Production of biomass and lutein by Chlorella protothecoides at various glucose concentrations in heterotrophic cultures

The influence of initial glucose concentrations on the production of biomass and lutein by Chlorella protothecoides CS-41 was investigated in batch cultures using both shake flasks and fermentors. The maximum biomass concentration increased from 4·9 to 31·2 g litre⁻¹ dry cells with an increase in initial glucose concentration from 10 to 80 g litre⁻¹. An even higher initial glucose concentration (100 g litre⁻¹) resulted in a lower biomass concentration, a lower specific growth rate, a lower growth yield coefficient and a considerably longer lag phase, which might be due to substrate inhibition. The initial glucose level also had a significant effect on the production of lutein. In a 3·7-litre fermentor an increase in lutein production from 19·39 to 76·56 mg litre⁻¹ was obtained with an increase in initial glucose concentration from 10 to 40 g litre⁻¹, within which range, lutein yield coefficient was constant (Y_Itn=1·90±0·02 mg g⁻¹). A simple substrate inhibition model was developed, which fitted the experimental data better than the classical Haldane model. A group of time-dependent kinetic models for algal cultivation in fermentors were also constructed, which were in good agreement with the experimental results and could be employed to predict the production of biomass and lutein, and the consumption of glucose in fermentor cultures.     

Effect of initial bacteria concentration on hydrogen gas production from cheese whey powder solution by thermophilic dark fermentation

Dark fermentative hydrogen gas production from cheese whey powder solution was realized at 55°C. Experiments were performed at different initial biomass concentrations varying between 0.48 and 2.86 g L^?1 with a constant initial substrate concentration of 26 ± 2 g total sugar (TS) per liter. The highest cumulative hydrogen evolution (633 mL, 30°C), hydrogen yield (1.56 mol H₂ mol^?1 glucose), and H₂ formation rate (3.45 mL h^?1) were obtained with 1.92 g L^?1 biomass concentration. The specific H₂ production rate decreased with increasing biomasss concentration from the highest value (47.7 mL g^?1 h^?1) at 0.48 g L^?1 biomass concentration. Total volatile fatty acid concentration varied beetween 10 and 14 g L^?1 with the highest level of 14.2 g L^?1 at biomass concentration of 0.48 g L^?1 and initial TS content of 28.4 g L^?1. The experimental data were correlated with the Gompertz equation and the constants were determined. The most suitable initial biomass to substrate ratio yielding the highest H₂ yield and formation rate was 0.082 g biomass per gram of TS. © 2012 American Institute of Chemical Engineers Biotechnol. Prog., 28: 931–936, 2012     

Hydrogen production by Rhodobacter sphaeroides strain O.U.001 using spent media of Enterobacter cloacae strain DM11

Combined dark and photo-fermentation was carried out to study the feasibility of biological hydrogen production. In dark fermentation, hydrogen was produced by Enterobacter cloacae strain DM11 using glucose as substrate. This was followed by a photo-fermentation process. Here, the spent medium from the dark process (containing unconverted metabolites, mainly acetic acid etc.) underwent photo-fermentation by Rhodobacter sphaeroides strain O.U.001 in a column photo-bioreactor. This combination could achieve higher yields of hydrogen by complete utilization of the chemical energy stored in the substrate. Dark fermentation was studied in terms of several process parameters, such as initial substrate concentration, initial pH of the medium and temperature, to establish favorable conditions for maximum hydrogen production. Also, the effects of the threshold concentration of acetic acid, light intensity and the presence of additional nitrogen sources in the spent effluent on the amount of hydrogen produced during photo-fermentation were investigated. The light conversion efficiency of hydrogen was found to be inversely proportional to the incident light intensity. In a batch system, the yield of hydrogen in the dark fermentation was about 1.86 mol H₂ mol⁻¹ glucose; and the yield in the photo-fermentation was about 1.5–1.72 mol H₂ mol⁻¹ acetic acid. The overall yield of hydrogen in the combined process, considering glucose as the preliminary substrate, was found to be higher than that in a single process.     

