Native-State Heterogeneity of β2-Microglobulin as Revealed by Kinetic Folding and Real-Time NMR Experiments

The kinetic folding of β₂-microglobulin from the acid-denatured state was investigated by interrupted-unfolding and interrupted-refolding experiments using stopped-flow double-jump techniques. In the interrupted unfolding, we first unfolded the protein by a pH jump from pH 7.5 to pH 2.0, and the kinetic refolding assay was carried out by the reverse pH jump by monitoring tryptophan fluorescence. Similarly, in the interrupted refolding, we first refolded the protein by a pH jump from pH 2.0 to pH 7.5 and used a guanidine hydrochloride (GdnHCl) concentration jump as well as the reverse pH jump as unfolding assays. Based on these experiments, the folding is represented by a parallel-pathway model, in which the molecule with the correct Pro32 cis isomer refolds rapidly with a rate constant of 5–6 s^? 1, while the molecule with the Pro32 trans isomer refolds more slowly (pH 7.5 and 25 °C). At the last step of folding, the native-like trans conformer produced on the latter pathway isomerizes very slowly (0.001–0.002 s^? 1) into the native cis conformer. In the GdnHCl-induced unfolding assays in the interrupted refolding, the native-like trans conformer unfolded remarkably faster than the native cis conformer, and the direct GdnHCl-induced unfolding was also biphasic, indicating that the native-like trans conformer is populated at a significant level under the native condition. The one-dimensional NMR and the real-time NMR experiments of refolding further indicated that the population of the trans conformer increases up to 7–9% under a more physiological condition (pH 7.5 and 37 °C).     

Catalytic removal of sulfide by an immobilized sulfide-oxidase bioreactor

A bioreactor packed with chitosan immobilized sulfide-oxidase from Streptomyces species LD048 was developed to treat a liquid stream of sulfide. The inoculation system was composed of glass with a 0.7 L working volume and enzyme activity of 2 mmol S g^?1 carrier. The sulfide removal efficiency was almost 100% when the volumetric loading was increased up to 3.9 mmol S L^?1 h^?1 at a space velocity of 18 h^?1. The maximal elimination capacity was 22.1 mmol S L^?1 h^?1 with a space velocity of 72 h^?1. When the aeration was increased from 0.05 to 0.1 L min^?1, the average removal efficiency improved from 81% to 94%. A removal efficiency of 90% was obtained after 15 days of operation with a load rate of 8.9 mmol S L^?1 h^?1 and a space velocity of 14.28 h^?1. An operational equation based on the ideal plug flow bioreactor and the Michaelis–Menten model predicted the performance of this bioreactor.     

Purification and efficient refolding process for recombinant tissue-type plasminogen activator derivative (reteplase) using glycerol and Tranexamic acid

In this study, a novel and economic method for refolding and purifying recombinant tissue plasminogen activator derivative (r-PA; reteplase) was developed. Reteplase with nine disulfide bonds in its complex structure is expressed in the form of inclusion bodies in Escherichia coli and requires tedious dissolving and refolding processes to achieve its biological activity. Among the different refolding additives that were evaluated, glycerol and tranexamic acid (Txa) were found to be more effective in increasing the refolding yield of reteplase. Using response surface methodology, a solution containing 3.5 M urea, 33% (v/v) glycerol, and 400 mM Txa was found to give the highest refolding yield. The synergic effect of urea, glycerol, and Txa under optimum conditions for a reteplase concentration of 25 μg ml⁻¹ resulted in a high refolding yield of 76.41%. Increased reteplase concentration in the refolding buffer was achieved using the pulse-fed method. In the pulse-fed method, a refolding yield of 49.53% was achieved for a final reteplase concentration of 300 μg ml⁻¹. Using Txa as a novel refolding aid for reteplase instead of ionic amino acids like l-Arginine allowed to purify the refolded reteplase directly by cation-exchange chromatography with high purity.     

