Kinetics of inclusion body production in batch and high cell density fed-batch culture of Escherichia coli expressing ovine growth hormone

Growth hormone receptor agonists and antagonists: From protein expression and purification to long-acting formulations

Recombinant human growth hormone (rhGH) and GH receptor antagonists (GHAs) are used clinically to treat a range of disorders associated with GH deficiency or hypersecretion, respectively. However, these biotherapeutics can be difficult and expensive to manufacture with multiple challenges from recombinant protein generation through to the development of long-acting formulations required to improve the circulating half-life of the drug. In this review, we summarize methodologies and approaches used for making and purifying recombinant GH and GHA proteins, and strategies to improve pharmacokinetic and pharmacodynamic properties, including PEGylation and fusion proteins. Therapeutics that are in clinical use or are currently under development are also discussed.

Heterologous expression of novel SUMO proteases from Schizosaccharomyces pombe in E. coli: Catalytic domain identification and optimization of product yields

Small ubiquitin-related modifier (SUMO) proteins are efficiently used to target the soluble expression of various difficult-to-express proteins in E. coli. However, its utilization in large scale protein production is restricted by the higher cost of Ulp, which is required to cleave SUMO fusion tag from protein-of-interest to generate an authentic N-terminus. This study identified and characterized two novel SUMO proteases i.e., Ulp1 and Ulp2 from Schizosaccharomyces pombe. Codon-optimized gene sequences were cloned and expressed in E. coli. The sequence and structure of SpUlp1 and SpUlp2 catalytic domains were deduced using bioinformatics tools. Protein-protein interaction studies predicted the higher affinity of SpUlp1 towards SUMO compared to its counterpart from Saccharomyces cerevisiae (ScUlp1). The catalytic domain of SpUlp1 was purified using Ni-NTA chromatography with 83.33% recovery yield. Moreover, In vitro activity data further confirmed the fast-acting nature of SpUlp1 catalytic domain, where a 90% cleavage of fusion proteins was obtained within 1 h of incubation, indicating novelty and commercial relevance of S. pombe Ulp1. Biophysical characterization showed 8.8% α-helices, 36.7% β-sheets in SpUlp1SD. From thermal CD and fluorescence data, SpUlp1SD T_m was found to be 45 °C. Further, bioprocess optimization using fed-batch cultivation resulted in 3.5 g/L of SpUlp1SD production with Y_P/X of 77.26 mg/g DCW and volumetric productivity of 205.88 mg/L/h.

Reprogramming Halomonas for industrial production of chemicals

Halomonas spp. are able to grow under a high salt concentration at alkali pH, they are able to resist contamination by other microbes. Development of Halomonas spp. as platform production strains for the next-generation industrial biotechnology (NGIB) is intensively studied. Among Halomonas spp., Halomonas bluephagenesis is the best studied one with available engineering tools and methods to reprogram it for production of various polyhydroxyalkanoates, proteins, and chemicals. Due to its contamination resistance, H. bluephagenesis can be grown under open and continuous processes not just in the labs but also in at least 1000 L fermentor scale. It is expected that NGIB based on Halomonas spp. be able to engineer for production of increasing number of products in a competitive manner.

Mathematical modeling of fed-batch fermentation of Schizochytrium sp. FJU-512 growth and DHA production using a shift control strategy

To obtain high-cell-density cultures of Schizochytrium sp. FJU-512 for DHA production, two stages of fermentation strategy were used and carbon/nitrogen ratio, DO and temperature were controlled at different levels. The final dry cell weight, total lipid production and DHA yield in 15 l bioreactor reached 103.9, 37.2 and 16.0 g/l, respectively. For the further study of microbial growth and DHA production dynamics, we established a set of kinetic models for the fed-batch production of DHA by Schizochytrium sp. FJU-512 in 15 and 100 l fermenters and a compensatory parameter n was integrated into the model in order to find the optimal mathematical equations. A modified Logistic model was proposed to fit the cell growth data and the following kinetic parameters were obtained: µ_m = 0.0525/h, X_m = 100 g/l and n = 4.1717 for the 15 l bioreactor, as well as µ_m = 0.0382/h, X_m = 107.4371 g/l and n = 10 for the 100 l bioreactor. The Luedeking-Piret equations were utilized to model DHA production, yielding values of α = 0.0648 g/g and β = 0.0014 g/g/h for the 15 l bioreactor, while the values of α and β obtained for the 100 l fermentation were 0.0209 g/g and 0.0030 g/g/h. The predicted results compared with experimental data showed that the established models had a good fitting precision and were able to exactly depict the dynamic features of the DHA production process.

