Demonstration of a strategy for product purification by high-gradient magnetic fishing: recovery of superoxide dismutase from unconditioned whey

A systematic approach for the design of a bioproduct recovery process employing magnetic supports and the technique of high-gradient magnetic fishing (HGMF) is described. The approach is illustrated for the separation of superoxide dismutase (SOD), an antioxidant protein present in low concentrations (ca. 0.15-0.6 mg L(-1)) in whey. The first part of the process design consisted of ligand screening in which metal chelate supports charged with copper(II) ions were found to be the most suitable. The second stage involved systematic and sequential optimization of conditions for the following steps: product adsorption, support washing, and product elution. Next, the capacity of a novel high-gradient magnetic separator (designed for biotechnological applications) for trapping and holding magnetic supports was determined. Finally, all of the above elements were assembled to deliver a HGMF process for the isolation of SOD from crude sweet whey, which consisted of (i) binding SOD using Cu2+ -charged magnetic metal chelator particles in a batch reactor with whey; (ii) recovery of the "SOD-loaded" supports by high-gradient magnetic separation (HGMS); (iii) washing out loosely bound and entrained proteins and solids; (iv) elution of the target protein; and (v) recovery of the eluted supports from the HGMF rig. Efficient recovery of SOD was demonstrated at approximately 50-fold increased scale (cf magnetic rack studies) in three separate HGMF experiments, and in the best of these (run 3) an SOD yield of >85% and purification factor of approximately 21 were obtained.     

Purification of equine chorionic gonadotropin (eCG) using magnetic ion exchange adsorbents in combination with high‐gradient magnetic separation

Current purification of the glycoprotein equine chorionic gonadotropin (eCG) from horse serum includes consecutive precipitation steps beginning with metaphosphoric acid pH fractionation, two ethanol precipitation steps, and dialysis followed by a numerous of fixed‐bed chromatography steps up to the specific activity required. A promising procedure for a more economic purification procedure represents a simplified precipitation process requiring only onethird of the solvent, followed by the usage of magnetic ion exchange adsorbents employed together with a newly designed ‘rotor‐stator’ type High Gradient Magnetic Fishing (HGMF) system for large‐scale application, currently up to 100 g of magnetic adsorbents. Initially, the separation process design was optimized for binding and elution conditions for the target protein in mL scale. Subsequently, the magnetic filter for particle separation was characterized. Based on these results, a purification process for eCG was designed consisting of (i) pretreatment of the horse serum; (ii) binding of the target protein to magnetic ion exchange adsorbents in a batch reactor; (iii) recovery of loaded functionalized adsorbents from the pretreated solution using HGMF; (iv) washing of loaded adsorbents to remove unbound proteins; (v) elution of the target protein. Finally, the complete HGMF process was automated and conducted with either multiple single‐cycles or multicycle operation of four sequential cycles, using batches of pretreated serum of up to 20 L. eCG purification with yields of approximately 53% from single HGMF cycles and up to 80% from multicycle experiments were reached, with purification and concentration factors of around 2,500 and 6.7, respectively. © 2014 American Institute of Chemical Engineers Biotechnol. Prog., 31:78–89, 2015     

Lumped parameter model for prediction of initial breakthrough profiles for the chromatographic capture of antibodies from a complex feedstock

A simple mathematical model to predict initial breakthrough profiles from preparative chromatographic separations of biological macromolecules has been developed. A lumped parameter approach was applied, employing Langmuirian adsorption kinetics to describe the rate of mass transfer (MT) from the bulk liquid in the column to the bound state. Equilibrium and kinetic adsorption data were determined for six different packed bed chromatographic adsorbents: two derivatised with rProtein A; and four functionalised with synthetic low molecular weight ligands. All adsorption isotherms were well described by the Langmuir model, whereas the data fitting to kinetic batch experiments showed that the model was inadequate after the first approximately 25 min of adsorption for four of the six adsorbents. The model underestimated the dynamic Ig breakthough on packed beds of rProtein A Sepharose FF, MabSelect, MBI HyperCel, and MabSorbent A1P, applying a feedstock of 20-100% (v/v) clarified rabbit antiserum. However, when employing a maximum adsorption capacity 25% greater than that determined in batch binding studies, excellent agreement was obtained at all antiserum strengths for most adsorbents. Useful insights into scale-up and process design can be obtained by applying the model, without determining tentative parameters specific for each adsorbent and target protein concentration. However, the model parameters are solvent dependent so a prerequisite for its true applicability is that binding is both Langmuirian and essentially independent of the ionic strength of the feedstock applied.     

