Applicability of Euglena gracilis for biorefineries demonstrated by the production of α-tocopherol and paramylon followed by anaerobic digestion.

In this study the use of Euglena gracilis biomass for α-tocopherol, paramylon and biogas production in a value-added chain was investigated. Therefore, we analyzed the dry cell weight and product concentrations at different growth phases during heterotrophic, photoheterotrophic and photoautotrophic cultivation in a low-cost minimal medium. Furthermore, the specific biogas yields for differently derived biomass with and without product recovery were investigated. We demonstrate that growth phase and cultivation mode not only have a significant impact on product formation, but also influence the yield of biogas obtained from anaerobic digestion of Euglena gracilis biomass. The maximum dry cell weight concentration ranged from 12.3±0.14gL(-1) for heterotrophically to 3.4±0.02gL(-1) for photoautotrophically grown Euglena gracilis cells. The heterotrophically grown biomass accumulated product concentrations of 5.3±0.12mgL(-1) of α-tocopherol and 9.3±0.1gL(-1) of paramylon or 805±10.9mL of biogasgvs(-1) (per gram volatile solids). The results for photoautotrophically grown cells were 8.6±0.22mgL(-1) of α-tocopherol and 0.78±0.01gL(-1) of paramylon or 648±7.2mL of biogasgvs(-1). For an energy-saving downstream procedure the extracting agent methanol does not have to be removed strictly. Samples with residual methanol showed a significantly increased biogas yield, because the solvent can be used as an additional substrate for methane production by archaebacteria.

Beta-glucanase productivity improvement via cell immobilization of recombinant Escherichia coli cells in different matrices.

The studies have been performed to analyze the production of beta-glucanase by a recombinant strain of Escherichia coli immobilized in different matrices. Porous sintered glass SIRAN, Ceramic supporting matrices and Broken Pumice stone as well as SIRAN Raschig-rings were examined for the immobilization of whole bacterial cells. The beta-glucanase activity of bacteria immobilized in CeramTec PST 5 (4-5 mm) was very low. CeramTec PST 5 (1.5-2.5 mm) was found to be the best carrier compared to all other matrices regarding glucanase production (630 U/ml) and compared to enzyme activity produced by free cells (500 U/ml). Different doses of matrices were applied (2, 5, 7, 10 g/lask) in the form of "matrix weight". Using 2 g/flask of CeramTec PST 5 (1.5-2.5 mm) yielded enzyme activity of 630 U/ml). CeramTec gives highest operational stability of beta-glucanase by repeated batch fermentation to 5 cycles, and activity reached 660 U/ml. Scanning electron microscopy observations showed a high number of vegetative cells that continued growth inside the matrices, indicating that beta-glucanase activity improvement was due to the immobilization of the cells.

Screening for conditions of enhanced production of a recombinant beta-glucanase secreted into the medium by Escherichia coli.

The extracellular production of a hybrid bacterial beta-glucanase using Escherichia coli was studied by using combinations of promoters of varying strength for both a beta-glucanase as the target protein and the Kil protein as the releasing factor. Four strains with different combinations of promoter strengths were cultivated in shake-flasks on four different media to assess the cross-influence of promoter and medium in a general manner. Promoters were taken from natural as well as synthetic sequences known to exhibit either weak or strong promoter strength. By far the highest extracellular glucanase activity (>200 U ml(-1)) was achieved when a strain harbouring the kil gene under control of a strong synthetic stationary-phase promoter and the glucanase gene under control of a strong synthetic constitutive promoter was cultivated on a complex medium mainly composed of casein peptone, yeast extract, and glycerol.

Integrated bioprocess for the production and purification of recombinant proteins by affinity chromatography in Escherichia coli.

In order to improve the effectiveness of the production of recombinant proteins in E. coli, integrated fermentation processes were developed. Therefore, expression vectors were constructed containing a strongly expressed gene for a beta-glucanase fused with a metal-chelating affinity tag and a leader peptide for directing the fusion protein into the periplasmic space. Its export into the medium was achieved by means of co-expression of a bacteriocin-release protein, the Kil protein from pColE1. Bioreactors were modified so that special devices containing metal chelate pentadentate chelator PDC resins were located within the bioreactor. Using the bioreactor with an internal device the Zn2+-PDC had a 4.3-fold higher binding capacity than metal-free PDC (12.3 and 2.6 kU ml(-1) PDC, respectively. Using the bioreactor with charged PDC in an external circuit revealed even higher beta-glucanase concentration (65.6 kU ml(-1)), i.e. 1.5-fold compared to the internal adsorbent system.

