Immobilized Triton X-100-assisted refolding of Green Fluorescent Protein-Tobacco Etch Virus protease fusion protein using β-cyclodextrin as the eluent

A new protein refolding technique based on the use of the non-charged detergent Triton X-100 immobilized to the cross-linked agarose gel Sepharose High Performance has been developed. The new solid phase was used in combination with soluble β-cyclodextrin (β-CD) to refold recombinant Green Fluorescent Protein fused to Tobacco Etch Virus protease (GFPTEVP) expressed as inclusion bodies in E. coli. Previous attempts to refold recombinant GFPTEVP by dilution had failed. In the new procedure a column packed with Triton X-100-coupled Sepharose High Performance was used to capture unfolded GFPTEVP followed by elution using an increasing β-CD concentration gradient. The yield of properly refolded GFPTEVP was 46% at a protein concentration of 380 μg/ml. In contrast, dilution refolding of GFPTEVP at 200 μg/ml refolding buffer resulted in only 4.7% of native protein.     

Matrix assisted refolding of proteins by ion exchange chromatography

Two different approaches of matrix assisted refolding have been evaluated and compared to conventional refolding by dilution. Bovine alpha-lactalbumin was used for the studies as model protein. It was adsorbed under denaturing conditions on an ion exchange matrix and refolding was completed on the column prior to elution or, depending on the buffer system, in the eluate. Agarose based chromatography matrices showed high capacities for the denatured alpha-lactalbumin. A positive effect on the yield of refolded protein by the matrix could be observed for Fractogel EMD DEAE and a negative for Toyopearl DEAE 650M, DEAE Sepharose FF and Q Sepharose FF. In the case of Fractogel EMD DEAE the ion exchange surface might act as a folding helper. This property may be caused by the grafted polymers. For Source 30Q only a marginal negative influence on the refolding kinetics was observed, thus the ion exchanger is only a mean for removal of chaotropic agents. Refolding on the column is characterized by a low yield but high productivity due to significant reduction of refolding time.     

Refolding of superoxide dismutase by ion-exchange chromatography

A new ion-exchange chromatography process was developed for refolding of iron superoxide dismutase (Fe-SOD) produced in Escherichia coli as an inclusion body. After adsorption on an ion-exchange matrix, the denatured protein was eluted by gradient decrease of urea concentration and pH of the elution buffer. The dual gradient allowed the denatured protein to refold to its correct native conformation with return of biological activity. Compared with the traditional dilution, refolding process, the new process increased the refolding yield five-fold. The process could also be carried out at high protein concentration to decrease the solution volume after refolding.     

Artificial chaperone-assisted refolding in a microchannel

Protein refolding using a simple dilution method in a microchannel often led to the formation of protein aggregates, which bound to the microchannel wall, resulting in low refolding yields. To inhibit aggregation and improve refolding yields, an artificial chaperone-assisted (ACA) refolding, which employed detergents and β-cyclodextrin was used. Model proteins, hen egg white lysozyme and yeast α-glucosidase, were successfully refolded in a microchannel. The microscopic observation showed that the ACA method suppressed protein aggregation and facilitated the refolding of lysozyme, whereas significant aggregation was observed when a simple dilution method was employed. The ACA method increased the lysozyme refolding yield by 40% over the simple dilution approach. Similarly, for α-glucosidase, the refolding yield using the ACA method (ca. 50%) was approximately three times compared with the simple dilution method. The ACA refolding method is a suitable approach to use in the refolding of proteins using a microfluidic system.     

