이오필터와 개선된 바이오필터시스템 각각의 미생물 population 분포도를 비교하였을 때에, 개선된 바이오필터의 미생물 population은 전통바이오필터보다 입상 활성탄 담체와 폐타이어담체의 경우에 각각 약 15배 및 2.5배 만큼 더 고르게 분포되었다. 【In this study, both pressure drop and microbe-population-distribution were observed while running a novel biofilter system with improved design in which the biofilter system is composed of two, upper and lower biofilters with both equal feed-rates of up-flow and down-flow, respectively. Then they were compared with the pressure drop and microbe-population-distribution observed in a conventional biofilter of the same effective volume with unidirectional flow. The pressure drop-value of biofilter system with improved design turned out to be less at the incipient stage of run or steady-state long term operation by more than 40~80% of that of the conventional biofilter. The microbe-population-distribution was observed to be lower and higher at higher and lower column of biofilter, respectively, for both the conventional biofilter and the biofilter system with improved design. The microbe-media of waste-tire crumb showed much greater CFU counts than GAC. In the biofilter system with improved design, the $bottom{\rightarrow}up$ feeding of waste air showed greater microbe-population growth than the $top{\rightarrow}down$ feeding for both the microbe-media of waste-tire crumb and GAC. However, it was more prominent for the former than the latter. Comparing the microbe-population-distributions of both of the conventional biofilter and the biofilter system with improved design, the microbe-population of latter was distributed ca. 15 and 2.5 times more evenly for GAC and the media of waste-tire crumb, respectively, than that of former.】

The effect of photocatalyst-carrying media porosity on the photocatalytic removal efficiency of malodor and VOC of waste air was evaluated when the photocatalytic removal efficiency of porous silica-based media was compared with that of glass bead as control. The amount of photocatalyst coated on the surface of porous silica-based media was observed to be , which was 250% as much as that of nonporous glass bead (control) of . The removal efficiencies of hydrogen sulfide and toluene in case of porous silica-based media were observed to be 22% and 82%, respectively, while the removal efficiencies of hydrogen sulfide and toluene in case of nonporous glass bead media were observed to be 19% and 53%, respectively. Therefore, the removal efficiencies of hydrogen sulfide and toluene increased by 16% and 55%, respectively, when the removal efficiencies of porous silica-based media were compared with those of nonporous glass bead media. Thus the increment ratio of the removal efficiency of toluene was observed to be 3.4 times higher than that of hydrogen sulfide.

A dynamic adsorption model was proposed using the lumping process for an adsorption system. This novel approach uses a four-component structure model: gas phase, enclosed aqueous phase, sorption volume and porous media surface adsorption. A clouding effect represented by ka (dynamic adsorption constant) was adopted to explain the adsorption process. The clouding effect assumes that the adsorption rate is decreased as the adsorption sites on the media surface are occupied. In the equilibrium stage the Freundlich adsorption isotherm was adopted. The proposed dynamic adsorption model was then predicted in comparison with the experimental data of an adsorption-column to estimate adsorption model parameter values in a biofilter fed with ethanol at 4,100 mg ethanol/m3 (or 2,000 ppmv). Model validation was performed for the adsorption column fed with ethanol at 2,050 mg ethanol/m3 (or 1,000 ppmv). Results showed that the mechanistic model was able to simulate the dynamic behavior of an adsorption process successfully according to the corresponding adsorption experimental data.

A dynamic biofilter model was suggested to integrate the effect of biofilter-medium adsorption capacity on the removal efficiency of volatile organic compound (VOC) contained in waste air. In particular, the suggested biofilter model is composed of four components such as biofilm, gas phase, sorption volume and adsorption phase and is capable of predicting the unsteady behavior of biofilter-operation. The process-lumping model previously suggested was limited in the application for the treatment of waste air since it was derived under the assumption that the adsorbed amount of VOC equilibrated with biofilter-media would be proportional to the concentration of dissolved VOC in the sorption volume of biofilter-media. Therefore a Freundlich adsorption isotherm was integrated into a robust biofilter process-lumping model applicable to a wide range of VOC concentration. The values of model parameters related to biofilter-medium adsorption were obtained from the dynamic adsorption column experiments in the preceding article and literature survey. Furthermore a separate biofilter experiment was conducted to treat waste air containing ethanol and the experimental result was compared with the model predictions with various values of Thiele modulus (). The obtained value of Thiele modulus () was close to 0.03.