Dynamics and stability analysis of the growth and astaxanthin production system of Haematococcus pluvialis

This paper investigated high cell density cultivation of Haematococcus pluvialis for astaxanthin production in 3.7-L bioreactors. A biomass concentration of 2.74 g L⁻¹and an astaxanthin yield of 64.4 mg L⁻¹ were obtained. Based on the experimental results, a new and simple dynamic model is proposed, differing from Monod kinetics, to describe cell growth, product formation and substrate consumption. Good agreement was found between the model predictions and experimental data. The model revealed that there was cell growth inhibition on product formation and product feedback compensation for substrate consumption, but no substrate inhibition or product inhibition of cell growth. Stability analysis demonstrated that no multiplicity of steady states was observed; the unique positive steady state was locally asymptotically stable; and the effect of dilution rate on steady states was greater than that of the initial substrate concentration. Received 23 February 1999/ Accepted in revised form 08 June 1999     

Fermentation of <Emphasis Type="SmallCaps">d</Emphasis>-glucose and <Emphasis Type="SmallCaps">d</Emphasis>-xylose mixtures by <Emphasis Type="Italic">Candida tropicalis</Emphasis> NBRC 0618 for xylitol production

The fermentation of d-glucose and d-xylose mixtures by the yeast Candida tropicalis NBRC 0618 has been studied under the most favourable operation conditions for the culture, determining the most adequate initial proportion in these sugars for xylitol production. In all the experiments a synthetic culture medium was used, with an initial total substrate concentration of 25 g L⁻¹, a constant pH of 5.0 and a temperature of 30 °C. From the experimental results, it was deduced that the highest values of specific rates of production and of overall yield in xylitol were achieved for the mixtures with the highest percentage of d-xylose, specifically in the culture with the initial d-glucose and d-xylose concentrations of 1 and 24 g L⁻¹, respectively, with an overall xylitol yield of 0.28 g g⁻¹. In addition, the specific rates of xylitol production declined over the time course of the culture and the formation of this bioproduct was favoured by the presence of small quantities of d-glucose. The sum of the overall yield values in xylitol and ethanol for all the experiments ranged from 0.26 to 0.56 g bioproduct/g total substrate.     

Production of a microbial lipase by Staphylococcus carnosus (pLipMut2) in a bubble column reactor and a centrifugal field bioreactor

Extracellular lipase production by the recombinant strain Staphylococcus carnosus (pLipMut2) has been studied. First substrate optimization was carried out in shaken cultures. As a result, the best substrate yield of 20 units/g (peptone + yeast extract) and maximum lipase activity in the culture supernatant of 1.7 units/cm³ could be obtained by a nutrient rich complex medium consisting of 75 kg/m³ yeast extract, 15 kg/m³ tryptone, 5 kg/m³ glucose and 0.5 kg/m³ K₂HPO₄. Higher initial substrate concentration caused inhibition of growth. Antifoam agent at higher levels than 1 cm³/ dm³ resulted in a negative influence on lipase yield. Comparative fermentation studies have been carried out in a bubble column reactor and in a centrifugal field bioreactor. Direct proportionality between growth, lipase production and oxygen consumption was observed. In the bubble column reactor usual superficial air velocities (4 cm/s) caused intensive foam generation, thus fermentation was only possible after installation of a broader column head to allow coalescence. In the centrifugal field bioreactor higher productivities were obtained without foam problems at superficial gas velocities which were one order of magnitude lower than in the bubble column. Fermentations have been performed batchwise and without holding pH constant. Neither pH control nor glucose feeding could improve the substrate yield further. Compared to former fermentation studies with the strain S. carnosus (pLipPS1) lipase yield (lipase activity/cell density) could be improved by 300% and substrate yield (lipase activity/substrate concentration) by 600%.     