Equilibrium and kinetic analysis of folding of ketosteroid isomerase from Comamonas testosteroni

Equilibrium and kinetic analyses have been carried out to elucidate the folding mechanism of homodimeric ketosteroid isomerase (KSI) from Comamonas testosteroni. The folding of KSI was reversible since the activity as well as the fluorescence and CD spectra was almost completely recovered after refolding. The equilibrium unfolding transitions monitored by fluorescence and CD measurements were almost coincident with each other, and the transition midpoint increased with increasing protein concentration. This suggests that the KSI folding follows a simple two-state mechanism consisting of native dimer and unfolded monomer without any thermodynamically stable intermediates. Sedimentation equilibrium analysis and size-exclusion chromatography of KSI at different urea concentrations supported the two-state model without any evidence of folded monomeric intermediates. Consistent with the two-state model, (1)H-(15)N HSQC spectra obtained for KSI in the unfolding transition region could be reproduced by a simple addition of the spectra of the native and the unfolded KSI. The KSI refolding kinetics as monitored by fluorescence intensity could be described as a fast first-order process followed by a second-order and a subsequent slow first-order processes with rate constants of 60 s(-)(1), 5.4 x 10(4) M(-)(1).s(-)(1), and 0.017 s(-)(1), respectively, at 0.62 M urea, suggesting that there may be a monomeric folding intermediate. After a burst phase that accounts for >83% of the total amplitude, the negative molar ellipticity at 225 nm increased slowly in a single phase at a rate comparable to that of the bimolecular intermediate step. The kinetics of activity recovery from the denatured state were markedly dependent upon the protein concentration, implying that the monomers are not fully active. Taken together, our results demonstrate that the dimerization induces KSI to fold into the complete structure and is crucial for maintaining the tertiary structure to perform efficient catalysis.     

Renaturation of Escherichia coli-derived recombinant human macrophage colony-stimulating factor.

Recombinant human macrophage colony-stimulating factor (rhM-CSF), a homodimeric, disulfide bonded protein, was expressed in Escherichia coli in the form of inclusion bodies. Reduced and denatured rhM-CSF monomers were refolded in the presence of a thiol mixture (reduced and oxidized glutathione) and a low concentration of denaturing agent (urea or guanidinium chloride). Refolding was monitored by nonreducing gel electrophoresis and recovery of bioactivity. The effects of denaturant type and concentration, protein concentration, concentration of thiol/disulfide reagents, temperature, and presence of impurities on the kinetics of rhM-CSF renaturation were investigated. Low denaturant concentrations (<0.5 M urea) and high protein concentrations (>0.4 mg/ml) in the refolding mixture resulted in increased formation of aggregates, although aggregation was never significant even when refolding was carried out at room temperature. Higher protein concentration resulted in higher rates but did not lead to increased yields, due to the formation of unwanted aggregates. Experiments conducted at room temperature resulted in slightly higher rates than those conducted at 4 degrees C. Although the initial renaturation rate for solubilized inclusion body protein without purification was higher than that of the reversed-phase purified reduced denatured rhM-CSF, the final renaturation yield was much higher for the purified material. A maximum refolding yield of 95% was obtained for the purified material at the following refolding conditions: 0.5 M urea, 50 mM Tris, 1.25 mM DTT, 2 mM GSH, 2 mM GSSG, 22 degrees C, pH 8, [protein] = 0.13 mg/ml.     

Operational regimes for a simplified one-step artificial chaperone refolding method

The "artificial chaperone method" for protein refolding developed by Rozema et al. (Rozema, D.; Gellman, S. H. J. Am. Chem. Soc. 1995, 117 (8), 2373-2374) involves the sequential dilution of denatured protein into a buffer containing detergent (cetyltrimethylammonium bromide, CTAB) and then into a refolding buffer containing cyclodextrin (CD). In this paper a simplified one-step artificial chaperone method is reported, whereby CTAB is added directly to the denatured solution, which is then diluted directly into a refolding buffer containing beta-cyclodextrin (beta-CD). This new method can be applied at high protein concentrations, resulting in smaller processing volumes and a more concentrated protein solution following refolding. The increase in achievable protein concentration results from the enhanced solubility of CTAB at elevated temperatures in concentrated denaturant. The refolding yields obtained for the new method were significantly higher than for control experiments lacking additives and were comparable to the yields obtained with the classical two-step approach. A study of the effect of beta-CD and CTAB concentrations on refolding yield suggested two operational regimes: slow stripping (beta-CD/CTAB approximately 1), most suited for higher protein concentrations, and fast stripping (beta-CD/CTAB approximately 2.7), best suited for lower protein concentrations. An increased chaotrope concentration resulted in higher refolding yields and an enlarged operational regime.     