Efficient process development of recombinant human granulocyte colony-stimulating factor (rh-GCSF) production in Escherichia coli

Background:

The protein hormone granulocyte colony-stimulating factor (GCSF) stimulates the production of white blood cells and plays an important role in medical treatment of cancer patients.

Methods:

An efficient process was developed for heterologous expression of the human GCSF in E. coli BL21 (DE3). The feeding rate was adjusted to achieve the maximum attainable specific growth rate under critical value. In this method, specific growth rate was maintained at the maximum value of 0.55 h^-1 at the beginning of feeding to 0.4 h^-1 at the induction time. Recombinant human GCSF (rh-GCSF) was produced as inclusion body. At first, inclusion bodies were released by cell disruption and then washed, solubilized and refolded. Finally, the rh-GCSF was purified by cation exchange chromatography.

Results:

Obviouly, higher specific growth rate decreases process time and consequently increases productivity. The final concentration of biomass and GCSF was achieved 126 g DCW.l^-1 and 32.1 g.l^-1. Also, the final specific yield (Y_P/X) and total productivity of rh-GCSF were obtained 254 mg.g^-1 DCW and 1.83 g.l^-1.h^-1, respectively. According to the available data, this is one of the highest Y_P/X and productivity that has been reported for any human protein which is expressed in E. coli. Recovery yield of purification process was %40 and purity of recombinant protein was over than 99%. The circular dichroism spectra of purified rh-GCSF, Neupogen® and PD-Grastim showed that all proteins have a similar secondary structure.

Conclusion:

Modified exponential feeding strategy for fed-batch cultivation of recombinant E. coli, results in minimum fed-batch duration and maximum productivity.

Recombinant production of biologically active giant grouper (Epinephelus lanceolatus) growth hormone from inclusion bodies of Escherichia coli by fed-batch culture

Growth hormone (GH) performs important roles in regulating somatic growth, reproduction, osmoregulation, metabolism and immunity in teleosts, and thus, it has attracted substantial attention in the field of aquaculture application. Herein, giant grouper GH (ggGH) cDNA was cloned into the pET28a vector and expressed in Shuffle® T7 Competent Escherichia coli. Recombinant N-terminal 6× His-tagged ggGH was produced mainly in insoluble inclusion bodies; the recombinant ggGH content reached 20% of total protein. For large-scale ggGH production, high-cell density E. coli culture was achieved via fed-batch culture with pH-stat. After 30h of cultivation, a cell concentration of 41.1g/l dry cell weight with over 95% plasmid stability was reached. Maximal ggGH production (4.0g/l; 22% total protein) was achieved via mid-log phase induction. Various centrifugal forces, buffer pHs and urea concentrations were optimized for isolation and solubilization of ggGH from inclusion bodies. Hydrophobic interactions and ionic interactions were the major forces in ggGH inclusion body formation. Complete ggGH inclusion body solubilization was obtained in PBS buffer at pH 12 containing 3M urea. Through a simple purification process including Ni-NTA affinity chromatography and refolding, 5.7mg of ggGH was obtained from 10ml of fed-batch culture (45% recovery). The sequence and secondary structure of the purified ggGH were confirmed by LC-MS/MS mass spectrometry and circular dichroism analysis. The cell proliferation-promoting activity was confirmed in HepG2, ZFL and GF-1 cells with the WST-1 colorimetric bioassay.

Genome engineering for improved recombinant protein expression in Escherichia coli

A metabolic engineering perspective which views recombinant protein expression as a multistep pathway allows us to move beyond vector design and identify the downstream rate limiting steps in expression. In E.coli these are typically at the translational level and the supply of precursors in the form of energy, amino acids and nucleotides. Further recombinant protein production triggers a global cellular stress response which feedback inhibits both growth and product formation. Countering this requires a system level analysis followed by a rational host cell engineering to sustain expression for longer time periods. Another strategy to increase protein yields could be to divert the metabolic flux away from biomass formation and towards recombinant protein production. This would require a growth stoppage mechanism which does not affect the metabolic activity of the cell or the transcriptional or translational efficiencies. Finally cells have to be designed for efficient export to prevent buildup of proteins inside the cytoplasm and also simplify downstream processing. The rational and the high throughput strategies that can be used for the construction of such improved host cell platforms for recombinant protein expression is the focus of this review.