The optimum mold design and the optimum process condition were constructed upon executing process simulation of rubber injection molding with the commercial CAE program of MOLDFLOW (Ver. 5.2) in order to solve the process-problems of K company relating to cracks, which occurs at the inner cavity wall of C. V. joint boots. As a result it was confirmed that the real cracks occurs at the exactly same position of the cavity as exhibits the defects of weld and meld line and unsatisfactory curing according to the result of simulation. In order to prevent the occurrence of weld and meld line at the defect-position, the location of gate was altered to the optimum position of the cavity. Consequently the filling pattern was established to minimize the degree of the melt-fronts confronting or the melt-flows melding to prevent the occurrence of weld and meld line at the defect-position. It was observed that both gate-positions to maximize the degree of the formation of weld and meld line and air traps are located, respectively, in opposite direction each other with reference to the optimum gate position. In addition, the temperature of mold was raised by and maintained at for satisfactory curing.

The objective of this study is to develop the process conditions of a w/o emulsification method for the preparation of the smallest agar nanoparticles possible in a low nanometer range with the highest yield, prior to adding an aqueous solution containing an unstable drug such as a protein drug for its encapsulation. The volume ratio between the organic phase and aqueous phase was set as 10 : 1, the lowest ratio among those of previous investigations. Agar solutions of 0.5, 1 and 2%w/v concentration were emulsified in soybean oil. Then, various homogenizer speeds were investigated for the yield of agar nanoparticles and their particle size distribution under those agar concentrations. The visual appearance of the re-dispersed emulsion-converted-to suspension was turbid without any visible aggregates, even though the suggested methodology is more economically efficient in terms of the ratio between the organic phase and aqueous phase, than those of previous investigations. In terms of agar concentration, the yields of agar nanoparticles were optimized at 1%w/v of agar concentration for all the homogenizer speeds of 13000, 15000 and 17000 rpm. Accordingly, the yield of 76.5% was the highest at the preparation conditions of 1%w/v agar concentration and 15000 rpm homogenizer speed.

The molecular weight and thermal properties of unfractionated by-product polyolefin wax (wax K) from a naphtha cracking unit, fractionated commercial paraffin wax (wax J) and their blend (wax M) were evaluated and were compared with each other using differential scanning calorimetry (DSC), normal and high-temperature gel per- meation chromatography (GPC), and wide-angle X-ray diffraction (WAXD). Such properties as molecular weight dis- tribution, melting temperature and degree of crystallization were altered by blending wax K with wax J. By blending with two parts of wax K and one part of wax J to prepare wax M, Mw of wax K was shifted, by half, to that of wax J in order to approach that of wax M, whereas the Mn of wax K remains almost unaltered to become that of wax M. In particular the effect of blending of wax K and wax J turned out co-crystallization for the sharper lower-melting-tem- perature endothermic peak of the blend, indicating narrower molecular distribution, than that of wax K at the melting temperature shifted even below that of wax J. The total degree of crystallinity for the blend, wax M, turns out less than that before blending wax K with wax J, which may be attributed to the effect of co-crystallization due to blending.

The surface compositions of crude by-product polyolefin wax (wax K) from a naphtha cracking unit, fractionated commercial paraffin wax (wax J) and their blend (wax M) were compared, under various conditions, by using FT-IR. Then a practical criterion was theoretically derived by back-of-the-envelope-calculation to estimate the diffusivity for the surface enrichment of hydrophilic functional groups. The hydrophobicity in terms of chemical structure and functional groups was altered by changing the environment as well as by blending wax K with wax J. The surface properties of wax J and wax M turned out more hydrophobic than that of wax K within the experimental period of water-submerged condition, even though the structure and functional groups on the surfaces of all waxes under ambient atmospheric condition are extremely similar. Thus the blend of wax M behaved unlike wax K but similarly to wax J in terms of alteration of hydrophobicity. Such values of diffusivity as 1.35×10−11 cm2/s and 1.96×10−11 cm2/s are established for wax J and wax M, respectively, under 1 day water-submerged condition. Furthermore, under 1 week water-submerged condition, the values of their diffusivity for wax J, wax K and wax M are estimated as 3.06×10−12 cm2/s, 7.23×10−11 cm2/s and 1.50×10−11 cm2/s, respectively. The obtained values of diffusivity are consistent, in terms of the order of magnitude, with the value of diffusion coefficient of 5.75×10−11 cm2/s obtained, using a very complicated empirical-formula, by Chen et al. for the investigation of surface-modifier enrichment. Thus, the suggested criterion may be very useful and practically applied to clarify the process of surface enrichment from general polymer-blends.