Influence of specific growth rate over the secretory expression of recombinant potato carboxypeptidase inhibitor in fed-batch cultures of Escherichia coli

A high cell density cultivation protocol was developed for the secretory production of potato carboxypeptidase inhibitor (PCI) in Escherichia coli. The strain BW25113 (pIMAM3) was cultured in fed-batch mode employing minimal media and an exponential feed profile where the specific growth rate was fixed by limitation of the fed carbon source (glycerol). Plasmid loss rates were found to be proportional to the specific growth rate. Distribution of PCI along the cell compartments and the culture media was also dependent on the fixed growth rate. When specific growth rate was kept at μ = 0.10 h⁻¹, 1.4 g PCI L⁻¹ were obtained when adding the product present in periplasmic extracts and supernatant fractions, with a 50% of the total expressed protein recovered from the extracellular medium. This constituted a 1.2-fold increase compared to growth at μ = 0.15 h⁻¹, and 2.0-fold compared to μ = 0.25 h⁻¹. Last, a cell permeabilization treatment with Triton X-100 and glycine was employed to direct most of the product to the culture media, achieving over 81% of extracellular PCI. Overall, our results point out that production yields of secretory proteins in fed-batch cultures of E. coli can be improved by means of process variables, with applications to the production of small disulfide-bridged proteins. Overall, our results point out that control of the specific growth rate is a successful strategy to improve the production yields of secretory expression in fed-batch cultures of E. coli, with applications to the production of small disulfide-bridged proteins.     

Poly(3-hydroxybutyrate) production by Cupriavidus necator using waste glycerol

Polyhydroxyalkanoates (PHAs) have been recognized as good substitutes for the non-biodegradable petrochemically produced polymers. However, their high (real or estimated) current production cost limits their industrial applications. This work exploits two strategies to enhance PHAs substitution potential: the increase in PHA volumetric productivity in high density cultures and the use of waste glycerol (GRP), a by-product from the biodiesel industry, as primary carbon source for cell growth and polymer synthesis. Cupriavidus necator DSM 545 was used to accumulate poly(3-hydroxybutyrate) (P(3HB)) from GRP and from commercial glycerol (PG) as control substrate. On PG, productivities between 0.6 g_PHB L^?1 h^?1 and 1.5 g_PHB L^?1 h^?1 were attained. The maximum cell DW was 82.5 g_DW L^?1, the P(3HB) content being 62%. When GRP was used, 68.8 g_DW L^?1 with a P(3HB) accumulation of 38% resulting in a final productivity of 0.84 g_PHB L^?1 h^?1 was obtained. By decreasing the biomass concentration at which accumulation was triggered, a productivity of 1.1 g_PHB L^?1 h^?1 (50% P(3HB), w/w) was attained using GRP. P(3HB) molecular weights (M_w) ranged from 7.9 × 10⁵ to 9.6 × 10⁵ Da.     

Refolding and purification of recombinant human granulocyte colony-stimulating factor using hydrophobic interaction chromatography at a large scale

High level expression of recombinant human granulocyte colony-stimulating factor (rhG-CSF) in Escherichia coli (E. coli) usually forms insoluble and inactive aggregates, i.e. inclusion bodies. In the present work, high performance hydrophobic interaction chromatography (HPHIC) was applied to the refolding of rhG-CSF, which was solubilized by 8.0 mol L^?1 urea from the inclusion bodies. First a laboratorial scale column (10 mm × 20 mm I.D.) was employed to study the refolding process. Several factors, including concentration of ammonium sulfate, pH of the mobile phase and flow rate, were investigated in details. The results indicated that the rhG-CSF produced by E. coli could be successfully refolded with simultaneous purification by using HPHIC. The refolding process was further scaled up by using a large column (50 mm × 200 mm I.D.). 200 mL of rhG-CSF solution solubilized by 8.0 mol L^?1 urea, with a total amount of protein around 1.6 g, could be loaded onto the large column at one time. Under these conditions, the obtained rhG-CSF had a specific activity of 2.3 × 10⁸ IU mg^?1 and a purity of 95.4%, the mass recovery during the purification was 36.9%. This work might have great impact on practical production of rhG-CSF, and it also shed a light on protein refolding using liquid chromatography at large scales.     

