Expression of xyloglucan endotransglycosylases of Gerbera hybrida and Betula pendula in Pichia pastoris

The plant enzyme xyloglucan endotransglycosylase (XET; EC 2.4.1.207, xyloglucan:xyloglucosyl transferase) participates in selective modification of plant cell walls during cell growth. XETs are potential catalysts in various applications. Here, sequences encoding two XETs from Gerbera hybrida and Betula pendula are reported. The encoded proteins, which are 51% identical at the amino acid level, were expressed in the yeast Pichia pastoris in secreted form with the aid of mating factor alpha signal sequence. XET production in shake flask cultivations was better at 22 degrees C than at 30 degrees C. Both the yield of protein of expected molecular mass and the XET activity improved at the lower temperature. Under all cultivation conditions studied, higher amounts of XET from B. pendula (BXET) were expressed than XET from G. hybrida (GXET). Both XET enzymes were produced in 16l fed-batch bioreactor cultures. GXET was produced in methanol-limited fed-batch cultivation in minimal medium, and BXET in temperature-limited fed-batch (TLFB) in minimal or complex medium. Production was highest in TLFB in complex medium. BXET was purified from the culture filtrate and characterized. Based on the specific activity of the purified protein, 60-70 mg l(-1) BXET was produced in the TLFB in complex medium.     

Fermentative capacity in high-cell-density fed-batch cultures of baker's yeast

High-cell-density fed-batch processes for bakers' yeast production will involve a low-average-specific growth rate due to the limited oxygen-transfer capacity of industrial bioreactors. The relationship between specific growth rate and fermentative capacity was investigated in aerobic, sucrose-limited fed-batch cultures of an industrial bakers' yeast strain. Using a defined mineral medium, biomass concentrations of 130 g dry weight/L were reproducibly attained. After an initial exponential-feed phase (mu = 0.18 h(-1)), oxygen-transfer limitation necessitated a gradual decrease of the specific growth rate to ca. 0.01 h(-1). Throughout fed-batch cultivation, sugar metabolism was fully respiratory, with a biomass yield of 0.5 g biomass/g sucrose(-1). Fermentative capacity (assayed off-line as ethanol production rate under anaerobic conditions with excess glucose) showed a strong positive correlation with specific growth rate. The fermentative capacity observed at the end of the process (mu = 0.01 h(-1)) was only half that observed during the exponential-feed phase (mu = 0.18 h(-1)). During fed-batch cultivation, activities of glycolytic enzymes, pyruvate decarboxylase and alcohol dehydrogenase in cell extracts did not exhibit marked changes. This suggests that changes of fermentative capacity during fed-batch cultivation were not primarily caused by regulation of the synthesis of glycolytic enzymes.     

Process strategies to enhance pyruvate production with recombinant Escherichia coli: from repetitive fed-batch to in situ product recovery with fully integrated electrodialysis

Using the pyruvate production strain Escherichia coli YYC202 ldhA::Kan different process alternatives are studied with the aim of preventing potential product inhibition by appropriate product separation. This strain is completely blocked in its ability to convert pyruvate into acetyl-CoA or acetate, resulting in acetate auxotrophy during growth in glucose minimal medium. Continuous experiments with cell retention, repetitive fed-batch, and an in situ product recovery (ISPR) process with fully integrated electrodialysis were tested. Although the continuous approach achieved a high volumetric productivity (QP) of 110 g L(-1) d(-1), this approach was not pursued because of long-term production strain instabilities. The highest pyruvate/glucose molar yield of up to 1.78 mol mol(-1) together with high QP 145 g L(-1) d(-1) and high pyruvate titers was achieved by the repetitive fed-batch approach. To separate pyruvate from fermentation broth a fully integrated continuous process was developed. In this process electrodialysis was used as a separation unit. Under optimum conditions a (calculated) final pyruvate titer of >900 mmol L(-1) (79 g L(-1)) was achieved.     

Fed-batch production of recombinant beta-galactosidase using the universal stress promoters uspA and uspB in high cell density cultivations

A high-level production system using the universal stress promoters uspA and uspB in a fed-batch cultivation based on minimal medium was designed. In development it was shown that a standard industrial fed-batch protocol could not be used for this purpose since it failed to induce the levels of product as compared to the basal level. Instead, a batch protocol followed by a low constant feed of glucose was shown to give full induction. The levels of the product protein, beta-galactosidase, corresponded to approximately 25% of the total protein. Higher levels were found using the uspA than uspB vectors where uspA showed considerably higher basal level. The data indicate that the sigma(70) regulated promoter, uspA, although affected by the alarmone guanosine tetraphosphate, ppGpp, worked partly in a similar manner to constitutive promoters. An industrial high cell density fed-batch cultivation on the basis of the suggested fed-batch protocol and the uspA promoter gave a final beta-galatosidase concentration of 7 g/L and a final cell concentration of 65 g/L. The heterogeneity in production of the individual cell was measured by fluorescence microscopy. The data show that there is a process time independent heterogeneity in production, which is suggested to be caused by heterogeneity in the substrate uptake rate of the individual cell.     