Increasing the secretion ability of the kil gene for recombinant proteins in Escherichia coli by using a strong stationary-phase promoter.

By using a beta-glucanase from Bacillus as a model protein, we investigated whether the secretion competence based on the action of the kil gene can be improved using stronger promoters for the expression of the kil gene. Since the production of extracellular target proteins also depends on the promoter strengths of the target gene, we constructed four expression vectors with all possible combinations of a weak and a strong stationary-phase promoter for the kil gene, and a weak and a strong constitutive promoter, respectively, for the beta-glucanase gene. The results of batch fermentations showed that the use of stronger promoters generally decreased the cell density. However, a drastic increase of productivity of the cells to produce and secrete beta-glucanase resulted in a significantly higher activity of extracellular beta-glucanase. The yield of extracellular beta-glucanase can be increased (to 168 %) by using a strong promoter for the beta-glucanase alone. However, the increase was much higher when the weak promoter of the kil gene was replaced by a strong stationary-phase promoter (to 221 %). An even higher yield of extracellular beta-glucanase was reached when beta-glucanase was expressed by a strong promoter in addition indicating a combinatorial effect. This shows that the extracellular production of a recombinant target gene can be optimized by tuning the promoter strengths of components, the kil gene and the target gene.

Improvement of a beta-glucanase activity test by taking into account the batch reactor balance of the test system.

Activity tests of enzymes are often applied for determining their concentration. In the easiest case, just one product concentration is measured after a given time. This often leads to nonlinear dependences of the apparent activity with enzyme protein concentration. A general solution of this problem consists in using the balance equation of the assay system, which commonly represents a batch reactor. Here, the balance equation of the batch for a general Michaelis Menten-type reaction kinetics is used as the calibration function. The correlation of the apparent activity and enzyme concentration was established by capturing the enzyme by means of metal chelate interaction owing to a hexahistidine tag attached to the beta-glucanase.

Bioactive compounds from Streptomyces nasri and its mutants with special reference to proteopolysaccharides.

The use of microbial exopolysaccharides (EPS) in the food, pharmaceutical, and chemical industries has steadily increased during the past decade. A bioactive EPS producing microorganism, Streptomyces nasri was isolated from Kuwait tropical soil and the proteopolysaccharide was tested for its antimicrobial activity. The isolate was subjected to ultraviolet (UV) radiation and acridine orange (AO) treatment to select for superior proteopolysaccharide producers. Among eight (five derived from UV exposure and three from AO exposure) morphological variants of Streptomyces nasri, two mutants showed increased EPS production, from 1.8 g/l to 2.3 g/l. The SDS-PAGE profiles of exopolysaccharides were determined. The molecular weight of the proteopolysaccharide ranged from 18 to 200 kDa. Mutants derived from UV exposure produced polysaccharides with higher molecular weight than those derived from acridine orange exposure. Acridine orange derived mutants produced lower molecular weight polysaccharides. Culture supernatants have been partially characterized and they show antimicrobial activity against a wide range of microorganisms. The structure of the exopolysaccharide was determined using NMR spectroscopy. The polysaccharide was also tested for cytotoxic activity against human brain tumor cell line using SRB assay.

Production of alkaline protease with Teredinobacter turnirae in controlled fed-batch fermentation.

By using our previously optimized media and a fed-batch operation controlled by LabVIEW Software, the key parameter for a high production of alkaline protease using the marine bacterium, Teredinobacter turnirae, was to maintain a low concentration of C and N-sources ( < 2 g sucrose l(-1) and < 0.2 g NH4C l l(-1)) using an appropriate fed-batch culture system. A maximum protease activity of 8250 U ml(-1 )was thus achieved.

Improvement of rifemycins production by Amycolatopsis mediterranei in batch and fed-batch cultures.

The production of rifamycins B and SV using glucose as main C-source by Amycolatopsis mediterranei in batch and fed-batch culture was investigated. Fed-batch culture using glucose as mono feeding substrate either in the form of pulse addition, in case of shake flask, or with constant feeding rate, in bioreactor level, proved to be an alternative production system with a significant increase in both volumetric and specific antibiotic production. The maximal concentrations of about 1146 mg/l and 2500 mg/l of rifamycins B and SV, respectively, was obtained in fed-batch culture in bioreactor level under non-oxygen limitation. On the other hand, the rate of rifamycins production was increased from 6.58 to 12.13 mg/l x h for rifamycin B and from 9.47 to 31.83 mg/l x h for rifamycin SV on the bioprocess transfer and improvement from the conventional batch cultivation in shake flask to fed-batch cultivation in stirred tank bioreactor.