Treatment of dye (Remazol Blue) and heavy metals using yeast cells with the purpose of managing polluted textile wastewaters

The bioaccumulation of chromium(VI), nickel(II), copper(II), and reactive dye by the yeast Rhodotorula mucilaginosa has been investigated in media containing molasses as a carbon and energy source. Optimal pH values for the yeast cells to remove the pollutants were pH 4 for copper(II) and dye, pH 6 for chromium(VI) and dye, and pH 5 for nickel(II) and dye in media containing 50 mg l^?1 heavy metal and 50 mg l^?1 Remazol Blue. The maximum dye bioaccumulation was observed within 4–6 days and uptake yields varied from 93% to 97%. The highest copper(II) removal yields measured were 30.6% for 45.4 mg l^?1 and 32.4% for 95.9 mg l^?1 initial copper(II) concentrations. The nickel(II) removal yield was 45.5% for 22.3 mg l^?1, 38.0% for 34.7 mg l^?1, and 30.3% for 62.2 mg l^?1. Higher chromium(VI) removal yields were obtained, such as 94.5% for 49.2 mg l^?1 and 87.7% for 129.2 mg l^?1 initial chromium(VI) concentration. The maximum dye and heavy metal bioaccumulation yield was investigated in media with a constant dye (approximately 50 mg l^?1) and increasing heavy metal concentration. In the medium with 48.9–98.8 mg l^?1 copper(II) and constant dye concentration, the maximum copper(II) bioaccumulation was 27.7% and 27.9% whereas the maximum dye bioaccumulation was 96.1% and 95.3%. The maximum chromium(VI) bioaccumulation in the medium with dye was 95.2% and 80.3% at 48.2 and 102.2 mg l^?1 chromium(VI) concentrations. In these media dye bioaccumulation was 76.1% and 35.1%, respectively. The highest nickel(II) removal was 6.1%, 20.3% and 16.0% in the medium with 23.8 mg l^?1 nickel(II) + 37.8 mg l^?1 dye, 38.1 mg l^?1 nickel(II) + 33.4 mg l^?1 dye and 59.0 mg l^?1 nickel(II) + 39.2 mg l^?1 dye, respectively. The maximum dye bioaccumulation yield in the media with nickel(II) was 94.1%, 78.0% and 58.7%, respectively.     

The modification of glucose levels and N source in the Hungate's medium to stimulate the production of fibrolytic enzymes of Anaeromyces sp. YQ3 grown on corn stalks

Hungate's method is a well-accepted protocol for the isolation or incubation of anaerobes with a roll tube technique. The aim of this study was to stimulate fungal enzyme production by optimizing the components of Hungate's medium for the growth of a rumen fungus Anaeromyces sp. YQ3. The organism was grown on corn stalks and incubated for 10 days in defined media with two glucose levels (G⁺, glucose in the Hungate's medium as a glucose control; G^?, glucose removed in a modified Hungate's medium) and four N sources (N1: yeast extract + tryptone + (NH₄)₂SO₄ in Hungate's medium (control); N2: yeast extract + (NH₄)₂SO₄; N3: tryptone + (NH₄)₂SO₄; and N4: tryptone + yeast extract). In the G^? media, the recovered activities of feruloyl esterase (FAE) (P<0.0001), acetyl esterase (AE) (P=0.0065) and xylanase (P<0.0001) were decreased, while the G⁺ media with N1 nitrogen stimulated the production of FAE and xylanase (P<0.0001). The G^? medium with N2 nitrogen increased the recovered activities of carboxymethyl cellulase (P=0.0001) and avicelase (P<0.0001), while the N3 and N4 media increased the recovered activity of AE (P=0.0015). The N4 medium was comparable to the N1 medium in stimulating the amount of recovered xylanase activity. The activities of FAE (P<0.0001), AE (P<0.0001), and xylanase (P<0.0001) showed a time-dependent increase and reached their peaks at day 10, while the avicelase activity peaked at day 8 (P=0.0071). The esterase activities (FAE and AE) were positively correlated with the enzyme activities of xylanase and carboxymethyl cellulase (r > 0.48, P<0.05). After a 10-day incubation, the glucose in the Hungate's media contributed to an increase in organic matter disappearance (P<0.0001) and volatile fatty acid (VFA) concentration (P<0.0001), except for molar acetate proportions. The N4 treatment increased organic matter disappearance and total VFA concentration (P=0.0002). The change in N source did not alter molar proportions of acetate, propionate and valerate, while the N2 treatment increased molar butyrate proportion (P<0.0035), and both N2 and N3 increased the molar proportion of branched chain VFAs (P<0.0041). In summary, the glucose in the Hungate's medium is beneficial for stimulating the production of esterases and xylanase, thereby promoting fungal growth. Amending the N source in Hungate's medium brings about different yields of rumen fungal esterases and polysaccharide hydrolases that have important nutritional impacts on fibre degradation in ruminant animals.     

