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.     

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.     

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     

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.     

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.     

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.     

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.     

Modelling and simulation of the adsorption of the lipase from Geotrichum sp. on hydrophobic interaction columns

The Langmuir model fitted well the adsorption isotherms of lipase on the hydrophobic resin. The model parameters, Q_m and k_d, were affected by NaCl concentration: Q_m increased from 31 to 80 U g^–1 resin, and k_d changed from 9.4 to 3 U ml^–1. Column modelling and the simulation data were compared with the experimental data with good agreement. The highest achieved column efficiency was 71%.     

Studies on the retention of plasmid DNA and Escherichia coli nucleic acids by hydrophobic interaction chromatography

This work presents studies on the interactions of supercoiled plasmid DNA and Escherichia coli genomic DNA (gDNA) and RNA, with an hydrophobic interaction chromatography (HIC) gel, obtained by derivatisation of Sepharose CL-6B with 1,4-butanediol diglycidyl ether. Nucleic acids purified from E. coli were injected separately in the above HIC column and eluted with 1.5 M (NH₄)₂SO₄ in the buffer. The column was able to separate single-stranded from double-stranded nucleic acids. RNA and denatured gDNA were retarded in a different way due to the interactions of the exposed hydrophobic bases with the ligands. Supercoiled plasmid DNA, on the contrary, eluted in the flowthrough. This revised version was published online in July 2006 with corrections to the Cover Date.     

Analytical characterization of a monoclonal antibody therapeutic reveals a three-light chain species that is efficiently removed using hydrophobic interaction chromatography

Size exclusion high performance liquid chromatography analysis of a human monoclonal antibody (mAb) showed the presence of a new species that eluted with a retention time between the dimeric and monomeric species of the antibody. Extensive characterization of this species, referred to as “shoulder,” indicated that it was a mAb containing an extra light chain and had a molecular weight of approximately 175 kDa. The extra light chain was found to be non-covalently associated with the Fab portion of the protein. The relative amount of shoulder (typically 1−3% of the total mAb present) varied with the Chinese hamster ovary cell line producing the mAb and was not influenced by the growth conditions. Our three-step mAb purification platform using protein A, anion exchange, and cation exchange process steps was successful at removing dimer and higher and lower molecular weight species, but not the shoulder impurity. It was found that hydrophobic interaction chromatography could be used in place of cation exchange to exploit the subtle differences in hydrophobicity between monomer and shoulder. We developed an antibody polishing process using Butyl Sepharose HP resin that is capable of removing the majority of high and low molecular weight impurities yielding 99% pure mAb monomer, virtually devoid of the shoulder species, with a step recovery of about 80%.     

Clarification and capture of high‐concentration refold pools for E. coli‐based therapeutics using expanded bed adsorption chromatography

Expanded bed adsorption (EBA) chromatography was investigated for clarification and capture of high‐concentration refold pools of Escherichia coli‐based therapeutics. Refolding of denatured inclusion bodies (IBs) at high protein concentration significantly improved product throughput; however, direct filtration of the refold materials became very challenging because of high content of protein precipitates formed during refolding. In addition, irreversible protein precipitation caused by high local concentration was encountered in packed bed capture during cation exchange chromatography elution, which limited column loading capacity and capture step productivity. In this study, the two issues are addressed in one unit operation by using EBA. Specifically, EBA can handle feed streams with significant amount of particles and precipitates, which eliminated the need for refold pool clarification through filtration. The relatively broad EBA elution profile is particularly suitable for proteins of low solubility and can effectively avoid product loss previously associated with on‐column precipitation during capture. As the EBA resin (RHOBUST^® FastLine SP IEX) used here has unique properties, it can be operated at high linear velocity (800–1,600 cm/h), while achieving a selectivity and impurity clearance largely comparable to the packed bed resin of the same ligand chemistry (SP Sepharose FF). Furthermore, the filtration of the EBA elution pool is easily manageable within facility capability. Overall, this study demonstrates that the EBA process helps debottleneck the purification of high‐turbidity refold pools by removing precipitates and concurrently capturing the product, which can be applied to other E. coli‐based therapeutics that also requires refolding of IBs. © 2013 American Institute of Chemical Engineers Biotechnol. Prog., 30:113–123, 2014     

Purification of cell culture‐derived modified vaccinia ankara virus by pseudo‐affinity membrane adsorbers and hydrophobic interaction chromatography

