Growth and fatty acid composition of Nannochloropsis sp. grown mixotrophically in fed-batch culture

The cell growth and eicosapentaenoic acid (EPA) yields of Nannochloropsis sp. were enhanced in the fed-batch cultures. With feeding glucose solution, the biomass reached 1.1 g dry wt l(-1) after 10 days' culture, which was 40% higher than that obtained in the batch culture (0.8 g dry wt l(-1)). With supplement of nitrate solution, the biomass reached 1 g dry wt l(-1), and reached the stationary phase 2 days earlier than the others. The maximum of biomass (1.2 g dry wt l(-1)) was obtained with the supplement of the mixture of glucose and nitrate solution. The EPA yields of Nannochloropsis sp. after 10 days' growth in the fed-batch cultures were 52 mg l(-1), 43 mg l(-1) and 56 mg l(-1) with, respectively, addition of nitrate, glucose and both together. In batch culture only 35 mg EPA l(-1) was obtained.     

Determination of the maximum specific uptake capacities for glucose and oxygen in glucose-limited fed-batch cultivations of Escherichia coli

A simple pulse-based method for the determination of the maximum uptake capacities for glucose and oxygen in glucose limited cultivations of E. coli is presented. The method does not depend on the time-consuming analysis of glucose or acetate, and therefore can be used to control the feed rate in glucose limited cultivations, such as fed-batch processes. The application of this method in fed-batch processes of E. coli showed that the uptake capacity for neither glucose nor oxygen is a constant parameter, as often is assumed in fed-batch models. The glucose uptake capacity decreased significantly when the specific growth rate decreased below 0.15 h(-1) and fell to about 0.6 mmol g(-1) h(-1) (mmol per g cell dry weight and hour) at the end of fed-batch fermentations, where specific growth rate was approximately 0.02 h(-1). The oxygen uptake capacity started to decrease somewhat earlier when specific growth rate declined below 0.25 h(-1) and was 5 mmol g(-1) h(-1) at the end of the fermentations. The behavior of both uptake systems is integrated in a dynamic model which allows a better fitting of experimental values for glucose in fed-batch processes in comparison to generally used unstructured kinetic models.     

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.     

High-level production of soluble tumor necrosis factor-related apoptosis-inducing ligand (Apo2L/TRAIL) in high-density cultivation of recombinant Escherichia coli using a combined feeding strategy

Recombinant Escherichia coli strain C600/pBV-TRAIL (encoding for 114-281 amino acids of TRAIL's soluble fragment) produced a recombinant human tumor necrosis factor-related apoptosis-inducing ligand (Apo2L/TRAIL). Using a combined strategy of exponential feeding and pH-stat feeding, high concentrations of biomass (65 g dry wt l(-1)) and active soluble TRAIL (1.4 g l(-1)) were obtained within 30 h. The accumulation of acetate, which usually occurs during the process of high-density culture of Escherichia coli and especially in the induction stage of protein synthesis, was avoided.     

Xylitol production by <Emphasis Type="Italic">Candida tropicalis</Emphasis> in a chemically defined medium

A chemically defined medium that included urea (5 g l(-1)) as a nitrogen source and various vitamins was substituted for a complex medium containing yeast extract (10 g l(-1)) in the production of xylitol by Candida tropicalis. In a fed-batch culture with the chemically defined medium, 237 g xylitol l(-1) was produced from 270 g xylose l(-1) after 120 h. The volumetric rate of xylitol production and the xylitol yield from xylose were 2 g l(-1) h(-1) and 89%, respectively. These values were about 5% lower and 4% higher, respectively, than those obtained using the complex medium. These results indicate that xylitol can be produced effectively in a chemically defined medium.     

Poly(3-hydroxybutyrate) synthesis from glycerol by a recombinant <Emphasis Type="Italic">Escherichia coli arcA</Emphasis> mutant in fed-batch microaerobic cultures

Poly(3-hydroxybutyrate) (PHB) synthesis was analyzed under microaerobic conditions in a recombinant Escherichia coli arcA mutant using glycerol as the main carbon source. The effect of several additives was assessed in a semi-synthetic medium by the 'one-factor-at-a-time' technique. Casein amino acids (CAS) concentration was an important factor influencing both growth and PHB accumulation. Three factors exerting a statistically significant influence on PHB synthesis were selected by using a Plackett-Burman screening design [glycerol, CAS, and initial cell dry weight (CDW) concentrations] and then optimized through a Box-Wilson design. Under such optimized conditions (22.02 g l(-1) glycerol, 1.78 g l(-1) CAS, and 1.83 g l(-1) inoculum) microaerobic batch cultures gave rise to 8.37 g l(-1) CDW and 3.52 g l(-1) PHB in 48 h (PHB content of 42%) in a benchtop bioreactor. Further improvements in microaerobic PHB accumulation were obtained in fed-batch cultures, in which glycerol was added to maintain its concentration above 5 g l(-1). After 60 h, CDW and PHB concentration reached 21.17 and 10.81 g l(-1), respectively, which results in a PHB content of 51%. Microaerobic fed-batch cultures allowed a 2.57-fold increase in volumetric productivity when compared with batch cultures.     

