Enhanced microfiltration of γ-globulin solution upon treatment of NaCl addition and/or DNase digestion

Microfiltration of a γ-globulin solution has been investigated through the virus removal membranes having different pore sizes (i.e. r=15, 35 and 75 nm) and a dialysis membrane (r=3.4 nm), which were all made of the same regenerated cellulose material. The addition of NaCl in the γ-globulin feed solution was effective to enhance the flux and transmission through the membranes having a pore size ranging from 15 to 75 nm. DNase treatment of a γ-globulin solution with Micrococcal nuclease enhanced the flux and transmission of γ-globulin through the membranes either with or without NaCl. The membranes having a pore size of 35 nm showed dramatically enhanced flux in the microfiltration of a γ-globulin solution containing NaCl and/or being treated with Micrococcal nuclease. This can be explained as a DNase treatment and NaCl addition in the protein solution dissociate protein aggregates of DNA–γ-globulin complex, which plugs the pores in the microfiltration membranes.     

A new route for the fabrication of TiO2 ultrafiltration membranes with suspension derived from a wet chemical synthesis

Titania ultrafiltration membranes were successfully fabricated by a new route, which was directly derived from the nanoparticles suspension that was the intermediate product prior to dry and calcine in the synthesis of nanoparticle by a wet chemical method. The morphology and the crystal structure of the prepared membrane were analyzed by SEM and XRD. The effect of various dipping time on the membrane thickness was investigated. The rejection of the bovine serum albumin (BSA, 67,000 Da) was used to evaluate the separation characteristics of these membranes, and the relationship between the dipping time and the optimization thickness of the membrane was built on the base of the data of the pure water flux. SEM images showed that the surface of the membrane was defect-free and XRD revealed that the titania crystalline phase was pure anatase. The membrane thickness increased linearly with the square root of the dipping time and the dipping time of 30 s was necessary to form a defect-free titania layer on the top of supports. The titania layer derived from the dipping time of 30 s could be of thickness of 5.9 μm and an average pore size of 60 nm. The pure water permeability of the membrane was 860 × 10⁻⁵ L/(m² h Pa) (860 L/(m² h bar)), and the BSA rejections of the membranes prepared reached to 90% after 20 min running.     

Preparation and characterization of nanoparticles formed by chitosan-caseinate interactions

Intermacromolecular complexation between chitosan and sodium caseinate in aqueous solutions was studied as a function of pH (3–6.5), using absorbance measurements (at 600 nm), dynamic light scattering (DLS), and transmission electron microscopy (TEM). The chitosan–caseinate complexes formed were stable and soluble in the pH range 4.8–6.0. In this pH range, the biopolymers had opposite charges. At higher concentrations of chitosan (0.15 wt%), the soluble complexes associated to form larger particles. DLS data showed that, between pH 4.8 and 6.0, the particles formed by the complexation of chitosan and caseinate had sizes between 250 and 350 nm and these nanoparticles were visualized using negative staining TEM. Above pH 6.0, the nanoparticles associated to form larger particles, causing phase separation. Addition of NaCl increased the particle size. The pH dependence of the zeta potential of the mixture solutions was appreciably different from that of the pure protein and pure chitosan solutions.     

Pd encapsulated and nanopore hollow fiber membranes: Synthesis and permeation studies

New types of supported Pd membranes were developed for high temperature H₂ separation. Sequential combinations of boehmite sol slip casting and film coating, and electroless plating (ELP) steps were designed to synthesize “Pd encapsulated” and “Pd nanopore” membranes supported on -Al₂O₃ hollow fibers. The permeation characteristics (flux, permselectivity) of a series of unaged and aged encapsulated and nanopore membranes with different Pd loadings were compared to those of a conventional 1 μm Pd/4 μm γ-Al₂O₃/-Al₂O₃ hollow fiber membrane. The unaged encapsulated membrane exhibited good performance with ideal H₂/N₂ separation factors of 3000–8000 and H₂ flux 0.4 mol/m² s at 370 °C and a transmembrane pressure gradient of 4 × 10⁵ Pa. The unaged Pd nanopore membranes had a lower initial flux and permselectivity, but exhibited superior performance with extended use (200 h). At the same conditions the unaged 2.6 μm Pd nanopore membrane had a H₂ flux of 0.16 mol/m² s and separation factor of 500 and the unaged 0.6 μm Pd nanopore membrane had a H₂ flux of 0.25 mol/m² s and separation factor of 50. Both nanopore membranes stabilized after 40 h of operation, in contrast to a continued deterioration of the permselectivity for the other membranes. An analysis of the permeation data reveals a combination of Knudsen and convective transport through membrane defects. A phenomenological, qualitative model of the synthesis and resulting structure of the encapsulated and nanopore membranes is presented to explain the permeation results.     