A purification scheme for cell culture‐derived smallpox vaccines based on an orthogonal downstream process of pseudo‐affinity membrane adsorbers (MA) and hydrophobic interaction chromatography (HIC) was investigated. The applied pseudo‐affinity chromatography, based on reinforced sulfated cellulose and heparin‐MA, was optimized in terms of dynamic binding capacities, virus yield and process productivity. HIC was introduced as a subsequent method to further reduce the DNA content. Therefore, two screens were undertaken. First, several HIC ligands were screened for different adsorption behavior between virus particles and DNA. Second, elution from pseudo‐affinity MA and adsorption of virus particles onto the hydrophobic interaction matrix was explored by a series of buffers using different ammonium sulfate concentrations. Eventually, variations between different cultivation batches and buffer conditions were investigated.The most promising combination, a sulfated cellulose membrane adsorber with subsequent phenyl HIC resulted in overall virus particle recoveries ranging from 76% to 55% depending on the product batch and applied conditions. On average, 61% of the recovered virus particles were infective within all tested purification schemes and conditions. Final DNA content varied from 0.01% to 2.5% of the starting material and the level of contaminating protein was below 0.1%. Biotechnol. Bioeng. 2010;107: 312–320. © 2010 Wiley Periodicals, Inc.     

Purification, immobilization, and characterization of a specific lipase from Staphylococcus warneri EX17 by enzyme fractionating via adsorption on different hydrophobic supports

Staphylococcus warneri strain EX17 produces three lipases with different molecular weights of 28, 30, and 45 kDa. The 45 kDa fraction (SWL-45) has been purified from crude protein extracts by one chromatographic step based on the selective adsorption of this lipase by interfacial activation on different hydrophobic supports at low ionic strength. The adsorption of SWL-45 on octyl-Sepharose increased the enzyme activity by 60%, but the other lipases were also adsorbed on this support. Using butyl-Toyopearl, which is a lesser hydrophobic support, the purification factor was close to 20, and the only protein band detected on the sodium dodecyl sulfate-polyacrylamide electrophoresis analysis gel was that corresponding to the SWL-45, which could be easily desorbed from the support by incubation with triton X-100, producing a purified enzyme. SWL-45 was immobilized under very mild conditions on cyanogen bromide Sepharose, showing similar activities and stability as for its soluble form but without intermolecular interaction. The effects of different detergents over the activity of the immobilized SWL-45 were analyzed, which was hyperactivated by factors of 1.3 and 2.5 with 0.01% Tween 80 and 0.1% Triton X-100, respectively, while ionic detergents produced detrimental effects on the enzyme activity even at very low concentrations. Optimal reaction conditions and the effect of other additives on the enzyme activity were also investigated.     

Influence of cosubstrate concentration on xylose conversion by recombinant, XYL1-expressing Saccharomyces cerevisiae: a comparison of different sugars and ethanol as cosubstrates.

Conversion of xylose to xylitol by recombinant Saccharomyces cerevisiae expressing the XYL1 gene, encoding xylose reductase, was investigated by using different cosubstrates as generators of reduced cofactors. The effect of a pulse addition of the cosubstrate on xylose conversion in cosubstrate-limited fed-batch cultivation was studied. Glucose, mannose, and fructose, which are transported with high affinity by the same transport system as is xylose, inhibited xylose conversion by 99, 77, and 78%, respectively, reflecting competitive inhibition of xylose transport. Pulse addition of maltose, which is transported by a specific transport system, did not inhibit xylose conversion. Pulse addition of galactose, which is also transported by a specific transporter, inhibited xylose conversion by 51%, in accordance with noncompetitive inhibition between the galactose and glucose/ xylose transport systems. Pulse addition of ethanol inhibited xylose conversion by 15%, explained by inhibition of xylose transport through interference with the hydrophobic regions of the cell membrane. The xylitol yields on the different cosubstrates varied widely. Galactose gave the highest xylitol yield, 5.6 times higher than that for glucose. The difference in redox metabolism of glucose and galactose was suggested to enhance the availability of reduced cofactors for xylose reduction with galactose. The differences in xylitol yield observed between some of the other sugars may also reflect differences in redox metabolism. With all cosubstrates, the xylitol yield was higher under cosubstrate limitation than with cosubstrate excess.     

A combination of cation exchange and ligand-affinity chromatography for purification of two molecular species of the folate binding protein in human milk,one equipped with a hydrophobic glycosyl phosphatidylinositol tail: characterization of hydrophobicity and electrical charge

Cation exchange chromatography combined with ligand (methotrexate) affinity chromatography on a column desorbed with a pH-gradient was used for separation and large scale purification of two folate binding proteins in human milk. One of the proteins, which had a molecular size of 27 kDa on gel filtration and eluted from the affinity column at pH 5-6 was a cleavage product of a 100 kDa protein eluted at pH 3-4 as evidenced by identical N-terminal amino acid sequences and a reduction in the molecular size of the latter protein to 27 kDa after cleavage of its hydrophobic glycosylphosphatidyl-inositol tail that inserts into Triton X-100 micelles. Chromatofocusing showed that both proteins possessed multiple isoelectric points within the pH range 7-9. The 100 kDa protein exhibited a high affinity to hydrophobic interaction chromatographic gels, whereas this was only the case with unliganded forms of the 27 kDa protein indicative of a decrease in the hydrophobicity of the protein after ligand binding.