Continuous sucrose hydrolysis by an immobilized whole yeast cell biocatalyst

An immobilized biocatalyst with invertase activity prepared by immobilization of whole yeast cells without use of any insoluble carrier was tested in tubular fixed-bed reactors from the point of view of possible application for continuous full-scale sucrose hydrolysis. At inlet sucrose concentration above 60% (w/w) and reaction temperature 60–70°C, total sucrose hydrolysis was achieved at a flow rate of 0.6–1.5 bed volumes per hour. At a flow rate about 10 bed volumes per hour, the conversion was still 0.5. The specific productivity of the biocatalyst was 3–25 h⁻¹; the productivity of the reactor was 1–9 kg l⁻¹ h⁻¹. The half-life of the biocatalyst invertase activity was 815 h at 70°C. The specific pressure drop over the biocatalyst bed was less than 23 kPa m⁻¹. The biocatalyst was proved to be fully capable of continuous sucrose hydrolysis in fixed-bed reactors.     

Production of high level of cellulase-free and thermostable xylanase by a wild strain of Thermomyces lanuginosus using beechwood xylan

Thermomyces lanuginosus, isolated from self-heated jute stacks in Bangladesh, was studied for production of high level of cellulase-free thermostable xylanase at 50°C using xylan. Optimization of the medium composition was carried out on shake-flask level using Graeco-Latin square technique. This increased xylanase production from 527 nkat ml⁻¹ in the original medium to 9168–9502 nkat ml⁻¹ in the optimized medium under optimized culture conditions e.g. initial medium pH (6.0–6.5), culture temperature (50°C) and time (5–6 d). The lag phase was very much shorter in the laboratory reactor compared to which existed in the shake cultures and 7111 nkat of xylanase activity were obtained per ml of culture filtrate at 60 h of cultivation. With a 15 min reaction time, the optimal pH and temperature for the xylanase activity were at 6.5 and 65°C, respectively. The enzyme was almost stable over a broad range of pH 3–9 at 20°C, with an optimum stability at pH 6.5. After 51 h heating at 50°C the enzyme retained 60%, 100% and 90% activity at pH 5.0, 6.5 and 8.0, respectively. The crude enzyme could hydrolyse xylan effectively and in only 6 h 67.3%, 54.0% and 49.2% saccharifications were achieved for 2%, 5% and 10% substrate levels, respectively. The principal product of hydrolysis was xylobiose together with smaller amounts of xylooligosaccharides (degree of polymerization 3–7) and xylose.     

Production of cyclodextrin by poly-lysine fused Bacillus macerans cyclodextrin glycosyltransferase immobilized on cation exchanger

Bacillus macerans cyclodextrin glycosyltransferase (CGTase) fused with 10 lysine residues at its C-terminus (CGTK10ase) was immobilized onto a cation exchanger by ionic interaction and used to produce -cyclodextrin (CD) from soluble starch. Poly-lysine fused immobilization increased the V_m of the immobilized CGTase by 40% without a change in K_m. The activation energies of thermal deactivation (E_a) were 41.4, 28.1, and 25.9 kcal mol⁻¹, respectively, for soluble wild-type (WT) CGTase, soluble CGTK10ase, and immobilized CGTK10ase, suggesting destabilization of CGTase by poly-lysine fusion and immobilization onto a cation exchanger. Maximum -CD productivity of 539.4 g l⁻¹ h⁻¹ was obtained with 2% soluble starch solution which was constantly fed at a flow rate of 4.0 ml min⁻¹ (D = 240 h⁻¹) in a continuous operation mode of a packed-bed reactor. The operational half-life of the packed-bed enzyme reactor was estimated 12 days at 25 °C and pH 6.0.     

Characterization of two-substrate fermentation processes for xylitol production using recombinant Saccharomyces cerevisiae containing xylose reductase gene

Fermentation characteristics of recombinant Saccharomyces cerevisiae containing a xylose reductase gene from Pichia stipitis were investigated in an attempt to convert xylose to xylitol, a natural five-carbon sugar alcohol used as a sweetener. Xylitol was produced with a maximum yield of 0.95 g g⁻¹ xylitol xylose consumed in the presence of glucose used as a co-substrate for co-factor regeneration. Addition of glucose caused inhibition of xylose transport and accumulation of ethanol. Such problems were solved by adopting glucose-limited fed-batch fermentations where a high ratio of xylose to glucose was maintained during the bioconversion phase. The optimized two-substrate fed-batch fermentation carried out with S. cerevisiae EH13.15:pY2XR at 30°C resulted in 105.2 g l⁻¹ xylitol concentration with 1.69 g l⁻¹ h⁻¹ productivity.     