Separation and permeation characteristics of a DD3R zeolite membrane

Permeation of various gases (carbon dioxide, nitrous oxide, methane, nitrogen, oxygen, argon, krypton, neon) and their equimolar mixtures through DD3R membranes have been investigated over a temperature range of 220–373 K and a feed pressure of 101–400 kPa. Helium was used as sweep gas at atmospheric pressure. Adsorption isotherms were determined in the temperature range 195–298 K, and modelled by a single and dual site Langmuir model. The permeation flux is determined by the size of the molecule relative to the window opening of DD3R, and its adsorption behaviour. As a function of temperature, bulky molecules (methane) show activated permeation, weakly adsorbing molecules decreasing permeation behaviour and strongly adsorbing molecules pass through a maximum. Counter diffusion of the sweep gas (helium) ranged from almost zero up to the order of the feed gas permeation and was strongly influenced by the adsorption of the feed gas.

DD3R membranes have excellent separation performance for carbon dioxide/methane mixtures (selectivity 100–3000), exhibit good selectivity for nitrogen/methane (20–45), carbon dioxide and nitrous oxide/air (20–400), and air/krypton (5–10) and only a modest selectivity for oxygen/nitrogen (2) separation. The selectivity of mixtures of a strongly and a weakly adsorbing component decreased with increasing temperature and pressure. The selectivity of mixtures of weakly adsorbing components was independent of pressure.

The permeation and separation characteristics of light gases through DD3R membranes can be explained by taking into account: (1) steric effects introduced by the window opening of DD3R leading to molecular sieving and activated transport, (2) competitive adsorption effects, as observed for mixtures involving strongly adsorbing gases, and (3) interaction between diffusing molecules in the cages of the zeolite.     

Asymmetric membranes with modified gold films as selective gates for metal ion separations

Thin layers of gold (700 Å) were deposited on manufactured alumina pourous supports to yield nanopores with openings of <7 nm. A self-assembled monolayer (SAM) of alkyl thiols was then attached to provide a hydrophobic support for trialkyl phosphine oxide-based metal ion carriers. The resulting gated membranes provided a barrier to ions including H⁺, and Ca²⁺, NO₃⁻, and CH₃COO⁻. When an aqueous feed solution of 4.2 mM uranyl nitrate and 1 M lithium nitrate pH 4, and a receiving solution of 1 M sodium acetate pH 5.5 were used 100% of the metal was transported across the membrane by facilitated transport via the phosphate or phosphine oxide carrier. The thin gates transported metal ions as neutral nitrate complexes with fluxes high enough to be limited by the alumina support. The flux rates of 200,000 metal ions per pore per second are only a factor of 5 below that observed for the potassium channel. High selectivity of U over Eu is observed until the [U] is <0.84 mM in the feed solution, despite the fact the Eu actually transports faster when U is not present. This work demonstrates that selectivity can be added without impeding transport by using thin selective layers.     

