• 한국막학회:학술대회논문집
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• 한국막학회 1999년도 춘계 총회 및 학술발표회
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• pp.61-62
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• 1999

• 멤브레인
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• 제27권3호
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• pp.263-272
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• 2017

분리막의 기공 크기 및 분포도를 분석하기 위한 다양한 측정법이 있지만 10-50 nm 범위의 한외여과막 기공크기를 정확하게 측정하기가 까다롭다. 따라서 gas-liquid displacement porometer (GLDP)와 liquid-liquid displacement porometer(LLDP) 기공 특성 측정법 두 가지를 이용하여, 10-100 nm의 기공크기를 갖는 세 종류의 세라믹 분리막(K-100, A-100, A-20)의 기공 크기 및 분포도를 비교 분석하였다. GLDP는 한외여과막의 최대 기공크기를 측정하는데 적합한 분석법으로 확인되었고, LLDP로 측정된 평균 기공크기가 분리막의 분리 성능 결과와 더 연계되어 있었다. 또한 LLDP는 10-50 nm 범위의 기공크기를 측정하는데 적합한 기공 분석법으로 확인되었으나, GLDP 보다 낮은 정밀도와 높은 민감도를 나타내었다. 다양한 기공 특성 분석법 가운데, 최근 상용화된 LLDP 기술은 종래의 측정법으로 알지 못했던 유용한 결과들을 제공할 수 있을 것으로 기대된다.

• Membrane and Water Treatment
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• 제3권2호
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• pp.77-98
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• 2012

A two-dimensional (2D) steady state numerical model of concentration polarisation (CP) phenomena in a membrane channel has been developed using the commercially available computational fluid dynamics (CFD) package CFX (Ansys, Inc., USA). The model incorporates the transmembrane pressure (TMP), axially variable permeate flux, variable diffusivity and viscosity, and osmotic pressure effects. The model has been verified against several benchmark analytical and empirical solutions from the membrane literature. Additionally, the model is able to predict the rejection of an arbitrary solute by the membrane using a pore model, given some basic knowledge of the geometry of the solute molecule or particle, and the membrane pore geometry. This allows for predictive design of membrane systems without experimental determination of the membrane rejection for the specified operating conditions. A demonstration of the model is presented against experimental results for two uncharged test compounds (sucrose and PEG1000) from the literature. The model will be extended to incorporate charge effects, transient simulations, three-dimensional (3D) geometry and turbulent effects in future work.

• 멤브레인
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• 제9권4호
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• pp.221-229
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• 1999

공칭크기가 0.2${\mu}m인 polytetrfluroethylene(PTFE Satorius사) 정밀여과막에 0.1wt% kaolin benotonite yeast 및 starch 용액을 각각 투과시키고 막을 세척한 후 순수/이소부탄올을 이용한 액체전이법으로 막의 세공분포를 추정하였다 액체전이법으로 추정한 오염되지 않은 PTFE 분리막의 세공분포는 수은침투법 및 전자 현미경 사진의 분포와도 유사하였다 PTFE 막의 세공크기보다 작은 입자가 존재하는 bentonite 및 starch 용액을 투과시킬 경우 분리막 세공이 상당히 오염되어 세공분포가 약 0.3${\mu}m이하로 축소되었다. 그러나 kaolin 용액의 경우에는 0.35${\mu}m 이상의 세공일부만이 부분적으로 오염된 것으로 나타났다 이와같이 액체전이법을 이용한 분리막의 세공분포 측정으로 막오염 현상을 보다 정량적으로 구명할수있었다.

• Membrane and Water Treatment
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• 제4권2호
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• pp.143-155
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• 2013

Four membranes were used to separate Chlorella sp. from their culture medium in cross-flow microfiltration (MF) experiments: cellulose acetate (CA), cellulose nitrate (CN), polypropylene (PP) and polyvinylidenefluoride (PVDF). It was found that the hydrophilic CA and CN membranes with a pore size of 1.2 ${\mu}m$ exhibited the best performances among all the membranes in terms of permeation flux. The hydrophobicity of each membrane material was determined by measuring the angle between the water (liquid) and membrane (solid). Contact angle measurements showed that deionized (DI) water had almost adsorbed onto the surfaces of the CA and CN membranes, which gave $0.00^{\circ}$ contact angle values. The PP and PVDF membranes were more hydrophobic, giving contact angle values of $95.97^{\circ}$ and $126.63^{\circ}$, respectively. Although the pure water flux increased with increasing pore diameter (0.8 < 1.2 < 3.0 ${\mu}m$) in hydrophilic CA and CN membranes, the best performance in term of filtration rate for filtering a microalgae suspension was attained by membranes with a pore size of 1.2 ${\mu}m$. The fouled membrane pore sizes and pore blocking were inspected using a scanning electron microscope (SEM). MF with large pore diameters was more sensitive to fouling that contributed to intermediate blocking, where the size of the membrane pores is almost equivalent to that of cells.

• 한국신재생에너지학회:학술대회논문집
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• 한국신재생에너지학회 2009년도 춘계학술대회 논문집
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• pp.278-281
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• 2009

Proton exchange membrane is the key material for proton exchange membrane fuel cells (PEMFC). Currently widely-used perfluorosulfonic acid membranes have some disadvantages, such as low thermal stability, easy swelling, excessive crossover of methanol and high price etc. Other membranes, including sulfonated polymer, radiation grafted membranes, organic-inorganic hybrids and acid-base blends, do not satisfy the criteria for PEMFC, which set a barrier to the development and commercialization of PEMFC. Pore-filling type proton exchange membrane is a new proton exchange membrane, which is formed by filling porous substrate with electrolytes. Compared with traditional perfluorosulfonic acid membranes, pore-filling type proton exchange membranes have many advantages, such as non- swelling, low methanol permeation, high proton conductivity, low cost and a wide range of materials to choose. In this research, preparation methodology of pore-filling membranes by particularly using all hydrocarbon polymers and fuel cell performances with the membranes are evaluated.

