• Proceedings of the Membrane Society of Korea Conference
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• 1998.10a
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• pp.163-165
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• 1998

한외여과 분리막을 이용한 공정은 화학공업을 비롯하여 의약품, 식품, 폐수 처리 및 반도체산업 등의 여러 분야에서 이용되고 있다. 그러나 한외여과 분리 공정에 잇어서 해결되어야 할 중요한 문제점은 투과유속의 감소현상이다. 용액의 투과유속이 순수의 투과유속보다 낮아지는 투과유속의 감소현상은 크게 농도분극과 막오염 현상에 기인한다. 농도분극에 의한 투과유속의 감소는 보통 1분 이내의 매우 짧은 시간 안에 일어나지만 시간이 지속됨에 따라 투과유속이 감소하는 현상은 막오염에 기인한다.

• Journal of the Korean Society of Food Science and Nutrition
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• v.17 no.4
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• pp.365-370
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• 1988

한외여과법을 이용한 식품 페액의 단백질 분리, 회수에 관한 조작조건의 최적화를 위하여 cheese whey의 투과유속에 대한 세정효과의 영향과 조작압과 한계유속의 상관관계를 측정하여 다음의 결과를 얻었다. 세정의 효과로부터 유지 전용세제를 사용한 경우가 막의 투과유속의 회복율이 가장 높았으므로 whey중에 소량 함유되어 있는 유지분이 막의 투과유속의 저하에 큰 영향을 미침을 알 수 있었고, cheese whey를 한외여과법에 의하여 농축, 분리하는 경우 사용압력범위 $1{\sim}10kg/cm^2$에서 분획분자량 100,000인 막을 사용하는 경우 조작압력 약 $7kg/cm^2$에서 한계유속에 달하였으며, 그 이상으로는 압력을 가하여도 투과유속은 상승하지 않았다. 또한 이력현상의존재도 고려하여 볼 때 과도한 압력은 한외여과의 경우 투과유속의 상승에 효과가 없음을 알 수 있었다.

• Membrane Journal
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• v.27 no.1
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• pp.43-52
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• 2017

The air injection nozzle tube was inserted inside of the tubular membrane module to reduce membrane fouling and improve the permeate flux. The average pore size of membrane was $0.1\;{\mu}m$ and the yeast was used as a foulant. All of permeate experiments were started without air injection for the module equipped with the nozzle tube, then carried out continuously with air injection. Finally, the nozzle tube was removed from the module and the permeate was measured without air injection. The measured permeate fluxes were compared to examine the effect of air injection. The fluxes for air injection were consistently maintained or increased. The fluxes of no-air injection with the nozzle tube were greater than those of the empty tubular module. As operating pressure decreased to 0.4 bar, the flux enhancement of air injection based on no-nozzle case increased to 21%. Flux enhancements of air injection were above 30% as the gas/liquid two-phase flow was changed from the stratified-smooth to the intermittent pattern due to increase of gas flowrate.

• Membrane Journal
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• v.15 no.4
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• pp.338-348
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• 2005

The permeate flux decline on microfiltration capillary membrane operation was investigated with inorganic colloidal solutions. The permeate flux of the alumina solution is two times higher in average than that of the bentonite solution. The flux decline with increase in operation time was less in the alumina solution than in the bentonite solution. The rate of initial flux decline until 10 min was higher on the bentonite solution over the alumina solution. The decline in permeate flux was due to both the cake formation and the pore blocking. The latter effect was higher in the operation of the bentonite solution. In comparing the ratio of each fouling component to the total fouling fur the $1.0\;kg_f/cm^2$ TMP condition, complete blocking was $9.35\%$, standard blocking was about $6.82\%$ and cake filtration was $83.83\%$, respectively. With the increase in cross flow velocity, the permeate flux increased by $6.0\%$ for the alumina solution and by 14.0 for the bentonite solution. With the increase in average pore size fromm $0.24\;{\mu}m\;to\;0.34\;{\mu}m$, the permeate flux increases 1.61 times for the alumina solution and 1.76 times far the bentonite solution.

• Membrane Journal
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• v.14 no.3
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• pp.207-217
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• 2004

In this study, we prepared nanofiltration membrane by applying the interfacial polymerization method as a way of manufacturing composite membranes. We have examined the effects of various preparation factors such as monomer concentration and composition, thermal curing condition, post treatment condition. In addition to preparation conditions, we also monitored the effects of operation conditions such as feed solution concentration and operation pressure on the permeation properties of the resulting nanofiltration membrane. We intended to increase the permeation rate of nanofiltration membrane by the enlargement of effective surface area using additives during interfacial polymerization step. With increasing the monomer concentration, membrane permeation rate are decreased with maintaining almost constant rejection. With respect to curing condition, with increasing the curing temperature both permeation rate and rejection are decreased. With increasing the ratio of MPD in amino monomer composition, permeation rate decreased drastically with high rejection. With increasing the feed solution concentration, both permeation rate and rejection decreased. Both permeation rates and rejection increased with increasing the operating pressure. Nanofiltration membrane have higher surface roughness with increasing additive concentration in the case of using MPD contained amine composition than using piperazine alone. Permeation rates are much lower than the nanofiltration membrane prepared by piperazine.