Micro-structural optimization of supported γ-alumina membranes

The micro-structural integrity of meso-porous inorganic membranes is of critical importance in their prolonged application. Inspection by transmission electron microscopy of state-of-the-art γ-alumina membrane cross-sections, made by focused ion beam milling, reveals structural defects which adversely affect performance, reproducibility, and lifetime. It is shown that the use of macro-porous supports with a smooth, defect-free deposition surface for membrane dip coating, in combination with purified precursor sols and clean processing, leads to major improvements in micro-structural homogeneity and properties of the membranes. Large particle contaminants/agglomerates can be effectively removed from precursor sols by high-speed centrifugation or ultrasound-assisted screening. While centrifugation is the most practical method for routine use, filter screening provides a more complete removal of agglomerates and larger particles (>80 nm Ø). Application of the purified membrane precursor sols results in membranes in which connected pore defects (pinholes) are no longer detectable for a membrane thickness of >500 nm thick. The almost complete absence of connected pinholes, obtained with improved membrane processing, is demonstrated by near-100% retention of CaCl₂ in aqueous solution by nano-filtration. The γ-alumina processing experience, collected in our group in the years 2002–2006, is accumulated in a 34-step processing protocol for γ-alumina membranes with a >500 nm single layer thickness.     

Synthesis and characterization of MCM-48 tubular membranes

MCM-48 membranes have been prepared on alumina supports of different pore sizes. A battery of characterization techniques has been used to study the physical properties and the quality of the membranes prepared. The highest quality membranes were prepared on supports with pore size of up to 60 nm. The MCM-48 membranes were tested in the separation of gas phase mixtures and a cyclohexane/O₂ selectivity higher than 270 was obtained. The selective separation of organic compounds from inert components is a result of the cooperative effects of capillary condensation in MCM-48 pores and of the specific interactions of the permeating compounds and the membrane material.     

Bio-ceramic hollow fiber membranes for immunoisolation and gene delivery: I: Membrane development

Zirconia bio-ceramic hollow fiber membranes were developed using a sequence of mixing, extrusion, phase inversion and sintering steps. ZrO₂ partially stabilized by Y₂O₃ was chosen as the starting membrane material. The prepared membranes were characterized by SEM, EDX, XRD and gas permeation techniques. Effects of the starting ZrO₂ particle size and sintering temperature on the physical properties of the resulted hollow fiber membranes were extensively studied. Sintered at 1400 °C for 10 h, membranes made from 80 nm sized ZrO₂ particles display cubic fluorite as the major crystalline phase and give rise to interesting microstructure for cell response. Without any surface modification, this tailor-made membrane with high mechanical strength and pore size less than 1 μm was selected for further test of osteoblast attachment. In vitro bio-compatibility was evaluated by using mouse MC-3T3-E1 osteoblast cell culture. A series of cell interactions with fiber surface (i.e. cell adhesion, proliferation, formation of bone nodules, mineralization, etc.) verified the bio-compatibility of the prepared membranes.     

Supported carbon molecular sieve membranes based on a phenolic resin

The preparation of a composite carbon membrane for separation of gas mixtures is described. The membrane is formed by a thin microporous carbon layer (thickness, 2 μm) obtained by pyrolysis of a phenolic resin film supported over a macroporous carbon substrate (pore size, 1 μm; porosity, 30%). The microporous carbon layer exhibits molecular sieving properties and it allows the separation of gases depending on their molecular size. The micropore size was estimated to be around 4.2 Å. Single and mixed gas permeation experiments were performed at different temperatures between 25°C and 150°C, and pressures between 1 and 3.5 bar. The carbon membrane shows high selectivities for the separation of permanent gases like O₂/N₂ system (selectivity≈10 at 25°C). Gas mixtures like CO₂/N₂ and CO₂/CH₄ are successfully separated by means of prepared membranes. For example, the membrane prepared by carbonization at 700°C shows at 25°C the following separation factors: CO₂/N₂≈45 and CO₂/CH₄≈160.     