Critical analysis of lysozyme refolding kinetics

The kinetics of lysozyme refolding and aggregation is studied using an existing competing first- and third-order reaction scheme. The existing model overestimates yield at high refolding concentrations (>1 mg/mL), thus limiting its use for reactor design at industrially relevant refolding concentrations. This study demonstrates that a pathway exists for the incorporation of refolded native protein into aggregates. Specifically, native lysozyme labeled with fluorescein isothiocyanate was added to the refolding buffer prior to dilution refolding of denatured and reduced lysozyme. Aggregates collected from these experiments showed significant fluorescence, indicating that labeled lysozyme had been incorporated into the aggregates during refolding. Although the precise pathway of incorporation has not been elucidated, it is clear from this work that the existing model for lysozyme refolding is not globally applicable. In particular, previous work has analytically demonstrated that neglect of a pathway from native to aggregate can result in the design of a grossly suboptimal reactor strategy. This study demonstrates that such a pathway can exist experimentally and emphasizes the need to critically assess refolding kinetic models before their use in reactor design equations.     

High recovery refolding of rhG-CSF from Escherichia coli, using urea gradient size exclusion chromatography

Protein folding liquid chromatography (PFLC) is a powerful tool for simultaneous refolding and purification of recombinant proteins in inclusion bodies. Urea gradient size exclusion chromatography (SEC) is a recently developed protein refolding method based on the SEC refolding principle. In the presented work, recombinant human granulocyte colony-stimulating factor (rhG-CSF) expressed in Escheriachia coli (E. coli) in the form of inclusion bodies was refolded with high yields by this method. Denatured/reduced rhG-CSF in 8.0 mol.L(-1) urea was directly injected into a Superdex 75 column, and with the running of the linear urea concentration program, urea concentration in the mobile phase and around the denatured rhG-CSF molecules was decreased linearly, and the denatured rhG-CSF was gradually refolded into its native state. Aggregates were greatly suppressed and rhG-CSF was also partially purified during the refolding process. Effects of the length and the final urea concentration of the urea gradient on the refolding yield of rhG-CSF by using urea gradient SEC were investigated respectively. Compared with dilution refolding and normal SEC with a fixed urea concentration in the mobile phase, urea gradient SEC was more efficient for rhG-CSF refolding--in terms of specific bioactivity and mass recovery, the denatured rhG-CSF could be refolded at a larger loading volume, and the aggregates could be suppressed more efficiently. When 500 microL of solubilized and denatured rhG-CSF in 8.0 mol.L(-1) urea solution with a total protein concentration of 2.3 mg.mL(-1) was loaded onto the SEC column, rhG-CSF with a specific bioactivity of 1.0 x 10(8) IU.mg(-1) was obtained, and the mass recovery was 46.1%.     

High productivity refolding of an inclusion body protein using pulsed-fed size exclusion chromatography

Protein refolding using size exclusion chromatography (SEC) is advantageous over conventional refolding methods in terms of ease of automation, simultaneous purification capabilities, and the non-adsorptive protein–matrix interaction which eliminates steric constraints. Despite these advantages, the widespread use of SEC refolding remains restricted by low process productivity and product concentration bottlenecks. This study aims to address those limitations and exploit SEC advantages for large-scale refolding applications. Specifically, this study reports the development of a pulsed-fed size exclusion chromatography (PF-SEC) refolding platform, which successfully refolded E. coli-derived α-fetoprotein (AFP) to achieve 53% refolding yield at 0.9 mg/ml AFP refolding concentration. AFP was introduced into the column by pulsed injection to increase feed load, while suppressing concentration-induced aggregation. Refolding was initiated by a urea gradient in the column, where the gradient length could be readily adjusted to complement pulsed feeding patterns. AFP refolding productivity with PF-SEC improved by 8- and 64-fold compared to ion-exchange chromatography refolding and pulsed dilution refolding, respectively, at a fixed refolding concentration. Through a unique integration of pulsed feeding and urea gradient development, this new PF-SEC refolding methodology overcomes ‘productivity and concentration’-related disadvantages inherent in SEC, and will be scalable for large-scale protein refolding applications.     

