Operational stability of Brevibacterium imperialis CBS 489-74 nitrile hydratase

Brevibacterium imperialis CBS 489-74 was grown in broths prepared with yeast and malt extract, bacteriological peptone and 2% glucose or differently modified with the addition of Na-phosphate buffer, FeSO₄, MgSO₄ and CoCl₂. The peak production of nitrile hydratase (NHase) did not change significantly. At the stationary growth phase, the units per milliliter of broth (60 units ml⁻¹) were more important than those at the exponential growth phase.

The NHase operational stability of whole resting cells was monitored following the bioconversion of acrylonitrile to acrylamide in continuous and stirred UF-membrane reactors. The rate of inactivation was independent on buffer molarity from 25 to 75 mM and on pH from 5.8 to 7.4. Enzyme stability and activity remained unchanged in distilled water. The initial reaction rate increased from 12.8 to 23.8 g acrylamide/g dry cell/h, but NHase half-life dropped from 33 to roughly 7 h when temperature was varied from 4°C to 10°C. The addition of butyric acid up to 20 mM did not improve enzyme operational stability, and largely reduced (94%) enzyme activity. Acrylonitrile caused an irreversible damage to NHase activity. High acrylonitrile conversion (86%) was attained using 0.23 mg cells/ml in a continuously operating reactor.     

Determination of kinetic constants for a two-stage anaerobic upflow packed-bed reactor for dairy wastewater

A two-stage upflow packed-bed (reactors in series) system was used for the treatment of dairy wastewater. Nylon pads were used as supporting media for the biomass. This investigation aimed at the determination of various kinetic constants for substrate, biomass and biogas based on various models. The maximum loadings that could be applied to reactor I and reactor II were 14·29 and 5·0 kg of chemical oxygen demand (COD) per m³ per day, respectively. The maximum COD removal efficiencies at various loading rates were in the ranges of 93·8–98·5% and 72·5–84% for the two reactor systems, respectively. The combined biogas yield was between 0·196 and 0·386 m³ gas/kg COD_a.     

Medium improvement by orthogonal array designs for cholesterol oxidase production by Rhodococcus equi No. 23

Medium improvement for the production of cholesterol oxidase (CO, EC 1.1.3.6) by Rhodococcus equi No. 23 was investigated using an orthogonal array design in two steps. Results revealed that yeast extract, Tween 80 and zinc sulphate had positive effects on CO production, but magnesium sulphate had an inhibitory effect. In addition, interaction between cholesterol and sodium chloride also had a significant effect on enzyme production. The improved medium consisted of 2·0 g/litre cholesterol, 8·0 g/litre yeast extract, 1·0 g/litre NH₄Cl, 1·0 g/litre NaCl, 0·50 g/litre KH₂PO₄, 0·25 g/litre Na₂HPO₄, 0·10 g/litre -valine, 0·15 g/litre -tyrosine, 0·15 g/litre MgSO₄·7H₂O, 0·01 g/litre ZnSO₄·7H₂O, 0·10 g/litre FeSO₄·7H₂O and 4·0 ml/litre Tween 80. CO production at 60 h (about 0·24 units/ml) was about four-fold greater than with the control medium.     

Kinetic study of anaerobic digestion of brewery wastewater

A study of the kinetics of the anaerobic digestion of brewery wastewater was carried out using a 1-litre, continuous-flow, completely-mixed, bioreactor operating at 35°C and containing a saponite-immobilized biomass at a concentration of 6·2 g volatile suspended solids (VSS)/litre. The bioreactor worked satisfactorily in a range of hydraulic retention times from 1·2 to 10 days and eliminated more than 95% of the initial chemical oxygen demand (COD) in all instances.

Guiot's kinetic model was used to determine the macroenergetic parameters of the system, and showed it to have a yield coefficient for the biomass (Y) of 0·080 g VSS/g COD and a specific rate of substrate uptake for cell maintenance (m) of 0·045 g COD/g VSS day.

The experimental results showed the rate of substrate uptake (R_s; g COD/g VSS day), correlated with the concentration of biodegradable substrate (S_b; g COD/litre), through an equation of the Michaelis-Menten type.     