A study in UF-membrane reactor on activity and stability of nitrile hydratase from Microbacterium imperiale CBS 498-74 resting cells for propionamide production

The bioconversion of propionitrile to propionamide was catalysed by nitrile hydratase (NHase) using resting cells of Microbacterium imperiale CBS 498-74 (formerly, Brevibacterium imperiale). This microorganism, cultivated in a shake flask, at 28 °C, presented a specific NHase activity of 34.4 U mg_DCW⁻¹ (dry cell weight). The kinetic parameters, K_m and V_max, tested in 50 mM sodium phosphate buffer, pH 7.0, in the propionitrile bioconversion was evaluated in batch reactor at 10 °C and resulted 21.6 mM and 11.04 μmol min⁻¹ mg_DCW⁻¹, respectively. The measured apparent activation energy, 25.54 kJ mol⁻¹, indicated a partial control by mass transport, more likely through the cell wall.

UF-membrane reactors were used for kinetic characterisation of the NHase catalysed reaction. The time dependence of enzyme deactivation on reaction temperature (from 5 to 25 °C), on substrate concentrations (from 100 to 800 mM), and on resting cell loading (from 1.5 to 200 μg  ml⁻¹) indicated: lower diffusional control (E_a=37.73 kJ mol⁻¹); and NHase irreversible damage caused by high substrate concentration. Finally, it is noteworthy that in an integral reactor continuously operating for 30 h, at 10 °C, 100% conversion of propionitrile (200 mM) was attained using 200 μg  ml⁻¹ of resting cells, with a maximum volumetric productivity of 0.5 g l⁻¹ h⁻¹.     

Characterization of a novel, ultra-large xylanolytic complex (xylanosome) from Streptomyces olivaceoviridis E-86

A novel, ultra-large xylanolytic complex (xylanosome) from Streptomyces olivaceoviridis E-86 was purified to homogeneity by ammonium sulfate precipitation and Sephacryl S-300 gel filtration chromatography. The purified xylanosome appeared as a single protein band on the non-denaturing (native) polyacrylamide gel electrophoresis (PAGE) gel with a molecular mass of approximately 1200 kDa. The optimal temperature and pH for xylanase activity was 60 °C and pH 6.0, respectively. The xylanase activity was stable within pH 4.1–10.3. It was stable up to 60 °C at pH 6.0. The xylanosome was highly specific towards oat-spelt xylan, and showed low activity towards corncob powder, but exhibited very low activity towards lichenan, CMC and p-nitrophenyl derivatives. Apparent K_m values of the xylansosome for birchwood, beechwood, soluble oat-spelt and insoluble oat-spelt xylans were 2.5, 3.6, 1.7 and 4.9 mg ml⁻¹, respectively. The main hydrolysis products of birchwood xylan were xylotriose, xylobiose and xylose. Analysis of the products from wheat arabinoxylan degradation by xylanosome confirmed that the enzyme had endoxylanase and debranching activities, with xylotriose, xylobiose, xylose and arabinose as the main degradation products. These unique properties of the purified xylanosome from Streptomyces olivaceoviridis E-86 make this enzymatic complex attractive for biotechnological applications.     

Semicontinuous production of lactic acid in a bioreactor coupled with nanofiltration membranes

The advantages of nanofiltration membranes coupled with a CSTR were demonstrated for the semicontinuous production of lactic acid from whey permeate. Lactic acid was removed from the growth medium while lactose was kept in the bioreactor with the bacterial cells; moreover, Mg²⁺ ions were also recycled in the bioreactor at 96% and the nanofiltrate color was greatly reduced. The highest volumetric productivity achieved with this device was 7.1 g l⁻¹ h⁻¹ and the lactate concentration was 55 g l⁻¹. The specific productivity was 3.54 h⁻¹. More than 99% of the membrane fouling after 44 h of fermentation was reversible. The initial permeate flux was restored easily by a water rinse. The performance of this type of membrane bioreactor was discussed.     

