Kinetics of Growth and Amylase Production of Saccharomycopsis fibuligera on Potato Processing Wastewater

The kinetics of growth and amylase production of Saccharomycopsis fibuligera were studied in a chemostat on a synthetic potato processing blancher water. Dilution rates (D) from 0.101 to 0.480 h⁻¹ were examined. A mathematical model based on the Monod equation was developed. The yield of cell mass from carbohydrates was constant and equal to 0.84. The maximum specific growth rate and the Monod constant were determined to be 0.596 h⁻¹ and 0.226 mg/ml, respectively. An equation for the steady-state starch concentrations was empirically derived. The steady-state noncarbohydrate carbon levels rose linearly with D. Reducing sugars were the growth-limiting substrate, and their steady-state levels conformed to Monod kinetics. The yield of amylase from the cell mass (Y_z) declined as D rose and was described by the equation Y_z = (−8.005D + 4.076). The model predicted that the maximum production of cell mass should occur at D = 0.35 h⁻¹ and the maximum production of amylase should occur at D = 0.22 h⁻¹. The mathematical model presented agreed with the experimental results in its prediction of the steady-state level of reducing sugar, starch, cell mass, and amylase concentrations as well as the productivity of amylase.     

Influence of operational parameters in the flocculation and production ofLactobacillus plantarum

Summary The influence of different operational parameters, such as the dilution rate (D) and the bleeding rate (B), in the production of a flocculent strain ofLactobacillus plantarum was studied. The effect of the dilution rate was demonstrated to be related to the lactic acid concentration inside the reactor. The effect of the bleeding rate was shown to be critical in the stabilization of the operation (due to a better pH control). It also allowed a continuous recovery of cells outside the reactor. Viability testing of the lactic starter cultures showed that operation with cell purge increased the viability of the starter cultures obtained.Nomenclature B Bleeding rate, h^–1 - D Dilution rate, h^–1 - F Feed flow rate, L h^–1 - I Feed velocity, m h^–1 - Specific growth rate, h^–1 - v Lactic acid specific productivity, g g^–1 h^–1 - P Product concentration (lactic acid), g L^–1 - P _out Product concentration leaving the system, g L^–1 - Q _b Bleeding flow rate, L h^–1 - R Recirculation velocity, m h^–1 - S Substract concentration, g L^–1 - t Time, h - T _p Time of ascensional flow (length of the column/total ascensional velocity), h - T _r Residence time (1/D), h - V Volume of the reactor, L - X Cell concentration, g L^–1 - X _out Cell concentration leaving the system, g L^–1     

Ethanol production by immobilized whole cells ofZymomonas mobilis in a continuous flow expanded bed bioreactor and a continuous flow stirred tank bioreactor

Continuous ethanol fermentation by immobilized whole cells ofZymomonas mobilis was investigated in an expanded bed bioreactor and in a continuous stirred tank reactor at glucose concentrations of 100, 150 and 200 g L^–1. The effect of different dilution rates on ethanol production by immobilized whole cells ofZymomonas mobilis was studied in both reactors. The maximum ethanol productivity attained was 21 g L^–1 h^–1 at a dilution rate of 0.36 h^–1 with 150 g glucose L^–1 in the continuous expanded bed bioreactor. The conversion of glucose to ethanol was independent of the glucose concentration in both reactors.     

