Evaluation of the potential of Aspergillus niger species for the bioconversion of L-phenylalanine into 2-phenylethanol

Aspergillus niger was explored, for the first time, for the production of 2-phenylethanol (a rose-like aroma) using L-phenylalanine as precursor. Among the strains screened, A. niger CMICC 298302 was shown to produce, in a culture medium containing 6 g L-phenylalanine l^–1 and 60 g glucose l^–1, 1375 mg 2-phenylethanol l^–1 with a productivity of 153 mg l^–1 day^–1 and a molar yield of 74%. 2-Phenylethanol concentrations of 1 to 2 g l^–1 led to a two-fold and ten-fold decrease, respectively, in the mycelial radial growth rate. However, 2-phenylethanol was synthesized as the sole aromatic product and accumulated in the culture broth.     

Bioconversion of <Emphasis Type="SmallCaps">l</Emphasis>-phenylalanine into 2-phenylethanol by <Emphasis Type="Italic">Kluyveromyces marxianus</Emphasis> in grape must cultures

A 2³ factorial design was employed to find the best conditions of pH, l-phenylalanine concentration and temperature for the production of 2-phenylethanol by Kluyveromyces marxianus CBS 6556. The cultivation was carried out on grape must, which contains a great amount of nitrogen compounds. Central composite design (CCD) was used for the analysis of treatment combinations. Results showed a second-degree polynomial regression model with good agreement of experimental data, with R ² = 0.92015 (p < 0.05). The maximum production of 2-phenylethanol was found at pH 7.0, temperature of 37 °C, and a concentration of 3.0 g of l-phenylalanine L⁻¹. Further experiments in bioreactors showed that oxygen concentration is also important to 2-phenylethanol production, with best results obtained at oxygen mass transfer rates of 2.0 h⁻¹.     

Production of mannitol by a novel strain of Candida magnoliae

A novel microorganism was isolated which is able to produce mannitol when grown in the presence of fructose and glucose as carbon sources. In flask culture in a medium containing 150 g fructose l^–1, it yielded 67 g mannitol l^–1 after 168 h. In fed-batch culture with 3–12% (w/v) fructose, production reached a maximum of 209 g mannitol l^–1 after 200 h, corresponding to an 83% yield and a 1.03 g l^–1 h^–1 productivity. The isolated strain was identified as Candida magnoliae based on identical sequences in the D1/D2 domain of its 26S rDNA and a similar carbon source utilization pattern with C. magnoliae reference strains.     

Isolation and study of two strains ofLeptospirillum-like bacteria from a natural mixed population cultured on a cobaltiferous pyrite substrate

Two strains ofLeptospirillum-like bacteria, L6 and L8, have been isolated from a mixed inoculum, also containingThiobacillus ferrooxidans andT. thiooxidans, cultured for one year with a colbaltiferous pyrite as energy substrate in a 100 I continuous bioleaching laboratory unit. Several physiological properties of the strains are described. The vibrio-shaped microorganisms grew at pH values lower than 1.3. Their growth rate was maximum between 2.5 and 8.0 g l¹ ferrous iron. The optimal growth temperature was 37.5° C. Ferric iron had a stimulative effect on bacterial development up to 8 g l^–1, and growth was as rapid at 14 g l^–1 ferric iron as at 8 g l^–1. The negative influence of cobalt on the final cell concentration was observed at 0.5 g l^–1, but the growth rate was not affected up to 2 g l^–1. The G + C content of strains L8 is 55.6 mol%.     

Production potential of eicosapentaenoic acid by the diatom Nitzschia laevis

To investigate the production potential of eicosapentaenoic acid (EPA) by the diatom Nitzschia laevis, the growth characteristics and fatty acid composition of the cells were studied under photoautotrophic, mixotrophic and heterotrophic conditions of growth. The specific growth rate and maximum biomass concentration were respectively 0.466 d^–1 and 2.27 g l^–1 for mixotrophic culture, 0.344 d^–1 and 2.04 g l^–1 for heterotrophic culture, and 0.167 d^–1 and 0.5 g l^–1 for photoautotrophic culture, respectively. As for EPA production, the yield and productivity were respectively 52.32 mg l^–1 and 10.46 mg l^–1 d for mixotrophic culture, 35.08 mg l^–1 and 6.37 mg l^–1 d for heterotrophic culture, and 6.78 mg l^–1 and 3.39 mg l^–1 d for photoautotrophic culture, respectively. Results suggest that mixotrophic culture is the most suitable growth mode for the production of EPA by the diatom Nitzschia laevis. The results are useful for the development of a cost-effective fermentation process for EPA production by Nitzschia laevis.     