Ethanol production from glucose and xylose by separated and co-culture processes using high cell density systems

Media containing xylose and/or glucose were tested utilizing Zymomonas mobilis or Saccharomyces diastaticus and Pichia stipitis. The best fermentation results were obtained in separated glucose (180 g/litre) and xylose (80 g/litre) fermentations utilizing Zymomonas mobilis and Pichia stipitis strains, respectively. In these conditions, the maximum ethanol concentrations achieved were 86·2 g/litre and 29 g/litre, respectively. The complete conversion of a glucose and xylose mixture (50 g/litre) was obtained using a respiratory deficient mutant of Saccharomyces diastaticus co-cultivated with Pichia stipitis in continuous culture. Using the co-culture process, the maximum ethanol concentration was 21·5 g/litre (Yp/s=0·45 g/g) and the maximum volumetric ethanol productivity was 4·3 g/(litre × h).     

Sorbitol and Gluconate Production in a Hollow Fibre Membrane Reactor by Immobilized Zymomonas Mobilis

This study describes the results of a hollow fibre membrane reactor with immobilized treated cells of Zymomonas mobilis which produced sorbitol and gluconic acid continuously from fructose and glucose respectively. A productivity of 10-20 g sorbitol · L^-1 · h^-1 and 10-20 gluconate · L^-1 · h^-1 (based on total bioreactor volume) from a feed of 100 g · L^-1 each of glucose and fructose was possible at high dilution rates. Kinetic parameters describing the reaction rate of treated cells in batch reactors were used to analyse the performance of the hollow fibre membrane reactor employing significant convective mass transfer. No significant mass transfer limitation was apparent.     

Influence of Growth and High Mould Concentration on the Pressure Drop in Solid State Fermentations

Aspergillus niger was grown on Amberlite IRA-900 imbibed with a solution containing high concentrations of sucrose (S_i = 100, 200, 300 and 400 g/litre) in static aerated fermentors. Growth was followed in dry biomass, biomass protein, CO₂ production and pressure drop (DP). The DP allowed the monitoring of germination, vegetative growth, limitation and the onset of sporulation for the four concentrations of sucrose studied. Concentrations up to 103 mg dry biomass/g dry support were obtained with S_i = 400 g/litre and these reduced the relative intrinsic permeability to 0·0125. Under this condition the mould occupies 34% of the free space. DP increase was related to CO₂ production.     

Growth and spore formation in Bacillus thuringiensis at high substrate concentrations

The work was aimed at studying the effect exerted by elevated concentrations of glucose, yeast extract and acetate on the growth of Bacillus thuringiensis subsp. galleriae, strain 69-6, and on the formation of spores and crystals by it. Glucose concentrations from 30 to 100 g per litre did not prevent spore formation. Yeast extract inhibited spore formation to a greater extent and stopped it almost completely at a concentration of 20 g per litre. Acetate at a concentration of 1.0 to 10 g per litre delayed spore formation and produced a less action on crystal formation, so that those processes were uncoupled in time.     

The Production of Polyunsaturated Fatty Acids by Microalgae: from Strain Selection to Product Purification

A selection programme to increase the cellular eicosapentaenoic acid (EPA) content has been carried out with the microalga Isochrysis galbana. The selection process involved two stages of single selection. EPA content continuously increased from 2·4% dry weight (d.w.) of the ‘parent’ culture to an average value of 5·3% d.w. in the final stage. The proportion of total EPA variation attributable to the genetic variation (heritability in a broad sense) was 0·99 showing the importance of the genome in the determination of this fatty acid. The growth and fatty acid profile of an EPA-rich isolate grown as a chemostat in a cylindrical photobioreactor have been studied. A decrease in EPA content was observed (5·21% w/w to 2·8% w/w) at the lowest dilution rate D = 0·024 h⁻¹, up close to the maximum growth rate, D = 0·038 h⁻¹. At the same time, the biomass concentration also decreased from 1015 mg/litre to 202 mg/litre over the abovementioned range of dilution rate (D). Nonetheless, the EPA productivity increases with D, with a maximum of 15·26 mg/litre/day at D = 0·0208 h⁻¹. Furthermore, steady-state dilution rates may be related to average internal light intensity. Reverse-phase, high-pressure liquid chromatography (HPLC) on octadecylsilyl semi-preparative columns was used to separate stearidonic acid (SA), EPA and docosohexaenoic acid (DHA) in polyunsaturated fatty acid concentrate obtained by the urea complexation method from a fatty acid solution previously obtained by direct saponification of biomass. Isolate SA, EPA and DHA fraction purity was 94·8, 96·0 and 94·9%, respectively, with yields of 100·0, 99·6 and 94·0%.     