Use of fed-batch cultivation for achieving high cell densities for the pilot-scale production of a recombinant protein (phenylalanine dehydrogenase) in Escherichia coli

A fed-batch process for the high cell density cultivation of E. coli TG1 and the production of the recombinant protein phenylalanine dehydrogenase (PheDH) was developed. A model based on Monod kinetics with overflow metabolism and incorporating acetate utilization kinetics was used to generate simulations that describe cell growth, acetate production and reconsumption, and glucose consumption during fed-batch cultivation. Using these simulations a predetermined feeding profile was elaborated that would maintain carbon-limited growth at a growth rate below the critical growth rate for acetate formation (mu < mu(crit)). Two starvation periods are incorporated into the feed profile in order to induce acetate utilization. Cell concentrations of 53 g dry cell weight (DCW)/L were obtained with a final intracellular product concentration of recombinant protein corresponding to approximately 38% of the total cell protein. The yield of PheDH was 129 U/mL with a specific activity of 1.2 U/mg DCW and a maximum product formation rate of 0.41 U/mg DCW x h. The concentration of aectate was maintained below growth inhibitory levels until 3 h before the end of the fermentation when the concentration reached a maximum of 10.7 g/L due to IPTG induction of the recombinant protein.     

Dissolved-oxygen-stat controlling two variables for methanol induction of rGuamerin in Pichia pastoris and its application to repeated fed-batch

A DO-stat control strategy for two variables was introduced to the rGuamerin production process in Pichia pastoris and applied to repeated fed-batch culture. Two interrelated variables, namely the ratio of partial pressure of pure O2 in the inlet air-stream and the methanol feed rate, were controlled simultaneously. By using this control strategy, methanol feeding for induction could be controlled automatically while efficiently controlling the dissolved oxygen level. As a result, the cell concentration reached more than 140 g l(-1) and rGuamerin expression level 450 iu l(-1). rGuamerin was secreted into the culture medium and reached a level that was 40% higher than achieved in a fed-batch process using manual control of the methanol feeding rate. Repeated rGuamerin induction was achieved by repeating the methanol feeding and withdrawing the culture broth during extended production. During more than 250 h of culture, expression of rGuamerin was maintained at an average of about 430 iu l(-1 )(473 mg l(-1)), without causing the cell density to decrease. In addition to the rGuamerin production process, the proposed control system might be applied to cultivation of other methylotrophic yeasts in the production of therapeutic proteins.     

Effect of phosphate supply and aeration on poly-β-hydroxybutyrate production in Azotobacter chroococcum

The effects of phosphate supply and aeration on cell growth and PHB accumulation were investigated in Azotobacter chroococcum 23 with the aim of increasing PHB production. Phosphate limitation favoured PHB formation in Azotobacter chroococcum 23, but inhibited growth. Azotobacter chroococcum 23 cells demonstrated intensive uptake of orthophosphate during exponential growth. At the highest phosphate concentration (1·5 g/litre) and low aeration the amount of intracellular orthophosphate/g residual biomass was highest. Under conditions of fed-batch fermentation the possibility of controlling the PHB production process by the phosphate level in the cultivation medium was demonstrated. A 36 h fed-batch fermentation resulted in a biomass yield of 110 g/litre with a PHB cellular concentration of 75% dry weight, PHB content 82·5 g/litre, PHB yield Y_P/S = 0·24 g/g and process productivity 2·29 g/litre·h.     

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.     

Growth rate control in fed-batch cultures of recombinant Saccharomyces cerevisiae producing hepatitis B surface antigen (HBsAg).

A recombinant Saccharomyces cerevisiae producing hepatitis B surface antigen (HBsAg) exhibited growth-associated product formation. By controlling the medium feed rate, based on the calculated amount of medium required for 1 h, a constant specific growth rate was obtained in the range of 0.12-0.18 h-1. In order to prolong the exponential growth phase, the medium feed rate was increased exponentially. A fed-batch cultivation method based on the production kinetics of batch culture enhanced HBsAg production ten times more than in batch culture. The reason for the increase can be explained by the fact that the production of HBsAg is expressed as an exponential function of time when the specific growth rate is controlled to a constant value in growth-associated product formation kinetics. In the scale-up of this culture to 91, the specific growth rate could also be maintained constant and the HBsAg production trend was similar to that in a 1-1 culture. However, ethanol accumulation occurred at a late stage in fed-bach culture. Ethanol produced was not reutilized and inhibited further cell growth.     