Effect of Specific Growth Rate on Fermentative Capacity of Baker’s Yeast

The specific growth rate is a key control parameter in the industrial production of baker’s yeast. Nevertheless, quantitative data describing its effect on fermentative capacity are not available from the literature. In this study, the effect of the specific growth rate on the physiology and fermentative capacity of an industrial Saccharomyces cerevisiae strain in aerobic, glucose-limited chemostat cultures was investigated. At specific growth rates (dilution rates, D) below 0.28 h⁻¹, glucose metabolism was fully respiratory. Above this dilution rate, respirofermentative metabolism set in, with ethanol production rates of up to 14 mmol of ethanol · g of biomass⁻¹ · h⁻¹ at D = 0.40 h⁻¹. A substantial fermentative capacity (assayed offline as ethanol production rate under anaerobic conditions) was found in cultures in which no ethanol was detectable (D < 0.28 h⁻¹). This fermentative capacity increased with increasing dilution rates, from 10.0 mmol of ethanol · g of dry yeast biomass⁻¹ · h⁻¹ at D = 0.025 h⁻¹ to 20.5 mmol of ethanol · g of dry yeast biomass⁻¹ · h⁻¹ at D = 0.28 h⁻¹. At even higher dilution rates, the fermentative capacity showed only a small further increase, up to 22.0 mmol of ethanol · g of dry yeast biomass⁻¹ · h⁻¹ at D = 0.40 h⁻¹. The activities of all glycolytic enzymes, pyruvate decarboxylase, and alcohol dehydrogenase were determined in cell extracts. Only the in vitro activities of pyruvate decarboxylase and phosphofructokinase showed a clear positive correlation with fermentative capacity. These enzymes are interesting targets for overexpression in attempts to improve the fermentative capacity of aerobic cultures grown at low specific growth rates.     

Synergistic Interaction Between Anabaena and Zoogloea spp. in Carbon Dioxide-Limited Continuous Cultures

Flocs consisting of Anabaena and Zoogloea spp. were used as a model system for the study of planktonic phototroph-heterotroph interactions. In CO₂-limited continuous culture (3.2 μmol of NaHCO₃ liter⁻¹ h⁻¹, 1.5 μmol of glucose liter⁻¹ h⁻¹, pH 8.5, D = 0.026 h⁻¹), the biomass of the phototroph increased 8.6-fold due to association. However, direct CO₂ exchange accounted for only a 3.8-fold increase. When the glucose supply rate was increased to 7.5 μmol liter⁻¹ h⁻¹, there was a 26-fold increase in biomass. When CO₂ was supplied in excess, there was no difference due to association. In batch culture, using the same medium, the specific growth rate was 0.029 h⁻¹ for the phototroph alone and 0.047 h⁻¹ for the phototroph in association with the heterotroph. The stimulatory effect of the heterotroph was found only under CO₂-limiting conditions and was directly related to the concentration of organic matter supplied in the medium. Both the biomass and the growth rate of the Anabaena sp. were increased by association with the Zoogloea sp. Thus, dissolved organic matter may substitute for CO₂ to maximize both growth rate and biomass production by phototrophs when heterotrophic bacteria are present.     

Efficient production of S-(+)-2-chlorophenylglycine by immobilized penicillin G acylase in a recirculating packed bed reactor

(S)-(+)-2-Chlorophenylglycine 1 is an important intermediate in the synthesis of Clopidogrel. A recirculating packed bed reactor (RPBR) was constructed for efficient production of (S)-1 by kinetic resolution of racemic N-phenylacetyl-2- chlorophenylglycine 2 using immobilized penicillin G acylase (PGA). The immobilized PGA exhibited maximum activity at 50 °C and pH 8.0 with (R,S)-2 as substrate. The kinetic constants (K_m and v_max) of immobilized PGA were calculated to be 20.61 mM and 83.2 mM/min/g, respectively. The substrate displayed inhibitory effect on immobilized PGA with inhibition constant of 221.23 mM. The immobilized PGA showed a strict enantiospecificity for substrate at different temperature, pH and substrate concentration examined. The performance and productivity of RPBR were evaluated by several critical parameters, including immobilized PGA load, substrate feeding rate, height to diameter ratio and so on. The kinetic resolution process shows higher initial reaction rate and conversion by recycling 100 mL of substrate solution (80 mM) through RPBRs packed with 6.0 g immobilized PGA with a feeding rate of 1.5 mL/min while the H/D ratio was 4.0. The immobilized PGA-catalyzed kinetic resolution of (R,S)-2 was successfully operated in the RPBR for 60 batches, with an average productivity of 1.2 g/L/h for (S)-1 in high optical purity (>97% enantiomeric excess) in semi-continuous operation. The residual (R)-2 can be easily racemized and then used as substrate.     