Evaluation of alpha-galactosidase biosynthesis by Streptomyces griseoloalbus in solid-state fermentation using response surface methodology

Aim: The present study was aimed at evaluating the effects of the three crucial factors, galactose concentration, inoculum size and moisture content, on α‐galactosidase production by the filamentous actinobacterium Streptomyces griseoloalbus in solid‐state fermentation. Methods and Results: Central Composite design was adopted to derive a statistical model for the optimization of fermentation conditions. Maximum α‐galactosidase yield (117 U g^–1 of dry fermented substrate) was obtained when soya bean flour supplemented with 1·5% galactose and with initial moisture content of 40% was inoculated with 1·9 × 10⁶ CFU g^?1 initial dry substrate. Conclusions: The model was valid and could result in considerably enhanced enzyme yield. Significance and Impact of the Study: The results indicated a cost effective method for the production of α‐galactosidase using soya bean flour. This is the first report on exploitation of the potential of filamentous bacterium for the production of α‐galactosidase, an enzyme having versatile applications.     

Fed-batch fermentation for production of Kluyveromyces marxianusFII 510700 cultivated on a lactose-based medium

A strain of Kluyveromyces marxianus was grown in batch culture in lactose-based media at varying initial lactose concentrations (10–60 g L^–1) at 30°C, pH 5.0, dissolved oxygen concentrations greater than 20%. Increasing the concentration of mineral salts three-fold at 40 g L^–1 and 60 g L^–1 initial lactose concentration showed only a small increase in the yield of biomass, from 0.38 g g^–1 to 0.41 g g^–1, indicating that the initial batch cultures were not significantly nutrient- (mineral salts)-limited. A relatively high biomass concentration (105 g L^–1) was obtained in fed-batch culture following extended lactose feeding. An average specific growth rate (0.27 h^–1), biomass yield (0.38 g g^–1) and overall productivity (2.9 g L^–1 h^–1) were obtained for these fed-batch conditions. This fed-batch protocol provides a strategy for achieving relatively high concentrations and productivities of K. marxianus on other lactose-based substrate streams (e.g., whey) from the dairy industry.     

Ethanol production from sweet sorghum juice in batch and fed-batch fermentations by <Emphasis Type="Italic">Saccharomyces cerevisiae</Emphasis>

Sweet sorghum juice supplemented with 0.5% ammonium sulphate was used as a substrate for ethanol production by Saccharomyces cerevisiae TISTR 5048. In batch fermentation, kinetic parameters for ethanol production depended on initial cell and sugar concentrations. The optimum initial cell and sugar concentrations in the batch fermentation were 1 × 10⁸ cells ml⁻¹ and 24 °Bx respectively. At these conditions, ethanol concentration produced (P), yield (Y _ps) and productivity (Q _p ) were 100 g l⁻¹, 0.42 g g⁻¹ and 1.67 g l⁻¹ h⁻¹ respectively. In fed-batch fermentation, the optimum substrate feeding strategy for ethanol production at the initial sugar concentration of 24 °Bx was one-time substrate feeding, where P, Y _ps and Q _p were 120 g l⁻¹, 0.48 g g⁻¹ and 1.11 g l⁻¹ h⁻¹ respectively. These findings suggest that fed-batch fermentation improves the efficiency of ethanol production in terms of ethanol concentration and product yield.     

Experimental studies and two-dimensional modelling of a packed bed bioreactor used for production of galacto-oligosaccharides (GOS) from milk whey

In the present study, extensive experimental investigations and detailed theoretical analysis of a two-dimensional packed bed bioreactor, employed for the production of galacto-oligosaccharides (GOS) from milk whey were performed. Model equations, in one- and two-dimensions, capable of predicting the substrate concentration distribution in the bioreactor were developed by coupling mass balance equation with appropriate velocity distribution equation and solved numerically. Validation of the proposed model equations was done by a set of experimental data obtained from the bioreactor. The effects of reactor to catalyst particle diameter ratio (d _t/d _p), feed flowrate (10^?6–10^?9 m³ s^?1), and initial lactose concentration (50–200 kg m^?3) on substrate concentration distribution were investigated in detail. While, the distribution of substrate concentration in axial direction was independent of d _t/d _p, it was observed that for d _t/d _p <40, significant radial concentration distribution existed. It was further observed that the substrate conversion and product yield obtained experimentally showed an excellent agreement (97 ± 2 %) with the results predicted by the two-dimensional model equation, whereas, the results predicted by the one-dimensional model equation did not lie within the desired confidence level (<90 %). The results were confirmed by both curve fitting and statistical analysis. The prediction of substrate concentration distribution in axial and radial directions using the developed two-dimensional model equation is necessary for computing the bioreactor volume to achieve the desired GOS yield.     

