High-resolution separation of neodymium and dysprosium ions utilizing extractant-impregnated graft-type particles.

An efficient method for rare metal recovery from environmental water and urban mines is in high demand. Toward rapid and high-resolution rare metal ion separation, a novel bis(2-ethylhexyl) phosphate (HDEHP)-impregnated graft-type particle as a filler for a chromatography column is proposed. To achieve rapid and high-resolution separation, a convection-flow-aided elution mode is required. The combination of 35 µm non-porous particles and a polymer-brush-rich particle structure minimizes the distance from metal ion binding sites to the convection flow in the column, resulting in minimized diffusional mass transfer resistance and the convection-flow-aided elution mode. The HDEHP-impregnated graft-type non-porous-particle-packed cartridge developed in this study exhibited a higher separation performance for model rare metals, neodymium (III) and dysprosium (III) ions, and a narrower peak at a higher linear velocity, than those of previous HDEHP-impregnated fiber-packed and commercially available Lewatit® VP OC 1026-packed cartridges.

High-throughput solid-phase extraction of metal ions using an iminodiacetate chelating porous disk prepared by graft polymerization.

A chelating porous sheet for use in solid-phase extraction was prepared by radiation-induced graft polymerization and subsequent chemical modifications. An epoxy-group-containing vinyl monomer was graft-polymerized onto a porous sheet made of polyethylene. The produced epoxy group of the graft chain was converted into an iminodiacetate group. The chelating porous sheet with a density of the iminodiacetate group of 2.1 mol/kg was cut into disks 13 mm in diameter to fit an empty cylindrical cartridge with a capacity of 6 mL. Breakthrough curves using the chelating-porous-disk-packed cartridge overlapped irrespective of the flow rate of the solution ranging up to 1500 mL/h because of negligible diffusional mass-transfer resistance of the copper ions to the iminodiacetate group of the graft chain.

Protein binding to amphoteric polymer brushes grafted onto a porous hollow-fiber membrane.

Three kinds of ampholites, i.e., 3-aminopropionic acid (NH2C2H4COOH), (2-aminoethyl)phosphonic acid (NH2C2H4PO3H2), and 2-aminoethane-1-sulfonic acid (NH2C2H4SO3H), were introduced into an epoxy group-containing polymer brush grafted onto a porous hollow-fiber membrane with a porosity of 70% and pore size of 0.36 microm. The amphoteric group density of the hollow-fiber ranged from 0.50 to 0.72 mmol/g. Three kinds of proteins, i.e., lactoferrin (Lf), cytochrome c (Cyt c), and lysozyme (Ly), were captured by the amphoteric polymer brush during the permeation of the protein solution across the ampholite-immobilized porous hollow-fiber membrane. Multilayer binding of the protein to the amphoteric polymer brush, with a degree of multilayer binding of 3.3, 8.6, and 15 for Lf, Cyt c, and Ly, respectively, with the (2-aminoethyl)phosphonic acid-immobilized porous hollow-fiber membrane, was demonstrated with a negligible diffusional mass-transfer resistance of the protein to the ampholite immobilized. The 2-aminoethane-1-sulfonic acid-immobilized porous hollow-fiber membrane exhibited the lowest initial flux of the protein solution, 0.41 m/h at a transmembrane pressure of 0.1 MPa and 298 K, and the highest equilibrium binding capacity of the protein, e.g., 130 mg/g for lysozyme. Extension and shrinkage of the amphoteric polymer brushes were observed during the binding and elution of the proteins.

Preparation of an extractant-impregnated porous membrane for the high-speed separation of a metal ion.

A novel impregnation method of extractants into a porous polymeric support is described. Bis(2-ethylhexyl)phosphate (HDEHP) was impregnated onto an n-octadecylamino group of the polymer chain grafted onto the pore surface of a porous hollow-fiber membrane. First, an epoxy-group-containing polymer chain was appended onto the porous membrane by radiation-induced graft polymerization of glycidyl methacrylate (GMA). Second, n-octadecylamine was added to the graft chain via an epoxy-ring opening reaction to yield a hydrophobic group density of 3.0 mmol/g of the GMA-grafted fiber. Finally, HDEHP was impregnated to the n-octadecylamino group. The amount of impregnated HDEHP of 2.1 mmol/g of the GMA-grafted fiber was attained while retaining the liquid permeability of the porous membrane. An yttrium solution was forced to permeate through the pores of the HDEHP-impregnated porous hollow-fiber membrane. The higher permeation rate of the yttrium solution led to the higher adsorption rate of yttrium because of a negligible diffusional mass-transfer resistance. In addition, a high stability of impregnated HDEHP was observed after the repeated use of adsorption with 50 mg-Y/L yttrium solution and elution with 7 M nitric acid.

