Expression of high levels of human tissue plasminogen activator in yeast under the control of an inducible GAL promoter

Summary The human tissue plasminogen activator (h-tPA) cDNA was fused either with the leader sequence of the killer toxin of Kluyveromyces lactis or with the Saccharomyces diastaticus glucoamylase leader peptide and cloned in the yeast expression vector under the control of the inducible UAS _gal/CYC1 promoter. The recombinant tPA is produced in yeast as a single-chain glycosylated polypeptide of 66–72 kDa, which accumulates intracellularly associated with a membrane fraction. Using two-step fed-batch fermentation, a productivity up to 100 mg/l of active intracellular tPA was obtained. Correspondence to: E. Martegani     

Effects of methanol concentration on expression levels of recombinant protein in fed-batch cultures of Pichia methanolica

The methylotrophic yeast Pichia methanolica can be used to express recombinant genes at high levels under the control of the methanol-inducible alcohol oxidase (AUG1) promoter. Methanol concentrations during the induction phase directly affect cellular growth and protein yield. Various methanol concentrations controlled by an on-line monitoring and control system were investigated in mixed glucose/methanol fed-batch cultures of P. methanolica expressing the human transferrin N-lobe protein. The PMAD18 P. methanolica strain utilized is a knock-out for the chromosomal AUG1 gene locus, resulting in a slow methanol utilization phenotype. Maximum growth of 100 g of dry cell weight per liter of culture was observed in cultures grown at 1.0% (v/v) methanol concentration. Maximum recombinant gene expression was observed for cultures controlled at 0.7% (v/v) methanol concentration, resulting in maximum volumetric production of 450 mg of transferrin per liter after 72 h of elapsed fermentation time.     

Efficient inducible expression of nitrile hydratase in Corynebacterium glutamicum

Nitrile hydratases are important industrial catalysts to produce valuable amides. In this study, we describe a comprehensive and systematic approach to the development of an inducible expression system for enhanced nitrile hydratase expression in Corynebacterium glutamicum. Through promoter engineering, codon optimization and design of ribosome binding site sequences, the nitrile hydratase activity toward 3-cyanopyridine was improved from 0.33 U/mg DCW to 12.03 U/mg DCW in shake-flask culture. By introduction of the novel inducible mmp expression system, the nitrile hydratase activity was further elevated to 14.97 U/mg DCW. Finally, a high nitrile hydratase yield of 1432 U/mL was achieved in a fed-batch fermentation process and used for nicotinamide production. These results provide new insights for the development of heterologous protein expression systems in C. glutamicum.     

Controlled fed-batch fermentation of recombinant Saccharomyces cerevisiae to produce hepatitis B surface antigen

We have performed controlled fed-batch fermentation experiments to compare the production level of hepatitis B surface antigen (HBsAg) by recombinant yeast Saccharomyces cerevisiae strains (YNN27/pYBH-1, YNN27/ p2mu-S11, YNN27/pDCB-S2) containing plasmid vector with alcohol dehydrogenase (ADH1), acid phosphatase (PHO5), and glyceraldehyde-3-phosphate dehydrogenase (GPD) promoter, respectively. Yeast cell concentrations of 15-35 g dry cell weight/L were obtained. By limiting phosphorous concentration, HBsAg expression level for the YNN27/p2mu-S11 strain with inducible PHO5 promoter reached 0.2-0.3 mg/L. By controlling nutrient addition rate and dissolved oxygen concentration, HBsAg concentrations of 3-10 mg/L were achieved in 60-70 h fermentation using the YNN27/pDCB-S2 strain with the constitutive GPD promoter.     

