High-level production of arbutin from hydroquinone in suspension cultures of Catharanthus roseus plant cells

Summary Plant cell suspensions of Catharanthus roseus efficiently converted exogenously supplied hydroquinone (HQ) into arbutin. Arbutin productivity of the cells was strongly influenced by the growth stage of the cultivated cells and by the manner of the addition of HQ. We have developed two methods: (i) cultivating suitable cells for producing arbutin at high density; (ii) efficiently adding toxic HQ to the cells. The yield of arbutin could be increased up to 9.2 g/l (45% of cell dry weight), which is the highest yield in the field of plant biotechnology. Repeated examinations and scaling up to a 20-l jar fermentor suggested that C. roseus cells stably produce arbutin in large amounts under the established conditions. Offprint requests to: S. Inomata     

Production of single cell protein from rice polishings using Candida utilis

Microbial protein was produced from defatted rice polishings using Candida utilis in shake-flasks and a 14-l fermentor to optimize fermentation conditions before producing biomass in a 50-l fermentor. The organism supported maximum values of 0.224 h⁻¹, 0.94, 1.35, 1.75, 2.12 g l⁻¹ h⁻¹, 0.62 g cells g⁻¹ substrate utilized and 0.38 g g⁻¹ for specific growth rate, true protein productivity, crude protein productivity, cell mass productivity, substrate consumption rate, cell yield, crude protein yield, respectively in 50-l fermentor studies using optimized cultural conditions. Maximum values compared favourably or were superior to published data in literature. The biomass protein in the 50-l fermentor contained 22.3, 27.8, 19.2, 9.5, 38.12, 8.5 and 0.27% true protein, crude protein, crude fibre, ash, carbon, cellulose and RNA content, respectively. The dried biomass showed a gross metabolizable energy value of 2678 kcal kg⁻¹ and contained all essential and non-essential amino acids. Yeast biomass as animal feed may replace expensive feed ingredients currently being used in poultry feed and may improve the economics of feed produced in countries like Pakistan. This revised version was published online in August 2006 with corrections to the Cover Date.     

The effect of low oxygen uptake rate on the fatty acid profile of the oleaginous yeast Apiotrichum curvatum

Summary The effect of limiting the available oxygen on the fatty acid profile of Apiotrichum curvatum ATCC 20509 during growth on sulphuric acid casein whey was studied. At oxygen uptake rates (OUR) lower than 7 mmol O₂/l per hour, applied during the oil accumulating phase of the fermentation, a decrease in total unsaturated fatty acids was observed. It was possible to decrease the unsaturated fatty acids (oleate from 55% to 41% and linoleate from 9% to 3%) by limiting the OUR of the culture to <3 mmol O₂/l per hour. However at this low OUR, a lower oil coefficient (a measure of the efficiency of lactose substrate conversion to oil) was recorded. Furthermore the fermentation time was increased. An OUR of 5 mmol O₂/l per hour appeared to be the limit below which adverse effects on oil yields and increased fermentation times occurred. At this OUR, the accumulated oil contained 45% oleate and 5% linoleate. These effects were demonstrated in a 20-l air-lift fermentor and confirmed in a scaled down 500-l industrial type bubble column fermentor. Offprint requests to: R. J. Davies     

Heterotrophic cultivation of Euglena gracilis Z for efficient production of α-tocopherol

Effects of hydrodynamic stress, dissolved oxygen (DO) concentration and carbon sources on heterotrophic α-tocopherol production by Euglena gracilis were investigated. In a jar fermentor without baffle plates, increasing the agitation speed up to 500 rpm had no significant effect on cell growth and α-tocopherol production. However, in a jar fermentor equipped with baffle plates, both the cell growth and α-tocopherol production were highly suppressed at 500 rpm. At high hydrodynamic stress, the cells secreted nucleic acid-related substances to the culture broth and the shape of the cells shifted from elongated toward spherical. High DO concentration had adverse effects on both cell growth and α-tocopherol production, the optimum DO concentration being below 0.8 ppm. In comparison with glucose, the growth rate was lower but the α-tocopherol content of the cells was almost four times higher when ethanol was used as the organic carbon source. In a fed-batch culture with ethanol, a very high cell concentration of 39.5 g L^-1 was obtained with α-tocopherol content of 1200 μg g-cell^-1. This α-tocopherol content is very close to the values reported for photoautotrophic and photoheterotrophic cultures. A very high α-tocopherol productivity of 102 μg L^-1 h^-1 was obtained, indicating that heterotrophic cultivation of E. gracilis has a very high potential as a substitute for the current method of extraction from vegetable oils. This revised version was published online in June 2006 with corrections to the Cover Date.     