Phosphogypsum biotransformation in cultures of sulphate reducing bacteria in whey

Assemblages of anaerobic sulphidogenic microorganisms were isolated from soil polluted by oil-derived products and grown using the microcosms method. The cultures were grown in minimal and Postgate media with phosphogypsum (PG) as the sole electron acceptor and with lactate, casein or lactose as the sole carbon source. The most effective was the assemblage in Postgate medium with lactose as the sole carbon source. A reduction of 980 mg COD l^?1 (reduction of about 40%) and 790 mg SO₄^2? l^?1 (reduction of 53% of phosphogypsum introduced to the medium) was noted in the culture. The lowest activity was observed for minimal medium with lactose as sole carbon source (reduction of 4.4% COD and 40% PG). The selected assemblage became an inoculum for a culture in Postgate, minimal and/or distilled water medium with PG (6 g l^?1) and cheese whey (2.5 and 4.5 g l^?1).A percentage reduction of COD and SO₄^2? of PG was observed in all cultures. After growth, the residues were weighed and in all cases a distinct mass reduction of PG was observed in comparison to the 6 g l^?1 introduced to the medium. Diffractometric studies of the residues confirmed the presence of calcite and apatite. The presence of these mineral phases in the residues allows their application as agricultural fertilisers.     

Enhanced ethanol production by continuous fermentation in a two-tank system with cell recycling

An experimental method for producing ethanol continuously was designed and tested with a cell-recycling two-tank system, which was composed of two fermentors, each of which was individually equipped with a settler for recycling flocculent yeast. This system was effective for the continuous fermentation of ethanol from sucrose at high cell-recycling (r = 0.8–0.9) and dilution (up to 0.48 h^?1) rates. The system has several advantages; the high cell concentration in the fermentors and relief of substrate and product inhibition. Thus, the enhanced productivity using this continuous fermentation with the two-tank cell-recycling system was significantly higher compared with that of the batch fermentation. The results indicate that increased recycling ratios caused an increase in biomass concentration and subsequently, product concentration in the tank. The ethanol productivity increased with the dilution rate, but higher dilution rates could render increasing amounts of sugar unconverted. Continuous fermentation with the sugar feed concentration of 160 g/l at r = 0.9 and dilution rate of 0.2 h^?1 achieved the highest productivity with less than 2% of the unconverted sugar in the product steam. Under the same cell recycling ratios a productivity range of 6.9–7.5 g/l h^?1 could be achieved with feeding concentrations of 80–200 g/l, while batch fermentation at these sugar concentrations led to productivities of 3.85–4.48 g/l h^?1.     

A stable immobilized d-psicose 3-epimerase for the production of d-psicose in the presence of borate

Maximal activity of the immobilized d-psicose 3-epimerase from Agrobacterium tumefaciens on Duolite A568 beads was achieved at pH 9.0 and 55 °C with borate, and at pH 8.5 and 50 °C without borate. The half-lives of the immobilized enzyme at 50 °C with and without borate were increased 4.2- and 128-fold compared to that of the free enzyme without borate, respectively. The immobilized enzyme with borate produced 441 g l^?1 psicose from 700 g l^?1 fructose at pH 9.0 and 55 °C, whereas 193 g l^?1 psicose was produced without borate at pH 8.5 and 50 °C after 120 min in a batch reaction. The immobilized enzyme in a packed-bed bioreactor without borate was produced continuously 325 g l^?1 psicose from 500 g l^?1 fructose at a dilution rate of 1.62 h^?1 over a 236 h period with productivity of 527 g l^?1 h^?1 while that without borate produced 146 g l^?1 psicose at 4.15 h^?1 over a 384-h period with productivity of 606 g l^?1 h^?1. The operational half-lives of the enzyme with and without borate in the bioreactor were 601 and 645 h, respectively. In the present study, psicose was produced stably with high productivity using the immobilized d-psicose 3-epimerase in the presence of borate.     