Optimisation of docosahexaenoic acid production in batch cultivations by Crypthecodinium cohnii

The heterotrophic micro alga Crypthecodinium cohnii was cultivated in media containing glucose, yeast extract and sea salt. Increasing amounts of yeast extract stimulated growth but influenced lipid accumulation negatively. Sea salt concentrations above half the average seawater salinity were required for good growth and lipid accumulation. C. cohnii was able to grow on a glucose concentration as high as 84.3 g l⁻¹, although concentrations above 25 g l⁻¹ decreased the growth rate. Comparison of growth at 27 and 30°C showed that the higher incubation temperature was more favourable for growth. However, lipid accumulation was higher at the lower incubation temperature. In a bioreactor the biomass concentration increased from 1.5 to 27.7 g l⁻¹ in 74 h. In the final 41 h of the process the lipid content of the biomass increased from 7.5 to 13.5%. In this period the percentage of docosahexaenoic acid of the lipid increased from 36.5 to 43.6%. The total amounts of lipid and docosahexaenoic acid after 91 h were 3.7 and 1.6 g l⁻¹, respectively.     

Anaerobic treatment of baker's yeast wastewater: I. Start-up and sodium molybdate addition

The anaerobic treatment of baker's yeast wastewater was studied using an anaerobic biological contact reactor (AnRBC) and a fixed-film reactor. The AnRBC had an active biomass developed within the reactor before this study commenced; however, the fixed-film reactor was started without attached biomass in a support structure. The gas production rates obtained for the AnRBC were between 0·55 and 0·61 litre methane per litre reactor per day. However, a gas production rate of only 0·46 litre methane per litre reactor per day was achieved after a four-month operating period for the fixed-film reactor. Higher chemical oxygen demand reduction was also found in the AnRBC. The results indicated that the presence of high sulfate concentration in baker's yeast wastewater affected teh start-up process. The reactor with fully developed active biomass was less susceptible to sulfate inhibition and showed improved anaerobic digestion. Results indicate that the reactor should be innoculated by feeding nutrient-balanced substrate before it was subjected to the digestion of baker's yeast wastewater. The fixed-film reactor was also fed with the substrate contianing sodium molybdate, an inhibitor of sulfate-reducing bacteria. The results indicated that both methanogenic and sulfate-reducing bacteria were inhibited.     

Pretreatment of beet molasses to increase pullulan production

Pretreatment of beet molasses with cation exchange resin, sulphuric acid, tricalcium phosphate, potassium ferrocyanide, and ethylenediaminetetraacetic acid and disodium salt (EDTA) to increase the production of pullulan was investigated. Among the above techniques used for the removal of heavy metals, sulphuric acid treatment gave better results regarding polysaccharide concentration, polysaccharide yield, and sugar utilization. Aureobasidium pullulans grown on beet molasses produced a mixture of pullulan and other polysaccharides. The pullulan content of the crude polysaccharide was 30–35%. The addition of nutrients improved the production of polysaccharide. A maximum polysaccharide concentration (32·0±1·0 g litre⁻¹) was achieved in molasses solution (70 g litre ¹ initial sugar concentration, pH 6·5–7·5) treated with sulphuric acid and supplemented with K₂HPO₄ 0·5%, -glutamic acid 1%, olive oil 2·5% and Tween 80 0·5%. In this case, the highest values of biomass dry weight (33·8±1·0 g litre⁻¹), polysaccharide yield (63·5±2·5%), and sugar utilization (97·5±1·5%) were obtained at pH 6·5, 3·5, and 4·5–7·5, respectively.     