Performance,kinetics, and substrate utilization in a continuous yeast fermentation with cell recycle by ultrafiltration membranes

Summary A continuous single stage yeast fermentation with cell recycle by ultrafiltration membranes was operated at various recycle ratios. Cell concentration was increased 10.6 times, and ethanol concentration and fermentor productivity both 5.3 times with 97% recycle as compared to no recycle. Both specific growth rate and specific ethanol productivity followed the exponential ethanol inhibition form (specific productivity was constant up to 37.5 g/l of ethanol before decreasing), similar to that obtained without recycle, but with greater inhibition constants most likely due to toxins retained in the system at hight recycle ratios.By analyzing steady state data, the fractions of substrate used for cell growth, ethanol formation, and what which were wasted were accounted for. Yeast metabolism varied from mostly aerobic at low recycle ratios to mostly anaerobic at high recycle ratios at a constant dissolved oxygen concentration of 0.8 mg/kg. By increasing the cell recycle ratio, wasted substrate was reduced. When applied to ethanol fermentation, the familiar terminology of substrate used for Maintenance must be used with caution: it is not the same as the wasted substrate reported here.A general method for determining the best recycle ratio is presented; a balance among fermentor productivity, specific productivity, and wasted substrate needs to be made in recycle systems to approach an optimal design.Nomenclature B Bleed flow rate, l/h - C _T Concentration of toxins, arbitrary units - D Dilution rate, h^-1 - F Filtrate or permeate flow rate, removed from system, l/h - F _o Total feed flow rate to system, l/h - K _s Monod form constant, g/l - P Product (ethanol) concentration, g/l - P _o Ethanol concentration in feed, g/l - PP} Adjusted product concentration, g/l - PD Fermentor productivity, g/l-h - R Recycle ratio, F/F _o - S Substrate concentration in fermentor, g/l - S _o Substrate concentration in feed, g/l - V Working volume of fermentor, l - V _MB Viability based on methylene blue test - X Cell concentration, g dry cell/l - X _o Cell concentration in feed, g/l - Y _ATP Cellular yield from ATP, g cells/mol ATP - Y _ATPS Yield of ATP from substrate, mole ATP/mole glucose - Y _G True growth yield or maximum yield of cells from substrate, g cell/g glucose - Y _P Maximum theoretical yield of ethanol from glucose, 0.511 g ethanol/g glucose - Y _P/S Experimental yield of product from substrate, g ethanol/g glucose - Y _x/s Experimental yield of cells from substrate, g cell/g glucose - S _NP/X Non-product associated substrate utilization, g glucose/g cell - k ₁, k₂, k₃, k₄ Constants - k ₁ ^APP , k ₂ ^APP Apparent k ₁, k₃ - k ₁ ^TRUE True k ₁ - m Maintenance coefficient, g glucose/g cell-h - m ^* Coefficient of substrate not used for growth nor for ethanol formation, g glucose/g cell-h - Specific growth rate, g cells/g cells-h, reported as h^-1 - _m Maximum specific growth rate, h^-1 - v Specific productivity, g ethanol/g cell-h, reported as h^-1 - v _m Maximum specific productivity, h^-1     

Production of single cell protein through fermentation of a perennial grass grown on saline lands with <Emphasis Type="Italic">Cellulomonas biazotea</Emphasis>

Microbial protein from alkali-treated Leptochloa fusca (kaller grass) was produced by growing Cellulomonas biazoteain shake flasks and in an aerated 6-l fermentor. Single cell protein, produced in the fermentor contained 56.10 ± 4.64, 60.00 ± 5.04, 11.50 ± 1.34, 12.95 ± 1.24, 3.50 ± 0.24 and 1.00 ± 0.44 true protein, crude protein, crude fibre, ash, cellulose and RNA content respectively. Maximum values compared favourably with published data. The biomass contained all desired amino acids with isoleucine as limiting acid. The dried biomass showed a gross metabolizable energy value of 3500 kcal kg⁻¹ and indicated that it might serve as energy as well as a protein source particularly when fed to poultry.     

