Fluidized bed ion exchange for improving purification of lactic acid from fermentation

A strong anionic exchange resin was used to recover lactic acid directly from fermentation in an upflow fluidized bed column, resulting in 0.18 g lactic acid/g resin bound with a subsequent elution of 94%. When the culture broth was heated and adjusted pH to 8.0, 0.4 g lactic acid was bound per g resin, with a subsequent elution of 90%. L(+) and D(–) lactic acid isomers distribution was analyzed in the elution product resulting in an increase of L(+) isomer concentration. The resin did not alter its binding capacity after 23 cycles.     

Anion exchange purification of plasmid DNA using expanded bed adsorption

Recent developments in gene therapy with non-viral vectors and DNA vaccination have increased the demand for large amounts of pharmaceutical-grade plasmid DNA. The high viscosity of process streams is of major concern in the purification of plasmids, since it can cause high back pressures in column operations, thus limiting the throughput. In order to avoid these high back pressures, expanded bed anion exchange chromatography was evaluated as an alternative to fixed bed chromatography. A Streamline 25 column filled with 100 ml of Streamline QXL media, was equilibrated with 0.5 M NaCl in TE (10 mM Tris, 1 mM EDTA, pH=8.0) buffer at an upward flow of 300 cmh^-1, E. coli lysates (obtained from up to 3 liters of fermentation broth) were injected in the column. After washing out the unbound material, the media was allowed to sediment and the plasmid was eluted with 1 M NaCl in TE buffer at a downward flow of 120 cmh^-1. Purification factors of 36±1 fold, 26±0.4 plasmid purity, and close to 100% yields were obtained when less than one settled column volume of plasmid feed was injected. However, both recovery yield and purity abruptly decreased when larger amounts were processed–values of 35±2 and 5±0.7 were obtained for the recovery yield and purity, respectively, when 250 ml of feedstock were processed. In these cases, gel clogging and expansion collapse were observed. The processing of larger volumes, thus larger plasmid quantities, was only possible by performing an isopropanol precipitation step prior to the chromatographic step. This step led to an enhancement of the purification step.     

Scaleup of monoclonal antibody purification using radial streaming ion exchange chromatography

A scaleup study of the radial streaming chromatography (ZetaPrep technique) using hybridoma culture supernatant as model protein solution is described in this article. Lab and pilot cartridges were tested. Scaleup factors were calculated from the lab experiments and compared to the data obtained at pilot level. The procedure consists of three different steps: microfiltration, diafiltration, and the ZetaPrep technique using QAE cartridges. Diafiltration was used to condition the clarified culture supernatant. Calculating the elution volumes for the pilot level (ZetaPrep 800) from the smallest lab cartridge (ZetaPrep 15), a difference between calculated and experimental values of 230% was obtained. The difference between calculated and experimental values using results from ZetaPrep 100, a preparative cartridge, was 120%. At pilot level it is possible to purify 10 L culture supernatant within 3 h including regeneration and reequilibration of the cartridge. This procedure is useful for monoclonal antibodies (mAb) with a low isoelectric point (pl). The pl's of the mAb which was used in this work are in the range 5.4-6.1.     

离子交换色谱在细菌素分离纯化中的应用

近年来,乳酸菌细菌素在食品防腐剂和医药领域有着广泛的应用前景,而细菌素的分离纯化是其分子结构及遗传学特性等相关研究的重要基础。离子交换色谱是细菌素分离纯化的主要手段之一。本文阐述了离子交换色谱原理,分析了影响离子交换色谱分离纯化细菌素的各种因素,探讨了细菌素分离纯化中离子交换色谱条件的选择。     

Mixed ion exchange supports as useful ion exchangers for protein purification: purification of penicillin G acylase from Escherichia coli

A support having similar amounts of carboxymethyl and amino groups has been prepared and evaluated as an ion exchanger. It has been found that this support was able to adsorb a high amount of protein from a crude extract of proteins (approximately 55%) at pH 5. Moreover, it was able to adsorb approximately 60% of the protein that did not become adsorbed on supports bearing just one kind of ionic groups. The use of divalent cations reinforced the adsorption of proteins on these supports. These results suggest that the adsorption of proteins on supports bearing almost neutral charge is not driven by the existence of opposite charges between the adsorbent and the biomacromolecule but just by the possibility of forming a high number of enzyme-support ionic bonds. This support has been used to purify the enzyme penicillin G acylase (PGA) from Escherichia coli. PGA was not significantly adsorbed at any pH value on either amino- or carboxyl-activated supports, while it can be fully adsorbed at pH 5 on this new carboxyl-amino matrix. Thus, we have been able to almost fully purify PGA from crude extracts with a very high yield by using these new supports.     