High-gradient magnetic affinity separation of trypsin from porcine pancreatin

We introduce a robust and scale-flexible approach to macromolecule purification employing tailor-made magnetic adsorbents and high-gradient magnetic separation technology adapted from the mineral processing industries. Detailed procedures for the synthesis of large quantities of low-cost defined submicron-sized magnetic supports are presented. These support materials exhibit unique features, which facilitate their large-scale processing using high magnetic field gradients, namely sufficiently high magnetization, a relatively narrow particle size distribution and ideal superparamagnetism. Following systematic optimization with respect to activation chemistry, spacer length and ligand density, conditions for preparation of effective high capacity (Q(max) = 120 mg g(-1)) strongly interacting (Kd < 0.3 microm) trypsin-binding adsorbents based on immobilized benzamidine were established. In small-scale studies approximately 95% of the endogenous trypsin present in a crude porcine pancreatin feedstock was recovered with a purification factor of approximately 4.1 at the expense of only a 4% loss in alpha-amylase activity. Efficient recovery of trypsin from the same feedstock was demonstrated at a vastly increased scale using a high-gradient magnetic separation system to capture loaded benzamidine-linked adsorbents following batch adsorption. With the aid of a simple recycle loop over 80% of the initially adsorbed trypsin was recovered in-line with an overall purification factor of approximately 3.5.     

Multi‐cycle recovery of lactoferrin and lactoperoxidase from crude whey using fimbriated high‐capacity magnetic cation exchangers and a novel “rotor–stator” high‐gradient magnetic separator

Cerium (IV) initiated “graft‐from” polymerization reactions were employed to convert M‐PVA magnetic particles into polyacrylic acid‐fimbriated magnetic cation exchange supports displaying ultra‐high binding capacity for basic target proteins. The modifications, which were performed at 25 mg and 2.5 g scales, delivered maximum binding capacities (Q_max) for hen egg white lysozyme in excess of 320 mg g^?1, combined with sub‐micromolar dissociation constants (0.45–0.69 µm) and “tightness of binding” values greater than 49 L g^?1. Two batches of polyacrylic acid‐fimbriated magnetic cation exchangers were combined to form a 5 g pooled batch exhibiting Q_max values for lysozyme, lactoferrin, and lactoperoxidase of 404, 585, and 685 mg g^?1, respectively. These magnetic cation exchangers were subsequently employed together with a newly designed “rotor–stator” type HGMF rig, in five sequential cycles of recovery of lactoferrin and lactoperoxidase from 2 L batches of a crude sweet bovine whey feedstock. Lactoferrin purification performance was observed to remain relatively constant from one HGMF cycle to the next over the five operating cycles, with yields between 40% and 49% combined with purification and concentration factors of 37‐ to 46‐fold and 1.3‐ to 1.6‐fold, respectively. The far superior multi‐cycle HGMF performance seen here compared to that observed in our earlier studies can be directly attributed to the combined use of improved high capacity adsorbents and superior particle resuspension afforded by the new “rotor–stator” HGMS design. Biotechnol. Bioeng. 2013; 110: 1714–1725. © 2013 Wiley Periodicals, Inc.     