Impact of liquid-to-gas hydrogen mass transfer on substrate conversion efficiency of an upflow anaerobic sludge bed and filter reactor

Efficient anaerobic degradation may be completed only under low levels of dissolved hydrogen in the liquid surrounding the microorganisms. This restraint can be intensified by the limitations of liquid-to-gas H₂ mass transfer, which results in H₂ accumulation in the bulk liquid of the reactor. Dissolved hydrogen proved to be an interesting parameter for reactor monitoring by showing a good correlation with short-chain volatile fatty acid concentration, namely propionate, which was not the case for the H₂ partial pressure. Biogas recycle was performed in a upflow anaerobic sludge bed and filter reactor. The effects of varying the ratio of recycled-to-produced gas from 2:1 (9 l/l reactor per day) to 8:1 (85 l/l reactor per day) were studied. By increasing the liquid—gas interface with biogas recycling, the dissolved hydrogen concentration could be lowered from 1.1 to 0.4 μ . Accordingly, the H₂ sursaturation factor was also reduced, leading to an important improvement of the H₂ mass transfer rate, which reached 20.86 h⁻¹ (±9.79) at a 8:1 gas recycling ratio, compared to 0.72 h⁻¹ (±0.24) for the control experiment. Gas recycling also lowered the propionate concentration from 655 to 288 mg l⁻¹ and improved the soluble chemical oxygen demand removal by 10–15%. The main problem encountered was the shorter solid retention time, which could lead to undesirable biomass washout at high gas recycling ratio. This could be circumvented by improving the reactor design to reduce the turbulence within the biomass bed.     

The catalytic potency of β-glucosidase from Pyrococcus furiosus in the direct glucosylation reaction

Enzymes from extremophiles operate at conditions that are different from their ‘normal’ counterparts, and are therefore a useful extension of the enzyme toolbox. In this paper, the direct glucosylation reaction mediated by a hyperthermophilic β-glucosidase from Pyrocuccus furiosus was investigated. Hexanol was successfully coupled to glucose with this enzyme. A preliminary study was conducted to improve the product yield. A maximum product concentration of 12.9 g.l⁻¹ was attainable by increasing the glucose concentration to the maximum solubility of 2000 g.(kg buffer solution)⁻¹ at the reaction temperature. The highest glucose based yield of 2.64% was achieved with a glucose concentration of 900 g.(kg buffer solution)⁻¹ at a reaction temperature of 65°C and a pH of 6.0. Performing the reaction at higher pH and temperature led to lower product concentrations. This was caused by deactivation of the enzyme accompanied by browning of the reaction mixture. A pH of 4.4 did have a negative effect on both the storage and the operational stability of the enzyme.     

Production of arachidonic acid byMortierella alpina ATCC 32222

Summary WhenMortierella alpina ATCC 32222 was incubated in a glucose salts medium at 25°C the biomass (17.5 g/l) contained 9.62% arachidonic acid which amounted to 54% (w/w) of total biomass lipids. When the glucose concentration in the medium was varied from 0 to 150 g/l, the percentage of arachidonic acid in biomass and in lipids was highest at a glucose concentration of 30 g/l, but highest yield of arachidonic acid per litre of culture broth was observed at a glucose concentration of 100 g/l. While production of biomass reached a plateau of 17 g/l after a 3-day incubation at 25°C, the percentage of arachidonic acid in lipids and biomass increased dramatically from 3 to 6 days with a concurrent arachidonic acid yield increase from 0.89 to 1.63 g/l. Optimum initial culture pH for arachidonic acid production was in the range 6.0–6.7. By increasing the concentration of the glucose salts medium three-fold, yields of biomass and arachidonic acid were increased to 35.8 g/l and 3.73 g/l, respectively.     

Waste Fe/Cr sludge as flocculant for the treatment of dairy wastewater

Variation in the characteristics of dairy wastewater with storage time is shown. The efficiency of Fe³⁺/Cr³⁺ sludge, a waste material from the wastewater treatment in the fertilizer industry, is compared with the conventional flocculants, ferric chloride and ferrous sulphate, in the treatment of dairy wastewater. The percentage removals of turbidity, BOD, COD, oil and grease and total phosphate were 81 ± 5, 68 ± 5, 70 ± 5, 52 ± 5 and 70 ± 5 respectively, by 1·043 g dosage of sludge per litre of the effluent, and the pH of the treated water was 5·7.     

Continuous production of galacto-oligosaccharides from lactose by Bullera singularis β-galactosidase immobilized in chitosan beads

Galacto-oligosaccharides (GalOS) were continuously produced using lactose and immobilized β-galactosidase from Bullera singularis ATCC 24193 in a packed bed reactor. Partially purified β-galactosidase was immobilized in Chitopearl BCW 3510 bead (970 GU/g resin) by simple adsorption. 55% (w/w) oligosaccharides was obtained continuously with a productivity of 4·4 g/(litre-h) from 100 g/litre lactose solution during a 15-day operation. Batch productivity was 6·5 g GalOS/(litre-h) from 300 g/litre lactose.     

