An improved method for purification of recombinant truncated heme oxygenase-1 by expanded bed adsorption and gel filtration

Recombinant truncated human heme oxygenase-1 (hHO-1) expressed in Escherichia coli was efficiently separated and purified from feedstock by DEAE-ion exchange expanded bed adsorption. Protocol optimization of hHO-1 on DEAE adsorbent resulted in adsorption in 0 M NaCl and elution in 150 mM NaCl at a pH of 8.5. The active enzyme fractions separated from the expanded bed column were further purified by a Superdex 75 gel filtration step. The specific hHO-1 activity increased from 0.82 ± 0.05 to 24.8 ± 1.8 U/mg during the whole purification steps. The recovery and purification factor of truncated hHO-1 of the whole purification were 72.7 ± 4.7 and 30.2 ± 2.3%, respectively. This purification process can decrease the demand on the preparation of feedstock and simplify the purification process.     

LdARL-1 His-tagged recombinant protein: purification by immobilized metal affinity expanded bed adsorption

Previously we have cloned three ADP-ribosylation factor-like (ARL) genes from the parasitic protozoan Leishmania donovani: LdARL-3A and 3B, LdARL-1. LdARL-3A was previously purified as an active native form, which was able to bind GTP in vitro. In this paper, we have performed the production and the purification of Histidine-tagged (His-tagged) LdARL-1 recombinant protein by immobilized metal affinity chromatography (IMAC) using expanded bed adsorption (EBA) technology. This protein was purified with more than 95% purity and could be successfully used for GTP-binding assay.     

Isolation of bacteriocins through expanded bed adsorption using a hydrophobic interaction medium

Two lactic acid bacterium bacteriocins were isolated from fermentation medium through expanded bed adsorption using a hydrophobic interaction gel. First, amylovorin L471, produced by Lactobacillus amylovorus DCE 471, was selected for the optimisation of the loading and eluting conditions. Secondly, the results of the optimisation were applied for the isolation of enterocin RZS C5, a bacteriocin produced by Enterococcus faecium RZS C5. Optimal adsorption was obtained for a medium with concentration of 1.0 M ammonium sulphate and adjusted to pH 4.0 (94.9% for amylovorin L471 and 75.0% for enterocin RZS C5). Elution with 50% ethanol, buffered at pH 6.0, resulted in an optimal total recovery of the bacteriocin activity of 47.6 and 57.6%, respectively. The highest fold purification expressed as the increase in specific activity (AU/mg) corresponded to the highest recovery, being 140- and 1677-fold, respectively. Nevertheless, a total recovery of only 25.6% with an increase of the specific activity of 121 times was obtained after conventional isolation by ammonium sulphate precipitation.     

Routine manufacture of recombinant proteins using expanded bed adsorption chromatography

Two different recombinant human proteins were purified directly from Pichia pastoris whole cell fermentation broth, containing 30–44% biomass (wet weight percent), by strong cation exchange expanded bed adsorption chromatography. Expanded bed adsorption chromatography provided clarification, product purification and product concentration in a single unit operation at large scale (2000-l nominal fermentation volume). The efficiency of expanded bed adsorption chromatography resulted in a short process time, high process yield, and limited proteolytic degradation of the target proteins. The separations were operated using a 60-cm (d) column run at 14 l/min. For one protein, expanded bed adsorption chromatography resulted in an average product recovery of 113% (relative to fermentation supernatant) and a purity of 89% (n=10). For the other protein, the average product recovery was 99% (relative to fermentation supernatant) and the purity was 62.1 (n=10). Laboratory experiments showed that biomass reduced product dynamic binding capacity for protein 2.     

Pilot scale production of a recombinant human epidermal growth factor, secreted by Bacillus brevis, using expanded bed adsorption

Recombinant Bacillus brevis which carried an expression plasmid encoding the human epidermal growth factor (EGF) gene on a cryptic high-copy number plasmid, pHT926, extracellularly produced EGF in its biologically active form at a concentration of over 1.5 g L⁻¹ in the culture broth in a 30-L jar fermenter. The culture broth also contained some other EGF compounds, which mainly consisted of oligomeric and polymeric forms with disulfide bonds. We developed a simple purification method for EGF, without prior cell removal from the culture broth, comprising cation exchange expanded bed adsorption followed by ultrafiltration with UF 10 000 and 3000 membranes. The EGF compounds were efficiently separated from the EGF in its native form in the expanded bed adsorption step. With this purification method, only EGF in its native form was recovered from the culture broth, with a yield of nearly 80%, and 90% purity. This efficient and economic system has made it possible to use EGF as a pharmaceutical in the livestock industry. Received 10 June 1998/ Accepted in revised form 10 September 1998     