Production of aglycone protopanaxatriol from ginseng root extract using Dictyoglomus turgidum β-glycosidase that specifically hydrolyzes the xylose at the C-6 position and the glucose in protopanaxatriol-type ginsenosides

The hydrolytic activity of a recombinant β-glycosidase from Dictyoglomus turgidum that specifically hydrolyzed the xylose at the C-6 position and the glucose in protopanaxatriol (PPT)-type ginsenosides followed the order Rf > Rg₁ > Re > R₁ > Rh₁ > R₂. The production of aglycone protopanaxatriol (APPT) from ginsenoside Rf was optimal at pH 6.0, 80 °C, 1 mg ml^?1 Rf, and 10.6 U ml^?1 enzyme. Under these conditions, D. turgidum β-glycosidase converted ginsenoside R₁ to APPT with a molar conversion yield of 75.6 % and a productivity of 15 mg l^?1 h^?1 after 24 h by the transformation pathway of R₁ → R₂ → Rh₁ → APPT, whereas the complete conversion of ginsenosides Rf and Rg₁ to APPT was achieved with a productivity of 1,515 mg l^?1 h^?1 after 6.6 h by the pathways of Rf → Rh₁ → APPT and Rg₁ → Rh₁ → APPT, respectively. In addition, D. turgidum β-glycosidase produced 0.54 mg ml^?1 APPT from 2.29 mg ml^?1 PPT-type ginsenosides of Panax ginseng root extract after 24 h, with a molar conversion yield of 43.2 % and a productivity of 23 mg l^?1 h^?1, and 0.62 mg ml^?1 APPT from 1.35 mg ml^?1 PPT-type ginsenosides of Panax notoginseng root extract after 20 h, with a molar conversion yield of 81.2 % and a productivity of 31 mg l^?1 h^?1. This is the first report on the APPT production from ginseng root extract. Moreover, the concentrations, yields, and productivities of APPT achieved in the present study are the highest reported to date.     

Continuous production ofl-lactic acid from whey permeate by immobilizedLactobacillus casei subsp.casei

Summary The production of l-lactic acid from whey permeate, a waste product of the dairy industry, by fermentation with the lactic acid bacterium Lactobacillus casei subsp. casei was investigated. A fermentation medium consisting of permeate and supplements, which enables exponential growth of the organisms, was developed. A fast method for determination of free and immobilized biomass in solid-rich media, based on measurement of cellular ATP, was evolved. Continuous fermentations in a stirred tank reactor (STR) and in a fluidized bed reactor (FBR) with immobilized biomass were compared. In the STR a volumetric productivity of 5.5 g/l per hour at 100% substrate conversion [dilution rate (D) = 0.22 h^–1] was determined. In the FBR porous sintered glass beads were used for immobilization and a maximum biomass concentration of 105 g/kg support was measured. A productivity of 10 g/l per hour was obtained at D = 0.4 h^–1 (substrate conversion 93%) and of 13.5 g/l per hour at D = 1.0 h^–1 (substrate conversion 50%). Offprint requests to: W. Krischke     

In glucose-limited continuous culture the minimum substrate concentration for growth,smin, is crucial in the competition between the enterobacterium Escherichia coli and Chelatobacter heintzii,an environmentally abundant bacterium