Hydrogen sulfide is heavier than air and is colorless, toxic and flammable, the gas odor threshold of which is about 0.47 ppbv, which causes nuisance odor at concentrations as low as about 8ppbv and corrosion problems in sewer systems. The transient behavior of biofilter packed with mixed media (of granular activated carbon and compost) inoculated with a pure culture of Thiobacillus sp. IW was observed at a height of four sampling ports to treat wasteair containing hydrogen sulfide in this investigation, which shall be used as control to be compared with the performance of a biofilter-involved integrated system for the treatment of waste-air containing hydrogen sulfide in a subsequent investigation. Unlike the previous studies of the other investigators, various process conditions were applied to successive biofilter runs in order to monitor and correlate each corresponding unsteady behavior of the biofilter at the height of each sampling port. During 10 days (20 times) after start-up of a biofilter hydrogen sulfide was continuously adsorbed on the media and that the adsorption of hydrogen sulfide was under way since the inlet loads of 1st and 2nd stage operations were very low. Afterwards it was obvious that the breakthrough curves at the 1st, 2nd, 3rd and 4th (exit) sampling ports responded rapidly to the change of operating conditions of a biofilter so that the breakthrough curve at each sampling port responded rapidly to approach a new state of saturation, which suggests that the adsorption capacity of biofilter-media may be relatively small or its affinity to hydrogen sulfide may be relatively high, compared to such volatile organic compound as ethanol. Up to the 3rd stage of operation the removal efficiency continued to be nearly 100%. However it began to decrease as inlet load increased. At the end of last stage of the biofilterrun removal efficiency was decreased and maintained at 94%. The maximum elimination capacity was observed to be ca. 95 g/m3/h, which was higher than that of the biofiltration-work of any other previous investigator except for that of the biofiltration-work with use of each of two inorganic packing materials (porous ceramics, calcinated and formed obsidian).

The microbes ofPseudomonas putida (KCTC1768) were fixed on the biofilter-packing media comprising an equivolume mixture of granular activated carbon (GAC) and compost, by recycling the liquid medium containing incubatedPseudomonas putida (KCTC1768). A biofilter experiment was performed to observe its transient behavior under the operating condition of 2,180 ppmv of ethanol-inlet concentration and 158 g/m3/h of ethanol-inlet load for the five consecutive temperature-stages of operation ranging from 25 °C to 40 °C. For the five temperaturestages of operation their removal efficiencies were measured and were compared with each other. The optimum operating temperature of the biofilter turned out to beca. 30 °C, which was consistent with the previous experimental result of Lim and Park. However, the optimum incubation-temperatures ofPseudomonas putida (KCTC1768) and the equivalent (i.e., NCIMB8858) were announced to be of 26 °C and 25 °C by Korea Collection for Type Cultures (KCTC) and National Collections of Industrial, Food and Marine Bacteria (NCIMB), respectively. It was also confirmed by the experiment in which the microbes were incubated in the same liquid medium as in the previous work of Lim and Park at temperature ranging from 20 °C to 40 °C and their growth rates were subsequently measured. Thus, the optimum operating temperature of a biofilter inoculated withPseudomonas putida (KCTC 1768) was proved to be 30 °C, which was higher than its optimum incubation-temperature byca. 5 °C