Enhancing toxic protein expression in Escherichia coli fed-batch culture using kinetic parameters: Human granulocyte-macrophage colony-stimulating factor as a model system

The kinetics of recombinant human granulocyte-macrophage colony-stimulating factor (hGM-CSF) expression was studied under the strong T7 promoter in continuous culture of Escherichia coli using complex medium to design an optimum feeding strategy for high cell density cultivation. Continuous culture studies were done at different dilution rates and the growth and product formation profiles were monitored post-induction. Recombinant protein expression was in the form of inclusion bodies with a maximum specific product formation rate (q(p)) of 63.5 mg g(-1) DCW h(-1) at a dilution rate (D) of 0.3 h(-1). The maximum volumetric product concentration achieved at this dilution rate was 474 mg l(-1), which translated a ~1.4 and ~1.75 folds increase than the values obtained at dilution rates of 0.2 h(-1) and 0.4 h(-1) respectively. The specific product yield (Y(P/x)) peaked at 138 mg g(-1) DCW, demonstrating a ~1.6 folds increase in the values obtained at other dilution rates. A drop in q(p) was observed within 5-6 h of induction at all the dilution rates, possibly due to protein toxicity and metabolic stress associated with protein expression. The data from the continuous culture studies allowed us to design an optimal feeding strategy and induction time in fed-batch cultures which resulted in a maximum product concentration of 3.95 g l(-1) with a specific hGM-CSF yield (Y(P/x)) of 107 mg g(-1) DCW.

On-chip cellomics assay enabling algebraic and geometric understanding of epigenetic information in cellular networks of living systems. 1. Temporal aspects of epigenetic information in bacteria

A series of studies aimed at developing methods and systems of analyzing epigenetic information in cells and in cell networks, as well as that of genetic information, was examined to expand our understanding of how living systems are determined. Because cells are minimum units reflecting epigenetic information, which is considered to map the history of a parallel-processing recurrent network of biochemical reactions, their behaviors cannot be explained by considering only conventional DNA information-processing events. The role of epigenetic information on cells, which complements their genetic information, was inferred by comparing predictions from genetic information with cell behaviour observed under conditions chosen to reveal adaptation processes, population effects and community effects. A system of analyzing epigenetic information was developed starting from the twin complementary viewpoints of cell regulation as an “algebraic” system (emphasis on temporal aspects) and as a “geometric” system (emphasis on spatial aspects). Exploiting the combination of latest microfabrication technology and measurement technologies, which we call on-chip cellomics assay, we can control and re-construct the environments and interaction of cells from “algebraic” and “geometric” viewpoints. In this review, temporal viewpoint of epigenetic information, a part of the series of single-cell-based “algebraic” and “geometric” studies of celluler systems in our research groups, are summerized and reported. The knowlege acquired from this study may lead to the use of cells that fully control practical applications like cell-based drug screening and the regeneration of organs.

Reduction of N-terminal methionylation while increasing titer by lowering metabolic and protein production rates in E. coli auto-induced fed-batch fermentation

A standard fed-batch fermentation process using 1 mM isopropyl-β-d-thiogalactopyranoside (IPTG) induction at 37 °C in complex batch and feed media had been developed for manufacturing of a therapeutic protein (TP) expressed in inclusion bodies (IBs) by E. coli BL21 (DE3) driven by T7 promoter. Six unauthentic TP N-terminal variants were identified, of which methionylated TP (Met-TP) ratio was predominant. We hypothesized that lowering metabolic and protein production rates would reduce the Met-TP ratio while improving TP titer. The standard process was surprisingly auto-induced without added IPTG due to galactose in the complex media. Without changing either the clone or the batch medium, a new process was developed using lower feed rates and auto-induction at 29 °C after glucose depletion while increasing induction duration. In comparison to the standard process, the new process reduced the unauthentic Met-TP ratio from 23.6 to 9.6 %, increased the TP titer by 85 %, and the specific production yield from 210 to 330 mg TP per gram of dry cell weight. Furthermore, the TP recovery yield in the purified IBs was improved by ~20 %. Adding together, ~105 % more TP recovered in the purified IBs from per liter of fermentation broth for the new process than the standard process. The basic principles of lowering metabolic and production rates should be applicable to other recombinant protein production in IBs by fed-batch fermentations.