Levan production using mutant strains of Zymomonas mobilis in different culture conditions

Several levan hyperproducing mutants of Zymomonas mobilis strains were selected by mutagenesis with N-methyl-N-nitro-nitrosoguanidine and caffeine. Highest levan production (41 g l^–1) was obtained with a mutant strain HL 29 in a culture medium containing 200 g sucrose l^–1 and 0.5 g (NH₄)₂SO₄ l^–1 stored at 7 °C for 29 days. This is the first report describing the levan synthesis by Z. mobilis at 7 °C.     

Selective production of bikaverin in a fluidized bioreactor with immobilized Gibberella fujikuroi

The best culture medium composition for the production of bikaverin by Gibberella fujikuroi in shake-flasks, i.e. 100 g glucose l^–1; 1 g NH₄Cl l^–1; 2 g rice flour l^–1; 5 g KH₂PO₄ l^–1 and 2.5 g MgSO₄ l^–1, was obtained through a fractional factorial design and then scaled-up to a fluidized bioreactor. The effects of carbon and nitrogen concentrations, inoculum size, aeration, flow rate and bead sizes on batch bikaverin production using immobilized G. fujikuroi in a fluidized bioreactor were determined by an orthogonal experimental design. Concentrations of up to 6.83 g bikaverin l^–1 were obtained when the medium contained 100 g glucose l^–1 and 1 g NH₄Cl l^–1 with an inoculum ratio of 10% v/v, an aeration rate of 3 volumes of air per volume of medium min^–1, and a bead size of 3 mm. Based on dry weight, the bikaverin production was 30–100 times larger than found in submerged culture and approximately three times larger than reported for solid substrate fermentation.     

Factorial design and response surface optimization of crude violacein for Chromobacterium violaceum production

Initially an eleven variable, sixteen assay 2^15–11 fractional factorial design, was used to determine the key factors in the production of violacein produced by Chromobacterium violaceum, CCT 3496. Subsequently five and three factor central composite designs were executed to determine response surfaces with the aim of optimizing cellular mass and crude violacein production. The 7.5 g l^–1 dry cell mass and 0.17 g l^–1 crude violacein productions obtained with our initial culture medium were increased to 21 g l^–1 and 0.43 g l^–1, respectively, for a medium investigated in the three factor design.     

Invertase production by Aspergillus niger in submerged and solid-state fermentation

Three Aspergillus nigerstrains were grown in submerged and solid state fermentation systems with sucrose at 100 g l^–1. Average measurements of all strains, liquid vs solid were: final biomass (g l^–1), 11 ± 0.3 vs 34 ± 5; maximal enzyme titres (U l^–1) 1180 ± 138 vs 3663 ± 732; enzyme productivity (U l^–1h^–1) 20 ± 2 vs 87 ± 33 and enzyme yields (U/gX) 128 ± 24 vs 138 ± 72. Hence, better productivity in solid-state was due to a better mould growth.     

Glucose repression of xylitol production in Candida tropicalis mixed-sugar fermentations

Glucose repressed xylose utilization inCandida tropicalis pre-grown on xylose until glucose reached approximately 0–5 g l^–1. In fermentations consisting of xylose (93 g l^–1) and glucose (47 g l^–1), xylitol was produced with a yield of 0.65 g g^–1 and a specific rate of 0.09 g g^–1 h^–1, and high concentrations of ethanol were also produced (25 g l^–1). If the initial glucose was decreased to 8 g l^–1, the xylitol yield (0.79 g g^–1) and specific rate (0.24 g g^–1 h^–1) increased with little ethanol formation (<5 g l^–1). To minimize glucose repression, batch fermentations were performed using an aerobic, glucose growth phase followed by xylitol production. Xylitol was produced under O₂ limited and anaerobic conditions, but the specific production rate was higher under O₂ limited conditions (0.1–0.4 vs. 0.03 g g^–1 h^–1). On-line analysis of the respiratory quotient defined the time of xylose reductase induction.     