New integrated bioprocess for the continuous production,extraction and purification of lipopeptides produced by Bacillus subtilis in membrane bioreactor

Recently, a bubbleless membrane bioreactor (BMBR) has been successfully developed for biosurfactant production by Bacillus subtilis [1]. In this study, for the first time, continuous culture were carried out for the production of surfactin in a BMBR, both with or without a coupled microfiltration membrane. Results from continuous culture showed that a significant part of biomass was immobilized onto the air/liquid membrane contactor. Immobilized biomass activity onto the air/liquid membrane contactor was monitored using a respirometric analysis. Kinetics of growth, surfactin and primary metabolites production were investigated. Planktonic biomass, immobilized biomass and surfactin production and productivity obtained in batch culture (3 L) of 1.5 days of culture were 4.5 g DW, 1.3 g DW, 1.8 g and 17.4 mg L^?1 h^?1, respectively. In continuous culture without total cell recycling (TCR), the planktonic biomass was leached, but immobilized biomass reached a steady state at an estimated 6.6 g DW. 11.5 g of surfactin was produced after 3 days of culture, this gave an average surfactin productivity of 54.7 mg L^?1 h^?1 for the continuous culture, which presented a surfactin productivity of 30 mg L^?1 h^?1 at the steady state. TCR was then investigated for the continuous production, extraction and purification of surfactin using a coupled ultrafiltration step. In continuous culture with TCR at a dilution rate of 0.1 h^?1, planktonic biomass, immobilized biomass, surfactin production and productivity reached 7.5 g DW, 5.5 g DW, 7.1 g and 41.6 mg L^?1 h^?1 respectively, after 2 days of culture. After this time, biomass and surfactin productions stopped. Increasing dilution rate to 0.2 h^?1 led to the resumption of biomass and surfactin production and these values reached 11.1 g DW, 10.5 g DW, 7.9 g and 110.1 mg L^?1 h^?1, respectively, after 3 days of culture. This study has therefore shown that with this new integrated bioprocess, it was possible to continuously extract and purify several grams of biosurfactant, with purity up to 95%.     

Fermentative production of succinic acid from straw hydrolysate by Actinobacillus succinogenes

In this work, straw hydrolysates were used to produce succinic acid by Actinobacillus succinogenes CGMCC1593 for the first time. Results indicated that both glucose and xylose in the straw hydrolysates were utilized in succinic acid production, and the hydrolysates of corn straw was better than that of rice or wheat straw in anaerobic fermentation of succinic acid. However, cell growth and succinic acid production were inhibited when the initial concentration of sugar, which was from corn straw hydrolysate (CSH), was higher than 60 g l^?1. In batch fermentation, 45.5 g l^?1 succinic acid concentration and 80.7% yield were attained after 48 h incubation with 58 g l^?1 of initial sugar from corn straw hydrolysate in a 5-l stirred bioreactor. While in fed-batch fermentation, concentration of succinic acid achieved 53.2 g l^?1 at a rate of 1.21 g l^?1 h^?1 after 44 h of fermentation. Our work suggested that corn straw could be utilized for the economical production of succinic acid by A. succinogenes.     

Membrane combined with hydrophilic macromolecules enhances protein refolding at high concentration

Membrane technology is important to the development of modern biotechnology. It has the potential to efficiently refold protein at high concentration that is still a challenge for pharmaceutical protein produced from inclusion bodies. This paper dealt with the application of a polysulfone hollow fiber membrane to protein refolding using recombinant human granulocyte colony-stimulating factor (rhG-CSF) as a model protein. Compared with dilution refolding at protein concentration of 1.0 mg/mL, the crossflow membrane system led to a 16% increase in soluble protein recovery, and a 3.3-fold increase in specific bioactivity. Addition of PEG 6 K at 2 g/L could further improve the soluble protein recovery up to 57%, the specific bioactivity up to 2.2 × 10⁸ IU/mL. Addition of dextran at 5 g/L could increase the soluble protein recovery up to 63.6%, the specific bioactivity up to 2.30 × 10⁸ IU/mL. By gently and gradually removing denaturant, ultrafiltration membrane system was demonstrated to be very helpful for protein refolding at high concentration. Combining with hydrophilic macromolecular of PEG or dextran could further increase its efficiency. PEG was able to promote the refolding intermediate of rhG-CSF to transfer into the native structure; whereas dextran could enhance protein refolding mainly by weakening shear stress-induced protein aggregation.     