The competition for glucose between Escherichia coli ML30, a typical copiotrophic enterobacterium and Chelatobacter heintzii ATCC29600, an environmentally successful strain, was studied in a carbon-limited culture at low dilution rates. First, as a base for modelling, the kinetic parameters μ_max and K_s were determined for growth with glucose. For both strains, μ_max was determined in batch culture after different precultivation conditions. In the case of C. heintzii, μ_max was virtually independent of precultivation conditions. When inoculated into a glucose-excess batch culture medium from a glucose-limited chemostat run at a dilution rate of 0.075 h⁻¹ C. heintzii grew immediately with a μ_max of 0.17±0.03 h⁻¹. After five transfers in batch culture, μ_max had increased only slightly to 0.18±0.03 h⁻¹. A different pattern was observed in the case of E. coli. Inoculated from a glucose-limited chemostat at D=0.075 h⁻¹ into glucose-excess batch medium E. coli grew only after an acceleration phase of ∼3.5 h with a μ_max of 0.52 h⁻¹. After 120 generations and several transfers into fresh medium, μ_max had increased to 0.80±0.03 h⁻¹. For long-term adapted chemostat-cultivated cells, a K_s for glucose of 15 μg l⁻¹ for C. heintzii, and of 35 μg l⁻¹ for E. coli, respectively, was determined in ¹⁴C-labelled glucose uptake experiments. In competition experiments, the population dynamics of the mixed culture was determined using specific surface antibodies against C. heintzii and a specific 16S rRNA probe for E. coli. C. heintzii outcompeted E. coli in glucose-limited continuous culture at the low dilution rates of 0.05 and 0.075 h⁻¹. Using the determined pure culture parameter values for K_s and μ_max, it was only possible to simulate the population dynamics during competition with an extended form of the Monod model, which includes a finite substrate concentration at zero growth rate (s_min). The values estimated for s_min were dependent on growth rate; at D=0.05 h⁻¹, it was 12.6 and 0 μg l⁻¹ for E. coli and C. heintzii, respectively. To fit the data at D=0.075 h⁻¹, s_min for E. coli had to be raised to 34.9 μg l⁻¹ whereas s_min for C. heintzii remained zero. The results of the mathematical simulation suggest that it is not so much the higher K_s value, which is responsible for the unsuccessful competition of E. coli at low residual glucose concentration, but rather the existence of a significant s_min.     

Mass transfer studies on the reduction of Cr(VI) using calcium alginate immobilized Bacillus sp. in packed bed reactor

This study presents the external mass transfer effects on the reduction of hexavalent chromium (Cr(VI)) using calcium alginate immobilized Bacillus sp. in a re-circulated packed bed batch reactor (RPBR). The effect of flow rate on the reduction Cr(VI) was studied. Theoretically calculated rate constants for various flow rates were analyzed using external film diffusion models and compared with experimental values. The external mass transfer coefficients for the bioconversion of Cr(VI) were also investigated. The external mass transfer effect was correlated with a model of the type J_D = K Re⁻⁽¹⁻ⁿ⁾. The model was tested with various K values and the mass transfer correlation J_D = 5.7 Re^−0.70 was found to predict the experimental data accurately. The proposed model would be useful for the design of industrial reactor and scale up.     

Efficient preparation of enantiopure l-tert-leucine through immobilized penicillin G acylase catalyzed kinetic resolution in aqueous medium

Racemic _DL-tert-leucine (_DL-Tle) was resolved to obtain enantiopure _L-Tle through enantioselective hydrolysis of its N-phenylacetyl derivative with immobilized penicillin G acylase (PGA). The effects of pH, reaction temperature, substrate concentration and reaction time on the reaction were investigated. The reaction was conveniently carried out at 0.4 M substrate concentration in water at pH 8.0 and 30 °C. Under the optimized reaction conditions, _L-Tle was obtained in an enantiopure form (>99% ee) with 45.8% substrate conversion after 4 h. The thermal stability and operational stability of immobilized PGA were examined. Furthermore, the preparation of _L-Tle was successfully performed in a recirculating packed bed reactor (RPBR) system and immobilized PGA exhibited a long-term stability for 51 days with a slight decrease of activity. The isolated _D-enantiomer was racemized at 160 °C for 15 min and reused as substrate. The results obtained clearly demonstrated a potential for industrial application of immobilized PGA in the preparation of _L-Tle through enantioselective hydrolysis of its N-phenylacetyl derivative.     