A photocatalytic membrane reactor for VOC decomposition using Pt-modified titanium oxide porous membranes

Porous titanium oxide membranes with pore sizes in the range of 2.5–22 nm were prepared by a sol–gel procedure, and were applied for decomposition of methanol and ethanol as model volatile organic compounds (VOCs) in a photocatalytic membrane reactor, where oxidation reaction occurs both on the surface and inside the porous TiO₂ membrane while reactants are permeating via one-pass flow. Methanol was completely photo-oxidized by black-light irradiation to CO₂ when methanol at a concentration of 100 ppm was used at a feed flow rate of 500 × 10⁻⁶ m³/min, but the conversion decreased when the MeOH concentration in the feed was increased. Pt-modification was carried out by photo-deposition, and led to a decrease in pore diameter. Using Pt-modified membranes, a nearly complete oxidation of methanol up to 10,000 ppm at a feed flow rate of 500 × 10⁻⁶ m³/min was observed. Thus, such membranes would be effective for purifying a permeate stream after one-pass permeation through the TiO₂ membranes. The decomposition of ethanol is also discussed.     

Morphology and characterization of 3D micro-porous structured chitosan scaffolds for tissue engineering

This research studies the morphology and characterization of three-dimensional (3D) micro-porous structures produced from biodegradable chitosan for use as scaffolds for cells culture. The chitosan 3D micro-porous structures were produced by a simple liquid hardening method, which includes the processes of foaming by mechanical stirring without any chemical foaming agent added, and hardening by NaOH cross linking. The pore size and porosity were controlled with mechanical stirring strength. This study includes the morphology of chitosan scaffolds, the characterization of mechanical properties, water absorption properties and in vitro enzymatic degradation of the 3D micro-porous structures. The results show that chitosan 3D micro-porous structures were successfully produced. Better formation samples were obtained when chitosan concentration is at 1–3%, and concentration of NaOH is at 5%. Faster stirring rate would produce samples of smaller pore diameter, but when rotation speed reaches 4000 rpm and higher the changes in pore size is minimal. Water absorption would reduce along with the decrease of chitosan scaffolds’ pore diameter. From stress–strain analysis, chitosan scaffolds’ mechanical properties are improved when it has smaller pore diameter. From in vitro enzymatic degradation results, it shows that the disintegration rate of chitosan scaffolds would increase along with the processing time increase, but approaching equilibrium when the disintegration rate reaches about 20%.     

Blended chitosan and polyvinyl alcohol membranes for the pervaporation dehydration of isopropanol

Homogeneous membranes were prepared by casting the solution of blended chitosan and polyvinyl alcohol (PVA) on a glass plate. The percent weight of chitosan in the membrane was varied from 0 to 100%. The membrane thickness was in the range of 15–30 μm. The membranes were heat treated at 150 °C for an hour. After that the membranes were crosslinked by glutaraldehyde and sulfuric acid in acetone aqueous solution. The membranes were tested at 30–60 °C for dehydration performance of 50–95% isopropanol aqueous solutions. At around 90% of isopropanol in the feed mixture, permeate flux increased whereas the percent of water in permeate tended to decrease when the feed temperature increased for all membranes, except that the water content in permeate from the membrane containing 75 wt.% chitosan remained constant. The swelling degree in water and the total flux increased with increasing chitosan content in membranes. The effect of temperature on permeate flux followed the Arrhenius relationship. The permeate flux decreased when isopropanol in the feed increased for all membranes. However, water content in permeate and isopropanol concentration in the feed formed complex relationship for different chitosan content membranes. Sorption did not appear to have significant effects on separation. The membrane containing chitosan 75% performed the best. For a feed solution containing 90% isopropanol at 60 °C, the permeate flux was 644 g/m² h with water content of nearly 100% in the permeate. At 55% isopropanol in the feed at 60 °C, the permeate flux was 3812 g/m² h. In the range of 55–95% of isopropanol in the feed, the water content in permeate was more than 99.5%. This membrane showed very excellent performance with good mechanical strength. It is promising to develop this membrane for industrial uses.     

Self‐Assembled Isoporous Block Copolymer Membranes with Tuned Pore Sizes

The combination of nonsolvent‐induced phase separation and the self‐assembly of block copolymers can lead to asymmetric membranes with a thin highly ordered isoporous skin layer. The effective pore size of such membranes is usually larger than 15 nm. We reduced the pore size of these membranes by electroless gold deposition. We demonstrate that the pore sizes can be controlled precisely between 3 and 20 nm leading to a tunable sharp size discrimination in filtration processes. Besides fractionation of nanoparticles and biomaterials, controlled drug delivery is an attractive potential application.     