Ion exchange purification of G6PDH from unclarified yeast cell homogenates using expanded bed adsorption

The use of expanded beds of STREAMLINE ion exchange adsorbents for the direct extraction of an intracellular enzyme glucose-6-phosphate dehydrogenase (G6PDH) from unclarified yeast cell homogenates has been investigated. It has been demonstrated that such crude feedstocks can be applied to the bed without prior clarification steps. The purification of G6PDH from an unclarified yeast homogenate was chosen as a model system containing the typical features of a direct extraction technique. Optimal conditions for the purification were determined in small scale, packed bed experiments conducted with clarified homogenates. Results from these experiments were used to develop a preparative scale separation of G6PDH in a STREAMLINE 50 EBA apparatus. The use of an on-line rotameter for measuring and controlling the height of the expanded bed when operated in highly turbid feedstocks was demonstrated. STREAMLINE DEAE has been shown to be successful in achieving isolation of G6PDH from an unclarified homogenate with a purification factor of 12 and yield of 98% in a single step process. This ion exchange adsorbent is readily cleaned using simple cleaning-in-place procedures without affecting either adsorption or the bed expansion properties of the adsorbent after many cycles of operation. The ability of combining clarification, capture, and purification in a single step will greatly simplify downstream processing flowsheets and reduce the costs of protein purification. (c) 1996 John Wiley & Sons, Inc.     

Investigation of parameters affecting a fixed bed bioreactor process for recombinant cell lines

A BHK 21 cell line expressing a recombinant antibody was grown in a fixed bed reactor (FBR) system using a porous support made of Siran glass beads. The contribution of five process variables (bead and inoculum sizes; circulation and dilution rates; glutamine concentration of the feed) to the productivity of the process (defined as production rate, effluent product concentration or yield of product on medium supplied) was investigated using a partial factorial experimental design. Individually, none of the variables tested had a significant affect upon productivity. The combination of smaller bead and inoculum sizes, higher circulation and dilution rates, plus higher feed glutamine concentration gave a markedly higher productivity than any other combination of variable levels tested. This combination of variable levels suggested that better results shold be obtained using a fluidised bed reactor system. However, comparison of the productivities of the two systems showed that the FBR gave the better results. This result can be explained in terms of the relationship of Qs_rAb to .Abbreviations C concentration - D dilution rate - FBR fixed bed bioreactor - FIBR fluidised bed bioreactor - Gln glutamine - Qs cell specific rate - Qv volumetric rate - rAb recombinant antibody - X_v viable cell density - specific growth rate     

Separation of fructooligosaccharides using zeolite fixed bed columns

Recent studies have shown that the chromatographic separation of mixtures of monosaccharides and disaccharides may be improved by employing Y zeolites, a procedure which holds promise in the separation of oligosaccharides. In the present study, a column packed with zeolite was employed to study the separation of fructooligosaccharides (FOS). FOS were produced by an enzyme isolated from Rhodotorula sp., which produces GF₂ (kestose), GF₃ (nystose) and GF₄ (frutofuranosyl nystose). The identification and quantification of the sugars were carried out by ion exchange chromatography with pulsed amperometric detection (HPAEC-PAD). The separation of fructooligosaccharides was carried out using a fixed bed column packed with Ba²⁺-exchange Y zeolites. The effects of temperature (40–50 °C), injected volume per bed volume (2.55–7.64%), superficial velocity (0.1–0.15 cm min⁻¹) and eluent composition (40–60% ethanol) were investigated using a fractionary factorial design with separation efficiency as the response. The results showed that the most favorable conditions for the separation of the oligosaccharide–glucose mixture were 60% ethanol as eluent, temperature of 50 °C, superficial velocity of 0.1 cm min⁻¹ and 2.55% injection volume per bed volume of injection mixture, using two columns in series. The values for separation efficiency were 0.60 for oligosaccharide–glucose, 1.00 for oligosaccharide–fructose, 0.22 for oligosaccharide–sucrose, 0.43 for glucose–fructose, 0.82 for glucose–sucrose and 1.23 for fructose–sucrose.     