A new metal chelate affinity adsorbent for cytochrome C

We have prepared a novel metal-chelate adsorbent utilizing N-methacryloyl-L-histidine methyl ester (MAH) as a metal-chelating ligand. MAH was synthesized by using methacryloyl chloride and l-histidine methyl ester dihydrochloride. Spherical beads with an average diameter of 75-125 microm were produced by suspension polymerization of 2-hydroxyethyl methacrylate (HEMA) and MAH carried out in an aqueous dispersion medium. Then, Cu(2+) ions were chelated directly on the chelating beads. Cu(2+)-chelated beads were used in the adsorption of cytochrome c (cyt c) from aqueous solutions. The maximum cyt c adsorption capacity of the Cu(2+)-chelated beads (658.2 micromol/g Cu(2+) loading) was found to be 31.7 mg/g at pH 10 in phosphate buffer. The nonspecific cyt c adsorption on the naked PHEMA beads was 0.2 mg/g. Cyt c adsorption increased with increasing Cu(2+) loading. Cyt c adsorption capacity was demonstrated for the buffer types with the effects in the order phosphate > HEPES > MOPS > MES > Tris-HCl. Cyt c molecules could be adsorbed and desorbed five times with these adsorbents without noticeable loss in their cyt c adsorption capacity.     

Use of high-gradient magnetic fishing for reducing proteolysis during fermentation

Proteolysis during fermentation may have a severe impact on the yield and quality of a secreted product. In the current study, we demonstrate the use of high-gradient magnetic fishing (HGMF) as an efficient alternative to the more conventional methods of preventing proteolytic degradation. Bacitracin-linked magnetic affinity adsorbents were employed directly in a fermenter during Bacillus licheniformis cultivation to remove trace amounts of unwanted proteases. The constructed magnetic adsorbents had excellent, highly specific binding characteristics in the fermentation broth (K(d) = 1.94 micromolar; Q(max) = 222.8 mg/g), which obeyed the Langmuir isotherm and had rapid binding kinetics (equilibrium in <300 s). When applied directly in shake-flask cultures or in a 1-L fermenter and then removed by HGMF, the degradation of the model protein bovine serum albumin was stopped. The adsorbents could be recycled and reused during the same fermentation to remove freshly produced proteases, extending the life of the model protein in the fermenter. HGMF may provide an efficient method of stabilizing heterologous proteins produced in cultivation processes.     

High gradient magnetic separation versus expanded bed adsorption: a first principle comparison

A robust new adsorptive separation technique specifically designed for direct product capture from crude bioprocess feedstreams is introduced and compared with the current bench mark technique, expanded bed adsorption. The method employs product adsorption onto sub-micron sized non-porous superparamagnetic supports followed by rapid separation of the loaded adsorbents from the feedstock using high gradient magnetic separation technology. For the recovery of Savinase® from a cell-free Bacillus clausii fermentation liquor using bacitracin-linked adsorbents, the integrated magnetic separation system exhibited substantially enhanced productivity over expanded bed adsorption when operated at processing velocities greater than 48 m h^–1. Use of the bacitracin-linked magnetic supports for a single cycle of batch adsorption and subsequent capture by high gradient magnetic separation at a processing rate of 12 m h^–1 resulted in a 2.2-fold higher productivity relative to expanded bed adsorption, while an increase in adsorbent collection rate to 72 m h^–1 raised the productivity to 10.7 times that of expanded bed adsorption. When the number of batch adsorption cycles was then increased to three, significant drops in both magnetic adsorbent consumption (3.6 fold) and filter volume required (1.3 fold) could be achieved at the expense of a reduction in productivity from 10.7 to 4.4 times that of expanded bed adsorption.     