Single step purification of a series of wheat recombinant proteins with expanded bed absorption chromatography

Expanded bed absorption chromatography (EBA) was used to improve and simplify the purification of several wheat recombinant proteins. Binding and elution conditions were set to allow the purification of the over expressed protein in a single step. In comparison with our previous multi step protocol, same purity was obtained while EBA required less time (one day instead of five) and gave a higher yield (63% instead of 10%). This new procedure was then used for the successful purification of five other wheat ns-LTP. Despite their important polymorphism (identity from 44 to 97 %-pHi from 8 to 10), the EBA protocol allowed their purification in a single step.     

Removal of poly-histidine fusion tags from recombinant proteins purified by expanded bed adsorption

Enzymatic methods have been used to cleave the C- or N-terminus polyhistidine tags from histidine tagged proteins following expanded bed purification using immobilized metal affinity chromatography (IMAC). This study assesses the use of Factor Xa and a genetically engineered exopeptidase dipeptidyl aminopeptidase-1 (DAPase-1) for the removal of C-terminus and N-terminus polyhistidine tags, respectively. Model proteins consisting of maltose binding protein (MBP) having a C- or N-terminal polyhistidine tag were used. Digestion of the hexahistidine tag of MBP-His(6) by Factor Xa and HT15-MBP by DAPase-1 was successful. The time taken to complete the conversion of MBP-His(6) to MBP was 16 h, as judged by SDS-PAGE and Western blots against anti-His antibody. When the detagged protein was purified using subtractive IMAC, the yield was moderate at 71% although the overall recovery was high at 95%. Likewise, a yield of 79% and a recovery of 97% was obtained when digestion was performed with using "on-column" tag digestion. On-column tag digestion involves cleavage of histidine tag from polyhistidine tagged proteins that are still bound to the IMAC column. Digestion of an N-terminal polyhistidine tag from HT15-MBP (1 mg/mL) by the DAPase-I system was superior to the results obtained with Factor Xa with a higher yield and recovery of 99% and 95%, respectively. The digestion by DAPase-I system was faster and was complete at 5 h as opposed to 16 h for Factor Xa. The detagged MBP proteins were isolated from the digestion mixtures using a simple subtractive IMAC column procedure with the detagged protein appearing in the flowthrough and washing fractions while residual dipeptides and DAPase-I (which was engineered to exhibit a poly-His tail) were adsorbed to the column. FPLC analysis using a MonoS cation exchanger was performed to understand and monitor the progress and time course of DAPase-I digestion of HT15-MBP to MBP. Optimization of process variables such as temperature, protein concentration, and enzyme activity was developed for the DAPase-I digesting system on HT15-MBP to MBP. In short, this study proved that the use of either Factor Xa or DAPase-I for the digestion of polyhistidine tags is simple and efficient and can be carried out under mild reaction conditions.     

Impact of operating variables on the expanded bed adsorption of Saccharomyces cerevisiae cells using a concanavalin A derivatized perfluorocarbon

The use of fluidizable affinity adsorbents for the adsorption of cells in expanded mode is investigated. Affinity adsorbents have been synthesized by immobilizing the lectin Concanavalin A onto the surface of triazine-activated perfluorocarbon-solids. The adsorbents were found to adsorb Saccharomyces cerevisiae cells from solution with adsorption capacities of up to 6.8 x 10(9) cells mL(-1). Adsorption kinetics were rapid with a time constant of 相似文献   

On-column refolding of recombinant human interferon-gamma inclusion bodies by expanded bed adsorption chromatography

A refolding strategy was described for on-column refolding of recombinant human interferon-gamma (rhIFN-gamma) inclusion bodies by expanded bed adsorption (EBA) chromatography. After the denatured rhIFN-gamma protein bound onto the cation exchanger of STREAMLINE SP, the refolding process was performed in expanded bed by gradually decreasing the concentration of urea in the buffer and the refolded rhIFN-gamma protein was recovered by the elution in packed bed mode. It was demonstrated that the denatured rhIFN-gamma protein could be efficiently refolded by this method with high yield. Under appropriate experimental conditions, the protein yield and specific activity of rhIFN-gamma was up to 52.7% and 8.18 x 10(6) IU/mg, respectively.     