High cell density fermentation of <Emphasis Type="Italic">Gluconobacter oxydans</Emphasis> DSM 2003 for glycolic acid production

Gluconobacter oxydans has a lower biomass yield. Uniform design (UD) was applied to determine the optimum composition of the critical media and their mutual interactions for increased biomass yield of Gluconobacter oxydans DSM 2003 in shake flasks. Fed-batch fermentation process for biomass was optimized in a 3.7-l fermentor. By undertaking a preliminary and improved fed-batch fermentation-process strategy, a cell density of 6.0 g/l (DCW) was achieved in 22 h and 14.1 g/l (DCW) in 35 h, which is the highest cell density of G. oxydans produced thus far in a 3.7-l bioreactor. The biomass production was increased by 135% compared with that using the original cultivation strategy. Bioconversion of ethylene glycol to glycolic acid was catalyzed by the resting cells of G. oxydans DSM 2003, and conversion rate reached 86.7% in 48 h. In summary, the approach including high-density fermentation of G. oxydans DSM 2003 and bioconversion process was established and proved to be an effective method for glycolic acid production.     

High-level production of arachidonic acid by fed-batch culture of <Emphasis Type="Italic"> Mortierella alpina</Emphasis> using NH<Subscript>4</Subscript>OH as a nitrogen source and pH control

Mortierella alpina was grown in a fed-batch culture using a 12-l jar fermenter with an initial 8-l working volume containing 20 g glucose l⁻¹ and 10 g corn-steep powder l⁻¹. Glucose was intermittently fed to give 32 g l⁻¹ at each time. The pH of culture was maintained using 14% (v/v) NH₄OH, which also acted as a nitrogen source. A final cell density of 72.5 g l⁻¹ was reached after 12.5 days with a content of arachidonic acid (ARA) at 18.8 g l⁻¹. These values were 4 and 1.8 times higher than the respective values in batch culture. Our results suggest that the combined feeding of glucose and NH₄⁺ to the growth of M. alpina could be applied for the industrial scale production of ARA.     

A study of polynucleotide phosphorylase production by <Emphasis Type="Italic">Escherichia coli</Emphasis> in a hollow fibre reactor

A 30-l hollow fibre reactor with continuous fermentation for cell recycling of Escherichia coli AS 1.183 was used to remove the inhibitory effects on cell growth and extend the fast growth phase to increase the yield of polynucleotide phosphorylase (PNPase) in E. coli cells. When the dilution rate was 1.5 h⁻¹, the cell concentration of E. coli reached 235 g/l (wet wt, 70% moisture content), with PNPase activity above 90 u/g (wet wt). With the dilution rate is 1.0 h⁻¹, the fermentor volumetric productivity of PNPase in a hollow fiber reactor can reach 974 (u/h * l) compared to 20 (u/h * l) in a conventional batch culture.     

Effect of ventilation on the production of acetaldehyde by Zymomonas mobilis

The production of acetaldehyde, a flavoring agent in food, by Zymomonas mobilis was carried out in batch culture. The volatilization rate constant (k_v) of acetaldehyde and the initial volumetric oxygen transfer coefficient (k_La⁰) in an Erlenmeyer flask with a cotton-plug (cotton-flask) and an aerated-flask with a forced-air system (aerated-flask) were measured. The culture environment in the aerated-flask was found to be very different from that in the cotton-flask. Cell growth in a cotton-flask was strongly inhibited, making practical acetaldehyde production in cotton-flask very difficult. On the other hand, acetaldehyde production in the aerated-flask increased while the fermentation time decreased with increases in the air flow rate. The k_v value of acetaldehyde in a jar fermentor was affected mainly by air flow rate. By considering both the oxygen transfer rate and the ventilation effect on the culture, it was possible to scale-up from the aerated-flask to a jar fermentor. In the jar fermentor, production of acetaldehyde and growth inhibition by acetaldehyde were affected mainly by the k_La⁰ and k_v, values, respectively. The overall production of acetaldehyde in the jar fermentor under the optimum k_La⁰ and k_v conditions was 6.64 g/l (Y_p/s: 0.27), which was about 1.5 times higher than the maximum concentration obtained in the aerated-flask.     

Production of C<Subscript>35</Subscript> isoprenoids depends on H<Subscript>2</Subscript> availability during cultivation of the hyperthermophile<Emphasis Type="Italic"> Methanococcus jannaschii</Emphasis>

A series of five progressively saturated C₃₅ isoprenoids has been identified in cell-free extracts of the deep-sea methanogen Methanococcus jannaschii. Production and relative abundance of the isoprenoids were dependent on culture conditions; significant production occurred in a 16-l fermentor (12-l working volume) and a 2.5-l fermentor (2-l working volume) but could not be duplicated in serum bottles. Several factors were investigated and shown not to account for the different production levels, including medium composition, pH, and temperature. However, the interphase mass transfer rate was shown to significantly affect the production of C₃₅ isoprenoids in a fermentor. The structures of the novel isoprenoids were confirmed by hydrogenation reactions and mass spectra of the isoprenoids. Indirect evidence based on genomics and mass spectrometry data implicates head-to-head condensation of farnesyl pyrophosphate (C₁₅) with geranylgeranyl pyrophosphate (C₂₀) as the mechanism for C₃₅ synthesis.Communicated by J. WiegelB.P. Manquin and J.A. Morgan contributed equally to this work.     

