Adsorption process is largely influenced by pore structures of adsorbents and physical properties of adsorbates and adsorbents. The previous studies of this laboratory was focused on the role of pore structures of adsorbents. And we found some pores of adsorbates which have larger pore diameters than the diameter of adsorbate are filled with easily. In this study the effects of physical and chemical properties of adsorbates and adsorbents, such as pore size distribution, vapor pressure on adsorption were investigated more thoroughly at the concentration of adsorbate of 1000 ppm. The adsorption in the pore ranges of 2～4 times of adsorbates's diameter could be explained by space filling concept. But there was some condensation phenomena at larger pore ranges. The errors between the adsorbed amount of non-polar adsorbates and the calculated amounts by considering factors were found to be 44.46%, positively, and -142%, negatively. When vapor pressure is considered, the errors between the adsorbed amount of non-polar adsorbates and the calculated amounts were in the range of 1.69%～32.25% positively, and negatively -1.08%～-63.10%.

In this study, the relationship between the pore size distribution and the adsorption amount of adsorbates is investigated in detail. Adsorption amounts of non-polar adsorbates were greater than those of polar adsorbates because of slight negative charge on surfaces of adsorbents. The adsorption of benzene on the surface of absorbents was largely influenced by the specific pore size of 2～4 times of benzene diameter. But in case of toluene, the adsorption of toluene was affected by pore sizes of 2～4 times as well as 4～6 times of the diameter of toluene. Both acetone and MEK were examined by the same method. The adsorption of acetone was influenced by pore sizes of 2～4 times of the diameter of acetone. But acetone does not look to be built up multi-layer on those pore sizes. Since acetone molecule is small and its mobility is so fast, it is assumed that the adsorption and desorption of acetone is simultaneously occurred at the same time even at room temperature. In case of MEK, MEK was effected by pore sizes of 2～4 times of the diameter of MEK.

This study is to investigate the relationship between pore structures of activated carbons and adsorption characteristics of toluene vapor using dynamic adsorption method. The surface areas of below 10Å in the pore diameter of activated carbons used in this experiment were in the range of 72～93％ of total cumulative surface area and the toluene vapor equilibrium adsorption capacities were in the range of 350～390mg/g. Activated carbons having larger toluene adsorption capacity than the compared activated carbons had relatively pores in the pore diameter range of 7～10Å. Linear relationship between equilibrium adsorption capacity and cumulative surface area was in the diameter range of over 7Å. It was thought that toluene vapor was relatively well adsorbed on surfaces of pores of over 7Å.

The properties of biosorption of dye(Rhodmine B) was investigated to figure out the effects of temperature as a function of dye concentration and sludge concentration by the Langmuir and Lagergen adsorption model. It was found that the uptake capacity of biosorption was increased at low temperature. The Langmuir adsorption model was found suitable for describing the biosorption of the dye. The experimental results indicated that the dye uptake process followed the pseudo-first-order kinetics.

The emission of volatile organic compounds (VOCs) generated from painting and coating processes is a worldwide problem as contributing factors to the development of photochemical smog and other environmental problems. Common methods of reducing VOC emissions are adsorption on activated carbon, membrane separation, absorption, incineration, or catalytic oxidation. In this article, the environmental issues caused by VOC emissions and the trend of legislation against such emissions will be surveyed first. Several conventional control technologies will then be summarized and the characteristics of each process will be introduced. Lastly, some examples will be described to show the hybrid processes which have been industrially applied for the recovery of VOC.

Physico-chemical properties of the activated sludges(Suyoung and Changlim treatment plant), such as SVI(sludge volume index), absorbance, specific surface area, and specific resistance using Buchener funnel test were investigated with changing anaerobic storage time. This experimental condition was found that it was possible to estimate a linear relationship between their parameters such as specific surface area, specific resistance, and sludge volume index(SVI). The specific surface area and the specific resistance to filtration of the activated sludges of Suyoung and Changlim treatment plant were found as 123.6～136.6㎡/gDS and 41.5～44.9㎡/gDS(dry solid), and 1.09×1014 ～ 5.48×1014m/kg and 1.05×1014 ～ 2.48×1014m/kg, respectively. The results gave a good linear relationship between the specific surface area and the specific resistance, r=2.25×1012s-8.10×1013(R2=0.8885) at Suyoung treatment plant and r=1.26×1013s-4.75×1014(R2=0.8756) at Changlim treatment plant.