Culture conditions of tannase production by Lactobacillus plantarum

Lactobacillus plantarum produced an extracellular tannase after 24 h growth on minimal medium of amino acids containing 2 g tannic acid l^–1. Enzyme production (6 U ml^–1) was optimal at 37 °C and pH 6 with 2 g glucose l^–1 and 7 g tannic acid l^–1 in absence of O₂.     

Establishment of Orthosiphon stamineus Cell Suspension Culture for Cell Growth

Callus of Orthosiphon stamineus could be induced successfully from petiole, leaf and stem tissues but not roots when cultured on MS medium containing different concentration of NAA (0–4.0 mg l^–1) and 2,4-D (0–2.0 mg l^–1). Highest fresh weight callus production was obtained from leaf explants and those with best friability were obtained on MS medium plus 1.0 mg l^–1 2,4-D plus 1.0 mg l^–1 NAA. Cell suspension cultures were established from these cultures. The appropriate cell inoculum size for the best cell growth was 0.75 g of cells in 20 ml culture medium. Cell suspension culture using MS medium supplemented with 1.0 mg l^–1 2,4-D promoted the best cell growth with maximum biomass of 8.609 g fresh weight and 0.309 g dry weight 24 days after inoculation. Cells that grew in MS medium supplemented with 1.0 mg l^–1 2,4-D reached the stationary growth phase in 15 days as compared to the cells that grew in MS medium supplemented with 1.0 mg l^–1 2,4-D + 1.0 mg l^–1 NAA reached the stationary phase in 24 days. MS medium supplemented with 1.0 mg l^–1 2,4-D was considered as the maintenance medium for maintaining the optimum cell growth of O. stamineus in the cell suspension cultures with 2-week interval subculture.     

Poly-3-hydroxybutyrate (P3HB) production by bacteria from xylose,glucose and sugarcane bagasse hydrolysate

Fifty-five bacterial strains isolated from soil were screened for efficient poly-3-hydroxybutyrate (P3HB) biosynthesis from xylose. Three strains were also evaluated for the utilization of bagasse hydrolysate after different detoxification steps. The results showed that activated charcoal treatment is pivotal to the production of a hydrolysate easy to assimilate. Burkholderia cepacia IPT 048 and B. sacchari IPT 101 were selected for bioreactor studies, in which higher polymer contents and yields from the carbon source were observed with bagasse hydrolysate, compared with the use of analytical grade carbon sources. Polymer contents and yields, respectively, reached 62% and 0.39 g g^–1 with strain IPT 101 and 53% and 0.29 g g^–1 with strain IPT 048. A higher polymer content and yield from the carbon source was observed under P limitation, compared with N limitation, for strain IPT 101. IPT 048 showed similar performances in the presence of either growth-limiting nutrient. In high-cell-density cultures using xylose plus glucose under P limitation, both strains reached about 60 g l^–1 dry biomass, containing 60% P3HB. Polymer productivity and yield from this carbon source reached 0.47 g l^–1 h^–1 and 0.22 g g^–1, respectively.     

Mn2 + improves surfactin production by Bacillus subtilis

Surfactin productivity by Bacillus subtilis was increased from 0.33 g l^–1 to 2.6 g l^–1 by adding 0.01 mM Mn²⁺ to a defined glucose medium. The final yield exceeded that of most reported values for genetically improved strains.     

Production of flavour esters by Rhizopus oryzae

Microbial production of different alipathic esters with flavour characteristic has been studied. Lyophilized whole cells of Rhizopus oryzae CBS 112-07 were found to be particularly suitable to catalyse the synthesis of different flavour esters (hexyl acetate, propionate, butyrate, caprylate; geranyl acetate, propionate, butyrate and 2- and 3-methylbutyl acetate, butyrate) in n-heptane. This strain was therefore utilized for the semipreparative production of geranyl butyrate by semicontinous and continous addition of the substrates with satisfactory yields (144 g l^–1 in 264 h and 142 g l^–1 in 48 h respectively).     