Production of bacterial cellulose by Acetobacter xylinum BPR2001 using molasses medium in a jar fermentor

Bacterial cellulose (BC) production by Acetobacter xylinum subsp. sucrofermentans BPR2001 using molasses medium was carried out in a jar fermentor. When molasses was subjected to H₂SO₄-heat treatment, the maximum BC concentration increased to 76% more than that achieved using untreated molasses, and the specific growth rate increased 2-fold. When the initial sugar concentrations in the H₂SO₄-heat treated molasses were varied from 23 g/l to 72 g/l, BC concentration, production rate, and yield were maximum at sugar concentrations of 23 g/l and 37 g/l, and production of by-products, such as polysaccharides and CO₂, was lower than at sugar concentrations of 48 g/l and 72 g/l, indicating that maintaining a lower molasses concentration is essential for efficient BC production in jar fermentors, this being due mainly to the complex nature of molasses. Molasses has a clear advantage over pure sugars as a carbon source from an economic viewpoint.     

High expression of Trigonopsis variabilis -amino acid oxidase in Pichia pastoris

To explore a new approach of high expression of -amino acid oxidase (DAAO) in Pichia pastoris, a gene encoding DAAO from Trigonopsis variabilis (TvDAAO gene) deleted intron was prepared by PCR amplification and cloned into the intracellular expression vector pPIC3.5K. The expression plasmid pPIC3.5K-DAAO linearized by SalI was transformed into Pichia pastoris strain GS115 (his⁻mut⁺). By means of MM and MD plates and PCR, the recombinant P. pastoris strains (his⁺mut⁺) were obtained. Activity assay and SDS-PAGE demonstrated that DAAO was intracellularly expressed in P. pastoris with the induction of methanol. The recombinant strain PD27 with the highest expression of DAAO was screened through activity assay and its high-density fermentation was carried out in a 1-l fermentor. Activity assay and SDS-PAGE demonstrated that DAAO was intracellularly expressed in P. pastoris with the induction of methanol. The recombinant cells with high expression of DAAO were screened and the high-density fermentation was carried out in a 1-l fermentor. Interestingly, the DAAO expression level reached up to 473 U/g dry cell weight in fermentation yield. Finally, 1-hexanol was used to break recombinant cells and the specific activity of DAAO was 1.46 U/mg protein in crude extraction.     

Transformation of Acetobacter polyoxogenes with Plasmid DNA by Electroporation

Acetobacter polyoxogenes was transformed with plasmid DNA by electroporation. The following points were essential for transformation: (i) dilution of the culture broth with cold water and air bubbling of the culture broth for transformation at discharging from a jar fermentor, and (ii) selection of transformants by liquid cultivation. For shortening of the lag time in cultivation for selection of transformants, the following treatments were useful: (i) addition of sucrose to the cell suspension during transformation and to the broth for cultivation, and (ii) addition of 1 mm MgCl₂ to a mixture of cells and DNA during electroporation.     

Hydroxyethylation of Comenic Acid

A small jar fermentor was developed in order to investigate the effect of oxygen supply on hydrocarbon fermentation. Several indices to oxygen transfer were examined with this small jar fermentor. Conditions for suitable oxygen supply were examined in l-glutamic acid fermentation from hydrocarbon by use of shaking flasks and these small jar fermentors. The data indicated that the rate of oxygen transfer ought to be more than 14.3 × 10^?7 mole/ml·min in order to obtain satisfactory results. The coefficient of oxygen transfer rate (K_La/H) decreased as the fermentation went on, so the supply of oxygen enriched gas mixture was effective to increase the production of l-glutamic acid.     