Immobilized beta-cyclodextrin polymer coupled to agarose gel properly refolding recombinant Staphylococcus aureus elongation factor-G in combination with detergent micelle

A novel artificial chaperone system using a combination of interactions between the unfolded protein, a detergent and a chromatographic column packed with immobilized beta-cyclodextrin (beta-CD) polymer coupled to an agarose gel, was introduced to refold recombinant Staphylococcus aureus elongation factor-G (EF-G). Pre-mixing of 10% Triton X-100 and unfolded EF-G at 24 mg/ml followed by a 20-fold dilution into refolding buffer led to successful capturing of EF-G by Triton X-100 resulting in formation of a detergent-protein complex at 1.2mg/ml of final protein concentration. The complex was subsequently applied to the immobilized beta-CD polymer column resulting in correct refolding of EF-G at a concentration of 530 microg/ml with 99% mass recovery. Detergent concentrations above critical micelle concentration were required for efficient capturing of EF-G at high protein concentration. Other detergents with hydrophile-lipophile-Balance values similar to that of Triton X-100 (Triton N-101, Noindet P40 (NP40), and Berol 185) also produced similar result. Soluble polymerized beta-CD was more efficient than the monomer to remove the detergent from the protein complex in a batch system. Immobilized beta-CD polymer column further improved the capability of detergent removal and was able to prevent aggregation that occurred with the addition of soluble beta-CD polymer at high protein concentration in the batch system. The mechanism for this system-assisted refolding was tentatively interpreted: the released protein could correctly refold in an enclosed hydrophilic environment provided by the integration of matrix and beta-CD polymer, and thus avoided aggregation during detergent removal.     

A mild hydrophobic interaction chromatography involving polyethylene glycol immobilized to agarose media refolding recombinant Staphylococcus aureus elongation factor G

Recombinant Staphylococcus aureus elongation factor G (EF-G) is difficult to refold by dilution due to the formation of large amounts of misfolded structures. However, refolding of EF-G by adsorption to a chromatographic column packed with immobilized polyethylene glycol 20,000 (PEG 20 K) followed by pulse elution with 8 M urea resulted in 88% mass recovery and 80% of correctly refolded structure. The PEG 20 K was coupled to brominated allyl group derivatized Sepharose High Performance to construct a mild hydrophobic adsorbent. Various other hydrophobic interaction adsorbents were also attempted to refold EF-G. However, ligands with high hydrophobicity tended to misfold EF-G, resulting in irreversible adsorption. Various solvents, detergents, and low temperature as well as 8 M urea were tried to release bound EF-G. Only pulse elution with 8 M urea was efficient. Urea concentrations favorable for efficiently refolding EF-G were investigated. Low urea concentration produced more misfolded structures.     

Preparative protein refolding

The rapid provision of purified native protein underpins both structural biology and the development of new biopharmaceuticals. The dominance of Escherichia coli as a cellular biofactory depends on technology for solubilizing and refolding proteins that are expressed as insoluble inclusion bodies. Such technology must be scale invariant, easily automated, generic for a broad range of similar proteins and economical. Refolding methods relying on denaturant dilution and column-based approaches meet these criteria. Recent developments, particularly in column-based methods, promise to extend the range of proteins that can be refolded successfully. Developments in preparing denatured purified protein and in the analysis of protein refolding products promise to remove bottlenecks in the overall process. Combined, these developments promise to facilitate the rapid and automated determination of appropriate refolding conditions and to simplify scale-up.     