Synthesis of recombinant human interleukin-2 via controlled feed of lactose-complex media in fed-batch cultures of Escherichia coli BL21(DE3)[pT7-G3IL2]

Using lactose as an inducer, recombinant human interleukin-2 (rhIL-2) was synthesized with an N-terminus fusion partner, G3 (three tandem-arranged glucagon peptides) in fed-batch cultures at high cell concentration (60–90 g l^–1) of Escherichia coli BL21(DE3) [pT7-G3IL2]. With batch additions of lactose (4 × 13.5 g), the fusion rhIL-2 was synthesized up to 9.3 g l^–1. However, if all the lactose (54 g) was added at once to the culture, synthesized fusion rhIL-2 decreased to 5.4 g l^–1 with a decreased cell growth rate. A statistical optimization of the production medium containing glucose, yeast extract, and lactose led to fusion rhIL-2 being produced at > 9 g l^–1.     

Preparation and testing of Sardinella protein hydrolysates as nitrogen source for extracellular lipase production by Rhizopus oryzae

Various fish protein hydrolysates (FPH) from sardinella (Sardinella aurita) were used as nitrogen sources for the production of extracellular lipase by the filamentous fungus Rhizopus oryzae. The best results were obtained with defatted meat–fish protein hydrolysates (DMFPH), indicating the presence in the lipid fraction of some constituents which may repress lipase synthesis. Furthermore, it was found that the extensive hydrolysis of fish proteins resulted in a higher lipase production. The use of 40 g DMFPH l^–1 for the growth of Rhizopus oryzae in medium R1 resulted in a lipase production of 394 U ml^–1, higher than the yield obtained with standard soy peptone as nitrogen source (373 U ml^–1). The most appropriate medium for the growth and the production of lipase is composed only of 24 g DMFPH l^–1 and 10 g glucose l^–1, indicating that the strain can obtain its nitrogen and salts requirements directly from fish substrate.     

Oxalic acid production from lipids by a mutant of Aspergillus niger at different pH

Crude rapeseed oil and post-refining fatty acids were used as substrates for oxalic acid production by a mutant of Aspergillus niger. Both the final concentration and the yield of the product were highest at pH 4 to 5. With a medium containing 50 g lipids l^–1, production reached a maximum of 68 g oxalic acid l^–1 after 7 d. A high yield of the product (up to 1.4 g oxalic acid g^–1 lipids consumed) was achieved with oil and fatty acids combined.     

Batch xylitol production from wheat straw hemicellulosic hydrolysate using Candida guilliermondii in a stirred tank reactor

Batch production of xylitol from the hydrolysate of wheat straw hemicellulose using Candida guilliermondii was carried out in a stirred tank reactor (agitation speed of 300 rpm, aeration rate of 0.6 vvm and initial cell concentration of 0.5 g l^–1). After 54 h, xylitol production from 30.5 g xylose l^–1 reached 27.5 g l^–1, resulting in a xylose-to-xylitol bioconversion yield of 0.9 g g^–1 and a productivity of 0.5 g l^–1 h^–1.     

L-Sorbose production in a continuous fermenter with and without cell recycle

The kinetics of continuous l-sorbose fermentation using Acetobacter suboxydans with and without cell recycle (100%) were investigated at dilution rates (D) of 0.05, 0.10, 0.15 and 0.3 h^–1. The biomass and sorbose concentrations for continuous fermentation without recycle increased as the dilution rate was increased from 0.05 to 0.10 h^–1. A maximum biomass concentration of 8.44 g l^–1 and sorbose concentration of 176.90 g l^–1 were obtained at D=0.10 h^–1. The specific rate of sorbose production and volumetric sorbose productivity at this dilution rate were 2.09 g g^–1 h^–1 and 17.69 g l^–1 h^–1. However, on further increasing the dilution rate to 0.3 h^–1, both biomass and sorbose concentrations decreased to 2.93 and 73.20 g l^–1 respectively, mainly due to washout of the reactor contents. However, the specific rate of sorbose formation and volumetric sorbose productivity at this dilution rate increased to 7.49 g g^–1 h^–1 and 21.96 g l^–1 h^–1 respectively. Continuous fermentation with 100% cell recycle served to further enhance the concentration of biomass and sorbose to 28.27 and 184.32 g l^–1 respectively (in the reactor at a dilution rate of 0.05 h^–1). Even though, there was a decline in the biomass and sorbose concentrations to 6.8 and 83.40 g l^–1 at a dilution rate of 0.3 h^–1, the specific rates of sorbose formation and volumetric sorbose productivity increased to 3.67 g g^–1h^–1 and 25.02 g l^–1 h^–1.