Influences of yeast extract on specific cellular yield of Ovine growth hormone during fed-batch fermentation of E. coli

In most cases of E. coli high cell density fermentation process, maximizing cell concentration helps in increasing the volumetric productivity of recombinant proteins usually at the cost of lower specific cellular protein yield. In this report, we describe a process for maintaining the specific cellular yield of Ovine growth hormone (oGH) from E. coli by optimal feeding of yeast extract during high cell density fermentation process. Recombinant oGH was produced as inclusion bodies in Escherichia coli. Specific cellular yield of recombinant oGH was maintained by feeding yeast extract along with glucose during fed-batch fermentation. Glucose to yeast extract ratio of 0.75 was found to be optimum for maintaining the specific cellular oGH yield of 66 mg/g of E. coli cells. Continuous feeding of yeast extract along with glucose helped in reducing acetic acid secretion and promoted higher cell growth during fed-batch fermentation. High cell growth of E. coli and high specific yield of recombinant oGH thus helped in achieving high volumetric productivity of the expressed protein. A maximum of 2 g/l of ovine growth hormone was expressed as inclusion bodies in 12 h of fed-batch fermentation.     

A process for the production of human proinsulin in Saccharomyces cerevisiae

In order to develop a large-scale fermentation process for the production of human proinsulin in yeast, the intra-cellular expression of a human superoxide dismutase-human proinsulin fusion product (SOD-PI) has been studied. The expression of SOD-PI in Saccharomyces cerevisiae is regulated by a hybrid alcohol dehydrogenase 2/glyceraldehyde-3-phosphate dehydrogenase promoter. The promoter is repressed by glucose and derepressed by depletion of glucose. Although the genetic stability of the construction is shown to be poor under product-inducing conditions, it is demonstrated in shake flask experiments that a stable expression potential can be maintained in a complex medium for more than 60 generations by maintaining excess glucose throughout the cultivations. These results have been confirmed in continuous cultures in chemostat and turbidostat experiments. Addition of the glucose analogs glucosamine, 2-desoxyglucose, methylglucose, and thioglucose also leads to repression of SOD-PI formation. The analogs, however, are not suitable for improving genetic stability during propagation because of growth inhibition. In batch fermentation experiments in a complex medium at 30 degrees C, it has been demonstrated that initial glucose concentrations up to 50 g/L result in high specific SOD-PI yields giving an overall yield of up to 700 mg SOD-PI/L whereas higher glucose concentrations lead to both lower specific and overall yields due to depletion of critical medium components in the production period. In fed-batch experiments at 30 degrees C it has been possible to obtain high specific SOD-PI yields even at high biomass concentrations by feeding glucose at a constant rate of 1.5 g/L/h for 40 h followed by a feeding of ethanol at 1.0 g/L/h for 24 h, thus giving an overall yield of 1200 mg/L. Decreasing the temperature from 30 to 26 degrees C leads to improved yields in batch as well as fed-batch experiments. The optimized fed-batch fermentation process which is suitable to be scaled up to the cubic meter level has been tested in 200-L fermentations resulting in yields of more than 1500 mg/L of the fusion protein which conveniently can be used as a precursor in the production of recombinant human proinsulin.     

The use of genetic engineering to obtain efficient production of porcine pancreatic phospholipase A2 by Saccharomyces cerevisiae

We have developed an efficient production system for porcine pancreatic phospholipase A2 in Saccharomyces cerevisiae (baker's yeast). The cDNA encoding the prophospholipase A2 was expressed under the control of the galactose inducible GAL7 promotor, and secretion was directed by the secretion signals of yeast invertase. This construct yielded up to 6 mg prophospholipase A2 activity per 1 fermentation broth, secreted as a glycosylated invertase prophospholipase A2 hybrid protein. Upon genetically deleting the glycosylation site, the level of secretion decreased to 3.6 mg prophospholipase A2 per 1. Changing the invertase secretion signals for an invertase/alpha-mating factor prepro sequence-fusion increased the secretion level up to 8 mg per 1. The secreted non-glycosylated prophospholipase A2 species was correctly processed. Our results demonstrate the promises and limitations for rational design to obtain high level expression and secretion of heterologous proteins by S. cerevisiae.     