Production of ginsenosides Rg1 and Rh1 by hydrolyzing the outer glycoside at the C-6 position in protopanaxatriol-type ginsenosides using β-glucosidase from Pyrococcus furiosus

The specific activity of a recombinant β-glucosidase from Pyrococcus furiosus for protopanaxatriol (PPT)-type ginsenosides followed the order Rf > R₁ > Re > R₂ > Rg₂, which were converted to Rh₁, Rg₁, Rg₁, Rh₁, and Rh₁, respectively. No activity was observed with Rg₁ and Rh₁. Thus, P. furiosus β-glucosidase hydrolyzed the outer glycoside at the C-6 position in PPT-type ginsenosides whereas the enzyme did not hydrolyze the inner glucoside at the C-6 position and the glucoside at the C-20 position. The activity for Rf was optimal at 95 °C, pH 5.5, 5 mM ginsenoside, and 32 U enzyme l^?1. Under these conditions, P. furiosus β-glucosidase completely converted from R₁ to Rg₁ after 10 h, with a productivity of 0.4 g l^?1 h^?1 and completely converted Rf to Rh₁ after 1.2 h, with a productivity of 2.74 g l^?1 h^?1.     

Kinetics of Denitrifying Growth by Fast-Growing Cowpea Rhizobia

Two fast-growing strains of cowpea rhizobia (A26 and A28) were found to grow anaerobically at the expense of NO₃⁻, NO₂⁻, and N₂O as terminal electron acceptors. The two major differences between aerobic and denitrifying growth were lower yield coefficients (Y) and higher saturation constants (K_s) with nitrogenous oxides as electron acceptors. When grown aerobically, A26 and A28 adhered to Monod kinetics, respectively, as follows: K_s, 3.4 and 3.8 μM; Y, 16.0 and 14.0 g · cells eq⁻¹; μ_max, 0.41 and 0.33 h⁻¹. Yield coefficients for denitrifying growth ranged from 40 to 70% of those for aerobic growth. Only A26 adhered to Monod kinetics with respect to growth on all three nitrogenous oxides. The apparent K_s values were 41, 270, and 460 μM for nitrous oxide, nitrate, and nitrite, respectively; the K_s for A28 grown on nitrate was 250 μM. The results are kinetically and thermodynamically consistent in explaining why O₂ is the preferred electron acceptor. Although no definitive conclusions could be drawn regarding preferential utilization of nitrogenous oxides, nitrite was inhibitory to both strains and effected slower growth. However, growth rates were identical (μ_max, 0.41 h⁻¹) when A26 was grown with either O₂ or NO₃⁻ as an electron acceptor and were only slightly reduced when A28 was grown with NO₃⁻ (0.25 h⁻¹) as opposed to O₂ (0.33 h⁻¹).     

Chemostat Enrichments of Human Feces with Resistant Starch Are Selective for Adherent Butyrate-Producing Clostridia at High Dilution Rates

Resistant starch (RS) enrichments were made using chemostats inoculated with human feces from two individuals at two dilution rates (D = 0.03 h⁻¹ and D = 0.30 h⁻¹) to select for slow- and fast-growing amylolytic communities. The fermentations were studied by analysis of short-chain fatty acids, amylase and α-glucosidase activities, and viable counts of the predominant culturable populations and the use of 16S rRNA-targeted oligonucleotide probes. Considerable butyrate was produced at D = 0.30 h⁻¹, which corresponded with reduced branched-chain fatty acid formation. At both dilution rates, high levels of extracellular amylase activity were produced, while α-glucosidase was predominantly cell associated. Bacteroides and bifidobacteria predominated at the low dilution rate, whereas saccharolytic clostridia became more important at D = 0.30 h⁻¹. Microscopic examination showed that within 48 h of inoculation, one particular bacterial morphotype predominated in RS enrichments at D = 0.30 h⁻¹. This organism attached apically to RS granules and formed rosette-like structures which, with glycocalyx formation, agglomerated to form biofilm networks in the planktonic phase. Attempts to isolate this bacterium in pure culture were repeatedly unsuccessful, although a single colony was eventually obtained. On the basis of its 16S rDNA sequence, this RS-degrading, butyrate-producing organism was identified as being a previously unidentified group I Clostridium sp. A 16S rRNA-targeted probe was designed using this sequence and used to assess the abundance of the population in the enrichments. At 240 h, its contributions to total rRNA in the chemostats were 5 and 23% at D = 0.03 and 0.30 h⁻¹, respectively. This study indicates that bacterial populations with significant metabolic potential can be overlooked using culture-based methodologies. This may provide a paradigm for explaining the discrepancy between the low numbers of butyrate-producing bacteria that are isolated from fecal samples and the actual production of butyrate.     