Optical microscope, SEM (Scanning Electron Microscopy) and fluorescent microscope were used for qualitative and morphological studies of the attached biomass on PE (polyethylene) substratum under anaerobic condition. It was shown by the observation of optical microscope that the initial attachment of biomass began in crevices of the surface of PE. The shape and structure of the attached biofilm could be observed by SEM photographs, but species of bacteria were and methanogens were not classified. A large number of methanogenic bacteria were identified on the surface of PE substratum by fluorescence under 480nm of radiation. It was estimated that methanogenic bacteria was also related to initial attachment of biomass under anaerobic condition.

The lab-scale anaerobic continuous reactor which was filled with the sludge of anaerobic digestion from Suyoung wastewater treatment plant was operated by feeding of various concentrations and flow rates. This experiment indicated that more than 6,870 mgCOD/L of substrate concentration was required to promote good metabolism and growth of anaerobic biomass. And increasing loading rate slowly was also required in order to treat substrate of higher concentration and higher loading rate. The substrate concentration of about 10,000 mgCOD/L was adequate to generate biogas efficiently. The pH was sharply decreased at the onset of higher loading rate, but the pH was restabilized soon at 8. During the experiment, the amount of the attached biomass was kept constant.

Activated carbons were prepared from Korean coal by steam activation in this study. The variation of pore structure of the activated carbons were investigated according to different carbonization temperatures. Yield, surface area, pore volume and pore structure of this activated carbon were compared with those of activated carbon prepared without carbonization. The investigated carbonization temperature ranged from 700℃ to 1,000℃. Carbonization was carried out in nitrogen atmosphere for 70 minutes and activation was performed by steam at 950℃ for 210 minutes. Surface area and pore volume of the resulting activated carbons increased with carbonization temperature. Also pore volume increased by 20% compared to the activated carbon without carbonization. Especially, in mesopore region, the activated carbon carbonized at 900℃ had more pores by 60% than that of activated carbon carbonized at other temperature.

Activated carbons were prepared from Youngwall coal by steam activation in this study. The feasibility of the Youngwall coal to commercial activated carbon was examined. The variation of pore structures and the development of porosity in activated carbons were investigated by changing activation conditions in batch type apparatus. The values of BET surface area and adsorption capacity of iodine and methylene blue of the resulting activated carbons were obtained as high as 1,000㎡/g, 900㎎/g, 150㎖/g, respectively. Youngwall activated carbon prepared in this study showed much higher pore volume in pore diameter over l0Å than that of commercial reference activated carbon(Ningxia Taihua ZJ-15C) produced from China anthracite.

The variation of microorganisms (activated sludge, Saccharomyces cerevisiae, Aureobasidium pullulans) caused by the biosorption of Pb2+ was observed by TEM and microscope. By the TEM observation of S. cerevisiae, the plasmolysis and lysis of cell wall or cell membrane were occurred by the penetration of Pb2+ into the inner cellular region. However, in the case of A pullulans, the plasmolysis and lysis of cell wall or cell membrane were not occurred because of the prevention of Pb2+ penetration by the extracelluar polymeric substances (EPS). A flocculation of microorganisms, in the case of A. pullulans, was observed by the Pb2+ accumulation after 3∼4 h and the color was changed from white to black after 1 day. The flocculation of activated sludge was improved by the accumulation Pb2+ after 1 h, however, the floc was broken up and the settling efficiency decreased after 1 day.

This paper discussed about the effect of Zoogloea ramigera on the initial microorganism attachment and the biofilm growth. The additions of 5, 10 and 15%(w/w) of Zoogloea ramigera were facilitated for the initial attachment on the surface of the acryl disk. At biofilm growth, the more Zoogloea ramigera added to the activated sludge, the more biofilm dry weight was obtained. In order to get the stable biofilm and to minimize the start-up periods, initial biofilm formation using activated sludge with floe forming microorganisms like Zoogloea ramigera was recommended rather than that without floe forming microorganisms.

In order to develop of support media for biofilm reactor, physicochemical properties and attachability of surface of activated carbon, clay mineral, non-clay mineral, and waste mold sand were examined. Measured physicochemical properties of materials were surface roughness, mean particle size, surface area, hydrophobicity, and surface charge. At a tested materials, activated carbon was the best attachable material and microorganisms were attached 20.1 × 10^7 CFU/㎠ at surface, compared with diatomaceous earth which were attached of 9.2 × 10^7 CFU/㎠. In our research, surface area and hydrophobicity showed more influence than any other factor on attachment of microorganisms.