Xylitol production from D-xylose byCandida guillermondii: Fermentation behaviour

Summary The ability ofCandida guillermondii to produce xylitol from xylose and to ferment individual non xylose hemicellulosic derived sugars was investigated in microaerobic conditions. Xylose was converted into xylitol with a yield of 0,63 g/g and ethanol was produced in negligible amounts. The strain did not convert glucose, mannose and galactose into their corresponding polyols but only into ethanol and cell mass. By contrast, fermentation of arabinose lead to the formation of arabitol. On D-xylose medium,Candida guillermondii exhibited high yield and rate of xylitol production when the initial sugar concentration exceeded 110 g/l. A final xylitol concentration of 221 g/l was obtained from 300 g/l D-xylose with a yield of 82,6% of theoretical and an average specific rate of 0,19 g/g.h.Nomenclature Q_p average volumetric productivity of xylitol (g xylitol/l per hour) - q_p average specific productivity of xylitol (g xylitol/g of cells per hour) - So initial xylose concentration (g/l) - tf incubation time (hours) - Y_P/S xylitol yield (g of xylitol produced/g of xylose utilized) - Y_E/S ethanol yield (g of ethanol produced/g of substrate utilized) - Y_X/S cells yield (g of cells/g of substrate utilized) - specific growth rate coefficient (h^–1) - _max maximum specific growth rate coefficient (h^–1)     

Comparison of saccharification process by acid and microwave-assisted acid pretreated swine manure

The saccharification process of swine manure by conventional and microwave-assisted acid pretreated were investigated using cellulose enzymes, respectively. The optima for microwave-assisted acid pretreated swine manure is achieved when swine manure of 50 g l⁻¹ of substrate concentration and water amount 40 ml was pretreated by 4% H₂SO₄ concentration with 445 W microwave powers for 30 min at pretreatment period, and temperature 50 °C, enzyme loading 2 mg g⁻¹ substrate, substrate concentration 5 g l⁻¹ and initial medium pH 4.8 at enzymes hydrolysis period by microwave-assisted acid pretreated, respectively. The optimal conditions by conventional acid pretreated is obtained when 50 g l⁻¹ swine manure was submerged in 40 ml, 4% H₂SO₄ maintained at 130 °C for 3 h at pretreatment period, and temperature 45 °C, enzyme loading 2 mg g⁻¹ substrate, substrate concentration 15 g l⁻¹ and initial medium pH 5.2 at enzymes hydrolysis period, respectively. Under the optimum conditions microwave-assisted acid pretreatment could achieve higher yield of reducing sugar, short reaction time, and lower energy consumption than from the conventional acid pretreatment, which indicates that microwave-assisted acid pretreatment is more suitable for swine manure pretreatment than by acid alone.     

Evaluation of growth yield of Spirulina (Arthrospira) sp. in photoautotrophic, heterotrophic and mixotrophic cultures

In microbial cultures, both cellular growth rate and yield (defined as the degree of substrate conversion into the biomass) are important. Although effect of culture conditions on growth kinetics has been well documented for various microbial strains, there is almost no literature concerning the effect of environmental conditions on growth equilibrium, expressed as biomass yield coefficients from substrate. The present paper discusses the effect of culture conditions: irradiance (physical substrate) and glucose concentration (chemical substrate) on biomass yield coefficients from two chemical substrates: glucose and nitrate-nitrogen in photoautotrophic, heterotrophic and mixotrophic culture of blue-green alga Spirulina (Arthrospira) sp. The efficiency of substrates incorporation into the biomass can be precisely determined only if the elemental composition of the biomass is known. The experimental results showed that culture conditions had a substantial influence on biomass yield coefficients (biomass yield from glucose and nitrate-nitrogen). It was found that, the increase of irradiance favoured increase of biomass yield coefficient from both, glucose and nitrate-nitrogen. However, in the case of yield from nitrogen in mixotrophic culture, the effect was opposite. The effect of glucose concentration was different: the higher the initial glucose concentration, the lower the biomass yield coefficients from chemical substrates.     