Comparison of the binding behavior of several histidine-containing proteins with immobilized copper(II) complexes of 1,4,7-triazacyclononane and 1,4-bis(1,4,7-triazacyclononan-1-yl)butane

The protein binding characteristics of the immobilized binucleating chelate system, 1,4-bis(1,4,7-triazacyclononan-1-yl)butane (tacn(2)butane), complexed with Cu(2+) ions have been investigated with hen egg white lysozyme, horse skeletal muscle myoglobin and horse heart cytochrome C, as well as three histidine-rich proteins, serum albumin, transferrin, and α(2)-macroglobulin, present in partially fractionated human serum. The effects of pH, ionic strength and elution buffers on protein binding have been examined and compared with those of the analogous immobilized mononuclear copper complex of 1,4,7-triazacyclononane (tacn). The Cu(2+)-tacn(2)butane system was generally found to exhibit higher protein binding affinities than the Cu(2+)-tacn system, suggesting that the presence of immobilized binuclear copper(II) species leads to enhanced coordinative interaction with surface-exposed amino acid residues of the studied proteins. However, under some buffer conditions the dependencies of protein binding and elution on pH and ionic strength with these immobilized metal ion affinity chromatographic (IMAC) systems were consistent with electrostatic, hydrophobic and π-bonding interactions playing a significant secondary role in addition to the dominant coordinative interactions. As such, the results indicated that the selectivities were not solely dependent on the histidine content of the protein. In accord with this conclusion, differences in the selectivities of the Cu(2+)-tacn and Cu(2+)-tacn(2)butane adsorbents for serum albumin, transferrin, and α(2)-macroglobulin were observed depending on the choice of elution buffer. This attribute suggests that additional selectivity features can be realised for the separation of specific proteins with this new class of adsorbent.     

Optimization of affinity and ion-exchange chromatographic processes for the purification of proteins

This study documents several alternative approaches for the optimization of the ion-exchange and affinity chromatographic purification of proteins. In these approaches, the chromatographic process has been treated as a four-stage (adsorption, washing, elution, and regeneration) operation. Central to these investigations has been the elaboration of practical iterative procedures based on the use of theoretical models describing each of these stages. Predictions derived from these models have then been evaluated in terms of experimental data obtained using batch adsorption measurements in finite bath configurations and frontal breakthrough measurements with packed beds of different dimensions, containing nonporous and porous adsorbents of different selectivities and capacities for proteins. Commencing with the kinetic and distribution parameters derived from batch equilibrium measurements, the effect of the initial concentration of the target protein, the solid-liquid volume ratio, the superficial velocity and the column dimensions on the pressure drop, production rate, concentration profile, column utilization, and yield have been determined with packed beds. The potential of these iterative approaches to simplify the determination of key mass transfer and interaction parameters required for scale-up and economic optimization of chromatographic purifications of proteins has been examined using ion exchange, immobilized metal ion affinity, and triazine dye pseudo-affinity adsorbents of different selectivity and adsorption capacities. (c) 1996 John Wiley & Sons, Inc.     

Designing chitosan based magnetic beads with conocarpus waste-derived biochar for efficient sulfathiazole removal from contaminated water

The development of a simple method to synthesize highly efficient and stable magnetic microsphere beads for sulfathiazole (STZ) removal from contaminated aqueous media was demonstrated in this study. Conocarpus (Conocarpus erectus L.) tree waste (CW) derived biochar (BC) was modified to fabricate chitosan-BC (CBC) and magnetic CBC (CBC-Fe) microsphere beads. Proximate, chemical, and structural properties of the produced adsorbents were investigated. Kinetics, equilibrium, and pH adsorption batch trials were conducted to evaluate the effectiveness of the synthesized adsorbents for STZ removal. All adsorbents exhibited the highest STZ adsorption at pH 5.0. STZ adsorption kinetics data was best emulated using pseudo-second order and Elovich models. The equilibrium adsorption data was best emulated using Langmuir, Freundlich, Redlich–Peterson, and Temkin models. CBC-Fe demonstrated the highest Elovich, pseudo-second order, and power function rate constants, as well as the highest apparent diffusion rate constant. Additionally, Langmuir isotherm predicted maximum adsorption capacity was the highest for CBC-Fe (98.67 mg g⁻¹), followed by CBC (56.54 mg g⁻¹) and BC (48.63 mg g⁻¹). CBC-Fe and CBC removed 74.5%–108.8% and 16.2%–25.6% more STZ, respectively, than that of pristine BC. π-π electron-donor–acceptor interactions and Lewis acid-base reactions were the main mechanisms for STZ removal; however, intraparticle diffusion and H-bonding further contributed in the adsorption process. The higher efficiency of CBC-Fe for STZ adsorption could be due to its magnetic properties as well as stronger and conducting microsphere beads, which degraded the STZ molecules through generation of HO^• radicals.     