Thermodynamics of Formate-Oxidizing Metabolism and Implications for H2 Production

Formate-dependent proton reduction to H₂ (HCOO⁻ + H₂O → HCO₃⁻ + H₂) has been reported for hyperthermophilic Thermococcus strains. In this study, a hyperthermophilic archaeon, Thermococcus onnurineus strain NA1, yielded H₂ accumulation to a partial pressure of 1 × 10⁵ to 7 × 10⁵ Pa until the values of Gibbs free energy change (ΔG) reached near thermodynamic equilibrium (−1 to −3 kJ mol⁻¹). The bioenergetic requirement for the metabolism to conserve energy was demonstrated by ΔG values as small as −5 kJ mol⁻¹, which are less than the biological minimum energy quantum, −20 kJ mol⁻¹, as calculated by Schink (B. Schink, Microbiol. Mol. Biol. Rev. 61:262-280, 1997). Considering formate as a possible H₂ storage material, the H₂ production potential of the strain was assessed. The volumetric H₂ production rate increased linearly with increasing cell density, leading to 2,820 mmol liter⁻¹ h⁻¹ at an optical density at 600 nm (OD₆₀₀) of 18.6, and resulted in the high specific H₂ production rates of 404 ± 6 mmol g⁻¹ h⁻¹. The H₂ productivity indicates the great potential of T. onnurineus strain NA1 for practical application in comparison with H₂-producing microbes. Our result demonstrates that T. onnurineus strain NA1 has a highly efficient metabolic system to thrive on formate in hydrothermal systems.     

In Situ Activity and Spatial Organization of Anaerobic Ammonium-Oxidizing (Anammox) Bacteria in Biofilms

We investigated autotrophic anaerobic ammonium-oxidizing (anammox) biofilms for their spatial organization, community composition, and in situ activities by using molecular biological techniques combined with microelectrodes. Results of phylogenetic analysis and fluorescence in situ hybridization (FISH) revealed that “Brocadia”-like anammox bacteria that hybridized with the Amx820 probe dominated, with 60 to 92% of total bacteria in the upper part (<1,000 μm) of the biofilm, where high anammox activity was mainly detected with microelectrodes. The relative abundance of anammox bacteria decreased along the flow direction of the reactor. FISH results also indicated that Nitrosomonas-, Nitrosospira-, and Nitrosococcus-like aerobic ammonia-oxidizing bacteria (AOB) and Nitrospira-like nitrite-oxidizing bacteria (NOB) coexisted with anammox bacteria and accounted for 13 to 21% of total bacteria in the biofilms. Microelectrode measurements at three points along the anammox reactor revealed that the NH₄⁺ and NO₂⁻ consumption rates decreased from 0.68 and 0.64 μmol cm⁻² h⁻¹ at P2 (the second port, 170 mm from the inlet port) to 0.30 and 0.35 μmol cm⁻² h⁻¹ at P3 (the third port, 205 mm from the inlet port), respectively. No anammox activity was detected at P4 (the fourth port, 240 mm from the inlet port), even though sufficient amounts of NH₄⁺ and NO₂⁻ and a high abundance of anammox bacteria were still present. This result could be explained by the inhibitory effect of organic compounds derived from biomass decay and/or produced by anammox and coexisting bacteria in the upper parts of the biofilm and in the upstream part of the reactor. The anammox activities in the biofilm determined by microelectrodes reflected the overall reactor performance. The several groups of aerobic AOB lineages, Nitrospira-like NOB, and Betaproteobacteria coexisting in the anammox biofilm might consume a trace amount of O₂ or organic compounds, which consequently established suitable microenvironments for anammox bacteria.     