Prevention of aggregate formation through mechanism analysis in refolding of recombinant pertactin from Escherichia coli

Production of natural pertactin for pharmaceutical use is limited by its low abundance. In this study, recombinant pertactin was highly expressed in the form of inclusion bodies in E. coli. However, up to 75% of the soluble turned out as aggregates when refolding by pulse-fed batch dilution. The conceivable route for aggregate formation was proposed as that the C-terminus of partially folded intermediate with a strong hydrophobic core would intertwine with that region of newly added denatured protein, resulting in aggregation between proteins with different folding states. The key factor for prevention of aggregate formation was to improve the synchronization of refolding. For this purpose, flash-batch dilution was conducted at a scale of 5 L and achieved a monomeric refolding yield of above 70%. Aggregates formed were efficiently removed along with impurities by one-step chromatography of Ni-resin. The purity of monomeric pertactin was >98%. An overall yield was 320 mg per liter fermentation liquor with a total recovery of about 59%. The purified protein was characterized by MALDI-TOF, circular dichroism, fluorescence, HPLC and DSC, and showed similar physiochemical properties compared to its natural counterpart. Animal study showed similar immunological responses and antibodies elicited demonstrated a comparable reactivity.     

Modeling and simulation of fed-batch protein refolding process

The simplified kinetic model that assumes competition between first-order folding and third-order aggregation was used to model the fed-batch refolding of denatured-reduced lysozyme. It was found that the model was able to describe the process at limited concentration ranges, i.e., 1-2 and 5-7 mg mL(-)(1), respectively, at extensive guanidinium chloride (GdmCl) concentrations and controlled concentrations of oxidizing and reducing agents. The folding or aggregation rate constant was different at the two protein concentration ranges and strongly dependent on the denaturant concentration. As a result, both rate constants at the two concentration ranges were expressed as functions of GdmCl concentration. The rate constants determined by fed-batch experiments could be employed for the prediction of the fed-batch process but were not able to be extended to a batch refolding by direct dilution. Computer simulations show that the denaturant concentration and fed-batch flow rate are important factors influencing the refolding yield. Prolonged fed-batch time is beneficial to keep the transient intermediate concentration at a low level and to increase the yield of correctly folded protein. This is of importance when the denaturant concentration in refolding buffer solution is low. Thus, at a low denaturant concentration, fed-batch time should be sufficiently long, whereas at an appropriately high GdmCl concentration, a short fed-batch time or a high feed rate of the denatured protein is effective to give a high refolding yield.     

Production of enzymatically active ketosteroid isomerase following insoluble expression in Escherichia coli

Enzymatically active Delta(5)-3-ketosteroid isomerase (KSI) protein with a C-terminus his(6)-tag was produced following insoluble expression using Escherichia coli. A simple, integrated process was used to extract and purify the target protein. Chemical extraction was shown to be as effective as homogenization at releasing the inclusion body proteins from the bacterial cells, with complete release taking less than 20 min. An expanded bed adsorption (EBA) column utilizing immobilized metal affinity chromatography (IMAC) was then used to purify the denatured KSI-(His(6)) protein directly from the chemical extract. This integrated process greatly simplifies the recovery and purification of inclusion body proteins by removing the need for mechanical cell disruption, repeated inclusion body centrifugation, and difficult clarification operations. The integrated chemical extraction and EBA process achieved a very high purity (99%) and recovery (89%) of the KSI-(His(6)), with efficient utilization of the adsorbent matrix (9.74 mg KSI-(His(6))/mL adsorbent). Following purification the protein was refolded by dilution to obtain the biologically active protein. Seventy-nine percent of the expressed KSI-(His(6)) protein was recovered as enzymatically active protein with the described extraction, purification, and refolding process. In addition to demonstrating the operation of this intensified inclusion body process, a plate-based concentration assay detecting KSI-(His(6)) is validated. The intensified process in this work requires minimal optimization for recovering novel his-tagged proteins, and further improves the economic advantage of E. coli as a host organism.     