Optimization of androstenedione production in an organic–aqueous two-liquid phase system

A systematic evaluation of the effect of key operational parameters on the selective cleavage of sitosterol to 4-androstene-3,17-dione (AD) with Mycobacterium sp. NRRL B-3805 in a dioctyl phthalate: aqueous buffer two-liquid phase system was performed. Of the parameters assessed, buffer composition, biomedium pH, temperature, and biomass and substrate concentration were those that mostly affected overall bioconversion rate. The optimum pH was 7.5 with Tris buffer. The highest bioconversion rate was observed at 35 °C, although at 40 °C bioconversion activity was virtually lost. Michaelis–Menten type kinetics adequately described the bioconversion system. Increasing biomass concentration from 10 to 70 g_{wet cell weight} l⁻¹ favored AD final yield, although the specific AD yield slightly decreased.     

Fermentation characteristics of Clostridium pasteurianum LMG 3285 grown on glucose and mannitol

Clostridium pasteurianum fermented glucose to acetate, butyrate, CO₂ and H₂. In batch cultures the fermentation pattern was only slightly affected by culture pH over the range 8·0 to 5·5. The acetate/butyrate ratio was always higher than or equal to one. Between 2·14 and 2·33 mol H₂ was produced per mol glucose fermented. At unregulated pH, more butanol and less butyrate was formed. In a carbon-limited chemostat, the steady-state acetate/butyrate ratio was always lower than one. H₂ production was approximately 1·70 mol per mol glucose consumed. Substantial amounts of extracellular protein were formed. With decreasing pH, acetate and formate production decreased, while H₂ production was highest at pH 6.0. With increasing dilution rate ( D ), the product spectrum hardly changed, but more biomass was formed. Y _glucose^max and Y _ATP^max were 55·97 and 31·48 g dry weight per mol glucose or ATP respectively. With increasing glucose input the formation of fatty acids and H₂ slightly decreased.
Continuous cultures fermented mannitol to acetate, butyrate, butanol, CO₂ and H₂. With acetate as co-substrate, butanol production and molar growth yields, Y _mannitol and Y _ATP, markedly decreased, while the butyrate and H₂ production increased. The latter reached a value of 2·21 mol H₂ per mol mannitol consumed.     

Mathematical modelling of the aerobic degradation of two-phase olive mill effluents in a batch reactor

A laboratory-scale study was conducted on the aerobic degradation of two-phase olive mill effluents (TPOME) made up of the mixture of the washwaters derived from the initial cleansing of the olives and those obtained in the washing and purification of virgin olive oil. The process was carried out in a 1-l working volume stirred tank reactor operating in batch mode at room temperature (25 °C). The reactor was operated at influent substrate concentrations of 2.80 g COD/l (TPOME 25%), 5.45 g COD/l (TPOME 50%), 8.18 g COD/l (TPOME 75%) and 10.90 g COD/l (TPOME 100%). After five days of operation time, total and soluble COD removal efficiencies of 64.3% and 66.6% were achieved respectively for the most concentrated influent used (TPOME 100%). A simplified kinetic model for studying the hydrolysis of insoluble organic matter, oxidation of soluble substrate and biomass production was proposed on the basis of the experimental results obtained. The following kinetic constants with their standard deviations were obtained for the above stages in the case of the most concentrated influent used (TPOME 100%): k₁ (kinetic constant for hydrolysis of suspended organic matter): 0.11 ± 0.01 l/(g VSS day); k₂ (kinetic constant for total consumption of soluble substrate): 0.30 ± 0.02 l/(g VSS day); k₃ (endogenous metabolism constant): 0.07 ± 0.01 per day). Finally, the biomass yield coefficient was found to be 0.30 g VSS/g COD_removed. The values of non-biodegradable total and soluble CODs obtained from the model were found to be 3 and 2 g/l, respectively. The kinetic constants obtained and the proposed equations were used to simulate the aerobic degradation process of TPOME and to obtain the theoretical values of non-soluble and soluble CODs and biomass concentration. The small deviations obtained (equal or lower than 10%) between the theoretical and experimental values suggest that the parameters obtained represent and predict the activity of the microorganisms involved in the overall aerobic degradation process of this wastewater.