Modeling of protein monomer/aggregate purification and separation using hydrophobic interaction chromatography

Hydrophobic interaction chromatography (HIC) is commonly used to separate protein monomer and aggregate species in the purification of protein therapeutics. Despite being used frequently, the HIC separation mechanism is quite complex and not well understood. In this paper, we examined the separation of a monomer and aggregate protein mixture using Phenyl Sepharose FF. The mechanisms of protein adsorption, desorption, and diffusion of the two species were evaluated using several experimental approaches to determine which processes controlled the separation. A chromatography model, which used homogeneous diffusion (to describe mass transfer) and a competitive Langmuir binary isotherm (to describe protein adsorption and desorption), was formulated and used to predict the separation of the monomer and aggregate species. The experimental studies showed a fraction of the aggregate species bound irreversibly to the adsorbent, which was a major factor governing the separation of the species. The model predictions showed inclusion of irreversible binding in the adsorption mechanism greatly improved the model predictions over a range of operating conditions. The model successfully predicted the separation performance of the adsorbent with the examined feed.     

Integration of the production and the purification processes of cutinase secreted by a recombinant Saccharomyces cerevisiae SU50 strain

By expanded bed adsorption (EBA) it was possible to simultaneously recover and purify the heterologous cutinase directly from the crude feedstock. However, it was observed that in a highly condensed and consequently economically advantageous purification process as EBA, the cultivation step highly influences the following purification step. Thus, the yeast cultivation and cutinase purification by EBA cannot be considered as independent entities, and the understanding of the interactions between them are crucial for the development of a highly cost effective overall cutinase production process. From the cultivation strategies studied, one batch, one continuous and two fed-batch cultivations, the strategy that resulted in a more economical cutinase overall production process was a fed-batch mode with a feeding in galactose. This last cultivation strategy, exhibited the highest culture cutinase activity and bioreactor productivity, being obtained 3.8-fold higher cutinase activity and 3.0-fold higher productivity that could compensate the 40% higher cultivation medium costs when compared with a fed-batch culture with a feeding on glucose and galactose. Moreover, a 3.8-fold higher effective cutinase dynamic adsorption capacity and 3.8-fold higher effective purification productivity were obtained in relation to the fed-batch culture with the feeding on glucose and galactose. The cultivation strategy with a feeding on galactose, that presented 5.6-fold higher effective purification productivity, could also compensate the 32% effective adsorption capacity obtained with a continuous cultivation broth. Furthermore, a 205-fold higher cutinase activity, 24-fold higher bioreactor productivity and 6% of the cultivation medium costs were obtained in relation to the continuous culture.     

Influence of mixed electrolytes on the adsorption of lysozyme,PEG, and PEGylated lysozyme on a hydrophobic interaction chromatography resin

In a recent work (Werner A and Hasse H in J Chromatogr A 2013;1315:135) the influence of mixed electrolytes on the adsorption of the macromolecules lysozyme, PEG and di‐PEGylated lysozyme on a hydrophobic resin has been studied, but only at one overall ionic strength (3000 mM). The present work, therefore, extends these studies to other ionic strengths (2400 and 2700 mM), and explores the application of a model to predict the entire data set. The adsorbent is Toyopearl PPG‐600M. The solvent is a 25 mM aqueous sodium phosphate buffer at pH 7.0. The studied salts are sodium chloride, sodium sulfate, ammonium chloride and ammonium sulfate. Pure salts as well as binary and ternary mixtures of these salts with varying ratios of the amounts of the salts are studied at 25 °C. The loading of the adsorbent increases with increasing salt concentration for all macromolecules. Synergetic effects of the mixed electrolytes are observed. © 2017 American Institute of Chemical Engineers Biotechnol. Prog., 33:1104–1115, 2017     

Partial purification properties of human epidermal growth factor from recombinant Escherichia coli by expanded bed adsorption