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.     

pH-stat fed-batch process to enhance the production of cis, cis-muconate from benzoate by Pseudomonas putida KT2440-JD1

Pseudomonas putida KT2440-JD1 is able to cometabolize benzoate to cis, cis-muconate in the presence of glucose as growth substrate. P. putida KT2440-JD1 was unable to grow in the presence of concentrations above 50 mM benzoate or 600 mM cis, cis-muconate. The inhibitory effects of both compounds were cumulative. The maximum specific uptake rate of benzoate was higher than the specific production rate of cis, cis-muconate during growth on glucose in the presence of benzoate, indicating that a benzoate derivative accumulated in the cells, which is likely to be catechol. Catechol was shown to reduce the expression level of the ben operon, which encodes the conversion of benzoate to cis, cis-muconate. To prevent overdoses of benzoate, a pH-stat fed-batch process for the production of cis, cis-muconate from benzoate was developed, in which the addition of benzoate was coupled to the acidification of the medium. The maximum specific production rate during the pH-stat fed-batch process was 0.6 g (4.3 mmol) g dry cell weight(-1) h(-1), whereas 18.5 g L(-1) cis, cis-muconate accumulated in the culture medium with a molar product yield of close to 100%. Proteome analysis revealed that the outer membrane protein H1 was upregulated during the pH-stat fed-batch process, whereas the expression of 10 other proteins was reduced. The identified proteins are involved in energy household, transport, translation of RNA, and motility.     

Production of heterologous protein by Methylobacterium extorquens in high cell density fermentation

The green fluorescent protein (GFP) was used as a model protein to study the recombinant protein production by the strain Methylobacterium extorquens ATCC 55366. Scale-up from shake flasks to 20 l fed-batch fermentation was achieved using methanol as a sole carbon and energy source and a completely minimal culture medium. Two different expression vectors were used to express GFP. Clone PCM-GFP containing the vector pCM110 with native promoter of the methanol dehydrogenase PmxaF produced approximately 100-fold more GFP than the clone PRK-GFP containing the vector pRK310 with the heterogeneous promoter Plac. Several fed-batch fermentations with and without selective pressure (tetracycline) were run in a 20 l stirred tank fermenter using the two different clones of M. extorquens. The methanol concentration was monitored with an on-line semiconductor gas sensor in the culture broth. It was maintained at a non-toxic level of 1.4 g l(-1) with an adaptative control which regulates the methanol feed rate. The same growth profile was achieved in all fermentations. The maximum growth rate (micro(max)) was 0.18 h(-1) with an overall yield (Y(X/S)) of 0.3 g g(-1) methanol. With this high cell density fermentation process, we obtained high levels (up to 4 g l(-1)) of GFP with the clone PCM-GFP. The maximum specific GFP production (Y(GFP/X)) with this clone was 80 mg g(-1) representing approximately 16% of the total cell protein. Additional feeding of pure oxygen to the fermenter permitted a longer phase of exponential growth but had no effect on the total yields of biomass and GFP. The specific GFP production of clone PCM-GFP remained unaffected in the presence or absence of selective pressure (tetracycline), within the initial 50 h of the fermentation culture. These results suggest that M. extorquens ATCC 55366 could be an interesting candidate for overexpression of recombinant proteins.     

Effect of specific production rate of recombinant protein on multimerization of plasmid vector and gene expression level

In fed-batch cultures of recombinant Escherichia coli BL21(DE3)[pT7-G3IL2] at high cell concentration, the post-induction specific growth rate was carefully regulated by controlled medium feed to maximize the synthesis level of recombinant fusion interleukin-2, G3.IL-2. A maximum concentration of G3.IL-2 (11.25 g l(-1)) was achieved in the induced recombinant culture growing at the rate of 0.056 h(-1). A steep decrease in the expression level of G3.IL-2 was observed at the post-induction specific growth rates higher than its optimal value (0.056 h(-1)). In the induced recombinant cultures, plasmid multimerization was observed and highly dependent on specific growth and production rate: a higher post-induction specific growth rate and an increased specific production rate tended to significantly promote it much further. Moreover, plasmid stability was found to decrease rapidly in a faster growing culture.     