Effects of high product and substrate inhibitions on the kinetics and biomass and product yields during ethanol batch fermentation

In ethanol fermentation, instantaneous biomass yield of the yeast Saccharmoyces cerevisiae was found to decrease (from 0.156 to 0.026) with increase in ethanol concentration (from 0 to 107 g/L), indicating a definite relationship between biomass yield and product inhibition. A suitable model was proposed to describe this decrease which incorporates the kinetic parameters of product inhibition rather than pure empirical constants. Substrate inhibition was found to occur when substrate concentration is above 150 g/L. A similar definite relationship was observed between substrate inhibition and instantaneous biomass yield. A simple empirical model is proposed to describe the declines in specfic growth rate and biomass yield due to substrate inhibition. It is observed that product inhibition does not have any effect on product yield whereas substrate inhibition significantly affects the product yield, reflecting a drop in overall product yield from 0.45 to 0.30 as the initial substrate concentration increases from 150 to 280 g/L. These results are expected to have a significant influence in formulating optimum fermentor design variables and in developing an effective control strategy for optimizing ethanol producitivity.     

Individual and combined effects of physicochemical parameters on ellagitannin acyl hydrolase and ellagic acid production from ellagitannin by <Emphasis Type="Italic">Aspergillus oryzae</Emphasis>

The individual and interactive effects of physicochemical parameters on ellagitannin acyl hydrolase activity and ellagic acid production by Aspergillus oryzae using ellagitannins from acorn fringe of oak as substrate were studied. Ellagitannins concentration, incubation time were identified as important physicochemical parameters influencing the enzyme synthesis and the production accumulation, and the substrate concentration with initial pH was determined to has an interactive effect on the enzyme synthesis, while ellagitannins concentration and initial pH with incubation time were found to have interactions on the production accumulation. Furthermore, the parameters were optimized by quadratic programming. Under optimum condition, the fermentation run lasted 84 h with 4 g L⁻¹ ellagitannins concentration, yielding 17.7% ellagic acid. However, the maximum enzyme activity was obtained in 96 h with 5 g L⁻¹ substrate concentration. The research demonstrated a possible way to develop an efficient approach for recovery of higher added-value product (ellagic acid) from forestry byproduct (acorn fringe of oak).     

Selection and Optimization of Culture Medium for Exopolysaccharide Production by Coriolus (Trametes) Versicolor

Summary Coriolus versicolor is a medicinal fungus producing exopolysaccharides (EPS). Five well-defined culture media were studied to select the medium that maximizes production of EPS by C. versicolor. Biomass, reducing sugars and EPS concentrations along with the rheological behaviour of the broth were followed during fermentations lasting 9 days. The yeast malt extract medium (YM) was shown to yield the highest production of EPS. Fermentation conditions with YM medium were further investigated to optimize EPS production by C. versicolor. An experimental design to do this was adopted, in which the effects of pH and initial substrate concentration were considered. The effects of initial glucose concentration (5, 15 and 25 g l⁻¹) and pH (4.0, 5.5 and 7.0) were evaluated. The initial glucose concentration was found to be the most important factor in EPS production and also cell growth.     

Kinetics of batch ethanol fermentation of cheese-whey powder (CWP) solution as function of substrate and yeast concentrations

A lactose utilizing yeast strain, Kluyveromyces marxianus DSMZ-7239 was used for ethanol formation from cheese-whey powder (CWP) solution in batch experiments. Effects of initial substrate (CWP) and yeast concentrations on the rate and extent of ethanol formation were investigated. The initial pH and oxidation-reduction potential (ORP) was kept at 5 and -250 mV, respectively. The rate and extent of ethanol formation increased with increasing CWP concentration up to 156 g l(-1) (75 g l(-1) sugar) and then decreased for larger CWP concentrations due to substrate inhibition at high sugar concentrations. The ethanol yield coefficient was also maximum (0.54 g EtOH/g sugar) and equal to the theoretical yield at CWP concentration of 156 g l(-1). The growth yield coefficient was found to be Y(x/s)=1.2+/-0.1g biomass g sugar(-1). The rate of sugar utilization and ethanol formation also increased linearly with increasing initial biomass concentrations. A kinetic model describing the rate of sugar utilization and substrate inhibition as function of the initial substrate and the biomass concentrations was developed. The kinetic constants were determined using the experimental data. Model predictions of sugar utilization rates were in good agreement with the experimental data. The results indicated that the initial sugar concentration should be below 75 g l(-1) (CWP<156 g l(-1)) and the initial biomass should be above 850 mg l(-1) to obtain high rates and yields of ethanol formation and to avoid substrate inhibition.     