Human epidermal growth factor is a polypeptide hormone having many diverse biological functions. This paper first presents the recovery results of human epidermal growth factor (hEGF) immediately from the fermentation broth of recombinant Escherichia coli by using an expanded bed system (a couple of STREAMLINE25 and ÄKTA explorer 100). The influences of operational conditions such as linear flow rate, gradient length of NaCl concentration, pH and sample concentration on the purification performances of hEGF in expanded and packed bed modes with STREAMLINE DEAE resin were systematically evaluated. After optimization, the practical recovery procedure in the expanded bed mode was carried out on a scaled-up system under the conditions of linear flow rates of 183 cm/h (upward) and 37 cm/h (downward), sample volume of 300 ml and column bed height of 13.8 cm which yielded a primary product of hEGF from the cell-free supernatant containing hEGF after centrifugation at 4000 rev/min for 15 min. As a result, the hEGF concentration in the product was higher than 20% (w/v), the concentration factor was greater than 4.3 and the total yield was higher than 80%, respectively. At the same time, the results of hEGF recovery by using expanded bed adsorption (EBA), packed bed chromatography (PBC) and salting out were compared. The results show that the procedure of hEGF recovery in expanded bed adsorption has some advantages over the other two procedures, because of its higher concentration factor, recovery yield, productivity, hEGF concentration in the primary product and shorter duration of purification run.     

Scale-up of hydrophobic interaction chromatography for the purification of a DNA vaccine against rabies

The purification of a DNA vaccine against rabies by hydrophobic interaction chromatography (HIC) using a Sepharose gel derivatised with 1,4-butanediol diglycidyl ether was scaled up 60 times. The purification profile was not affected by increased loadings (up to 15 mg DNA) and a product with a consistent quality was obtained. Fourteen mg of plasmid with an HPLC purity of 100% were obtained in one run, corresponding to a 95% yield.     

The influence of complex biological feedstock on the fluidization and bed stability in expanded bed adsorption

The stability of expanded bed adsorption systems (EBA) was studied in biomass containing culture broth by residence time distribution (RTD) experiments, using pulse inputs of fluorescent molecules as tracers. Different commercial adsorbents (Streamline DEAE, SP, Phenyl, Chelating, and AC) were tested at various biomass concentrations (2.5–12 %, wet weight) of whole (Saccharomyces cerevisiae) yeast, yeast cell homogenate, and Escherichia coli homogenate. Analyzing the RTD according to the PDE model (PDE: axially dispersed plug‐flow exchanging mass with stagnant zones) allowed the calculation of three parameters: the number of transfer units for mass exchange between mobile and stagnant fraction (N), the Peclet number for overall axial dispersion (P), and the mobile fraction of the liquid in axially dispersed plug flow (φ). When fluidization was performed in particle‐free buffer the normalized response signal (after perfect input pulse) was symmetric (N:0; P: 50–100; φ: 1), thus, demonstrating the formation of a homogeneous fluidized (expanded) bed. Upon application of suspended biomass the RTD was skewed, depending on the adsorbent used and the type and level of biomass present in the sample. This situation leads to three different characteristic pictures: the well‐fluidized system (N: ≥ 7–10; P: ≥ 40; φ: 0.80–0.90), the system exhibiting bottom channeling (N: < 1–2; P: ≥ 40; φ: 0.5–0.7) and, the system where extensive agglomeration develops (N: 4–7; P: 20–40; φ: < 0.5). These results demonstrate that changes in the hydrodynamics of EBA already take place in the presence of moderate concentrations of biomass. Furthermore, those changes can be quantitatively described mainly in terms of the fraction of stagnant zones in the system, which are formed due to the interaction of biomass and adsorbent. The technique described here can be used to evaluate a certain combination of adsorbent and biomass with regard to its suitability for expanded bed adsorption from whole broth. © 1999 John Wiley & Sons, Inc. Biotechol Bioeng 64: 484–496, 1999.     

Defining process design space for a hydrophobic interaction chromatography (HIC) purification step: Application of quality by design (QbD) principles

The concept of design space has been taking root under the quality by design paradigm as a foundation of in‐process control strategies for biopharmaceutical manufacturing processes. This paper outlines the development of a design space for a hydrophobic interaction chromatography (HIC) process step. The design space included the impact of raw material lot‐to‐lot variability and variations in the feed stream from cell culture. A failure modes and effects analysis was employed as the basis for the process characterization exercise. During mapping of the process design space, the multi‐dimensional combination of operational variables were studied to quantify the impact on process performance in terms of yield and product quality. Variability in resin hydrophobicity was found to have a significant influence on step yield and high‐molecular weight aggregate clearance through the HIC step. A robust operating window was identified for this process step that enabled a higher step yield while ensuring acceptable product quality. Biotechnol. Bioeng. 2010;107: 985–997. © 2010 Wiley Periodicals, Inc.     