Production of glycoprotein vaccines in Escherichia coli

BACKGROUND

Conjugate vaccines in which polysaccharide antigens are covalently linked to carrier proteins belong to the most effective and safest vaccines against bacterial pathogens. State-of-the art production of conjugate vaccines using chemical methods is a laborious, multi-step process. In vivo enzymatic coupling using the general glycosylation pathway of Campylobacter jejuni in recombinant Escherichia coli has been suggested as a simpler method for producing conjugate vaccines. In this study we describe the in vivo biosynthesis of two novel conjugate vaccine candidates against Shigella dysenteriae type 1, an important bacterial pathogen causing severe gastro-intestinal disease states mainly in developing countries.

RESULTS

Two different periplasmic carrier proteins, AcrA from C. jejuni and a toxoid form of Pseudomonas aeruginosa exotoxin were glycosylated with Shigella O antigens in E. coli. Starting from shake flask cultivation in standard complex medium a lab-scale fed-batch process was developed for glycoconjugate production. It was found that efficiency of glycosylation but not carrier protein expression was highly susceptible to the physiological state at induction. After induction glycoconjugates generally appeared later than unglycosylated carrier protein, suggesting that glycosylation was the rate-limiting step for synthesis of conjugate vaccines in E. coli. Glycoconjugate synthesis, in particular expression of oligosaccharyltransferase PglB, strongly inhibited growth of E. coli cells after induction, making it necessary to separate biomass growth and recombinant protein expression phases. With a simple pulse and linear feed strategy and the use of semi-defined glycerol medium, volumetric glycoconjugate yield was increased 30 to 50-fold.

CONCLUSIONS

The presented data demonstrate that glycosylated proteins can be produced in recombinant E. coli at a larger scale. The described methodologies constitute an important step towards cost-effective in vivo production of conjugate vaccines, which in future may be used for combating severe infectious diseases, particularly in developing countries.

Kinetic studies of recombinant human interferon-gamma expression in continuous cultures of E. coli

A series of continuous cultures was performed to understand the product formation kinetics of recombinant human interferon gamma (rhIFN-gamma) in Escherichia coli at different dilution rates ranging from 0.1 to 0.3 h(-1) in different media. A T7 promoter-based vector was used for expression of IFN-gamma in E. coli BL21 (DE3) cells. The recombinant protein was produced as inclusion bodies, thus allowing a rapid buildup of rhIFN-gamma inside the cell, with the specific product yield (Y(p/X)) reaching a maximum value of 182 mg g(-1) dry cell weight (DCW). In all the media tested, the specific product formation rate (q(p)) was found to be strongly correlated with the specific growth rate (mu), demonstrating the growth-associated nature of product formation. The q(p) values show no significant decline with time postinduction, even though the recombinant protein has been over produced inside the cell. The maximum q(p) level of 75.5 mg g(-1) h(-1) was achieved at the first hour of induction at the dilution rate of 0.3 h(-1). Also, this correlation between q(p) and mu was not critically dependent on media composition, which would made it possible to grow cells in defined media in the growth phase and then push up the specific growth rate just before induction by pulse addition of glucose and yeast extract. This would ensure the twin objectives of high biomass and high specific productivities, leading to high volumetric product concentration.

Investigation of inclusion body formation in recombinant Escherichia coli with a bioimaging system

A bioimaging system using giant protoplasts of recombinant Escherichia coli was developed for examining conditions affecting the formation of inclusion bodies. After the giant protoplasts were prepared, isopropyl-beta-d-thiogalactopyranoside (IPTG) was used to induce expression of the blue fluorescence protein (BFP) gene. Fluorescence microscopy revealed that two types of fluorescence were emitted; one by soluble BFP and the other by aggregated BFP. As a result, the parameters that influence the formation of inclusion bodies can be examined by observing the fluorescence emitted by BFP, in real-time, with a fluorescence microscope. It was found that the aggregated BFP decreased with decreasing cultivation temperature, and the formation of inclusion bodies increased with decreased pH and increased IPTG concentrations. In addition, the aggregated form of BFP emitted fluorescence, indicating that BFP inclusion bodies might remain, at least partially, in a properly folded native-like form.