Co-remediation of pentachlorophenol and Cr6+ by free and immobilized cells of native Bacillus cereus isolate: Spectrometric characterization of PCP dechlorination products,bioreactor trial and chromate reductase activity

In this study, Bacillus cereus isolate efficiently remediated 57% PCP and 74% Cr⁶⁺ simultaneously with uptake rate of 0.65 mg Cr⁶⁺ g^?1 biomass h^?1 at initial 200 mg Cr⁶⁺ and 500 mg PCP l^?1 concentration under optimized 0.4% glucose, 0.2% NH₄Cl, pH 7.0, 35 °C, 1.0% inoculum during 60 h incubation. Optimization of agitation (100 rpm) and aeration (0.6 vvm) in bioreactor further enhanced PCP dechlorination by ～5.0% and Cr⁶⁺ removal 7.5%. Presence of other heavy metals variedly affected bioremediation of both the toxicants. Maximum and minimum inhibition was exhibited by mercury and lead, respectively. Out of 74% Cr⁶⁺ remediated, 90% reduced to Cr³⁺, of which 52.8% was associated with cell biomass and 37.2% with culture supernatant. Maximum chromate reductase activity was evident in culture supernatant followed by cytosolic fraction and cell debris. A direct correlation existed between chromate reductase activity and reduced Cr³⁺ in different cell fractions. Among matrices, alginate was most suitable for biomass immobilization, which enhanced Cr⁶⁺ removal by 20.2% compared to free cells at 36 h. Gas chromatography and mass spectrometry detected 2,3,4,6-tetrachlorophenol, 2,4,6-trichlorophenol, 2,6-dichlorophenol and 6-chlorohydroxyquinol as PCP dechlorination products. Our promising strain can be efficiently employed for simultaneous bioremediation of PCP and Cr⁶⁺ under wide environmental conditions.     

Aerobic granulation in sequencing batch reactors with different reactor height/diameter ratios

Effects of reactor height/diameter ratios ranged from 24 to 4 corresponding to reactor settling velocities from 12 to 2 m h^?1 on aerobic granulation were investigated. It was found that granules appeared after 1-week operation and granule volume percentages exceeded 50% after 2–3 weeks in four reactors. In addition, similar granule fraction of 94–96% was found at steady state in all four reactors. Sludge volume index (SVI), average sludge size, biomass density and granule settling velocity at steady state were around 50 ml g^?1, 1800 μm, 53 g l^?1 and 40 m h^?1, respectively, in four reactors. Extracellular polymeric substances (EPS) and specific oxygen uptake rate (SOUR) were around 38 mg g^?1 VSS and 40 mg O₂ g^?1 VSS h^?1, respectively. Denaturing gradient gel electrophoresis (DGGE) fingerprint of sludge in four reactors showed the same microbial population shift during the start-up period and same microbial community structure during steady-state period. These results recommended strongly that reactor height/diameter ratio or reactor setting velocity in the used range in this study did not affect granule formation, physical characteristics, microbial community structure of granules and stable operation of granular sludge reactor. Reactor height/diameter ratio thus can be very flexible in the practice, which is important for the application of aerobic granule technology.     

Methanol vapor biofiltration coupled with continuous production of recombinant endochitinase Ech42 by Pichia Pastoris

Methanol biofiltration using methylotrophic microorganisms has been previously reported by various authors. In a previous study, a modified strain of Pichia pastoris was tested for the ability to produce endochitinase (Ech42) when coupled with methanol vapor biodegradation in batch tests. The next challenge was to validate the process in a continuous system. Thus, in the present study, a biofilter packed with perlite and inoculated with P. pastoris transformed with the plasmid pPIC-ech42 was used for methanol vapor biofiltration and the continuous production of recombinant endochitinase (Ech42) for 60 days. The maximum elimination capacity (EC) of methanol obtained was 1320 g m^?3 h^?1 at a loading rate of 1465 g m^?3 h^?1. The extracellular protein production rate in the leachate was 2360 μg h^?1 with a chitinase enzymatic activity of 123 U L^?1. The protein content on the biofilm samples was negligible, indicating the effectiveness of the overall process and of P. pastoris to excrete proteins. The carbon balance indicated that 81% of the consumed methanol was mineralized and 5.8% was incorporated into biomass. The results of this study and the economic balance underscore the promising application of linking methanol vapor biofiltration to the continuous production of recombinant proteins.     