Optimization of the production and purification processes of carnobacteriocins Cbn BM1 and Cbn B2 from Carnobacterium maltaromaticum CP5 by heterologous expression in Escherichia coli

An optimization of the production and purification processes of carnobacteriocins Cbn BM1 and Cbn B2 from Carnobacterium maltaromaticum CP5, by heterologous expression in Escherichia coli is described. The genes encoding mature bacteriocin were cloned into an E. coli expression system and expressed as a fusion protein with a thermostable thioredoxin. Recombinant E. coli were cultivated following a fed-batch fermentation process with pH, temperature and oxygenation regulation. The overexpression of the fusion proteins was improved by replacing IPTG by lactose. The fusion proteins were purified by thermal coagulation followed by affinity chromatography. The thioredoxin fusion protein was removed by using CNBr instead of enterokinase and the carnobacteriocins were recovered by reverse-phase chromatography. These optimizations led us to produce up to 320 mg of pure protein per liter of culture, which is four to ten fold higher than what is described for other heterologous expression systems.     

Operational strategies, monitoring and control of heterologous protein production in the methylotrophic yeast Pichia pastoris under different promoters: A review

The methylotrophic yeast Pichia pastoris has been widely reported as a suitable expression system for heterologous protein production. The use of different phenotypes under PAOX promoter, other alternative promoters, culture medium, and operational strategies with the objective to maximize either yield or productivity of the heterologous protein, but also to obtain a repetitive product batch to batch to get a robust process for the final industrial application have been reported. Medium composition, kinetics growth, fermentation operational strategies from fed-batch to continuous cultures using different phenotypes with the most common PAOX promoter and other novel promoters (GAP, FLD, ICL), the use of mixed substrates, on-line monitoring of the key fermentation parameters (methanol) and control algorithms applied to the bioprocess are reviewed and discussed in detail.     

High level expression of proinsulin in the yeast, Saccharomyces cerevisiae

Human proinsulin (PI) has been expressed to a high level (100 mg/liter) as a human superoxide dismutase-PI fusion protein in the yeast, Saccharomyces cerevisiae. At the junction of the two proteins is a methionine residue, allowing PI to be released from the fusion by reaction with cyanogen bromide. The fusion is expressed using a regulated, hybrid promoter containing the regulatory region of the alcohol dehydrogenase II promoter and the 3' end of a glyceraldehyde-3-phosphate dehydrogenase promoter, allowing the recombinant yeast cells to be stably maintained. Production of the fusion protein is induced by growth in medium lacking a fermentable carbon source. The heterologous fusion protein is probably insoluble within the cell, since electron microscopy reveals the presence of 'inclusion bodies'. In a cell-free extract the fusion protein is also insoluble, but can be solubilized with sodium dodecyl sulfate, and cleaved with cyanogen bromide. The PI that is produced contains incorrect disulfide bonds. After sulfitolysis, the product can be easily purified, renatured, and processed to yield insulin.     

Tightly regulated, beta-estradiol dose-dependent expression system for yeast

We have refined the regulated expression of UASGAL1, 10-driven genes in yeast by modifying a vector encoding the beta-estradiol inducible activator, GAL4.ER.VP16 (GEV). The expression of GEV was placed under the regulation of the low-level, constitutive MRP7 promoter, and beta-estradiol-regulated expression was monitored by the expression of an integrated UASGAL10-lacZ reporter and by immunoblot analysis of a UASGAL1-regulated gene product. Target gene expression regulated by low levels of GEV has several advantages over the standard galactose-inducible expression systems. (i) Most importantly, the target gene expression is undetectable in the absence of hormone; (ii) target gene expression is beta-estradiol dose-dependent, and variable levels of target gene expression from low to several hundred-fold induction can be achieved; and (iii) induction or depletion studies can be conducted independent of carbon source in gal4 delta strains. In addition, any UASGAL1,10 expression construct can be used without modification of the target gene or many gal4 delta host strains, and GEV vectors are compatible with other inducible yeast expression systems. This method may be useful to researchers investigating the functions of essential genes, dominant negative mutants, mitochondrial genes, and viral, plant, and mammalian genes in yeast assay systems.     