An experiment for five stages of a biofilter-run was performed to investigate the effect of hydrophilic ethanol and hydrophobic toluene on the biodegradation of hydrophobic toluene and hydrophilic ethanol, respectively, when waste-air containing toluene and ethanol was treated by a biofilter. Removal efficiencies of toluene and ethanol began to decrease when inlet load surpassed 90 g/m3/h and 100 g/m3/h consistent with maximum elimination capacities of toluene and ethanol, respectively. At the end of the biofilter-run, removal efficiencies for toluene and ethanol were decreased and maintained at 65% and 40%, respectively. The concentration of toluene at 1st sampling port was raised by factor of two in the 3rd stage of the biofilter run when the inlet load of ethanol co-feed was increased by 1.5 times, while the process conditions of toluene were maintained the same as those of the 2nd stage of biofilter-run. According to the result of Mohseni and Allen, it may be interpreted that removal efficiency of hydrophobic toluene was affected by the presence of hydrophilic ethanol when high load of hydrophobic toluene was applied like that of the 1st sampling port of the biofilter. However it was not the case when a low load of hydrophobic toluene was applied like those of the 2nd, 3rd and 4th sampling ports since hydrophobicity of toluene is much less that of α-pinene. Thus, it may be suggested that biodegradation of hydrophobic VOC was interfered by hydrophilic VOC dissolved in the biolayer and the degree of interference was proportional to the inlet load of hydrophobic VOC as well as that of hydrophilic VOC and was inversely proportional to the solubility of hydrophobic VOC. However, it was inferred that the existence of hydrophobic toluene from waste-air can hardly inversely hinder the removal of hydrophilic ethanol in the biofilter when timeevolutions of hydrophilic ethanol concentrations of this experiment were compared with those of the previous experiment of biofilter to treat waste-air containing ethanol only.

The transient behavior of a hybrid system composed of biofilter and photo-catalytic reactor was observed at the height of each sampling port to treat waste-air containing ethanol. The biofilter packed with mixed media (of granular activated carbon and compost) was inoculated with a pure culture ofBurkholderia cepacia G4 andPseudomonas putida, while a photo-catalytic reactor was composed of 15W UV-A lamps and annular pyrex tubes packed with glass beads coated with sol type of TiO2 before calcination. The maximum elimination capacities of toluene and ethanol turned out to be 130 g/m3/h and 230 g/m3/h, respectively, which were greater by 40 g/m3/h and 130 g/m3/h, respectively, than those from the experiments performed with a biofilter only. Thus, the maximum elimination capacities for toluene and ethanol increased by 44% and 130%, respectively, by use of a hybrid system. The photo-catalytic process contributed to the maximum elimination capacities of hybrid system on toluene and ethanol by 30.8% and 56.5%, respectively, which contributions for the elimination capacities on toluene and ethanol were allocated indirectly by 25.4% and 44.3% as well as directly by 5.4% and 12.2%, respectively. Direct contributions of photo-catalytic process were 17.5% and 21.5% to the increments of the elimination capacities on toluene and ethanol, respectively, while its indirect contributions were 82.5% and 78.5% to those on toluene and ethanol, respectively.

In such a complex situation as the cavity of two squa re plates connected to cavities composed of four pipes with same length and different diameter connected in series and parallel, the resistance of cavity of two square plates should be combined with that of pipes to determine the gas direction in gas assisted injection molding (GAIM). The flow model of Newtonian fluid was previously suggested under the fan-shaped geometry incuding relatively thin cavity of two square plates when ρ rH/µ(H/R0)<

Transient behavior of a biofilter packed with mixed media (of granular activated carbon and compost) inoculated with a pure culture ofPseudomonas putida was observed at the height of each sampling port to treat wasteair containing ethanol. In addition, flooding effects of an excess supply of buffer solution was observed at each sampling port of the biofilter until it recovered the status prior to the flooding. Unlike previous investigations, various process conditions were applied to successive biofilter runs in order to monitor the corresponding unsteady behavior of the biofilter in this work. In early stage of biofilter run the removal efficiency of ethanol maintained almost 100%. However, it began to decrease when inlet load surpassed 100 g/m3/h consistent with maximum elimination capacity. At the end of biofilter-run removal efficiency was decreased and maintained at 40%. The results of this work were compared to those of such biofiltration studies as the work of Christen et al. from the point of view that pure cultures of microorganism were used in both works. Except for the period of flooding effect of the 2nd stage, the inlet load and removal efficiency continued at 105.5 g/m3/h and 95%, respectively, while they were 93.7 g/m3/h and 95%, respectively, according to the result of Christine et al. Removal efficiency remained at 90% for the beginning period of 3 days of the 3rd stage, and it gradually decreased to 60% for remaining 5 days of the stage with an inlet load of 158.26 g/m3/h, which may be interpreted as better than the result of Christine et al. Their result was that the removal efficiency on the inlet load of 154 g/m3/h of ethanol was continued to be 60% for 6 days of a separate biofilter run and decreased to 40% later. Thus, with similar inlet loads of ethanol, removal efficiency of this work was equivalent to or higher than that of Christine et al.