Culture parameters affecting xylitol production by Debaryomyces hansenii immobilized in alginate beads

Yeast immobilization offers operational advantages such as high cell concentration, and some drawbacks related to cell leaking and restricted mass transfer inside particles. The influence of bead size, chitosan, bead charge, volume of liquid media, and the use of corncob hydrolyzates and vinasses as culture medium were analyzed on xylitol production by Debaryomyces hansenii immobilized in alginate beads. The results showed a profuse growth of free cells, accounting 75–95% of total biomass, but electron micrographs revealed the generation of a dense biofilm with hyphal morphology at the bead surface and a very low intraparticular growth. Xylitol production was not affected by the size of particle; however chitosan had a negative effect. The use of corn cob as carbon source and twofold diluted vinasses as economic nutrients incremented xylitol concentration to 13.7 g L^?1 (Y_P/S = 0.56 g g^?1; Q_P = 0.29 g L^?1 h^?1). The best conditions corresponded to high bead charges and intermediate liquid volumes (44 g Na-alginate and 110 mL liquid medium). These results showed the feasibility of employing these cheap substrates, reflected the importance of the microaerobical conditions, and pointed to the favorable effect of cell immobilization on the metabolism of xylitol production.     

Improved β-carotene production of Rhodotorula glutinis in fermented radish brine by continuous cultivation

Fermentation kinetics of growth and β-carotene production by Rhodotorula glutinis DM28 in batch and continuous cultures using fermented radish brine, a waste generated from fermented vegetable industry, as a cultivation medium were investigated. The suitable brine concentration for β-carotene production by R. glutinis DM28 was 30 g l^?1. Its growth and β-carotene production obtained by batch culture in shake flasks were 2.2 g l^?1 and 87 μg l^?1, respectively, while, in a bioreactor were 2.6 g l^?1 and 186 μg l^?1, respectively. Furthermore, its maximum growth rate and β-carotene productivity in continuous culture obtained at the dilution rate of 0.24 h^?1 were 0.3 g l^?1 h^?1 and 19 μg l^?1 h^?1, respectively, which were significantly higher than those in the batch. Therefore, improved growth rate and β-carotene productivity of R. glutinis in fermented radish brine could be accomplished by continuous cultivation.     

Nitrate removal rates in woodchip media of varying age

A variety of low-cost carbonaceous solids have been successfully tested in bioreactors designed for nitrate treatment. In many agricultural and wastewater settings, however, such reactors may be practical only if they are maintenance free for a number of years after installation. Although field installations have demonstrated consistent treatment over multi-year timeframes, the ability to accurately quantify slowly declining reaction rates in field settings is problematic because of variations in reactor flow rates, ambient temperatures and influent chemistry. In this study, laboratory column tests were undertaken on four samples of coarse wood particle media (woodchips), two that were fresh and two that had been in continuous operation in subsurface denitrifying bioreactors for periods of 2 and 7 years respectively. Four experimental runs were undertaken at increasing influent NO₃-N concentrations of from 3.1 to 48.8 mg N L^?1. Nitrate mass removal rates remained relatively constant and did not systematically increase in successive runs at higher NO₃ concentrations indicating that NO₃ was not the rate-limiting substrate at these concentrations. Thus, zero-order reaction kinetics were used to model the attenuation reaction (presumably denitrification). The 7-year-old media had a mean NO₃-N removal rate of 9.1 mg N L^?1 d^?1 (6.4 g N m^?3 media d^?1), which remained within 75% of the rate for the 2-year-old media (12.1 mg N L^?1 d^?1 or 8.5 g N m^?3 media d^?11) and within 40–59% of the rate for the fresh chips (15.4–23.0 mg N L^?1 d^?1 or 10.8–16.1 g N m^?3 media d^?1). Results support field experience indicating that woodchips loose about 50% of their reactivity during their first year of operation as soluble organic compounds are leached out, but then relatively stable rates persist for a considerable number of years thereafter.