This paper discussed effect of the surface roughness and the hydrophobicity of support material on the microbial attachment in a rotating biological contactor. The hydrophobicity of each support material was determined by the measurement of contact angle of water and the surface roughness was measured by the surface roughness instrument. Microorganisms have well attached on the surface of more hydrophilic support material like Nylon6 than that of the hydrophobic support material like PE. When the relatively hydrophilic surface was roughen, the microbial attachment was increased but when the relatively hydrophobic surface was roughen, the attachment was slightly increased because the hydrophobicity of support material was increased by roughening the hydrophobic surface. Although both variables, the surface hydrophobicity and the surface roughness, have influenced the microbial attachment, the influence of the surface roughness overruled that of the surface hydrophobicity. Support material whose surfaces were roughened about l㎛, 6㎛ and 11㎛ were allowed for attached 3, 7 and 24hr, but the differences of maximum and minimum attachment of each material gave nearly constant values and similar trend with time.

The variations of gas hold-up, overall volumetric oxygen mass transfer coefficients and liquid circulation velocity in an internal loop reactor were investigated to manifest scale-up effect. The relationship between superficial gas velocity and gas hold-up were found as Ugr = 0.045 εr in the pilot-scale and Ugr = 0.056 εr in the bench-scale reactor. The overall volumetric oxygen mass transfer coefficient, K_La was slightly increased in the pilotscale than in the bench-scale reactor. Flow regime was changed from the bubble flow to the churn-turbulent flow when the superficial gas velocity reached to 3.5 - 4 ㎝/sec in the pilot-scale.

The objective of this study was to examine the transient response to hydraulic shocks in an inverse fluidized bed biofilm reactor(IFBBR) for the treatment of apartment sewage. The hydraulic shock experiments, when the system were reached at steady state with each HRT 12, 7, and 4hr, were conducted by changing twice HRT per day during 3days. The SCOD, SS, DO, and pH of the effluent stream were increased with hydraulic shock, but easily recovered to the steady state of pre-hydraulic shock condition. In spite of hydraulic shock, there were not much variation of biomass concentration, biofilm thickness, and biofilm dry density.

An inverse fluidized-bed biofilm reactor (IFBBR) was used for the treatment of highly-emulsified oily wastewater. When the concentration of biomass which was cultivated in the synthetic wastewater reached to 6000㎎/L, the oily wastewater was employed to the reactor with a input COD concentration range of 50㎎/L to 1900㎎/L. Virtually the IFBBR showed a high stability during the long operation period although some fluctuation was observed. The COD removal efficiency was maintained over 90% under the condition that organic loading rate should be controlled under the value of 1.5 ㎏COD/㎥/day, and F/M ratio is 1.0㎏COD/㎏VSS/day at 22℃ and HRT of 12 hrs. As increasing organic loading rates, the biomass concentration was decreased steadily with decreasing of biofilm dry density rather than biofilm thickness. Based on the experimental results, It was suggested that the decrease in biofilm dry density was caused by a loss of biomass inside the biofilm.

Hydrodynamic characteristics such as gas holdup, liquid circulation velocity and bed expansion in a hexagonal inverse fluidized bed were investigated using air-water system by changing the ratio (Ad/Ar) of cross-sectional area between the riser and the downcomer, the liquid level(Hl/H), and the superficial gas velocity(Ug). The gas holdup and the liquid circulation velocity were steadily increased with the superficial gas velocity increasing, but at high superficial gas velocity, some of gas bubbles were carried over to a downcomer and circulated through the column. When the superficial gas velocity was high, the Ad/Ar ratio in the range of 1 to 2.4 did not affect the liquid circulation velocity, but the maximum bed expansion was obtained at Ad/Ar ratio of 1.25. liquid circulation velocity was expressed as a model equation below with variables of the cross-sectional area ratio(Ad/Ar) between riser to downcomer, the liquid level(H1/H), the superficial gas velocity(Ug), the sparger height[(H-Hs)/H], and the draft plate level(Hb/H). Uld=11.62g^0.75(Hl/H)^10.30(Ad/Ar)^-0.52(H-Hs/H)^0.91(Hb/H)^0.13

Continuous deodorization of malodorous sulfur compounds by Thiobacillus neapolitanus R-10 immobilized onto a polypropylene pellet was studied using a column reactor at 30℃. The maximum amounts of immobilized cells was 5.3 g/ℓ polypropylene with 5 × 7.5㎜ in pellet size, and the amounts of immobilized cells in the higher part of the column was as twice as in the lower part. The optimum pH and temperature for removal of dimethyl sulfide were 6.0 and 30℃, respectively. When 5-20 ㎕/ℓ of hydrogen sulfide and methylmercaptan were employed 98% of removal efficiency were achieved. In contrast, lower concentrations of dimethyl sulfide and dimethyldisulfide should be supplied to meet satisfactory deodorization efficiency. The immobilized cell column was successfully operated for the deodorization of mixture of sulfur compounds over 15 days without significant loss of initial activity achieving high efficiency.