Improvement of a mammalian cell culture process by adaptive,model-based dialysis fed-batch cultivation and suppression of apoptosis

Both conventional and genetic engineering techniques can significantly improve the performance of animal cell cultures for the large-scale production of pharmaceutical products. In this paper, the effect of such techniques on cell yield and antibody production of two NS0 cell lines is presented. On the one hand, the effect of fed-batch cultivation using dialysis is compared to cultivation without dialysis. Maximum cell density could be increased by a factor of ~5–7 by dialysis fed-batch cultivation. On the other hand, suppression of apoptosis in the NS0 cell line 6A1 bcl-2 resulted in a prolonged growth phase and a higher viability and maximum cell density in fed-batch cultivation in contrast to the control cell line 6A1 (100)3. These factors resulted in more product formation (by a factor ~2). Finally, the adaptive model-based OLFO controller, developed as a general tool for cell culture fed-batch processes, was able to control the fed-batch and dialysis fed-batch cultivations of both cell lines.Abbreviations A membrane area (dm²) - c _Glc,F glucose concentration in nutrient feed (mmol L^–1) - c _Glc,FD glucose concentration in dialysis feed (mmol L^–1) - c _Glc,i glucose concentration in inner reactor chamber (mmol L^–1) - c _Glc,o glucose concentration in outer reactor chamber (dialysis chamber) (mmol L^–1) - c _Lac,FD lactate concentration in dialysis feed (mmol L^–1) - c _Lac,i lactate concentration in inner reactor chamber (mmol L^–1) - c _Lac,o lactate concentration in outer reactor chamber (dialysis chamber) (mmol L^–1) - c _LS,FD limiting substrate concentration in dialysis feed (mmol L^–1) - c _LS,i limiting substrate concentration in inner reactor chamber (mmol L^–1) - c _LS,o limiting substrate concentration in outer reactor chamber (dialysis chamber) (mmol L^–1) - c _Mab monoclonal antibody concentration (mg L^–1) - F _D feed rate of dialysis feed (L h^–1) - F _Glc feed rate of nutrient concentrate feed (L h^–1) - K _d maximum death constant (h^–1) - k _d,LS death rate constant for limiting substrate (mmol L^–1) - k _Glc monod kinetic constant for glucose uptake (mmol L^–1) - k _Lac monod kinetic constant for lactate uptake (mmol L^–1) - k _LS monod kinetic constant for limiting substrate uptake (mmol L^–1) - K _Lys cell lysis constant (h^–1) - K _S,Glc monod kinetic constant for glucose (mmol L^–1) - K _S,LS monod kinetic constant for limiting substrate (mmol L^–1) - µ cell-specific growth rate (h^–1) - µ _d cell-specific death rate (h^–1) - µ _d,min minimum cell-specific death rate (h^–1) - µ _max maximum cell-specific growth rate (h^–1) - P _Glc membrane permeation coefficient for glucose (dm h^–1) - P _Lac membrane permeation coefficient for lactate (dm h^–1) - P _LS membrane permeation coefficient for limiting substrate (dm h^–1) - q _Glc cell-specific glucose uptake rate (mmol cell^–1 h^–1) - q _Glc,max maximum cell-specific glucose uptake rate (mmol cell^–1 h^–1) - q _Lac cell-specific lactate uptake/production rate (mmol cell^–1 h^–1) - q _Lac,max maximum cell-specific lactate uptake rate (mmol cell^–1 h^–1) - q _LS cell-specific limiting substrate uptake rate (mmol cell^–1 h^–1) - q _LS,max maximum cell-specific limiting substrate uptake rate (mmol cell ^–1 h^–1) - q _Mab cell-specific antibody production rate (mg cell^–1 h^–1) - q _MAb,max maximum cell-specific antibody production rate (mg cell^–1 h^–1) - t time (h) - V _i volume of inner reactor chamber (culture chamber) (L) - V _o volume of outer reactor chamber (dialysis chamber) (L) - X _t total cell concentration (cells L^–1) - X viable cell concentration (cells L^–1) - Y _Lac/Glc kinetic production constant (stoichiometric ratio of lactate production and glucose uptake) (–)     