A coupled two-stage continuous fermentation for solvent production by Clostridium acetobutylicum

The effects of nitrogen and phosphate in batch and continuous AEB fermentations were tested. Both nitrogen- and phosphate-limited fermentations favored acid formation but not solvent production. A coupled two-stage continuous fermentation was performed for 30 days with a nitrogen-limited first stage fermentation for enhanced acid production. The bacteria from the acidogenic phase (first stage) fermentation were continuously pumped into a 14-l second stage fermentor with supplemental glucose and nitrogen for solvent production. The second stage fermentor had a maximum butanol productivity of 0.4 g l⁻¹ h⁻¹ (total solvent production was 0.6 g l⁻¹ h⁻¹) at a dilution rate of 0.06 h⁻¹.     

Production of xylanolytic enzymes during growth on pulverized grass by Aspergillus ochraceus-42

Xylanase and β-xylosidase with activity of 6.46 U mg^-1 and 0.500 U mg^-1, respectively, were produced extracellularly by Aspergillus ochraceus during growth on pulverized grass in liquid state fermentation, compared to 9.3 U mg^-1 and 0.74 U mg^-1 when pure xylan was used. The culture filtrate was devoid of any cellulase activity. Xylanolytic enzymes were produced optimally in 144 h of incubation on 1% pulverized grass, pH 6.5. About 8.43% (w/w) sugars were liberated from alkali-treated grass in 6 h by the synergistic effect of xylanolytic enzymes. The half-lives for xylanase and β-xylosidase at 50°C were 210 min and 300 min, respectively, and half-life increased with the increase in protein concentration. Both mono- and divalent cations, especially K⁺ and Zn²⁺, exhibited a profound effect on the rate of enzyme saccharification.     

Photosynthetic response of Myriophyllum salsugineum A.E. orchard to photon irradiance, temperature and external free CO2

The photosynthetic capacity of Myriophyllum salsugineum A.E. Orchard was measured, using plants collected from Lake Wendouree, Ballarat, Victoria and grown subsequently in a glasshouse pond at Griffith, New South Wales. At pH 7.00, under conditions of constant total alkalinity of 1.0 meq dm⁻³ and saturating photon irradiance, the temperature optimum was found to be 30–35°C with rates of 140 μmol mg⁻¹ chlorophyll a h⁻¹ for oxygen production and 149 μmol mg⁻¹ chlorophyll a h⁻¹ for consumption of CO₂. These rates are generally higher than those measured by other workers for the noxious Eurasian water milfoil, Myriophyllum spicatum L., of which Myriophyllum salsugineum is a close relative. The light-compensation point and the photon irradiance required to saturate photosynthetic oxygen production were exponentially dependent on water temperature. Over the temperature range 15–35°C the light-compensation point increased from 2.4 to 16.9 μmol (PAR) m⁻² s⁻¹ for oxygen production while saturation photon irradiance increased from 41.5 to 138 μmol (PAR) m⁻² s⁻¹ for oxygen production and from 42.0 to 174 μmol (PAR) m⁻² s⁻¹ for CO₂ consumption. Respiration rates increased from 27.1 to 112.3 μmol (oxygen consumed) g⁻¹ dry weight h⁻¹ as temperature was increased from 15 to 35°C. The optimum temperature for productivity is 30°C.     

Influence of phosphorus concentration on the growth kinetics and stoichiometry of the microalga Scenedesmus obliquus

The growth of the freshwater microalga Scenedesmus obliquus was studied at 30°C in a mineral culture medium with phosphorus concentrations of between 0 and 372 μ . The values for the specific growth rates, between and , fitted a semistructured substrate-limitation model with μ_m1 = 0·0466 h⁻¹, μ_m2 = 0·0256 h⁻¹ and . The specific uptake rate of phosphorus reached a maximum value of q_Sm1 = 658·01 × 10⁻⁴ μmol P mg⁻¹ biomass h⁻¹.     

Continuous production of lactic acid from whey permeate by Lactobacillus helveticus in two chemostats in series

The effect of dilution rate on the production of lactic acid from whey permeate by Lactobacillus helveticus has been investigated. In the first chemostat of a two-stage system, total conversion (98.1%) and maximum lactic acid concentration (43.7 g l⁻¹) were obtained at a dilution rate (D_Itot) of 0.06 h⁻¹. Maximum volumetric productivities of lactic acid (8.27 g l⁻¹ h⁻¹) and biomass (1.90 g l⁻¹ h⁻¹) occurred at D_Itot of 0.40 h⁻¹. The fraction of -lactate in the product was found to increase with dilution rate and reached a maximum of 66% at the same dilution rate. The maximum specific growth rate (μ_max) on this medium was 0.7 h⁻¹. A Y_ATP (max) value of 22.4 g dry weight (mol ATP)⁻¹ and a maintenance coefficient of 8.0 mmol ATP (g dry weight h)⁻¹ were determined. The second stage, in series with the first, confirmed these results and further showed that the total residence time could be reduced by 50%, compared with a single chemostat for the same nearly complete level of substrate conversion.     