Adaptation of a recombinant xylose-utilizing Saccharomyces cerevisiae strain to a sugarcane bagasse hydrolysate with high content of fermentation inhibitors

Adaptation of a xylose-utilizing genetically engineered strain of Saccharomyces cerevisiae to sugarcane bagasse hydrolysates by cultivation during 353h using medium with increasing concentrations of inhibitors, including phenolic compounds, furaldehydes and aliphatic acids, led to improved performance with respect to ethanol production. The remaining xylose concentration in the medium at the end of the cultivation was 5.2g l(-1), while it was 11gl(-1) in the feed, indicating that approximately half of the xylose was consumed. The performance of the adapted strain was compared with the parental strain with respect to its ability to ferment three bagasse hydrolysates with different inhibitor concentration. The ethanol yield after 24h of fermentation of the bagasse hydrolysate with lowest inhibitor concentration increased from 0.18gg(-1) of total sugar with the non-adapted strain to 0.38gg(-1) with the adapted strain. The specific ethanol productivity increased from 1.15g ethanol per g initial biomass per h with the non-adapted strain to 2.55gg(-1) h(-1) with the adapted strain. The adapted strain performed better than the non-adapted also in the two bagasse hydrolysates containing higher concentrations of inhibitors. The adapted strain converted the inhibitory furaldehydes 2-furaldehyde (furfural) and 5-hydroxymethyl-2-furaldehyde (HMF) at a faster rate than the non-adapted strain. The xylose-utilizing ability of the yeast strain did not seem to be affected by the adaptation and the results suggest that ethanol rather than xylitol was formed from the consumed xylose.     

Fed-batch cultivation of Wautersia eutropha

Batch kinetics of polyhydroxybutyrate (PHB) synthesis in a bioreactor under controlled conditions of pH and dissolved oxygen gave a biomass of 14 g l(-1) with a PHB concentration of 6.1 g l(-1) in 60 h. The data of the batch kinetics was used to develop a mathematical model, which was then extrapolated to fed-batch by incorporating the dilution due to substrate feeding. Offline computer simulation of the fed-batch model was done to develop the nutrient feeding strategies in the fed-batch cultivation. Fed-batch strategies with constant feeding of only nitrogen and constant feeding of both nitrogen and fructose were tried. Constant feeding strategy for nitrogen and fructose gave a better PHB production rate of 0.56 g h(-1) over the value obtained in batch cultivation (PHB production rate - 0.4 g h(-1)).     

Production of excreted human epidermal growth factor (hEGF) by an efficient recombinant Escherichia coli system

Recombinant Escherichia coli JM101 strains harbouring plasmids pWKW2 or lacUV5par8EGF, both encoding human epidermal growth factor (hEGF), were used in fermentations to optimize levels of excreted hEGF. Medium composition, inducer level, growth stage at induction and culture conditions, were optimized with respect to volumetric production of the recombinant protein. MMBL medium, with glucose at 5 g/l and tryptone as nitrogen source, was chosen. Isopropyl-β- -thiogalactopyranoside(IPTG) concentrations of 0.1 mM for E. coli JM101[pWKW2] and 0.2 mM for E. coli K-12 JM101[lacUV5par8EGF], were found to give the best hEGF production levels. The volumetric yields of hEGF were maximal when the cultures were induced in the mid-logarithmic phase. Growth temperature had a significant effect on hEGF yield. A simple continuous fed-batch process for cultivation of E. coli JM101[pWKW2] was developed. The maximum concentration of excreted hEGF attained in continuous fed-batch cultivation was 325 mg/l, as compared to 175 mg/l, in batch cultivation. The hEGF produced from the continuous fed-batch cultivation was substantiated by SDS-PAGE and immunoblotting.     