Immobilization of invertase on a new type of macroporous glycidyl methacrylate

Invertase was immobilized via its carbohydrate moiety. The immobilized enzyme has a specific activity of 5500 IU g^–1, with 45% activity yield on immobilization. In a packed bed reactor, 90% 2.5 M sucrose was converted at a flow rate of 4 bed volumes h^–1. The obtained specific productivity at 40 °C of 3 kg l^–1 h^–1 is the best one so far. Long-term stability was 290 days in 2.5 M sucrose at 40 °C and at a flow rate of 3 bed volumes h^–1.     

Ethanol from Whey: Continuous Fermentation with a Catabolite Repression-Resistant Saccharomyces cerevisiae Mutant

An alternative method for the conversion of cheese whey lactose into ethanol has been demonstrated. With the help of continuous-culture technology, a catabolite repression-resistant mutant of Saccharomyces cerevisiae completely fermented equimolar mixtures of glucose and galactose into ethanol. The first step in this process was a computer-controlled fed-batch operation based on the carbon dioxide evolution rate of the culture. In the absence of inhibitory ethanol concentrations, this step allowed us to obtain high biomass concentrations before continuous fermentation. The continuous anaerobic process successfully incorporated a cell-recycle system to optimize the fermentor productivity. Under conditions permitting a low residual sugar concentration (≤1%), maximum productivity (13.6 g liter⁻¹ h⁻¹) was gained from 15% substrate in the continuous feed at a dilution rate of 0.2 h⁻¹. Complete fermentation of highly concentrated feed solutions (20%) was also demonstrated, but only with greatly diminished fermentor productivity (5.5 g liter⁻¹ h⁻¹).     

The metabolic origins of non-photorespiratory CO2 release during photosynthesis: a metabolic flux analysis

Respiration in the light (R_L) releases CO₂ in photosynthesizing leaves and is a phenomenon that occurs independently from photorespiration. Since R_L lowers net carbon fixation, understanding R_L could help improve plant carbon-use efficiency and models of crop photosynthesis. Although R_L was identified more than 75 years ago, its biochemical mechanisms remain unclear. To identify reactions contributing to R_L, we mapped metabolic fluxes in photosynthesizing source leaves of the oilseed crop and model plant camelina (Camelina sativa). We performed a flux analysis using isotopic labeling patterns of central metabolites during ¹³CO₂ labeling time course, gas exchange, and carbohydrate production rate experiments. To quantify the contributions of multiple potential CO₂ sources with statistical and biological confidence, we increased the number of metabolites measured and reduced biological and technical heterogeneity by using single mature source leaves and quickly quenching metabolism by directly injecting liquid N₂; we then compared the goodness-of-fit between these data and data from models with alternative metabolic network structures and constraints. Our analysis predicted that R_L releases 5.2 μmol CO₂ g⁻¹ FW h⁻¹ of CO₂, which is relatively consistent with a value of 9.3 μmol CO₂ g⁻¹ FW h⁻¹ measured by CO₂ gas exchange. The results indicated that ≤10% of R_L results from TCA cycle reactions, which are widely considered to dominate R_L. Further analysis of the results indicated that oxidation of glucose-6-phosphate to pentose phosphate via 6-phosphogluconate (the G6P/OPP shunt) can account for >93% of CO₂ released by R_L.