High throughput purification of recombinant human growth hormone using radial flow chromatography

Recombinant human growth hormone (r-hGH) was expressed in Escherichia coli as inclusion bodies. Using fed-batch fermentation process, around 670 mg/L of r-hGH was produced at a cell OD600 of 35. Cell lysis followed by detergent washing resulted in semi-purified inclusion bodies with more than 80% purity. Purified inclusion bodies were homogenous in preparation having an average size of 0.6 microm. Inclusion bodies were solubilized at pH 12 in presence of 2M urea and refolded by pulsatile dilution. Refolded protein was purified with DEAE-anion exchange chromatography using both radial and axial flow column (50 ml bed volume each). Higher buffer flow rate (30 ml/min) in radial flow column helped in reducing the batch processing time for purification of refolded r-hGH. Radial column based purification resulted in high throughput recovery of diluted refolded r-hGH in comparison to axial column. More than 40% of inclusion body protein could be refolded into bioactive form using the above method in a single batch. Purified r-hGH was analyzed by mass spectroscopy and found to be bioactive by Nb2 cell line proliferation assay. Inclusion body enrichment, mild solubilization, pulsatile refolding and radial flow chromatography worked co-operatively to improve the overall recovery of bioactive protein from inclusion bodies.

Improving the yield of soluble 6xHis-tagged interferon-alpha via the addition of repressor of the araBAD promoter system in Escherichia coli

The inhibition of inclusion body formation in Escherichia coli by the addition of alpha-D-glucopyranoside or D-fucose after induction improved the purification yield of soluble recombinant interferon-alpha. When D-fucose was added after induction, more soluble 6xHis-tagged interferon-alpha could be purified compared to when methyl alpha-D-glucopyranoside was added. It was shown that, on the basis of 1 mg dry cell weight, 16.6 microg of soluble 6xHis-tagged interferon-alpha was purified when D-fucose was added after induction and 6 ml nickel-chelated agarose gel column was used. This was about 15 times greater than when induction only was performed and 1 ml nickel-chelated agarose gel was used.

Lactose-induced production of human soluble B lymphocyte stimulator (hsBLyS) in E. coli with different culture strategies

Over-production of human soluble B lymphocyte stimulator (hsBLyS) was carried out with four different fed-batch culture strategies using lactose as inducer, instead of IPTG, in a fed-batch culture of Escherichia coli. As lactose acted as both inducer and carbon source, the best and simplest culture strategy was direct feeding of lactose after batch culture, thereby giving hsBLyS at 3.7 g l(-1) and a productivity of 0.11 g l(-1) h(-1).

Expression and purification of human placenta lactogen in Escherichia coli

There are many growth factors secreted by placenta including growth hormone, placenta lactogen (PL), prolactin, follicle stimulating hormone, luteinizing hormone, thyroid stimulating hormone, and chorionic gonadotropin. For a systematic study of how these growth factors work together to result in the various biological functions and future clinical applications, it is needed to produce enough quantities of each protein. In this paper, we report the cloning of human PL (hPL) and expression by Escherichia coli (E. coli). Four kinds of expression vectors containing the hPL gene were transformed into several kinds of suitable host strains and grown at 37 and/or 30 degrees C. Determination of the yield of recombinant hPL by SDS-PAGE reveals that among the various conditions, pQE30-PL in E. coli strain M15[pREP4] expressed the largest amount of recombinant hPL at 37 degrees C. However, the expressed recombinant hPL was accumulated in inclusion body forms. The inclusion bodies were solubilized in 8M urea and purified by a His6 tagged affinity column under denaturing condition and the final yield of hPL was determined to be 48 mg/L. Intra-chain disulfide bonds could be formed either by oxidation in the refolding buffer or by air oxidation in the presence of urea. The biological activity was examined by the fact that hPL could stimulate erythroid maturation by the formation of hemoglobin in K-562 cells in the presence of erythropoietin. Initial optimization studies resulted in the production of 282.4 mg/L of hPL.