High-performance purification of gelsolin from plasma using anion-exchange porous hollow-fiber membrane.

Gelsolin was purified from bovine plasma using an anion-exchange porous hollow-fiber membrane. The anion-change porous hollow-fiber membrane was prepared by radiation-induced graft polymerization of an epoxy-group-containing monomer, glycidyl methacrylate, and subsequent chemical modifications. Some of the epoxy groups of the polymer chain grafted onto the pore surface were converted into diethylamino groups, and the remaining epoxy groups were converted into 2-hydroxyethylamino groups. First, a gelsolin-containing dialyzed protein solution, prepared by pretreatments of ammonium sulfate precipitation and dialysis of plasma, was forced to permeate through the pores of an anion-exchange porous hollow-fiber membrane. Various proteins including gelsolin were adsorbed onto the anion-exchange polymer brush at a high rate with negligible diffusional mass-transfer resistance. Second, adsorbed gelsolin was specifically eluted by permeating 2mM calcium chloride. The amount of recovered gelsolin was 0.1 mg per 1 mL of plasma. Third, the remaining adsorbed proteins were quantitatively eluted with 1M sodium chloride, leading to a constant amount of recovered gelsolin during four cycles of purification. The total time required for gelsolin purification from 30 mL of bovine plasma was 11h, during which the time for selective adsorption of various proteins and affinity elution of gelsolin using the anion-exchange porous hollow-fiber membrane was 20 min.

Production of tripeptide from gelatin using collagenase-immobilized porous hollow-fiber membrane.

Tripeptide was produced during the permeation of a gelatin solution through the pore of a collagenase-immobilized porous hollow-fiber membrane. Gelatin was obtained via hydrolysis of fish collagen. First, an epoxy-group-containing monomer was graft-polymerized onto an electron-beam-irradiated porous hollow-fiber membrane. Second, the 2-hydroxyethylamino group was introduced into the epoxy group to bind collagenase on the basis of electrostatic interaction. Third, adsorbed collagenase was cross-linked with glutaraldehyde to prevent leakage of the enzyme. Gelatin solution (10-50 g/L) was forced to permeate across the collagenase-immobilized porous hollow-fiber membrane with a density of immobilized collagenase of 52 mg/g at various residence times of the gelatin solution ranging from 0.13 to 20 min. Fourteen percent in weight of 10 g/L gelatin solution was hydrolyzed into tripeptide at a residence time of 20 min.

Highly multilayered urease decomposes highly concentrated urea.

Urease was immobilized at a density of 1.2 g of urease per gram of a matrix via ion-exchange binding of urease to an anion-exchange polymer chain grafted onto a pore surface of a porous hollow-fiber membrane and subsequent cross-linking of urease with transglutaminase. Urea was hydrolyzed during the permeation of a urea solution, the concentration of which ranged from 2 to 8 M, through the pores of the resultant membrane with a thickness of approximately 1 mm. Quantitative hydrolysis of 4 M urea was achieved at a permeation rate lower than 1 mL/h, i.e., a residence time longer than 5.1 min, at ambient temperature. This performance is ascribed to convective transport of urea through the pores rimmed by the urease-immobilized polymer chains at a high density. Urease was denatured in the presence of urea at concentrations higher than 6 M while hydrolyzing urea.

Production of cycloisomaltooligosaccharides from dextran using enzyme immobilized in multilayers onto porous membranes.

Anion-exchange porous hollow-fiber membranes with a thickness of about 1.2 mm and a pore size of about 0.30 microm were used as a supporting matrix to immobilize cycloisomaltooligosaccharide glucanotransferase (CITase). CITase was immobilized to the membrane via anion-exchange adsorption and by subsequent enzymatic cross-linking with transglutaminase, the amount of which ranged from 3 to 110 mg per gram of the membrane. The degree of enzyme multilayer binding was equivalent to 0.3-9.8. Dextran, as the substrate, was converted into seven- to nine-glucose-membered cycloisomaltooligosaccharides (CI-7, -8, and -9) at a maximum yield of 28% in weight at a space velocity of 10 per hour during the permeation of 2.0% (w/w) dextran solution across the CITase-immobilized porous hollow-fiber membrane. The yield of CIs increased with increasing degree of CITase multilayering.