Lactate from cultures of Lactobacillus casei recovered in a fluidized bed column using ion exchange resin

Summary Lactic acid produced by continuous culture of L.casei in an upflow packed bed reactor, was recovered with Amberlite IRA 400 in a fluidized bed column. Bed expansions of 1.25 and 2.25 were applied. Reutilization did not alter the capability of net recovery of 0.048 ± 0.01 g lactic acid/g resin. When 2200 cm/h of ascensional velocity was used, (bed expansion of 2.25), the resin adsorbed 39.3% of the initial lactic acid and 63.5% was eluted. This resin supported the highest exchange capacity of 0.126 g lactic acid/g resin. Applying high flow rates, the process has potential industrial applications due to the short time employed.     

Integration of ion exchange and ultrafiltration steps studied during purification of formate dehydrogenase using DEAE dextran

Summary Purification of formate dehydrogenase based on ionic properties combined with ultrafiltration is described. The enzyme was allowed to bind to high molecular weight DEAE dextran at low ionic strength forming a complex of high molecular weight retained behind an ultrafiltration membrane with a cut-off range of 300 000 dalton. When the ionic strength was increased, the enzyme dissociated from the DEAE dextran and could be recovered in the filtrate.     

Technical viability of the production,partial purification and characterisation of inulinase using pretreated agroindustrial residues

The present work aimed to study the viability of the use of sugarcane molasses and corn steep liquor (CSL) in a sequential inulinase production performing an up-stream pretreatment of these agroindustrial residues. A sequential strategy was used applying three central composite rotatable designs (CCRDs) to optimise medium composition, followed by a down-stream step. The medium containing 150 g L⁻¹ molasses, 50 g L⁻¹ CSL and 6 g L⁻¹ yeast extract, yielded a maximum inulinase production of 1,294 ± 7 U mL⁻¹, after 72 h of fermentation. A down-stream evaluation was carried out using an expanded bed of Streamline DAE resin (Pharmacia), with and without the up-stream treatment. The results showed that the enzyme could not be recovered from the non-pretreated medium, whereas a yield of 91% was obtained in the adsorption stage from the medium prepared with the up-stream treatment, showing the viability of producing the enzyme inulinase from agroindustrial residues using the integrated process.     

Single-step ion exchange purification of the coagulant protein from Moringa oleifera seed

The coagulant protein from Moringa oleifera (MO) seed was purified using a single-step batch ion exchange (IEX) method. Adsorption and elution parameters were optimized. Impact of the purification on the reduction of organic and nutrient release to the water was studied. The matrix was equilibrated using ammonium acetate buffer, and the optimum ionic strength of NaCl for elution was 0.6 M. The time for adsorption equilibrium was between 90 and 120 min. Maximum adsorption capacity of the matrix, estimated with the Langmuir model, was 68 mg protein/g adsorbent. The purified protein does not release organic and nutrient loads to the water, which are the main concerns of the crude extract. This work suggests that a readily scalable single-step IEX purification method can be used to produce the coagulant protein and it can be carried out with locally available facilities. This will promote the use of MO in large water treatment plants and other industries.     

Pressurised pyrolysis of Miscanthus using a fixed bed reactor

Miscanthus x giganteus was pyrolysed, in a fixed bed reactor in a constant flow of dinitrogen gas, at a rate of 13°C/min from ambient to 550°C, then held for 25 min at this temperature. The pressures employed ranged from atmospheric to 26 bar. The major compounds identified in the bio-oil were water, phenol, and phenol derivatives. The water contents impact on the usefulness of the bio-oil as a fuel. However, the phenols could provide useful platform chemicals and products. The properties of the char were determined using elemental analyses, surface area measurements using the Brunauer-Emmett-Teller equation, a calorimetric bomb, Scanning Electron Microscopy, and solid state (13)C NMR spectroscopy. The chars were highly carbonised, especially at the higher pressures, and provided thermally stable materials. Pressure impacted greatly on the surface area. Char formed at atmospheric pressure had a surface area of 162 m(2)/g, whereas that from the highest pressure applied was only 0.137 m(2)/g.     