High-throughput screening for expression of heterologous proteins in the yeast Pichia pastoris

The methylotrophic yeast Pichia pastoris has become a powerful host for the heterologous expression of proteins. In order to provide proteins for the 'protein structure factory', a structural genomics initiative, we are working on the high-throughput expression of human proteins. Therefore, cDNAs are cloned for intracellular expression. The resulting fusion proteins carry affinity tags (6*HIS and StrepII, respectively) at the N- and C-terminus for the immunological detection and chromatographic purification of full-length proteins. Expression is controlled by the tightly regulated and highly inducible alcoholoxidase 1 (AOX1) promoter. We have developed a cultivation and induction protocol amendable to automation to increase the number of clones screened for protein expression. The screening procedure is based on a culture volume of 2 ml in a 24-well format. Lysis of the cells occurs via a chemical lysis without mechanical disruption. Using the optimized feeding and induction protocol, we are now able to screen for and identify expression clones which produce heterologous protein with a yield of 5 mg l(-1) culture volume or higher.     

Scalable,two-stage,autoinduction of recombinant protein expression in E. coli utilizing phosphate depletion

We report the scalable production of recombinant proteins in Escherichia coli, reliant on tightly controlled autoinduction, triggered by phosphate depletion in the stationary phase. The method, reliant on engineered strains and plasmids, enables improved protein expression across scales. Expression levels using this approach have reached as high as 55% of the total cellular protein. The initial use of the method in instrumented fed-batch fermentations enables cell densities of ∼30 gCDW/L and protein titers up to 8.1 ± 0.7 g/L (∼270 mg/gCDW). The process has also been adapted to an optimized autoinduction media, enabling routine batch production at culture volumes of 20 μl (384-well plates), 100 μl (96-well plates), 20 ml, and 100 ml. In batch cultures, cell densities routinely reach ∼5–7 gCDW/L, offering protein titers above 2 g/L. The methodology has been validated with a set of diverse heterologous proteins and is of general use for the facile optimization of routine protein expression from high throughput screens to fed-batch fermentation.     

Production of recombinant bacteriocin divercin V41 by high cell density <Emphasis Type="Italic">Escherichia coli</Emphasis> batch and fed-batch cultures

To increase the yield of heterologous production of the class II bacteriocin DvnRV41 with Escherichia coli Origami (DE3) (pLysS/pCR03), induction of bacteriocin gene expression was optimized by varying the inducer isopropyl beta-D-thiogalactopyranoside (IPTG) concentration (0-2 mM), and controlled batch and fed-batch cultures were tested on a 2-L scale. A concentration of 0.5 mM IPTG was found to be optimal for cell growth and bacteriocin production. Shake flask cultivation of E. coli Origami (DE3) (pLysS/pCR03) gave biomass and bacteriocin yields of 1.54 +/- 0.06 g cdw/l and 18 +/- 1 mg DvnRV41/l, respectively. Biomass (2.70 +/- 0.06 and 6.8 +/- 0.6 g cdw/l, respectively) and bacteriocin yields (30 and 74 mg DvnRV41 per liter, respectively) were both increased with batch and fed-batch compared to shake flask cultures. Bacteriocin yields reported in this study are among the highest published for other heterologous expression systems in shake flasks.     

Induction by hypoxia of heterologous-protein production with the KlPDC1 promoter in yeasts

The control of promoter activity by oxygen availability appears to be an intriguing system for heterologous protein production. In fact, during cell growth in a bioreactor, an oxygen shortage is easily obtained simply by interrupting the air supply. The purpose of our work was to explore the possible use of hypoxic induction of the KlPDC1 promoter to direct heterologous gene expression in yeast. In the present study, an expression system based on the KlPDC1 promoter was developed and characterized. Several heterologous proteins, differing in size, origin, localization, and posttranslational modification, were successfully expressed in Kluyveromyces lactis under the control of the wild type or a modified promoter sequence, with a production ratio between 4 and more than 100. Yields were further optimized by a more accurate control of hypoxic physiological conditions. Production of as high as 180 mg/liter of human interleukin-1beta was obtained, representing the highest value obtained with yeasts in a lab-scale bioreactor to date. Moreover, the transferability of our system to related yeasts was assessed. The lacZ gene from Escherichia coli was cloned downstream of the KlPDC1 promoter in order to get beta-galactosidase activity in response to induction of the promoter. A centromeric vector harboring this expression cassette was introduced in Saccharomyces cerevisiae and in Zygosaccharomyces bailii, and effects of hypoxic induction were measured and compared to those already observed in K. lactis cells. Interestingly, we found that the induction still worked in Z. bailii; thus, this promotor constitutes a possible inducible system for this new nonconventional host.     