Concentration of L-phenylalanine with a reverse osmosis membrane

A high flux, thin film composite reverse osmosis (RO) membrane was used to concentrate L-phenylalanine (L-Phe) from clarified bioreactor harvest media. At pH 10±0.5 and 50°C, concentrations of 100 g l⁻¹ were easily achieved and at fluxes from 17 to 119 1 m⁻² h⁻¹. Rejection coefficient for L-Phe was inversely proportional (as the log) to retentate concentration. A preliminary system study showed that stages in a cascade could be used to recover essentially all of the product from clarified harvests. The study shows the importance of empirical evaluation as the basis of design and suggests that bioprocess applications of RO are likely to be case specific.     

Medium optimization for the production of the secondary metabolite squalestatin S1 by a Phoma sp. combining orthogonal design and response surface methodology

In the present work, a combined statistical approach of orthogonal design (L₂₇(3¹³)), response surface techniques and polynomial regression were applied to optimize the composition and concentration of a liquid fermentation medium for the production of squalestatin S1 by a fungus (a Phoma species). Optimal conditions for maximal titres and productivity were determined based on 13 parameters at three different levels. Initially, a screening design methodology was used to evaluate the process variables, which were relevant to S1 titre and the response surfaces applied to find optimal regions for production. The sources of carbon and concentration, and their interactions with oily precursors were statistically significant factors. The combined orthogonal design and response surface methodology predicted optimal conditions for of 273 mg l⁻¹ of squalestatin S1. Confirmatory experiments of the optimal medium composition produced titres of 434 mg l⁻¹ in a 5-day fermentation at 25 °C. This represented a 60% improvement in the maximum titre predicted, and a two-fold higher productivity when compared with reported S1 yields of various fungal species. This combined statistical approach enables rapid identification and integration of key medium parameters for optimising secondary metabolite production and could be very useful in pharmaceutical screening programmes.     

Batch and continuous fermentation of succinic acid from wood hydrolysate by Mannheimia succiniciproducens MBEL55E

Batch and continuous cultures of Mannheimia succiniciproducens MBEL55E were carried out in a complex medium containing a NaOH-treated wood hydrolysate for the production of succinic acid. The wood hydrolysate based medium was treated with NaOH before sterilization to reduce the formation of inhibitory compounds. M. succiniciproducens MBEL55E utilized xylose as well as glucose in the wood hydrolysate based medium as a carbon source for the succinic acid production. In batch cultures, the final succinic acid concentration of 11.73 g l⁻¹ was obtained from the pre-treated wood hydrolysate based medium, resulting in a succinic acid yield of 56% and a succinic acid productivity of 1.17 g l⁻¹ h⁻¹, while the corresponding continuous cultures gave the succinic acid yield and productivity of 55% and 3.19 g l⁻¹ h⁻¹, respectively. These results suggest that succinic acid can be produced economically and efficiently by the fermentation of M. succiniciproducens MBEL55E from an inexpensive biomass-based wood hydrolysate.     

Studies on composition and stability of a large membered bacterial consortium degrading phenol

A ten member microbial consortium (AS) consisting of eight phenol-degrading and two non-phenol-degrading strains of bacteria was developed and maintained in a fed-batch reactor by feeding 500 mg l⁻¹ phenol for four years at 28 ± 3 °C. The consortium could degrade 99% of 500 mg l⁻¹ phenol after 24 hours incubation with a biomass increase of 2.6 × 10⁷ to 4 × 10¹² CFU ml⁻¹. Characterization of the members revealed that it consisted of 4 principal genera, Bacillus, Pseudomonas, Rhodococcus, Streptomyces and an unidentified bacterium. Phenol degradation by the mixed culture and Bacillus subtilis, an isolate from the consortium was compared using a range of phenol concentrations (400 to 700 mg l⁻¹) and by mixing with either 160 mg l⁻¹ glucose or 50 mg l⁻¹ of 2,4-dichlorophenol in the medium. Simultaneous utilization of unrelated mixed substrates (glucose/2,4-dichlorophenol) by the consortium and Bacillus subtilis, indicated the diauxic growth pattern of the organisms. A unique characteristic of the members of the consortia was their ability to oxidize chloro aromatic compounds via meta pathway and methyl aromatic compounds via ortho cleavage pathway. The ability of a large membered microbial consortia to maintain its stability with respect to its composition and effectiveness in phenol degradation indicated its suitability for bioremediation applications.     