Influence of linearly decreasing feeding rates on fed-batch ethanol fermentation of sugar-cane blackstrap molasses

Summary The ethanol yield was not affected and the ethanol productivity increased (10%) when linearly decreasing feeding rates were used instead of constant feeding rates in fed-batch ethanol fermentations.Nomenclature F reactor feeding rate (L.h^–1) - M_E mass of ethanol in the fermentor (g) - M_s mass of TRS in the fermentor (g) - M_x mass of yeast cells (dry matter) in the fermentor (g) - P ethanol productivity (g.L^–1.h^–1) - s standard deviation - S_o TRS concentration in the feeding mash (g.L^–1) - t time (h) - T fermentor filling-up time (h) - TRS total reducing sugars calculated as glucose (g.L^–1) - X_o yeast cells concentration (dry matter) in the inoculum (g.L^–1) - average ethanol yield (% of the theoretical value)     

Development of a defined medium fermentation process for physostigmine production by Streptomyces griseofuscus

Physostigmine is a plant alkaloid of great interest as a therapeutic candidate for the treatment of Alzheimer's disease. Fortunately, this compound is also produced by Streptomyces griseofuscus NRRL 5324 during submerged cultivation. A fermentation process that used chemically defined medium was therefore developed for its production. By means of statistical experimentation, the physostigmine titer was quickly increased from 20 mg/l to 520 mg/l with a culture growth of 19 gl dry cell weight on the shake-flask scale. Further medium optimization resulted in a yield of 790 mg/l in a 23-l bioreactor using a batch process. A titer of 880 mg/l was attained during scale-up in a 800-l fermentor by employing a nutrient-feeding strategy. This production represents a 44-fold increase over the yield from the initial process in shake-flasks. The defined-medium fermentation broth was very amenable to downstream processing.     

Luffa cylindrica and phytosterols bioconversion: from shake flask to jar bioreactor

Bioconversion of lipophilic compounds poorly soluble in water, such as sterols, required the use of chemicals and solubilizing agents. On the other hand, it was shown that immobilization of Mycobacterium species on the dried fruit of Luffa cylindrica (DFLC) allows a close interaction between immobilized cells and cholesterol particles and increases by then the product’s yield. In this work, the use of DFLC in a 5-l jar bioreactor with phytosterols mixture (1 g/l) as substrate was assessed without addition of any chemicals or solubilizing agents. DFLC increased by a factor of four the volumetric productivity of androstenones (0.08 g/l day). Products were accumulated in the aqueous medium while substrates remained on the fibers of DFLC. This observation lets envisage a green semi-continuous process of androstenone production. DFLC has no influence on cell growth, and is moreover natural, inexpensive, non-toxic, and mechanically strong.     

Gradient of anthocyanin in cell aggregates of Daucus carota in suspension cultures

Summary The size distribution of cell aggregates, and the effect of cell aggregate size on anthocyanin content of Daucus carota cells in suspension cultures, was studied. The profile of biomass distribution in various size groups of cell aggregates indicated that over 92% of biomass was present in the aggregates of 500–1500 m in diameter. The anthocyanin content increased initially with the increase in cell aggregate diameter up to 500–850 m, and decreased rapidly with the increase in the cell aggregate size above this critical diameter. On the other hand, the surface colour intensity showed a steady increase with the increase in cell aggregate size, indicating a steep radial gradient of anthocyanin content along the radius of the larger cell aggregates.     

Production of fatty acids and lipid by a Candida sp. growing on a fraction of n-alkanes predominating in tridecane

A Candida sp. was grown on a fraction of n-alkanes (dodecane 22%, tridecane 48%, tetradecane 28%) as sole carbon source. The growth rate was increased most markedly by using high concentrations of n-alkanes (16.7% v/v). When grown in a 5 liter fermentor, the yeast reached its highest yield (60 g. of cell dry wt/l) with a concomitant high yield of fatty acids (21 g of fatty acids/l), by using a nitrogen-deficient medium. To achieve good growth, it was essential to use an inoculum (1 part into 10) of rapidly growing cells and beneficial to increase the agitation rate gradually once growth had begun. After 108 hr maximum conversions of substrate to product were: 71.5% (w/w) for alkanes into cells and 24.8% (w/w) for alkanes into fatty acids. Of the, total fatty acids at the end of the fat-accumulating phase of growth 54% were shorter in chain length than palmitic acid (C₁₆H₃₂O₂). When grown on glucose, as sole carbon source, less than 2% of the total fatty acids were shorter than palmitic acid. When n-alkanes were added to cells growing on glucose, short-chain fatty acids (C₁₀ to C₁₄) were synthesized immediately, indicating a derepressed enzyme system for hydrocarbon assimilation and the absence of diauxie. The production of these acids was at the apparent sacrifice of linoleic acid synthesis. In spite of the high conversion ratios, it is concluded that it would be uneconomical to produce fatty acids, even expensive ones such as lauric acid, by microbial transformation of n-alkanes.