For such conditions that (H/R0)2 is replaced by e (that is the order of 10-1) and $$\hat \theta ^2 $$ is the order of one, the rule of thumb for an approximated flow model was introduced in part 1 of the paper to show, in qualitative way, whether the resistance of the relatively thick cavity of two square plates might affect the gas direction in GAIM under the aforesaid geometry. Subsequently, various simulations were performed by using Moldflow (version of MPI 4.0) under the conditions that all dimensions of cavity of two square plates and pipes were fixed except for the diameters of pipes, and the results of simulation were compared with the results of a rule of thumb (RT1) containing the approximated flow model as well as those of another rule of thumb (RT2) without the resistance of the relatively thick cavity of two square plates. There were some exceptional cases where RT1 or RT2 were not consistent with the simulation results (i.e., flow directions). Thus such a developed model as time-dependent model was required to describe transient behavior of the interface between gas phase and resin phase instead of comparison of initial velocities in upper side and lower side of the configuration, which was proposed and utilized to compare with the results of Moldflow in this 2 nd part of the paper. The predictions of the developed flow model were so quite consistent with the results of simulation that the proposed time-dependent flow model may be referred to describe very well the transient behavior of the movement of the interface of gas and melt-resin in the cavities. In addition, a timedependent model was also established and was used to compare with the results of Moldflow when cavities of pipes and runners were involved in configuration. It is amazing that the proposed developed model was able to predict exactly the cross-over between the trajectories of interface of upper and lower side, and it is also surprising to describe the time dependent behavior so well that the result of the predictions by the developed model were quite consistent to the results of simulation by Moldflow.

This paper proposes a relative charge density model of prepared chitosan-fucoidan nanoparticles (CFNs) to provide insight into an analysis of the ionic interactions in terms of polyelectrolyte complexes. Using the relative charge density model, the extent of the ionic interactions is predicted in terms of the pH (2 through 6) and used fucoidan to chitosan mass ratio (FCMR) (1:0.05 through 1:1), through which the formation of CFNs can be controlled to be ranked qualitatively according to size and stability. It was confirmed by the measurements of their zeta potentials and sizes and by the analysis of their decay with time. Moreover, the relative charge density model was validated to predict the isoelectric condition of a polyelectrolyte complexed suspension of CFNs. Elemental analysis with a proper mass-conversion showed that the ratio of the stoichiometric coefficients of sulfate groups to amino groups in CFNs formed were almost consistent to that of the sulfate groups to amino groups in a chitosan solution mixed with a fucoidan solution prior to the occurrence of polyelectrolyte complexation. In a pH 2-environment, there were locally intensive electrostatic interactions with a low yield to form sulfate group-rich CFNs. In contrast, in a pH 6-environment, extensive electrostatic interactions occurred to form sulfate group-poor CFNs with a high yield. In addition to the chitosan-amide groups, the separate yield-distribution of loaded chitosan indicated the possible involvement of positively charged amino groups in the electrostatic interactions among chitosan molecules.

In part 1 of this paper a qualitative analytical method to predict the preferred gas flow direction in gasassisted injection molding (GAIM), which involves flow through panel-areas of various fan-shaped geometries, and the criteria to apply the method were presented with appropriate assumptions. Then the definition of a resistance to initial velocity was proposed as a rule of thumb, by which the gas directions of GAIM were predicted under various fan-shaped geometries. Upon performing the simulation on them with commercial software (MOLDFLOW), we compared the ratio of simulated gas penetration lengths to both directions with the predicted ratio of resistances as well as the predicted direction of the gas flow in GAIM using the suggested rule of thumb herein presented. The predictions with the suggested rule of thumb were generally quite consistent with the results of simulation (MOLDFLOW). However the discrepancy between the ratio of gas penetration lengths and the ratio of resistances was observed to increase as the ratio $$\left( {\frac{{more(H/R_0 )(one - side)}}{{less(H/R_0 )(the other - side)}}} \right)$$ of the values of H/R0 on both sides of fan-shaped cavities became bigger even though the suggested rule of thumb was assumed adequate to use until the case met the condition of (H/R0)2 $$1/\hat \theta ^2 \ll 1$$ and (H/R0)2≪1. Nevertheless, the suggested rule of thumb was still effective as far as the direction of gas flow was concerned.