Initial protein concentration and residual denaturant concentration strongly affect the batch refolding of hen egg white lysozyme

The effects of several variables on the refolding of hen egg white lysozyme have been studied. Lysozyme was denatured in both urea, and guanidine hydrochloride (GuHCl), and batch refolded by dilution (100 to 1000 fold) into 0.1M Tris-HCl, pH 8.2, 1 mM EDTA, 3 mM reduced glutathione and 0.3 mM oxidised glutathione. Refolding was found to be sensitive to temperature, with the highest refolding yield obtained at 50°C. The apparent activation energy for lysozyme refolding was found to be 56 kJ/mol. Refolding by dilution results in low concentrations of both denaturant and reducing agent species. It was found that the residual concentrations obtained during dilution (100-fold dilution: [GuHCl]=0.06 mM, [DTT]=0.15 mM) were significant and could inhibit lysozyme refolding. This study has also shown that the initial protein concentration (1–10 mg/mL) that is refolded is an important parameter. In the presence of residual GuHCl and DTT, higher refolding yields were obtained when starting from higher initial lysozyme concentrations. This trend was reversed when residual denaturant components were removed from the refolding buffer.     

Dialysis strategies for protein refolding: preparative streptavidin production

We have investigated different dialysis strategies for the refolding of recombinant streptavidin, and present a novel dialysis setup featuring gradual dilution dialysis and continuous protein feeding into a dialysis sack. A denaturing dialysis buffer is exchanged gradually by dilution with refolding buffer and it is demonstrated that the refolding yield can be increased from 45 to 75% by lowering the dilution rate. In addition, continuous feeding of protein to the dialysis sack increases the yield by 5 to 10%. The principle of gradual dilution dialysis is amenable to stringent regulation and we suggest it to be applied for other insoluble protein targets.     

Effects of ionic speciation of lysine on its adsorption and desorption through a sulfone-type ion-exchange column

Lysine produced during microbial fermentation is usually recovered by an ion-exchange process, in which lysine is first converted to the cationic form (by lowering the pH to less than 2.0 with sulfuric acid) and then fed to a cation-exchange column containing an exchanger that has a sulfone group with a weak counterion such as NH4+. Ammonia water with a pH above 11 is then supplied to the column to displace the purified lysine from the column and allow its recovery. To enhance the adsorption capacity and for a possible reduction in chemical consumption, monovalent lysine fed at pH 4 was investigated in comparison with conventional divalent lysine fed at pH 1.5. The adsorption capacity increased by more than 70% on a mass basis using pH 4 feeding compared with pH 1.5 feeding. Lysine adsorbed at pH 4 started to elute earlier than that adsorbed at pH 1.5 when ammonia water was used as the eluant solution, and the extent of early elution became more notable at lower concentrations of ammonia. Moreover, the elution of monovalent lysine fed at pH 4 displayed a stiffer front boundary and higher peak concentration. However, when the ammonium concentration was greater than 2.0 N, complete saturation of the bed was delayed during adsorption and the percent recovery yield from elution was lowered, both drawbacks that were considered inevitable features originating from the increased adsorption of monovalent lysine.     

The refolding of denatured rabbit muscle pyruvate kinase.

The refolding of rabbit muscle pyruvate kinase after denaturation by guanidine hydrochloride was studied. On dilution of the denaturing agent, enzyme activity is only partially regained. The extent of regain of activity is dependent on protein concentration, showing a marked decrease at higher concentrations. The failure to regain complete activity appears to be related to the formation of inactive aggregates, which can be separated from active enzyme by gel filtration. Insoluble aggregates can be partially re-activated after solubilization in guanidine hydrochloride. Changes in the circular-dichroism and fluorescence spectra during refolding suggest that a partially folded, inactive species is formed rapidly; this differs from native enzyme in being more susceptible to proteolysis by trypsin.