Purification of penicillin G acylase using immobilized metal affinity membranes

The immobilized metal affinity membrane (IMAM) with modified regeneration cellulose was employed for purification of penicillin G acylase (PGA). For studying PGA adsorption capacity on the IMAM, factors such as chelator surface density, chelating metal, loading temperature, pH, NaCl concentration and elution solutions were investigated. The optimal loading conditions were found at 4 degrees C, 0.5 M NaCl, 32.04 micromol Cu(2+) per disk with 10 mM sodium phosphate buffer, pH 8.5, whereas elution conditions were: 1 M NH(4)Cl with 10 mM sodium phosphate buffer, pH 6.8. By applying these chromatographic conditions to the flow experiments in a cartridge, a 9.11-fold purification in specific activity with 90.25% recovery for PGA purification was obtained. Meanwhile, more than eight-times reusability of the membrane was achieved with the EDTA regeneration solutions.     

Purification of recombinant enhanced green fluorescent protein expressed in Escherichia coli with new immobilized metal ion affinity magnetic absorbents

A new immobilized metal ion affinity (IMA) adsorbent containing superparamagnetic nanoparticles and coated with hydrophilic resins are proposed here to improve the purification of His-tagged proteins. The magnetic chelating resin was prepared by radical polymerization of magnetite (Fe3O4), styrene, divinyl benzene (DVB) and glycidyl methacrylate-iminodiacetic acid (GMA-IDA) in ethanol/water medium. IDA is immobilized on magnetite as a ligand and pre-charged Cu2+, Zn2+ and Ni2+ as metal ions. To identify the GMA-IDA magnetic particles easily, we named these particles MPGI. The MPGI adsorbent was used to test their suitability for the direct recovery of an intracellular, polyhistidine-tagged protein, enhanced green fluorescent protein [EGFP-(His)(6)], from Escherichia coli lysates in a single step. Parameters influencing the purification efficiencies such as pH, ionic strength and imidazole concentration were optimized to achieve improved separation. The optimal selectively was observed in binding buffer (0.2M NaCl, 0.02M imidazole), washing buffer (0.4M NaCl, 0.03 M imidazole) and elution buffer (0.50M imidazole). The Cu2+-charged MPGI adsorbent had the highest yield and purification factor at 70.4% and 12.3, respectively. The calculated isotherm parameters (Q(m)=53.5 mg/g, K(d)=5.84 mg/mL and Q(m)/K(d)=9.2 mL/g) indicated that the MPGI adsorbent could be used as a suitable adsorbent for EGFP from an aqueous solution.     

Comparison of two matrices for selective recovery of C595 diabody fragment (dbFv) from Escherichia coli lysates

A comparative study of the performance of two types of adsorbent (Streamline Quartz Base and Upfront Matrices), derivatized with the same affinity ligand (RPAP) to recover C595 diabody fragment (dbFv) from Escherichia coli lysates has been undertaken. Both streamline and Upfront Matrices are characterized by a particle size range of 100–300 μm. Streamline has a density of 1.20 g cm⁻³ and ligand concentration of 0.85 μmol ml⁻¹. Upfront has a density of 1.35 g cm⁻³ and ligand concentration of 0.83 μmol ml⁻¹. The release of C595 dbFv from E. coli cells was achieved by a chemical lysis method. The recovery performance of both adsorbents was evaluated in terms of operational productivity and elution yield of C595 dbFv in packed bed (clarified feedstock) and expanded bed (unclarified and clarified feedstock) chromatography systems. Streamline and Upfront adsorbents exhibited diabody operational productivities of 131 and 202 mg l⁻¹, respectively, with an elution yield of 92 and 94%, respectively, in packed bed operation. Streamline and Upfront adsorbents exhibited diabody operational productivities of 54.5 and 123.7 mg l⁻¹, respectively, with an elution yield of 89 and 92%, respectively, in expanded bed operation.     