Factors affecting the fermentative production of a lysozyme-binding antibody fragment in Escherichia coli

Fed-batch fermentation for production of a single-chain Fv antibody fragment (scFv) expressed as a recombinant periplastic protein from Escherichia coli was investigated. A high cell density of 50 g dry cell weight per liter was routinely achieved in a 14-L vessel by controlled exponential feeding of glucose to impose a constant specific growth rate. Following biomass accumulation, induction of the tac promoter by addition of IPTG was accompaied by a linear feed of yeast extract. The concentration of yeast extract feed was found to be highly influential upon both concentration and location of active product. Although scFv fragments were specifically targeted to the periplasmic space, at yeast extract feed rates of 0.72 g/h the final location was largely extracellular (68% to 79%). Total concentrations (extracellular + periplasmic) were of the order of 5 to 8 mg/L. A ten-fold increase in yeast extract supply increased total scFv concentration to almost 200 mg/L and 78% of this yield was retained in the periplasm. Control of such leakage of the recombinant product is fundamental to process design of downstream operations for product recovery. (c) 1997 John Wiley & Sons, Inc. Biotechnol Bioeng 53: 611-622, 1997.     

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

A process for maximizing the volumetric productivity of recombinant ovine growth hormone (r-oGH) expressed in Escherichia coli during high cell density fermentation process has been devised. Kinetics of r-oGH expression as inclusion bodies and its effect on specific growth rates of E. coli cells were monitored during batch fermentation process. It was observed that during r-oGH expression in E. coli, the specific growth rate of the culture became an intrinsic property of the cells which reduced in a programmed manner upon induction. Nutrient feeding during protein expression phase of the fed-batch process was designed according to the reduction in specific growth rate of the culture. By feeding yeast extract along with glucose during fed-batch operation, high cell growth with very little accumulation of acetic acid was observed. Use of yeast extract helped in maintaining high specific cellular protein yield which resulted in high volumetric productivity of r-oGH. In 16 h of fed-batch fermentation, 3.2 g l-1 of r-oGH were produced at a cell OD of 124. This is the highest concentration of r-oGH reported to date using E. coli expression system. The volumetric productivity of r-oGH was 0.2 g l-1 h-1, which is also the highest value reported for any therapeutic protein using IPTG inducible expression system in a single stage fed-batch process.     

Production of human proinsulin inE. coli in a non-fusion form

Summary A method for direct expression of the gene encoding human proinsulin inE. coli and a simple purification procedure has been established. The temperature inducible promoter is employed for rapid induction as well as high level expression, After simple down-stream processing, 80–160mg recombinant product with a purity of up to 90% can easily be obtained from 1 liter of high density fermentation medium by a single Sephadex G50 column.     

Broad-host-range plasmid pJB658 can be used for industrial-level production of a secreted host-toxic single-chain antibody fragment in Escherichia coli

In industrial scale recombinant protein production it is often of interest to be able to translocate the product to reduce downstream costs, and heterologous proteins may require the oxidative environment outside of the cytoplasm for correct folding. High-level expression combined with translocation to the periplasm is often toxic to the host, and expression systems that can be used to fine-tune the production levels are therefore important. We previously constructed vector pJB658, which harbors the broad-host-range RK2 minireplicon and the inducible Pm/xylS promoter system, and we here explore the potential of this unique system to manipulate the expression and translocation of a host-toxic single-chain antibody variable fragment with affinity for hapten 2-phenyloxazol-5-one (phOx) (scFv-phOx). Fine-tuning of scFv-phOx levels was achieved by varying the concentrations of inducers and the vector copy number and also different signal sequences. Our data show that periplasmic accumulation of scFv-phOx leads to cell lysis, and we demonstrate the importance of controlled and high expression rates to achieve high product yields. By optimizing such parameters we show that soluble scFv-phOx could be produced to a high volumetric yield (1.2 g/liter) in high-cell-density cultures of Escherichia coli.