Molecular chaperones facilitate the soluble expression of N-acyl-d-amino acid amidohydrolases in Escherichia coli

The overproduction of D-aminoacylase ( D-ANase, 233.8 U/mg), N-acyl-D-glutamate amidohydrolase (D-AGase, 38.1 U/mg) or N-acyl-D-aspartate amidohydrolase (D-AAase, 6.2 U/mg) in Escherichia coli is accompanied by aggregation of the overproduced protein. To facilitate the expression of active enzymes, the molecular chaperones GroEL-GroES (GroELS), DnaK-DnaJ-GrpE (DnaKJE), trigger factor (TF), GroELS and DnaKJE or GroELS and TF were coexpressed with the enzymes. D-ANase (313.3 U/mg) and D-AGase (95.8 U/mg) were overproduced in an active form at levels 1.3- and 1.8-fold higher, respectively, upon co-expression of GroELS and TF. An E. coli strain expressing the D-AAase gene simultaneously with the TF gene exhibited a 4.3-fold enhancement in d-AAase activity (32.0 U/mg) compared with control E. coli expressing the D-AAase gene alone.

Production of recombinant proteins using multiple-copy gene integration in high-cell-density fermentations of Ralstonia eutropha

We have previously reported the development of a novel protein expression system based on Ralstonia eutropha. In this study we report on the influence of gene copynumber on recombinant protein expression in R. eutropha. We compare recombinant gene stability and expression levels of chromosomal integration with a plasmid-based expression system. Single, double, and triple copies of a gene encoding organophosphohydrolase (OPH), an enzyme prone to inclusion-body formation in E. coli, were integrated into the R. eutropha chromosome. A linear increase between the concentration of soluble, active OPH and gene copynumber was found. Using a triple-copy integrant, we were able to produce approximately 4.3 g/L of OPH in a high-cell-density fermentation. This represents the highest titer reported to date for this enzyme, and is approximately 30 times greater than expression levels reported in E. coli.

Bioprocessing of therapeutic proteins from the inclusion bodies of Escherichia coli

Escherichia coli has been most extensively used for the large-scale production of therapeutic proteins, which do not require complex glycosylation for bioactivity. In recent years tremendous progress has been made on the molecular biology, fermentation process development and protein refolding from inclusion bodies for efficient production of therapeutic proteins using E. coli. High cell density fermentation and high throughput purification of the recombinant protein from inclusion bodies of E. coli are the two major bottle necks for the cost effective production of therapeutic proteins. The aim of this review is to summarize the developments both in high cell density, high productive fermentation and inclusion body protein refolding processes using E. coli as an expression system. The first section deals with the problems of high cell density fermentation with an aim to high volumetric productivity of recombinant protein. Process engineering parameters during the expression of ovine growth hormone as inclusion body in E. coli were analyzed. Ovine growth hormone yield was improved from 60 mg L(-1) to 3.2 g L(-1) using fed-batch culture. Similar high volumetric yields were also achieved for human growth hormone and for recombinant bonnet monkey zona pellucida glycoprotein expressed as inclusion bodies in E. coli. The second section deals with purification and refolding of recombinant proteins from the inclusion bodies of E. coli. The nature of inclusion body protein, its characterization and isolation from E. coli has been discussed in detail. Different solubilization and refolding methods, which have been used to recover bioactive protein from inclusion bodies of E. coli have also been discussed. A novel inclusion body protein solubilization method, while retaining the existing native-like secondary structure of the protein and its subsequent refolding in to bioactive form, has been discussed. This inclusion body solubilization and refolding method has been applied to recover bioactive recombinant ovine growth hormone, recombinant human growth hormone and bonnet monkey zona pellucida glycoprotein from the inclusion bodies of E. coli.