The role of oxygen limitation in the formation of poly-β-hydroxybutyrate during batch and continuous culture of Azotobacter beijerinckii

Azotobacter beijerinckii was grown in ammonia-free glucose-mineral salts media in batch culture and in chemostat cultures limited by the supply of glucose, oxygen or molecular nitrogen. In batch culture poly-beta-hydroxybutyrate was formed towards the end of exponential growth and accumulated to about 74% of the cell dry weight. In chemostat cultures little poly-beta-hydroxybutyrate accumulated in organisms that were nitrogen-limited, but when oxygen limited a much increased yield of cells per mol of glucose was observed, and the organisms contained up to 50% of their dry weight of poly-beta-hydroxybutyrate. In carbon-limited cultures (D, the dilution rate,=0.035-0.240h(-1)), the growth yield ranged from 13.1 to 19.8g/mol of glucose and the poly-beta-hydroxybutyrate content did not exceed 3.0% of the dry weight. In oxygen-limited cultures (D=0.049-0.252h(-1)) the growth yield ranged from 48.4 to 70.1g/mol of glucose and the poly-beta-hydroxybutyrate content was between 19.6 and 44.6% of dry weight. In nitrogen-limited cultures (D=0.053-0.255h(-1)) the growth yield ranged from 7.45 to 19.9g/mol of glucose and the poly-beta-hydroxybutyrate content was less than 1.5% of dry weight. The sudden imposition of oxygen limitation on a nitrogen-limited chemostat culture produced a rapid increase in poly-beta-hydroxybutyrate content and cell yield. Determinations on chemostat cultures revealed that during oxygen-limited steady states (D=0.1h(-1)) the oxygen uptake decreased to 100mul h(-1) per mg dry wt. compared with 675 for a glucose-limited culture (D=0.1h(-1)). Nitrogen-limited cultures had CO(2) production values in situ ranging from 660 to 1055mul h(-1) per mg dry wt. at growth rates of 0.053-0.234h(-1) and carbon-limited cultures exhibited a variation of CO(2) production between 185 and 1328mul h(-1) per mg dry wt. at growth rates between 0.035 and 0.240h(-1). These findings are discussed in relation to poly-beta-hydroxybutyrate formation, growth efficiency and growth yield during growth on glucose. We suggest that poly-beta-hydroxybutyrate is produced in response to oxygen limitation and represents not only a store of carbon and energy but also an electron sink into which excess of reducing power can be channelled.     

Selection and evaluation of astaxanthin-overproducing mutants of Phaffia rhodozyma

Mutagenesis of Phaffia rhodozyma with NTG yielded a mutant with an astaxanthin content of 1688 g (g dry biomass)^-1, a cell yield coefficient of 0.47 on glucose and a maximum specific growth rate of 0.12 h^-1. Re-mutation of the mutant decreased the cell yield and maximum specific growth rate but increased the astaxanthin content. The use of mannitol or succinate as carbon sources enhanced pigmentation, yielding astaxanthin contents of 1973 g g^-1 and 1926 g g^-1, respectively. The use of valine as sole nitrogen source also increased astaxanthin production, but severely decreased the maximum specific growth rate and cell yield coefficient. The optimum pH for growth of P. rhodozyma was between pH 4.5 and 5.5, whereas the astaxanthin content remained constant above pH 3.     

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.     

Kinetic parameters of continuous cultures of Bacillus thermoleovorans sp. A2 degrading phenol at 65 degrees C

In this paper, we report on the kinetics of phenol degradation and cell growth in continuous cultures of suspended cells of Bacillus thermoleovorans sp. A2 at 65 degrees C. A high yield coefficient of Y(x/s)=0.84 g cell dry weight g(-1) phenol was measured at a dilution rate of 0.5 h(-1). At the same dilution rate the coefficient for maintenance metabolism (m(s)) was determined to be 0.045 g phenol g(-1) cell dry weight h(-1). The maximal growth rate (wash-out) determined at a phenol inlet concentration of 188 mg l(-1) was 0.9 h(-1). Up to 7 g phenol l(-1) per day were degraded in a continuously operated 2-l stirred tank reactor with suspended cells (feed concentration 660 mg l(-1)). Additionally, yield coefficients for oxygen and ammonium are reported.     

High-cell-density cultivation of Schizochytrium sp. in an ammonium/pH-auxostat fed-batch system

Thraustochytrids, in particular Schizochytrium spp., are used for the production of the valuable polyunsaturated fatty acid, docosahexaenoic acid (DHA; 22:6 n-3). Growth of Schizochytrium sp. G13/2S in a defined medium was initially made in shake-flask cultures to determine the optimum concentrations of glucose (100-200 g l(-1)) and ammonia ( approximately 300 mg l(-1)) that could be used by this microorganism. In subsequent fermenter cultures, a pH-auxostat method was used to maintain NH(3) from 200-300 mg l(-1). During the first 49 h of fermentation, 150 g glucose l(-1) produced 63 g cell dry wt l(-1). Although growth was not limited by the supply of nitrogen, total fatty acids were at 25% cell dry wt which is more than half the final lipid content of commercially-grown Schizochytrium biomass which uses N-limited medium in the final stages for maximum lipid accumulation. This strategy is therefore useful for the cultivation of Schizochytrium to a high cell density up to the point when lipid accumulation can be triggered by N exhaustion.     