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.     

Purification and characterization of five cellulases and one xylanase from Penicillium brasilianum IBT 20888

The filamentous fungus Penicillium brasilianum IBT 20888 was cultivated on a mixture of 30 g l⁻¹ cellulose and 10 g l⁻¹ xylan for 111 h and the resulting culture filtrate was used for protein purification. From the cultivation broth, five cellulases and one xylanase were purified. Hydrolysis studies revealed that two of the cellulases were acting as cellobiohydrolases by being active on only microcrystalline cellulose (Avicel). Three of the cellulases were active on both Avicel and carboxymethyl cellulose indicating endoglucanase activity. Two of these showed furthermore mannanase activity by being able to hydrolyze galactomannan (locust bean gum). Adsorption studies revealed that the smaller of the two enzymes was not able to bind to cellulose. Similarity in molecular mass, pI and hydrolytic properties suggested that these two enzymes were identical, but the smaller one was lacking the cellulose-binding domain or an essential part of it. The basic xylanase (pI>9) was only active towards xylan. Two of the purified cellulases with endoglucanase activity were partly sequenced and based on sequence homology with known enzymes they were classified as belonging to families 5 and 12 of the glycosyl hydrolases.     

Effect of iron concentration on hydrogen fermentation

The effect of the iron concentration in the external environment on hydrogen production was studied using sucrose solution and the mixed microorganisms from a soybean-meal silo. The iron concentration ranged from 0 to 4000 mgFeCl₂ l⁻¹. The temperature was maintained at 37°C. The maximum specific hydrogen production rate was found to be 24.0 mlg⁻¹ VSSh⁻¹ at 4000 mgFeCl₂ l⁻¹. The specific production rate of butyrate increased with increasing iron concentration from 0 to 20 mgFeCl₂ l⁻¹, and decreased with increasing iron concentration from 20 to 4000 mgFeCl₂ l⁻¹. The maximum specific production rates of ethanol (682 mgg⁻¹ VSSh⁻¹) and butanol (47.0 mgg⁻¹ VSSh⁻¹) were obtained at iron concentrations of 5 and 3 mgFeCl₂ l⁻¹, respectively. The maximum hydrogen production yield of 131.9 mlg⁻¹ sucrose was obtained at the iron concentration of 800 mgFeCl₂ l⁻¹. The maximum yields of acetate (389.3 mgg⁻¹ sucrose), propionate (37.8 mgg⁻¹ sucrose), and butyrate (196.5 mg g⁻¹ sucros) were obtained at iron concentrations of 3, 200 and 200 mgFeCl₂ l⁻¹, respectively. The sucrose degradation efficiencies were close to 1.0 when iron concentrations were between 200 and 800 mgFeCl₂ l⁻¹. The maximum biomass production yield was 0.283 gVSSg⁻¹ sucrose at an iron concentration of 3000 mgFeCl₂ l⁻¹.     

Effects of medium glucose concentration and pH on docosahexaenoic acid content of heterotrophic Crypthecodinium cohnii

The effects of medium glucose concentration and pH on growth and docosahexaenoic acid (DHA, C22:6 ω-3) content of Crypthecodinium cohnii were investigated. Over a range of glucose concentrations (5–40 g l⁻¹) investigated, the highest specific growth rate (0.12 h⁻¹), highest cell dry weight concentration (3.13 g l⁻¹) and highest growth yield on glucose (0.6 g g⁻¹) were obtained at 20 g l⁻¹ glucose. However, the highest degree of fatty acid unsaturation (3.2) and highest DHA proportion (53.4% of total fatty acids) were achieved at 5 g l⁻¹ glucose. Low glucose concentrations enhanced the degree of fatty acid unsaturation and DHA formation. Medium pH also affected cell growth, fatty acid unsaturation and DHA proportion. When medium pH was 7.2, the highest specific growth rate (0.089 h⁻¹), highest cell dry weight concentration (2.73 g l⁻¹), highest growth yield on glucose (0.564 g g⁻¹), highest degree of fatty acid unsaturation (3.4) and highest DHA proportion (56.8% of total fatty acids) were obtained. Results suggest that glucose concentration and pH value could be effectively manipulated to achieve maximum DHA production by C. cohnii.