In part 2 of the paper simplified unsteady-mass (and momentum-) balance equations of melt polymer resin in the cavities of GAIM were proposed, as a time-dependent rule of thumb, to constitute a novel flow model in GAIM under the configuration of two fan-shaped geometries connected with a gas nozzle. Upon performing a simulation on them with commercial software (MOLDFLOW), we compared the time evolution of simulated gas penetration lengths with the those of unsteady trajectory on the gas flow in GAIM by the suggested novel flow model in the fan-shaped cavities in order to check the precision of model-predicted gas penetration lengths as well as the consistency of its predicted direction. The results by the suggested novel flow model were satisfactory to fit the trajectory simulated with commercial software (MOLDFLOW).

In the prediction of gas flow-direction for gas-assisted injection molding (GAIM), the statement“Gas goes to the direction of the last area to fill with resin”, has been accepted as a correct one. When there exists more than one area to fill with resin, a mold design engineer for GAIM technologies has to determine to which direction gas goes that commercial software for GAIM (e.g., Moldflow) may be utilized for its mold design. However commercial software is generally expensive and is sometimes hard to become familiar with. As a rule of thumb, it is suggested that the resistance to the initial velocity of melt polymer at the nearest geometry to a gas injection point should be used as its criterion since gas goes in the direction of least resistance to initial resin-velocity. Neither the flow rate nor the resistance to flow rate can be a criterion in the prediction. Thus the statement“Gas goes to the direction of the least resistance to flow rates”, should be corrected to“More flow rate goes to the direction of the least resistance to flow rates.”, The rule of thumb suggested in this paper was verified by using commercial software, Moldflow, in the prediction of gas flow directions in GAIM under geometries where cavities and runners were involved. When the ratio of initial resin-velocity is so close to unity it is proposed as the adapted rule of thumb to calculate new emerging resin-velocities and resistances to resin-velocity at the first coming change of diameters in series of pipes and to compare those for upper and lower sides each other to predict the gas direction. Thus the judgment as to which point is the point where gas starts to choose a preferred direction is very important in the prediction.

The types of biofilter modeling may be primarily classified in accordance with whether a biofilm is differ- entiated from other phases in each model. It may be a secondary classification with regard to biofilter-modeling whether sorption volume and/or adsorption are adopted as reservoirs or not. Thirdly, biofilter models are classified as to whether adsorption is assumed to exist through gas phase and/or a biofilm. Among all the biofilter-models of previous inves- tigators all model-components including gas phase, a biofilm, sorption volume and adsorption surface are considered only in the model of Lim. Since his model does not require a numerical solution but an algebraic solution to describe the concentration of organic pollutants in waste-air-streams along the height of a biofilter even under unsteady-state conditions, it satisfies the condition of simplicity that is one of the important model requirements. In spite of its simplicity, Lim's model predictions are fairly good to fit Hodge and Devinny's experimental data.

Potential use of iron oxide particles (IOPs) as adsorbents for removal of residual phosphorus from the secondary effluent discharged from activated sludge treatment was investigated under various operating conditions. Substantial phosphorus removal was achieved with IOPs including ferrihydrite, goethite, and hematite, though the adsorption capability for phosphorus depended on the types of IOPs tested. Adsorption isotherm tests and SEM images helped to understand the behavior of the adsorptive properties of phosphorus on different IOPs. Phosphorus removal efficiencies for secondary effluent remained constant or further increased over the wide pH range of below neutral to alkaline values, in contrast to those for a synthetic phosphorus solution. This could be in close association with the interaction of phosphorus with Ca and Mg ions present in secondary effluent leading to chemical precipitation, such as apatite, dolomite, calcite, and brucite. The reactivity of IOPs with phosphorus at neutral pH appeared...

Many different oligosaccharides were produced by transferring the fructose residue of sucrose to maltose, cellobiose, lactose and sucrose (self-transfer), where their yields of fructosylated acceptor products accounted for 26–30% (w/w). The maximum conversion yield (30%) was obtained in fructosyl cellobioside formation with 500 g sucrose l−1 (substrate) and 200 g cellobiose l−1 (acceptor). These four acceptors gave various products having DP (degree of polymerization) 2–7 by successive transfer reactions.