Operating parameters for glutamic acid crystallization in displacement ion exchange chromatography

Glutamic acid can be crystallized inside cation exchange column when displacer NaOH concentration is high enough to concentrate displaced glutamic acid beyond its solubility limit. Resulting crystal layer of glutamic acid was moved with liquid phase through the column, and thus could be eluted from the column and recovered in fraction collector. For the purpose of enhancing crystal recovery, effects of operating parameters on the crystal formation were investigated. The increase in the degree of crosslinking of resin favored crystal recovery because of its low degree of swelling. Higher concentration of displacer NaOH was advantageous. If NaOH concentration is too high, however, crystal recovery was lowered due to the solubility-enhancing effects of high pH and ionic strength. The decrease of mobile phase flow rate enhanced crystal recovery because enough time to attain local equilibrium could be provided, but film diffusion would control the overall crystal formation with extremely low flow rate. Lower temperature reduced solubility of glutamic acid and thus favored crystal formation unless the rate of ion exchange was severely reduced. The ion exchange operated by displacement mode coupled with crystallization was advantageous in reducing the burden of further purification steps and in preventing purity-loss resulted from overlapping between adjacent bands.     

Intensified process for the purification of an enzyme from inclusion bodies using integrated expanded bed adsorption and refolding

This work describes the integration of expanded bed adsorption (EBA) and adsorptive protein refolding operations in an intensified process used to recover purified and biologically active proteins from inclusion bodies expressed in E. coli. Delta(5)-3-Ketosteroid isomerase with a C-terminal hexahistidine tag was expressed as inclusion bodies in the cytoplasm of E. coli. Chemical extraction was used to disrupt the host cells and simultaneously solubilize the inclusion bodies, after which EBA utilizing immobilized metal affinity interactions was used to purify the polyhistidine-tagged protein. Adsorptive refolding was then initiated in the column by changing the denaturant concentration in the feed stream from 8 to 0 M urea. Three strategies were tested for performing the refolding step in the EBA column: (i) the denaturant was removed using a step change in feed-buffer composition, (ii) the denaturant was gradually removed using a gradient change in feed-buffer composition, and (iii) the liquid flow direction through the column was reversed and adsorptive refolding performed in the packed bed. Buoyancy-induced mixing disrupted the operation of the expanded bed when adsorptive refolding was performed using either a step change or a rapid gradient change in feed-buffer composition. A shallow gradient reduction in denaturant concentration of the feed stream over 30 min maintained the stability of the expanded bed during adsorptive refolding. In a separate experiment, buoyancy-induced mixing was completely avoided by performing refolding in a settled bed, which achieved comparable yields to refolding in an expanded bed but required a slightly more complex process. A total of 10% of the available KSI-(His(6)) was recovered as biologically active and purified protein using the described purification and refolding process, and the yield was further increased to 19% by performing a second iteration of the on-column refolding operation. This process should be applicable for other polyhistidine tagged proteins and is likely to have the greatest benefit for proteins that tend to aggregate when refolded by dilution.     

Biological purification of exhaust air using fixed bacterial monocultures

Summary This paper presents the results of basic investigations on reactions and process engineering in the biological purification of exhaust air in a trickle-bed reactor. The biocatalysts used were pollutant-specific bacterial monocultures, which were immobilized on various carriers. By using different pollutants (e.g. acetone, propionaldehyde, naphthalene and toluence, crude gas concentrations: 5–35 ppm), the effect of the water solubility of the gaseous substances on separation efficiency was studied. Furthermore, a combination of monocultures was used for degradation of a mixture of pollutants. The results show that, with suitable combinations of bacteria, pollutants and carriers, conversions of more than 80% at a space velocity of about 1000^-1 can be achieved by this method.