Automatic inducer addition and harvesting of recombinant Escherichia coli cultures based on indirect on-line estimation of biomass concentration and specific growth rate

This article describes a novel bioreactor configuration for production optimization of recombinant proteins in Escherichia coli. Inducer addition and harvesting are controlled on-line based on indirect estimation of biomass concentration and specific growth rate from addition of NaOH to maintain constant pH. When either a predetermined biomass concentration is reached or the cultures have obtained, a constant specific growth rate inducer is introduced automatically. The induction period is ended by automatic harvesting of the cultures either at a predetermined biomass concentration or when substrate (in this study glucose) is depleted, detected as an increase of pH, or dissolved oxygen tension. During harvesting, metabolic activities are quenched within 3 min by cooling of the cell suspension. The system has been used to optimize expression of glutathione S-transferase (GST) fusion protein of the ligand binding domain of mouse peroxisome proliferator-activated receptor, GST-PPARalpha LBD. Total yield of GST-PPARalpha LBD was independent of the time of inducer addition as long as the length of induction period corresponded to at least 0.25 cell divisions while the yield of soluble GST-PPARalpha LBD, the only active form, increased with the length of induction period. Highest yields were obtained when the inducer was added at low cell concentration as soon as constant specific growth rate was detected, resulting in induction periods corresponding to 3.4 +/- 0.4 cell divisions. The specific growth rate remained almost constant for one cell division after inducer addition, whereafter it decreased. No decrease of specific growth rate was observed when inducer was added in the lag-phase, and no soluble protein was produced. These results suggest that solely soluble GST-PPARalpha LBD acts as a growth inhibitor and that GST-PPARalpha LBD is expressed predominantly as inclusion bodies immediately after inducer addition whereas the proportion expressed as soluble protein is increased after 1 h of induction. Compared to the procedures, which are generally used for protein expression in the laboratory, this system is less labor intensive, it automatically provides recording of biomass concentration and specific growth rate, and it allows direct comparisons between expression of different proteins and performance of different constructs since the induction period is linked to growth.

Optimization of inclusion body solubilization and renaturation of recombinant human growth hormone from Escherichia coli

Recombinant human growth hormone (r-hGH) was expressed in Escherichia coli as inclusion bodies. In 10 h of fed-batch fermentation, 1.6 g/L of r-hGH was produced at a cell concentration of 25 g dry cell weight/L. Inclusion bodies from the cells were isolated and purified to homogeneity. Various buffers with and without reducing agents were used to solubilize r-hGH from the inclusion bodies and the extent of solubility was compared with that of 8 M urea as well as 6 M Gdn-HCl. Hydrophobic interactions as well as ionic interactions were found to be the dominant forces responsible for the formation of r-hGH inclusion bodies during its high-level expression in E. coli. Complete solubilization of r-hGH inclusion bodies was observed in 100 mM Tris buffer at pH 12.5 containing 2 M urea. Solubilization of r-hGH inclusion bodies in the presence of low concentrations of urea helped in retaining the existing native-like secondary structures of r-hGH, thus improving the yield of bioactive protein during refolding. Solubilized r-hGH in Tris buffer containing 2 M urea was found to be less susceptible to aggregation during buffer exchange and thus was refolded by simple dilution. The r-hGH was purified by use of DEAE-Sepharose ion-exchange chromatography and the pure monomeric r-hGH was finally obtained by using size-exclusion chromatography. The overall yield of the purified monomeric r-hGH was approximately 50% of the initial inclusion body proteins and was found to be biologically active in promoting growth of rat Nb2 lymphoma cell lines.

Effect of the codon following the ATG start site on the expression of ovine growth hormone in Escherichia coli

For expression of ovine growth hormone (OGH) in inclusion bodies without an affinity histidine tag at either end of the protein, three clones, differing only in the second codon following the ATG start site, were constructed. Their expression was studied by SDS-PAGE followed by immunoblotting. Clone Ala.OGH (clone 1), beginning with Met.Ala.Phe.Pro ellipsis, did not show any expression. Clone Phe.OGH (clone 3), beginning with Met.Phe.Pro ellipsis, gave very high levels of OGH expression following IPTG induction. However, in clone Gly.OGH (clone 2), in which the Ala codon was replaced with a Gly codon at the second position after the start site, a lower level of expression was obtained. Northern hybridization analysis showed that upon IPTG induction, OGH mRNA was transcribed from all three clones. These results therefore, imply that lack of expression in clone 1 and a lower level of expression in clone 2 are not due to a failure of transcription; however, they may be due to inefficient initiation of translation. The secondary structure analysis of mRNA predicts inaccessibility of different elements of the RBS in the case of Ala.OGH (clone 1). The present study highly underscores the importance of mRNA secondary structure at the start site in regulation of expression of a cloned gene in Escherichia coli, a prokaryotic expression system.