• Membrane and Water Treatment
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• 제4권2호
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• pp.127-142
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• 2013

In order to investigate the significance of "salting-out" and "pore swelling" effects on the nanofiltration of neutral solutes, rejection properties of two NF ceramic and polymeric membranes were studied with single polyethyleneglycol (PEG) solution and mixed PEG/inorganic electrolyte solutions. For both membranes, the rejection rate of PEG was found to decrease significantly in the presence of ions. In the case of the ceramic membrane (rigid pores), this phenomenon was imputed to the sole partial dehydration of PEG molecules induced by the surrounding ions. This assumption was confirmed by the lowering of the PEG rejection rates which followed the Hofmeister series. Experimental data were used to compute the resulting decrease in the Stokes radius of PEG molecules in the presence of the various salts. Concerning the polymeric membrane, the decrease in the rejection rate was found to be systematically higher than for the ceramic membrane. The additional decrease was then ascribed to the swelling of the pores. The experimental data of rejection rates were then used to compute the variation in the mean pore radius in the presence of the various salts. The pore swelling phenomenon due to accumulation of counterions inside pores was supported by electrokinetic charge density measurements.

• 멤브레인
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• 제18권1호
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• pp.53-64
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• 2008

벤토나이트 현탁액에 의한 폴리에틸렌 정밀여과 모세관 막의 오염특성에 대하여 검토하였다. 막오염의 윈인은 막표면 위에서 생성되는 케익층의 성장과 입자들이 세공을 막는 표준 및 완전세공막힘 때문이었으며, 막오염은 이들 세 가지 오염형태가 동시에 발생하지만 케익여과오염에 의해 크게 지배를 받는다. 운전압력 $1.0kg/cm^2$에서 총 막오염에 대한 성분오염의 비율은 표준세공막힘 3.36%, 완전세공막힘 3.18% 그리고 케익여과오염 93.46%이었다. 현탁액의 농도가 1000 ppm인 경우에는 완전세공막힘 1.71%, 표준세공막힘 1.90% 그리고 케익여과오염이 96.39%이었으며, 운전초기에 총 오염의 96.14%가 발생했다. 총 오염에 대한 케익여과의 영향은 세공이 $0.34{\mu}m$막에서 컸다. 순환흐름속도의 증가로 인해 성분오염은 약 10.20% 감소하였고, 총 오염에 대한 세공막힘의 비율은 높았다.

• 멤브레인
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• 제15권1호
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• pp.52-61
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• 2005

폴리에틸렌 정밀여과 모세관막을 이용한 벤토나이트 콜로이드 현탁액의 투과유속 감소특성을 검토하였다. 운전시간이 경과하면서 투과유속이 감소되는 원인은 막표면 위에서 케익층의 성장과 입자들에 의한 세공막힘 때문이었으며, 운전시간이 경과하여 정상상태에 도달하면 투과유속은 케익여과 모델에 의해 지배받는다. 운전압력이 높은 경우의 투과유속 감소는 세공막힘과 케익층이 치밀해졌기 때문이다. 운전압력이 증가함에 따라 J/J₁는 감소하였으며, 0.5 kg/sub f//㎠일 때의 45%, 2.0 kg/sub f//㎠일 때 38%로 감소하였다. 운전압력 0.5 kg/sub f//㎠에서 총 막오염에 대한 성분오염의 비율은 표준세공막힘 14.6%, 완전세공막힘 23.4% 그리고 케익여과 62.0% 이었다. 순환흐름속도의 증가로 인해 투과유속은 증가하였고, 그 효과는 운전압력이 1.0 kg/sub f//㎠일 때가 운전압력 2.0 kg/sub f//㎠ 경우보다 컸다. 세공크기가 0.34 ㎛인 막의 투과유속은 세공의 크기가 0.24 ㎛인 막보다 컸으며, 용액의 농도에 따른 투과유속은 농도가 낮은 용액이 컸다. 세공크기가 0.34 ㎛인 막의 막오염 형태는 유사하지만 농도가 200 ppm인 용액의 경우 1000 ppm인 용액에 비하여 상대적으로 미약한 세공막힘 현상을 보였다.

• Membrane and Water Treatment
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• 제13권6호
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• pp.313-320
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• 2022

Theoretical calculation results are presented for the enhancement of the water mass flow rate through the hydrophobic micro/nano pores in the membrane respectively on the micrometer and nanometer scales. The water-pore wall interfacial slippage is considered. When the pore diameter is critically low (less than 1.82nm), the water flow in the nanopore is non-continuum and described by the nanoscale flow equation; Otherwise, the water flow is essentially multiscale consisting of both the adsorbed boundary layer flow and the intermediate continuum water flow, and it is described by the multiscale flow equation. For no wall slippage, the calculated water flow rate through the pore is very close to the classical hydrodynamic theory calculation if the pore diameter (d) is larger than 1.0nm, however it is considerably smaller than the conventional calculation if d is less than 1.0nm because of the non-continuum effect of the water film. When the driving power loss on the pore is larger than the critical value, the wall slippage occurs, and it results in the different scales of the enhancement of the water flow rate through the pore which are strongly dependent on both the pore diameter and the driving power loss on the pore. Both the pressure drop and the critical power loss on the pore for starting the wall slippage are also strongly dependent on the pore diameter.