It has been reported that highly adsorptive granular activated carbon improves the biofilter performance. In this work the effect of adsorption property of the medium, on the biofilter capacity of eliminating organic components in waste gas streams is theoretically discussed using a biofilter model. In this first paper adsorption capacity is assumed to be in excess and steady-state solutions are compared with Ottengraf's solutions in various limiting situations. When first-order kinetics is used in the substrate utilization rate, as the value of α increases, the corresponding values of the dimensionless pollutant concentration in a biofilm and the dimensionless pollutant concentration in waste-gas streams through a biofilter become lower at a given value of Thiele modulus, through the thickness of the biofilm and the height of the biofilter, respectively. However, the effect of α becomes insignificant when the value of Thiele modulus becomes larger than a certain number. With zero order kinetics in the substrate utilization rate, for both situations of reaction limiting and diffusion limiting, their steady-state solutions are obtained.

The morphology of gelatin nanoparticles loaded with three different drugs (Tizanidine hydrochloride, Gatifloxacin and Fluconazole) and their characteristics of entrapment and release from gelatin nanoparticles were investigated by the analysis on nanoparticle size distribution, SEM and FT-IR in this study. The particles were prepared by nanoprecipitation using water and ethanol as a solvent and a nonsolvent, respectively. The exclusion of a crosslinking agent from the procedure led the system to have an irregularly-shaped morphology. Nonetheless, the uncrosslinked case of Gatifloxacin loading generally led to a more homogeneous population of nanoparticles than the uncrosslinked case of Tizanidine hydrochloride loading. No loading was achieved in the case of Fluconazole, whereas both Tizanidine hydrochloride and Gatifloxacin are observed of being capable of being loaded by nanoprecipitation. Tizanidine hydrochloride-loaded, blank and Gatifloxacin-loaded nanoparticles yielded, under crosslinked condition, 59.3, 23.1 and 10.6% of the used dried mass. The crosslinked Tizanidine hydrochloride-loaded particles showed the loading efficiency of 13.8%, which was decreased to 1.1% without crosslinking. A crosslinker such as glutaraldehyde is indispensable to enhance the Tizanidine hydrochloride-loading efficiency. To the contrary, the Gatifloxacin-loading efficiency for crosslinked ones was lower by a factor of 2–3 times than that for uncrosslinked ones. This is due to the carboxylic groups of Gatifloxacin and the aldehyde groups of glutaraldehyde competing with each other during the crosslinking process, to react with the amino groups of gelatin molecules. The loading efficiency of gelatin nanoparticles reported by other investigators greatly varies. Nevertheless, the loading efficiency reported by us is in good agreement with the drug-loading data of gelatin nanoparticles reported by other investigators. The 80% of loaded Tizanidine hydrochloride was released around 15 h after start-up of the release experiment, while the 20% of loaded Gatifloxacin was released more rapidly, as free Gatifloxacin, than the loaded Tizanidine hydrochloride and it showed the trend of sustained slow release during the remaining period of its release experiment. Furthermore, the result of comparative FT-IR analysis is consistent to that of the corresponding drug release study.

There is considerable evidence that lipoprotein cholesterol, after crossing the arterial endothelium and entering the intima from the vascular lumen, lodges in extracellular lipid packets (labeled "liposomes") bound to the extracellular matrix. These liposomes appear to form by occasional attachment of a low-density lipoprotein (LDL) to the intimal matrix and to grow in place mainly by appending available free LDL. The liposome size distributions observed in chronically hypercholesteremic (WHHL) and in short-term cholesterol-fed rabbits are quite different. We propose a hierarchy of simple nucleation-polymerization models to describe liposome formation and growth. Even the simplest of these (with only one adjustable parameter) agrees extremely well with the WHHL data. In contrast, the cholesterol-fed rabbit data seem to result from the short-term nonuniform intimal history of LDL supply, which is a consequence of the focal nature of the transendothelial LDL flow through isolated transient leakyjunctions. The same models used for the WHHL data, together with this intimal nonuniformity, superimposed on a slow uniform transendothelial seepage also account very well for this cholesterol-fed rabbit data.