Convection-aided collection of metal ions using chelating porous flat-sheet membranes.

Chelating porous membranes were prepared by radiation-induced graft polymerization of an epoxy-group-containing monomer onto a polyethylene flat sheet and subsequent conversion of the epoxy group to an iminodiacetate group as a chelate-forming group. The chelating group density on the resultant porous flat-sheet membrane of 1.0 mol/kg was comparable to that of commercially available chelating beads. The pure water permeability of the membrane was 40% that of the trunk porous membrane, which was used for microfiltration. During the permeation of a copper chloride solution through the membrane, diffusional mass-transfer resistance of copper ion was negligible, since the ion was transported by convective flow through the pore. The tensile strength and elongation at break of the membranes were measured as a function of dose of electron-beam irradiation, the degree of grafting, and the chelating group density to determine an applicable range for practical use.

Binding of ionic surfactants to charged polymer brushes grafted onto porous substrates.

A polymer brush containing a sulfonic acid group was appended onto the pore surface of a porous hollow-fiber membrane about 1 mm thick. During the permeation of a N-alkylpyridinium chloride (CnPyCl; n=4, 12, and 16) solution, the feed concentration of which ranged from 0.10 to 500 mM, through the pores at a constant transmembrane pressure of 0.2 MPa, C12PyCl was bound to the charged polymer brush. Prepermeation of a magnesium chloride solution through the pores was effective in regaining the liquid permeability via ionic crosslinking of the charged groups with the magnesium ion at a degree of crosslinking of 54%. The charged polymer brush captured C12PyCl without releasing the magnesium ion. At a surfactant concentration of about 70% of its critical micelle concentration, the equilibrium binding capacity of the charged polymer brush started to decrease due to micelle formation. In contrast, C4PyCl and PyCl without micelle formation increased the equilibrium binding capacity with increasing concentration while expelling the magnesium ion.

Solvent effect on protein binding by polymer brush grafted onto porous membranes.

An epoxy-group-containing polymer chain was grafted onto the hollow-fiber form of a porous polyethylene membrane by the immersion of the electron beam-irradiated trunk polymer in glycidyl methacrylate diluted with methanol and 1-butanol. The epoxy group density ranged from 8.5 to 13.4 mol per kg of the trunk polymer. Subsequently, the epoxy groups produced were converted into sulfonic acid and diethylamino groups. The density of -SOH and -N(C2H5), groups was 0.40 and 2.2 mol per kg of the product. respectively. The polymer brush, defined as a polymer chain extending from the surface of a pore toward the interior of the pore, was evaluated from the determination of an equilibrium binding capacity of hen egg lysozyme (HEL) and bovine serum albumin (BSA). The polymer brush prepared in 1-butanol was found to be longer than that prepared in methanol from the determinations of liquid permeability and protein adsorptivity. The proteins were bound to the polymer brush prepared in 1-butanol, followed by the functionalization, at higher degrees of multilayer binding: about 30 for HEL and 6 for BSA.

Conversion of dextran to cycloisomaltooligosaccharides using an enzyme-immobilized porous hollow-fiber membrane.

This paper describes a cycloisomaltooligosaccharide glucanotransferase (CITase)-multilayer-immobilized porous hollow-fiber membrane used as an enzyme bioreactor. Dextran, a substrate with an average molecular mass of 43000, is converted into seven- to nine-glucose-membered cycloisomaltooligosaccharides, effective as a preventive for dental caries, aided by convective transport of the substrate to the vicinity of the enzyme through the pores. Epoxy-group-containing graft chains were uniformly appended onto the surface of pores throughout a porous hollow-fiber membrane by radiation-induced graft polymerization. Subsequently, a diethylamino group was introduced, as an anion-exchange moiety, to the graft chains, which caused the chains to expand toward the interior of the pores due to mutual electrostatic repulsion. The expanding graft chain provided multilayer binding sites for CITase. Fifty-five milligrams of adsorbed CITase per gram of membrane is equivalent to the degree of multilayer binding of 5. Finally, 80% of the multilayer-adsorbed CITase was immobilized via enzymatic cross-linking with transglutaminase to prevent the leakage of enzymes. CITase, with a degree of multilayer immobilization of 4, produced the target cycloisomaltooligosaccharides at a conversion yield of 55% in weight at 310 K during permeation by the dextran solution at a space velocity defined as the permeation rate divided by membrane volume of 6 per hour.