Fabrication of porous collagen/chitosan scaffolds with controlling microstructure for dermal equivalent

Two sets of homemade apparatus have been utilized to fabricate collagen/chitosan porous membranes by quenching its acetic solution and subsequently extracting the solvent with ethanol. The influence of chitosan concentration on the surface morphology of the collagen/chitosan membranes was studied using a quenching cold plate (apparatus 1). The pore size was enlarged along with an increase in the chitosan content, accompanied with the emergence of a sheet‐like microstructure. Due to the large thermal conductivity of the membrane‐forming platform (stainless steel), collagen/chitosan membranes prepared using apparatus 1 at freezing temperature between ?60 to ?20 °C present similar pore size (2–4 nm) and surface morphology. However, a large difference in pore size is generated using apparatus 2 (membrane preparation in a cold ethanol bath) and using a membrane‐forming platform of poor thermal conductivity (polymethylmethacrylate), e.g. ～10 to 20 μm at freezing temperature of ?60 to ?40 °C, and 265 μm at ?20 °C accompanied with the transformation from fiber‐ to sheet‐dominated morphology. The spongy collagen/chitosan membranes with pore sizes ranging from tens to hundreds of micrometers and porosity higher than 95%, which could be used as dermal regeneration template, have thus been fabricated. Copyright © 2003 John Wiley & Sons, Ltd.     

Sequential injection sample introduction microfluidic-chip based capillary electrophoresis system

A sequential injection micro-sample introduction system was coupled to a microfluidic-chip based capillary electrophoresis system through a split–flow sampling interface integrated on the micro-chip. The microfluidic system measured 20×70×3 mm in dimension, and was produced using a non-lithographic approach with components readily available in the analytical laboratory. In the H-configuration channel design the horizontal separation channel was a 75 μm I.D.×60 mm quartz capillary, with two vertical side arms produced from plastic tubing. The conduits were embedded in silicon elastomer with a planar glass base. Sequential introduction of a series of samples with about 2.5% carryover was achieved at 48 h⁻¹ throughput with samples containing a mixture of fluorescein isothiocyanate (FITC)-labeled amino acids using SI sample volumes of 3.3 μl and carrier flow-rate of 2.0 ml min⁻¹. Baseline separation was achieved for FITC-labeled arginine, phenylalanine, glycine and FITC (laser induced fluorescence detection) in sodium tetraborate buffer (pH 9.2) within 8–80 s, at separation lengths of 25–35 mm and electrical field strengths of 250–1500 V cm⁻¹, with plate heights in the 0.7–3 μm range.     

Indirect fluorescent determination of selected nitro-aromatic and pharmaceutical compounds via UV-photolysis of 2-phenylbenzimidazole-5-sulfonate

An indirect fluorescence (FL) detection method via the reactivity of UV-photolyzed 2-phenylbenzimidazole-5-sulfonate (PBSA) has been developed for non-fluorescent aromatic compounds. At high pH with UV photolysis, PBSA in the excited state is known to be quenched by reaction with oxygen species and analyte compounds that are reactive toward these oxygen species produced during photolysis can lessen the loss of PBSA FL. After off-line photolysis of PBSA in the presence of various nitro-aromatic test compounds, the increase in PBSA FL is clearly evident. A flow injection (FI) instrument using a PBSA mobile phase propelled through a Teflon coil wrapped around a Hg lamp is optimized and modified for use for liquid chromatography (LC). For the on-line FI determination of the non-fluorescent nitro-aromatic compounds such as 4-nitroaniline, 2-nitrophenol, 3-nitrophenol, 4-nitrophenol, and -nitronaphthalene, a positive linear response for PBSA FL from about 0.5 to 15 μM and detection limits generally between 0.2 and 1 μM (4–20 pmol) are found. Linear responses and detection limits of selected pharmaceutical compounds such as the antibacterial nitrofurantoin, antihistamines chlorpheniramine and brompheniramine, and other compounds were similar. In general, detection limits using UV detection at about 214 nm were not as good in the 1–2 μM range but linearity extended up to 100 μM. The amino acid phenylalanine and small peptides containing this aromatic amino acid were also determined using this method. Application of this detection method for the liquid chromatography determination of 4-nitroaniline, 2-nitrophenol, nitrofurantoin, and salicylate is shown.     