Process development for production of recombinant human interferon-γ expressed in<Emphasis Type="Italic"> Escherichia coli</Emphasis>

A simple fed-batch process was carried out using constant and variable specific growth rates for high-cell-density cultivation of Escherichia coli BL21 (DE3) expressing human interferon-(hIFN-). The feeding rate was adjusted to achieve an appropriate specific growth rate. The dissolved oxygen level was maintained at 20–30% of air saturation by control of airflow and stirrer speed and, where necessary, by enrichment of inlet air with pure oxygen. Glucose was the sole source of carbon and energy and was provided by following a simple exponential feeding rate. The final cell density in the fed-batch fermentation with constant and variable specific growth rate feeding strategies was ~100 g dry cell wt l^–1 after 36 and 20 h, respectively. The final specific yield and overall productivity of recombinant hIFN- in the variable specific growth rate strategy were 0.35 g rHu-IFN- g^–1 dry cell wt and 0.9 g rHu-IFN- l^–1 h^–1, respectively. A new chromatographic purification procedure involving anion exchange and cation exchange chromatographies was developed for purification of rHu-IFN- from inclusion bodies. The established purification process is reproducible and the total recovery of rHu-IFN- was ~30% (100 mg rHu-IFN- g^–1 dry cell wt). The purity of the rHu-IFN- was determined using HPLC. Sterility, pyrogenicity, and DNA content tests were conducted to assure the absence of toxic materials and other components of E. coli in the final product. The final purified rHu-IFN- has a specific antiviral activity of ~2×10⁷ IU/mg protein, as determined by viral cytopathic effect assay. These results certify the product for clinical purposes.     

Fed-batch cultivation of the docosahexaenoic-acid-producing marine alga Crypthecodinium cohnii on ethanol

The heterotrophic marine microalga Crypthecodinium cohnii produces docosahexaenoic acid (DHA), a polyunsaturated fatty acid with food and pharmaceutical applications. So far, DHA production has been studied with glucose and acetic acid as carbon sources. This study investigates the potential of ethanol as an alternative carbon source for DHA production by C. cohnii. In shake-flask cultures, the alga was able to grow on ethanol. The specific growth rate was optimal with 5 g l(-1) ethanol and growth did not occur at 0 g l(-1) and above 15 g l(-1). By contrast, in fed-batch cultivations with a controlled feed of pure ethanol, cumulative ethanol addition could be much higher than 15 g l(-1), thus enabling a high final cell density and DHA production. In a representative fed-batch cultivation of C. cohnii with pure ethanol as feed, 83 g dry biomass l(-1), 35 g total lipid l(-1) and 11.7 g DHA l(-1) were produced in 220 h. The overall volumetric productivity of DHA was 53 mg l(-1 )h(-1), which is the highest value reported so far for this alga.     

Batch cultivation of Methylosinus trichosporium OB3b. I: Production of soluble methane monooxygenase

Methanotrophs have promising applications in bioremediation and in the production of fuel-related chemicals due to their nonspecific enzyme, methane monooxygenase (MMO). The optimal conditions for cell growth and production of the soluble from of MMO (sMMO) were determined from batch cultivations of an obligatory methanotrophs, Methylosinus trichosporium OB3b, in shake flasks and a 5-L bioreactor. It was confirmed that a copper deficiency is essential for the formation of the cytoplasmic sMNO. Optimum cell growth without added copper was observed at pH 6.0-7.0, temperature of 30-34 degrees C, and phosphate concentration of 10-40 mM. In the bioreactor experiments, external CO(2) addition eliminated the long lag period observed in the absence of added CuSO(4), i.e., prior to the exponential cell growth phase. When methane was continuously supplied, the profile of the cell growth showed two different phases depending on the availability of nitrate, an initial fast exponential growth phase (specific growth rate, mu = 0.08 h(-1)) and a later slow growth phase (mu = 0.008 h(-1)). The cell density at the transition from a fast to a slow growth rate was proportional to the initial medium nitrate concentration in the range 5-20 mM and cell yield was estimated to be 7.14 g dry cell wt/g N. Whole-cell sMNO activity remained essentially constant regardless of the growth rate unit cell growth stopped. With an initial medium iron concentration below 40 mM, an abrupt decrease in sMNO activity was observed. The lower sMNO activity could be restored by supplying additional iron to the bioreactor culture. Cell yield on iron was estimated to be 1.3 x 10(3) g dry cell wt/g Fe.