Copper and zinc binding modulates the aggregation and neurotoxic properties of the prion peptide PrP106-126.

The abnormal form of the prion protein (PrP) is believed to be responsible for the transmissible spongiform encephalopathies. A peptide encompassing residues 106-126 of human PrP (PrP106-126) is neurotoxic in vitro due its adoption of an amyloidogenic fibril structure. The Alzheimer's disease amyloid beta peptide (Abeta) also undergoes fibrillogenesis to become neurotoxic. Abeta aggregation and toxicity is highly sensitive to copper, zinc, or iron ions. We show that PrP106-126 aggregation, as assessed by turbidometry, is abolished in Chelex-100-treated buffer. ICP-MS analysis showed that the Chelex-100 treatment had reduced Cu(2+) and Zn(2+) levels approximately 3-fold. Restoring Cu(2+) and Zn(2+) to their original levels restored aggregation. Circular dichroism showed that the Chelex-100 treatment reduced the aggregated beta-sheet content of the peptide. Electron paramagnetic resonance spectroscopy identified a 2N1S1O coordination to the Cu(2+) atom, suggesting histidine 111 and methionine 109 or 112 are involved. Nuclear magnetic resonance confirmed Cu(2+) and Zn(2+) binding to His-111 and weaker binding to Met-112. An N-terminally acetylated PrP106-126 peptide did not bind Cu(2+), implicating the free amino group in metal binding. Mutagenesis of either His-111, Met-109, or Met-112 abolished PrP106-126 neurotoxicity and its ability to form fibrils. Therefore, Cu(2+) and/or Zn(2+) binding is critical for PrP106-126 aggregation and neurotoxicity.     

Evaluation of a silica-coated magnetic nanoparticle for the immobilization of a His-tagged lipase

Magnetic particles of size 10 nm have been coated with silica to a mean diameter of 40 nm and charged with Cu²⁺ ions via a multidentate ligand, iminodiacetic acid (IDA), for the immobilization of His-tagged Bacillus stearothermopilus L1 lipase. Microporous (average pore diameter of 60 Å) silica gel with a mean particle diameter of 115 µm has been used as a comparative support material. The molar ratio of Cu²⁺ to IDA was found to be 1:1.14 and 1:1.99 in the silica gel and the silica-coated magnetic nanoparticles (SiMNs), respectively. The specific activity of the immobilized enzyme was found to conform to the following order: Cu²⁺-charged SiMN>SiMN>Cu²⁺-charged silica gel>silica gel. When it was immobilized on the Cu²⁺-charged SiMNs, over 70% of the initial activity of the lipase remained after it had been reused five times. However, only 20% of the initial activity remained after the enzyme immobilized on the Cu²⁺-charged silica gel had been reused five times. For the enzyme immobilized on supports without Cu²⁺ cations, all activity was lost after threefold reuse. The differences in the specific activities and the efficiencies of reuse of the enzymes immobilized on the various support materials are discussed in terms of immobilization mechanisms (physical adsorption vs. coordination bonding), mass transfer of a substrate and a product of the enzyme reaction, and the status of the Cu (Cu bound to the IDA on the silica layer vs. Cu directly adsorbed on the silica layer).     