Uricase production by a recombinant <Emphasis Type="Italic">Hansenula polymorpha</Emphasis> strain harboring <Emphasis Type="Italic">Candida utilis</Emphasis> uricase gene

Uricase is an important medical enzyme which can be used to determine urate in clinical analysis, to therapy gout, hyperuricemia, and tumor lysis syndrome. Uricase of Candida utilis was successfully expressed in Hansenula polymorpha under the control of methanol oxidase promoter using Saccharomyces cerevisiae alpha-factor signal peptide as the secretory sequence. Recombinant H. polymorpha MU200 with the highest extracellular uricase production was characterized with three copies of expression cassette and selected for process optimization for the production of recombinant enzyme. Among the parameters investigated in shaking flask cultures, the pH value of medium and inoculum size had great influence on the recombinant uricase production. The maximum extracellular uricase yield of 2.6 U/ml was obtained in shaking flask culture. The yield of recombinant uricase was significantly improved by the combined use of a high cell-density cultivation technique and a pH control strategy of switching culture pH from 5.5 to 6.5 in the induction phase. After induction for 58 h, the production of recombinant uricase reached 52.3 U/ml (about 2.1 g/l of protein) extracellularly and 60.3 U/ml (about 2.4 g/l) intracellularly in fed-batch fermentation, which are much higher than those expressed in other expression systems. To our knowledge, this is the first report about the heterologous expression of uricase in H. polymorpha.     

Metabolic engineering to improve 1,5-diaminopentane production from cellobiose using β-glucosidase-secreting Corynebacterium glutamicum

Microbial production of 1,5-diaminopentane (DAP) from renewable feedstock is a promising and sustainable approach for the production of polyamides. In this study, we constructed a β-glucosidase (BGL)-secreting Corynebacterium glutamicum and successfully used this strain to produce DAP from cellobiose and glucose. First, C. glutamicum was metabolically engineered to produce l -lysine (a direct precursor of DAP), followed by the coexpression of l -lysine decarboxylase and BGL derived from Escherichia coli and Thermobifida fusca YX (Tfu0937), respectively. This new engineered C. glutamicum strain produced 27 g/L of DAP from cellobiose in CGXII minimal medium using fed-batch cultivation. The yield of DAP was 0.43 g/g glucose (1 g of cellobiose corresponds to 1.1 g of glucose), which is the highest yield reported to date. These results demonstrate the feasibility of DAP production from cellobiose or cellooligosaccharides using an engineered C. glutamicum strain.     

Large-scale production of endotoxin-free plasmids for transient expression in mammalian cell culture

Transient expression of recombinant proteins in mammalian cell culture in a 100-L scale requires a large quantity of plasmid that is very labour intensive to achieve with shake flask cultures and commercially available plasmid purification kits. In this paper we describe a process for plasmid production in 100-mg scale. The fermentation is carried out in a 4-L fed-batch culture with a minimal medium. The detection of the end of batch and triggering the exponential (0.1 h(-1)) feed profile was unattended and controlled by Multi-fermenter Control System. A restricted specific growth rate in fed-batch culture increased the specific plasmid yield compared to batch cultures with minimal and rich media. This together with high biomass concentration (68-107 g L(-1) wet weight) achieves high volumetric yields of plasmid (95-277 mg L(-1) depending on the construct). The purification process consisted of alkaline lysis, lysate clarification and ultrafiltration, two-phase extraction with Triton X-114 for endotoxin removal, anion-exchange chromatography as a polishing step, ultrafiltration and sterile filtration. Both fermentation and purification processes were used without optimisation for production of four plasmids yielding from 39 to 163 mg of plasmids with endotoxin content of 2.5 EU mg(-1) or less.     

Whey Fermentation by Anaerobiospirillum succiniciproducens for Production of a Succinate-Based Animal Feed Additive

Anaerobic fermentation processes for the production of a succinate-rich animal feed supplement from raw whey were investigated with batch, continuous, and variable-volume fed-batch cultures with Anaerobiospirillum succiniciproducens. The highest succinate yield, 90%, was obtained in a variable-volume fed-batch process in comparison to 80% yield in a batch cultivation mode. In continuous culture, succinate productivity was 3 g/liter/h, and the yield was 60%. Under conditions of excess CO₂, more than 90% of the whey-lactose was consumed, with an end product ratio of 4 succinate to 1 acetate. Under conditions of limited CO₂, lactose was only partially consumed and lactate was the major end product, with lower levels of ethanol, succinate, and acetate. When the succinic acid in this fermentation product was added to rumen fluid, it was completely consumed by a mixed rumen population and was 90% decarboxylated to propionate on a molar basis. The whey fermentation product formed under excess CO₂, which contained mainly organic acids and cells, could potentially be used as an animal feed supplement.     