• Clean Technology
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• v.5 no.2
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• pp.69-78
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• 1999

Separation characteristics of cutting oil-in-water emulsions were studied experimentally by using various kinds of flat-type microfiltration and ultrafiltration membranes. For ultrafiltration membranes the permeation behavior of cutting oil emulsions obeys the film model, whereas a significant deviation from the model was observed for ASYPOR microfiltration membranes. The experimental data obtained for all the membranes showed that the effect of operating pressure on the permeation flux of oil-in-water emulsions is not very significant. At low transmembrane pressures the permeation flux decreased gradually with increasing filtration time, whereas the permeation flux at high transmembrane pressures decreased steeply for early filtration time. However, every flux eventually reached a constant value that depends only on the applied transmembrane pressure. For the hydrophobic polycarbonate microfiltration membrane the permeation flux increased with the filtration time. The critical permeation pressures were also determined from the data obtained from unstirred cell experiments.

• Membrane Journal
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• v.26 no.2
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• pp.166-172
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• 2016

In this study critical permeation flux was measured by the flux-step method with respect to aeration rate. The hollow fiber membrane module which has $85cm^2$ of effective area and $0.4{\mu}m$ nominal pore size was submerged in the activated sludge solution of MLSS 5,000 mg/L. The critical flux for without aeration was measured of $15.2L/m^2{\cdot}h$. However, the critical flux increased from 20.6 to $32.5L/m^2{\cdot}h$ as the aeration rate increased from 100 to 1,000 mL/min.

• Korean Chemical Engineering Research
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• v.52 no.3
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• pp.328-334
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• 2014

This study examined the effect of concentration polarization on permeate flux in forward osmosis (FO) membrane process for saline and sucrose solution. The reduction in permeate flux during the FO membrane process is largely due to the formation of concentration polarization on membrane surfaces. The flux reduction due to internal concentration polarization formed on the porous support layer was larger than that due to the external concentration polarization on the active membrane surface. Water permeate flux through the FO membrane increased nonlinearly with the increase in osmotic pressure. The water permeability coefficient was $1.8081{\times}10^{-7}m/s{\cdot}atm$ for draw solution on active layer (DS-AL) mode and $1.0957{\times}10^{-7}m/s{\cdot}atm$ for draw solution on support layer (DS-SL) mode in NaCl solution system. The corresponding membrane resistance was $5.5306{\times}10^6$ and $9.1266{\times}10^6s{\cdot}atm/m$, respectively. With respect to the sucrose solution, the permeate flux for DS-AL mode was 1.33~1.90 times higher than that for DS-SL mode. The corresponding variation in the permeation flux (J) due to osmotic pressure (${\pi}$) would be expressed as $J=-0.0177+0.4506{\pi}-0.0032{\pi}^2$ for the forward and $J=0.0948+0.3292{\pi}-0.0037{\pi}^2$ for the latter.

• Membrane Journal
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• v.15 no.1
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• pp.52-61
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• 2005

Permeate flux decline in a microfiltration was analyzed by measuring the permeability of bentonite colloidal solution through polyethylene capillary membranes. The flux decline with time was due to the growth of cake layer on the membrane surface and to the pore blocking by particles. As the time approaches to steady state, the permeate flux is almost controlled by the cake filtration model. Faster flux decline at high trans-membrane pressure was attributed to the formation of denser packed cake layer and pore blocking. The ratio of permeate flux to the initial permeate flux, J/J₁, decreased with increasing the trans-membrane pressure, from 45% for 0.5 kg/sub f//㎠ to 38% for 2.0 kg/sub f//㎠. In comparing the ratio of each fouling component to the total fouling for the 0.5 kg/sub f//㎠ TMP condition, complete blocking was 23.4%, standard blocking was about 14.6% and cake filtration was 62.0%, respectively. Permeate flux through the membrane increases with cross flow velocity, and the effect of the variation of velocity is more significant at 1.0 kg/sub f//㎠ rather than at 2.0 kg/sub f//㎠ of the operation pressure. Permeate flux for the membrane having the average pore diameter of 0.34 ㎛ was higher than that for the membrane of 0.24 ㎛ pore size, with the higher flux with the low concentration of feed. On the operation using the membrane of 0.34 ㎛ pore, the pore blocking in the low concentration of 200 ppm is negligible relative to the pore blocking in the 1000 ppm feed.

• Membrane Journal
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• v.8 no.1
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• pp.42-49
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• 1998

Effects of operating time, pH, temperature, concentration and addition of proteolytic enzyme on permeate flux for the ultrafiltration of gelatin and bovine serum albumin(BSA) solutions were studied. The results showed that permeate flux of gelatin solution was maintained almost constant during the operating time, and that of BSA solution was decreased to 66% of the initial value after 40 min operation. The permeate flux of gelatin solution was increased by increasing temperature. The permeate flux of BSA solution was constant in the temperature range of 30~$50{\circ}C$, but increased at $60{\circ}C.$. The permeate fluxes of gelatin and BSA solution showed minimum values near the isoelectric point of pH 5.0. The permeate fluxes of 1%(w/v) and 6% gelatin solution were $43.0l/m^2\cdot hr$ and $13.5l/m^2\cdot hr$, respectively. Those of 1% and 4% BSA solution were $33.0l/m^2\cdot hr$ and $14.0l/m^2\cdot hr$, respectively. The permeate fluxes of gelatin and BSA solutions were decreased to 68.6% and 57.6% of their initial values by increasing their concentration, respectively. The permeate fluxes of gelatin and BSA solutions were enhanced by 30% with the addition of proteolytic enzyme.