Gum Arabic coated magnetic nanoparticles with affinity ligands specific for antibodies

A novel magnetic support based on gum Arabic (GA) coated iron oxide magnetic nanoparticles (MNP) has been endowed with affinity properties towards immunoglobulin G (IgG) molecules. The success of the in situ triazine ligand synthesis was confirmed by fluorescence assays. Two synthetic ligands previously developed for binding to IgG, named as ligand 22/8 (artificial Protein A) and ligand 8/7 (artificial Protein L) were immobilized on to MNPs coated with GA (MNP_GA). The dimension of the particles core was not affected by the surface functionalization with GA and triazine ligands. The hydrodynamic diameters of the magnetic supports indicate that the coupling of GA leads to the formation of larger agglomerates of particles with about 1 µm, but the introduction of the triazine ligands leads to a decrease on MNPs size. The non‐functionalized MNP_GA bound 28 mg IgG/g, two times less than bare MNP (60 mg IgG/g). MNP_GA modified with ligand 22/8 bound 133 mg IgG/g support, twice higher than the value obtained for ligand 8/7 magnetic adsorbents (65 mg/g). Supports modified with ligand 22/8 were selected to study the adsorption and the elution of IgG. The adsorption of human IgG on this support followed a Langmuir behavior with a Q_máx of 344 mg IgG/g support and K_a of 1.5 × 10⁵ M. The studies on different elution conditions indicated that although the 0.05 M citrate buffer (pH 3) presented good recovery yields (elution 64% of bound protein), there was occurrence of iron leaching at this acidic pH. Therefore, a potential alternative would be to elute bound protein with a 0.05 M glycine‐NaOH (pH 11) buffer. Copyright © 2010 John Wiley & Sons, Ltd.     

Adsorption of methyl violet from aqueous solutions by the biochars derived from crop residues

The adsorption of methyl violet by the biochars from crop residues was investigated with batch and leaching experiments--adsorption capacity varied with their feedstock in the following order: canola straw char>peanut straw char>soybean straw char>rice hull char. This order was generally consistent with the amount of negative charge of the biochars. Zeta potentials and Fourier transform infrared photoacoustic spectroscopy, combined with adsorption isotherms and effect of ionic strength, indicated that adsorption of methyl violet on biochars involved electrostatic attraction, specific interaction between the dye and carboxylate and phenolic hydroxyl groups on the biochars, and surface precipitation. Leaching experiments showed that 156 g of rice hull char almost completely removed methyl violet from 18.2 L of water containing 1.0 mmol/L of methyl violet. The biochars had high removal efficiency for methyl violet and could be effective adsorbents for removal of methyl violet from wastewater.     

Performance of hydrophobic chromatography in purification of alpha-amylase

Hydrophobic ligands were introduced onto agarose beads, and the adsorption capacity of the beads was measured. The adsorption capacity increased with increase in the carbon number of the ligand, ionic strength of the buffer solution, and temperature. Crude alpha-amylase was purified with these hydrophobic adsorbents and the breakthrough and elution curves were estimated based on the mass transfer theory. Under strongly hydrophobic conditions, impurities contained in crude feeds and the lack of uniformity of packing caused by aggregation of beads affected adsorption and elution behaviors.     

Nonporous magnetic materials as enzyme supports: studies with immobilized chymotrypsin.

Chymotrypsin has been immobilized to several nonporous magnetic materials. Nickel particles were considered to be most suitable as immobilized enzyme supports. Chymotrypsin immobilized to nonporous magnetic supports was not fouled significantly by either whole milk or clarified yeast homogenate. AE-cellulose-chymotrypsin was rapidly fouled by both these materials and chymotrypsin immobilized to acrylic-based ion exchangers was slowly fouled. Immobilized enzyme activity was found to be inversely proportional to particle diameter for nonporous rock magnetic particles. Immobilization by adsorption and then glutaraldehyde crosslinking was used to produce controlled amounts of chymotrypsin on the particles. Esterolytic activity increased with enzyme loading but caseinolytic activity did not increase. Chymotrypsin is inhibited by metal ions from the magnetic supports. It is partially protected by use of a preliminary protein coating and may be reactivated by incubation with EDTA or BSA.