Production of recombinant β-galactosidase in bioreactors by fed-batch culture using DO-stat and linear control

β-Galactosidase enzymes continue to play an important role in food and pharmaceutical industries. These enzymes hydrolyze lactose in its constituent monosaccharides, glucose and galactose. The industrial use of enzymes presents an increase in process costs reflecting in higher final product value. An alternative to enhance processes’ productivity and yield would be the use of recombinant enzymes and their large-scale fed-batch production. The overexpression of recombinant β-galactosidase from Kluyveromyces sp. was carried out in 2-L bioreactors using Escherichia coli strain BL21 (DE3) as host. Effect of induction time on recombinant enzyme expression was studied by adding 1?mM isopropyl thiogalactoside (IPTG) at 12?h, 18?h and 24?h of cultivation. Glucose feeding strategies were compared employing feedback-controlled DO-stat and ascendant linear pump feeding in bioreactor fed-batch cultivations. Linear feeding strategy with IPTG addition at 18?h of cultivation resulted in approximately 20?g/L and 17,745?U/L of biomass and β-galactosidase activity, respectively. On the other hand, although the feedback-controlled DO-stat feeding strategy induced at 12?h of cultivation led to lower final biomass of 18?g/L, it presented an approximately 2.5 increase in enzymatic activity, resulting in 42,367?U/L, and most importantly it led to the most prominent specific enzymatic activity of approximately 40?U/mg_protein. Comparing to previous results, these results suggest that the DO-stat feeding is a promising strategy for recombinant β-galactosidase enzyme production.     

Simple fed-batch cultivation strategy for the enhanced production of a single-sugar glucuronic acid-based oligosaccharides by a cellulose-producing <Emphasis Type="Italic">Gluconacetobacter hansenii</Emphasis> strain

The production of water-soluble single-sugar glucuronic acid-based oligosaccharides (WSOS) by a cellulose producing strain Gluconacetobacter hansenii PJK was studied in a periodically recycled and fed-batch cultivations using glucose/ethanol or glucose only. Fermentations were carried out in a 2 L jar fermenter equipped with a turbine impeller with 6 flat blades. WSOS were produced constantly but the bacterial cellulose (BC) production stopped at 48 h of cultivation in a periodically recycled culture using the exhausted medium supplemented with glucose and ethanol. Tremendous quantities of WSOS were obtained in fed-batch cultivations using glucose/ethanol (35.6 g/L at 132 h of cultivation) or glucose only (86 g/L after 240 h of cultivation) as the nutritional source. However, the BC production yield under these nutritional conditions decreased significantly in comparison to previous studies about the BC production by the same strain. The overall results revealed that G. hansenii is capable of producing enormous quantities of WSOS compared to those reported previously for compounds of a related chemical nature. Moreover, the WSOS production was found to be dependent on the pH of the culture broth.     

A cost-effective cane molasses medium for enhanced cell-bound phytase production by Pichia anomala

AIM: Formulation of an inexpensive cane molasses medium for improved cell-bound phytase production by Pichia anomala. METHODS AND RESULTS: Cell-bound phytase production by Pichia anomala was compared in synthetic glucose-beef extract and cane molasses media. The yeast was cultivated in 250 ml flasks containing 50 ml of the medium, inoculated with a 12 h-old inoculum (3 x 10(6) CFU ml(-1)) and incubated at 25 degrees C for 24 h at 250 rev min(-1). Different cultural parameters were optimized in cane molasses medium in batch fermentation. The cell-bound phytase content increased significantly in cane molasses medium (176 U g(-1) dry biomass) when compared with the synthetic medium (100 U g(-1) dry biomass). In fed-batch fermentation, a marked increase in biomass (20 g l(-1)) and the phytase yield (3000 U l(-1)) were recorded in cane molasses medium. The cost of production in cane molasses medium was pound 0.006 per 1000 U, which is much lower when compared with that in synthetic medium (pound 0.25 per 1000 U). CONCLUSIONS: An overall 86.6% enhancement in phytase yield was attained in optimized cane molasses medium using fed-batch fermentation when compared with that in synthetic medium. Furthermore, the production in cane molasses medium is cost-effective. SIGNIFICANCE AND IMPACT OF THE STUDY: Phytase yield was improved in cane molasses when compared with the synthetic medium, and the cost of production was also significantly reduced. This enzyme can find application in the animal feed industry for improving the nutritional status of feed and combating environmental pollution.     

Heat-Induced Production of Human Growth Hormone by High Cell Density Cultivation of Recombinant Escherichia Coli

The temperature-induced, over-expression of the human growth hormone gene in a recombinant E. coli during high cell density cultivation is reported. Human growth hormone (hGH) production and stability were tested under different heat shock conditions. Cell densities were 25 and 60 g l(-1) in a pH-stat fed-batch mode in defined and complex medium, respectively, and the fermentation time was decreased from 41 to 32 h. hGH was produced at 2 g l(-1) in complex medium. By using glycerol as main carbon source in the complex medium with exponential feeding, cell density and hGH production were increased to 100 g l(-1) and 2.7 g l(-1), respectively.