Phenol degradation by a psychrotrophic strain of Pseudomonas putida

Summary Cell growth and phenol degradation kinetics were studied at 10°C for a psychrotrophic bacterium, Pseudomonas putida Q5. The batch studies were conducted for initial phenol concentrations, S_o, ranging from 14 to 1000 mg/1. The experimental data for 14<=S_o<=200 mg/1 were fitted by non-linear regression to the integrated Haldane substrate inhibition growth rate model. The values of the kinetic parameters were found to be: _m=0.119 h^–1, K _S=5.27 mg/1 and K _I=377 mg/1. The yield factor of dry biomass from substrate consumed was Y=0.55. Compared to mesophilic pseudomonads previously studied, the psychrotrophic strain grows on and degrades phenol at rates that are ca. 65–80% lower. However, use of the psychrotrophic microorganism may still be economically advantageous for waste-water treatment processes installed in cold climatic regions, and in cases where influent waste-water temperatures exhibit seasonal variation in the range 10–30°C.Nomenclature K _S saturation constant (mg/l) - K _I substrate inhibition constant (mg/l) - specific growth rate (h^–1) - _m maximum specific growth rate without substrate inhibition (h^–1) - _max maximum achievable specific growth rate with substrate inhibition (h^–1) - S substrate (phenol) concentration (mg/l) - S_o initial substrate concentration (mg/l) - S_max substrate concentration corresponding to _max (mg/l) - t time (h) - X cell concentration, dry basis (mg DW/l) - X_f final cell concentration, dry basis (mg DW/l) - X_o initial cell concentration, dry basis (mg DW/l) - Y yield factor (mg DW cell produced/mg substrate consumed)     

Effect of controlled substrate feeding on butyric acid production byClostridium tyrobutyricum

Summary Production of butyric acid from wheat flour hydrolysate was studied withClostridium tyrobutyricum. The mode of substrate supply was found a key parameter for fermentation performance as large improvements were obtained by feeding with a non-limiting supply of substrate. With this procedure, increases in product concentration and productivity but also in selectivity and yield for butyrate were obtained. Substrate feeding controlled by the rate of gas production was found preferable to constant rate feeding for reason of convenience and flexibility. In these conditions, a butyrate concentration of 62.8 gl^–1 was obtained with a productivity of 1.25 gl^–1 h^–1, a selectivity of 91.5% and a yield of 0.45 g per g of glucose.     

Biotransformation of phenylpyruvic acid to l-phenylalanine using a strain of Pseudomonas fluorescens ATCC 11250 with high transaminase activity

The rate of l-phenylalanine production from phenylpyruvic acid by whole cells of Pseudomonas fluorescens strain ATCC 11250 was greater than 3 g·l^-1 h^-1. Synthesis of transaminase was constitutive but activity was greatest in medium containing d- or l- phenylalanine as sole nitrogen source. Maximum conversion was observed at 34–40° C and at alkaline pH, with over six times initial rate of conversion at pH 12 than at pH 5. The optimum catalyst (cell) concentration was between 10–20 mg ml^-1 dry weight. The initial rate of conversion was directly proportional to phenylpyruvate concentration, up to 4%, but the conversion yield steadily decreased between 2% and 4% substrate concentration. The rate of conversion, as expected, increased as the concentration of glutamate increased. Whole cells were still capable of over 63% conversion after 40 days providing reactions were supplemented with pyridoxal phosphate. Immobilisation of cells in calcium alginate and operation of a packed bed bioreactor enabled the continuous production of l-phenylalanine in concentrations greater than 15 g·l^-1 after 60 days operation.