Sieve mechanism of microfiltration separation

A theoretical model of dead-end microfiltration (MF) of dilute suspensions is proposed. The model is based on a sieve mechanism of MF and takes into account the probability of membrane pore blocking during MF of dilute colloidal suspensions. An integro-differential equation (IDE) that includes both the membrane pore size and the particle size distributions is deduced. According to the suggested model a similarity property is applicable, which allows one to predict the flux through the membrane as a function of time for any pressure, and dilute concentration, based on one experiment at a single pressure and concentration. The suggested model includes only one fitting parameter, β>1, which takes into account the range of the hydrodynamic influence of a single pore. For a narrow pore size distribution in which one pore diameter predominates (track-etched membranes), the IDE is solved analytically and the derived equation is in good agreement with the measurements on different track-etched membranes. A simple approximate solution of the IDE is derived and that approximate solution, as well as the similarity principal of MF processes, is in good agreement with measurements using a commercial Teflon microfiltration membrane. The theory was further developed to take into account the presence of multiple pores (double, triple and so on pores) on a track-etched membrane surface.

A series of new dead-end filtration experiments are compared with the proposed initial and modified pore blocking models. The challenge suspension used was nearly monodispersed suspension of latex particles of 0.45 μm filtered on a track-etched membrane with similar sized pores 0.4 μm. The filtered suspension concentration ranged from 0.00006 to 0.01% (w/w) and the cross-membrane pressures varied from 1000 to 20,000 Pa. Three stages of microfiltration have been observed. The initial stage is well described by the proposed pore blocking model. The model required only a single parameter that was found to fit all the data under different experimental operational conditions. The second stage corresponds to the transition from the blocking mechanism to the third stage, which is cake filtration. The latter stage occurred after approximately 10–12 particle layers were deposited (mass = 0.006 g) on the surface of the microfiltration membrane.     

Donor–acceptor interaction of fullerene C60 with triptycene in molecular complex TPC·C60

A molecular complex of fullerene C₆₀ with triptycene, TPC·C₆₀ is obtained. The complex has a three-dimensional packing of C₆₀ molecules. According to the IR spectra, the freezing of free rotation of C₆₀ molecules in the complex is maintained up to 360 K. The XP-spectra of TPC·C₆₀ show the suppression of π–π^* transitions of TPC phenylene rings. The separation of C₆₀ molecules by TPC ones in TPC·C₆₀ results in low intensity of the C₆₀ transitions in the 420–500 nm range in an optical spectrum. This absorption is assumed as that attributed to intermolecular transitions between adjacent C₆₀ molecules.     

A three mechanism model to describe fouling of microfiltration membranes

Mathematical modeling of flux decline during filtration plays an important role in both sizing membrane systems and in the understanding of membrane fouling. Protein fouling is traditionally modeled using one of three classical fouling mechanisms: pore blockage, pore constriction or cake filtration. Here, we have developed a mathematical model to describe flux decline behavior during microfiltration accounting for all three classical fouling mechanisms. Pore constriction was assumed to first reduce the size of internal pores. Pore blockage then occurs at the top of the membrane, preventing further fouling to the interior structure. Finally the foulants at the top of the membrane form a cake, which controls the late stages of the filtration. The model prediction shows excellent agreement with experimental data for 0.25 μm polystyrene microspheres filtered through 0.22 μm Isopore membranes (where pore constriction is expected to be minimal) as well as non-aggregated bovine serum albumin solution through hydrophobic Durapore membranes (where pore constriction is expected to dominate). The effects of different fouling mechanisms on the flux decline were characterized by the ratio of characteristic fouling times of the different mechanisms. In this way the model can provide additional insights into the relative importance of different fouling mechanisms as compared to an analysis by a single mechanism model or by derivative plots, and it can be used to provide important insights into the flux decline characteristics.