Screen-less expanded bed column: new approach for the recovery and purification of a malaria transmission blocking vaccine candidate from Pichia pastoris

An experimental malaria transmission blocking vaccine antigen, Pfs25H, expressed and secreted from Pichia pastoris was recovered and purified using a screenless expanded bed column equipped with a rotating fluid distribution system. This column was able to accommodate feed stock, containing 30% biomass, at a flow rate of 300–400 cm/h without affecting column stability. This capability is three times higher than the capability of the expanded bed column currently in use, which is equipped with a perforated plate fluid distribution system; this design could accommodate biomass concentrations of only up to 10%. The screen-less design did not affect the binding capacity, purification level or process yield and, therefore, shorten the process. Purified Pfs25H of 6.4 g were recovered from 37 l of Pichia pastoris culture in one step.     

Purification of recombinant aprotinin from transgenic corn germ fraction using ion exchange and hydrophobic interaction chromatography

Plants have attracted interest as hosts for protein expression because of the promise of a large production capacity and a low production cost. However, recovery costs remain a challenge as illustrated for recovery of recombinant aprotinin, a trypsin inhibitor, with removal of native corn trypsin inhibitor from transgenic corn (Azzoni et al. in Biotechnol Bioeng 80:268–276, 2002). When expression is targeted to corn grain fractions, dry milling can separate germ and endosperm fractions. Hence, only the product-containing fraction needs to be extracted, reducing the cost of extraction and the impurity level of the extract. Selective extraction conditions can reduce impurity levels to the point that low-cost adsorbents can result in relatively high purity levels. In this work, we attempted to achieve comparable purity with these lower cost methods. We replaced whole grain extraction and purification of recombinant aprotinin with sequential trypsin affinity and IMAC steps with an alternative of germ fraction extraction and purification with ion exchange and hydrophobic interaction chromatography (HIC). Using germ extraction at acidic pH supplemented with heat precipitation to remove additional host proteins resulted in a higher specific activity feed to the chromatographic steps. The cation exchange step provided 7.6× purification with 76.4% yield and no sodium dodecyl sulfate–polyacrylamide gel electrophoresis detectable native corn trypsin inhibitor. After the HIC step (2.7× step purification with 44.0% yield), the final product had a specific activity that was 75.3% of that of the affinity-purified aprotinin.     

Evaluation of exosome loading characteristics in their purification via a glycerol-assisted hydrophobic interaction chromatography method on a polyester,capillary-channeled polymer fiber phase

Exosomes are membrane-secreted vesicles, with sizes ranging from 30 to 150 nm, which play key roles in intercellular communication. There is intense interest in developing methods to isolate and quantify exosomes toward clinical diagnostics, fundamental studies of intercellular processes, and use of exosomes as delivery vehicles for therapeutic agents. Current methods for exosomes isolation and quantification are time consuming and have operational high costs; few combine isolation and quantification into a singular operation unit. This report describes the use of hydrophobic interaction chromatography on a polyester capillary-channeled polymer fiber column, employing a step gradient for exosome elution, including use of glycerol as a solvent modifier. The entire procedure is completed in 8 min, while maintaining the structural integrity and biological activity of the isolated exosomes. Electron microscopy was used to verify the size and structural fidelity of single exosomes. Absorbance response curves for a commercial exosome sample were used for exosome quantification in the chromatographic separations. In order to determine the dynamic loading capacity for exosomes, different volumes of Dictyostelium discoideum cell culture milieu supernatant were loaded at different column lengths (5–30 cm) and loading flow rates (0.2–0.5 ml/min). A loading capacity of 5.4 × 10¹² exosomes derived from D. discoideum milieu was obtained on a 0.8 × 300 mm column; yielding recoveries of over 80%. It is believed that this isolation and purification strategy holds many advantages toward the use of exosomes across a wide breadth of medical and biotechnology applications.     

On the use of mild hydrophobic interaction chromatography for "method scouting" protein purification strategies in aqueous two-phase systems: a study using model proteins

The behavior of a series of pure proteins partitioned in aqueous two-phase systems is compared with their behavior during mild hydrophobic interaction chromatography (HIC). A simple theoretical rationale for this comparison is presented based upon solvophobic theory. Similarities were found in the behavior of the model proteins in the two forms of partition chromatography. This indicates that HIC may be employed as a rapid instrumental technique for the broad characterization of protein behavior, which may be of benefit in the development of liquid-liquid partitioning strategies. However, it has proved difficult to completely account for this behavior on the basis of the known physical and structural properties of the proteins used. The variety in the detailed partitioning behavior of this small sample of protein types suggests that partition in aqueous two-phase systems is uniquely sensitive to subtle differences in surface properties of complex macromolecules. (c) 1994 John Wiley & Sons, Inc.