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1.
Summary A new control policy for the on-line optimization of the nutrient supply in bakers yeast process is proposed. A feed rate corresponding to minimal substrate uptake time was shown to be optimal for cell yield and specific growth rate. Cultivation results of baker's yeast are presented.Nomenclature c glucose concentration in wort (mol.l–1) - C total glucose used (mol) - ce ethanol concentration in wort (mg.l–1) - cp glucose concentration in fresh medium (mol.l–1) - dt/dc glucose consumption time (sec.mol–1) - F substrate feed rate (litre.hr–1) - qc glucose uptake rate (mol.hr–1) - Qc specific glucose uptake rate (moll.g–1.hr–1) - qO2 oxygen uptake rate (mol.hr–1) - QO2 specific oxygen uptake rate (mol.g–1.hr–1) - rx productivity (g.l–1.hr–1) - t time (hr) - x biomass concentration (g.l–1) - X total biomass (g) - Yx/c cell yield (g.g–1): (g.mol–1) - Yo/c consumed oxygen to glucose ratio (mol.mol–1)  相似文献   

2.
Summary Chaetomium cellulolyticum (ATCC 32319) was cultivated on glucose, Avicel and/or Sigmacell in a 20-1 stirred tank batch reactor. The substrate (cellulose) concentration, the cell mass concentration (through protein and/or nitrogen content), reducing sugar concentration, the enzyme activity, the alkali consumption rate, the dissolved O2 and CO2 concentrations in the outlet gas were measured. The specific growth rate, the substrate yield coefficient, cell productivity, the oxygen consumption rate, the CO2 production rate and the volumetric mass transfer coefficient were determined. At the beginning of the growth phase the oxygen utilization rate exhibits a sharp maximum. This maximum could be used to start process control. Because of the long lag phase periodic batch operation is recommended.Symbols CP cell protein concentration (g l–1) - FPA FP enzyme activity (IU l–1) - GP dissolved protein concentration (g l–1) - IU international unit of enzyme activity - kLa volumetric mass tranfer coefficient (h–1) - LG alkali (1 n NaOH) consumption (ml) - LGX specific alkali consumption rate per cell mass (ml g–1 h–1) - P cell mass productivity (g l–1 h–1) - specific oxygen consumption rate per cell mass (g g–1 h–1) - Q aeration rate (volumetric gas flow rate per volume of medium, vvm) (min–1) - N impeller speed (revolution per minute, rpm) (min–1) - S substrate concentration (g l–1) - S0 S at tF=0 (g l–1) - S0 S in feed (g l–1) - SR acid consumption (ml) - TDW total dry weight (g l–1) - T temperature (° C) - tF cultivation time (h) - U substrate conversion - X cell mass concentration (g l–1) - YX/S vield coefficient - specific growth rate (h–1) - m maximum specific growth rate (h–1)  相似文献   

3.
Summary The growth parameters ofPenicillium cyclopium have been evaluated in a continuous culture system for the production of fungal protein from whey. Dilution rates varied from 0.05 to 0.20 h–1 under constant conditions of temperature (28°C) and pH (3.5). The saturation coefficients in the Monod equation were 0.74 g l–1 for lactose and 0.14 mg l–1 for oxygen, respectively. For a wide range of dilution rates, the yield was 0.68 g g–1 biomass per lactose and the maintenance coefficient 0.005 g g–1 h–1 lactose per biomass, respectively. The maximum biomass productivity achieved was 2 g l–1 h–1 biomass at dilution rates of 0.16–0.17 h–1 with a lactose concentration of 20 g l–1 in the feed. The crude protein and total nucleic acid contents increased with a dilution rate, crude protein content varied from 43% to 54% and total nucleic acids from 6 to 9% in the range of dilution rates from 0.05 to 0.2 h–1, while the Lowry protein content was almost constant at approximately 37.5% of dry matter.Nomenclature (mg l–1) Co initial concentration of dissolved oxygen - (h–1) D dilution rate - (mg l–1) K02 saturation coefficient for oxygen - (g l–1) Ks saturation coefficient for substrate - (g g–1 h–1) lactose per biomass) m maintenance energy coefficient - (mM g–1 h–1O2 per biomass) Q02 specific oxygen uptake rate - (g l–1) S residual substrate concentration at steady state - (g l–1) So initial substrate concentration in feed - (min) t1/2 time when Co is equal to Co/2 - (g l–1) X biomass concentration - (g l–1) X biomass concentration at steady state - (g g–1 biomass per lactose) YG yield coefficient for cell growth - (g g–1 biomass per lactose) Yx/s overall yield coefficient - (h–1) specific growth rate  相似文献   

4.
A murine hybridoma cell line producing a monoclonal antibody against penicillin-G-amidase and a murine transfectoma cell line secreting a monovalent chimeric human/mouse Fab-antibody fragment were cultivated in three different media (serum-containing, low protein serum-free, and iron-rich protein-free) in flask cultures, stirred reactors and a fixed bed reactor. In static batch cultures in flasks both cell lines showed similar good growth in all three media.In suspension in a stirred reactor, the hybridoma cell line could be cultivated satisfactory only in serum-containing medium. In low protein serum-free medium, Pluronic F68 had to be added to protect the hybridoma cells against shear stress. But even with this supplement only batch, not chemostat mode was possible. In iron-rich protein-free medium the hybridoma cells grew also in continuous chemostat mode, but the stability of the culture was low. The transfectoma cell line did not grow in stirred reactors in any of the three media.Good results with both cell lines were obtained in fixed bed experiments, where the cells were immobilized in macroporous Siran®-carriers. The media, which were optimized in flask cultures, could be used without any further adaptation in the fixed bed reactor. Immobilization improved the stability and reliability of cultures of non-adherent animal cells in serum-free media tremendously compared to suspension cultures in stirred reactors. The volume-specific glucose uptake rate, an, indicator of the activity of the immobilized cells, was similar in all three media. Deviations in the metabolism of immobilized and suspended cells seem to be mainly due to low oxygen concentrations within the macroporous carriers, where the cells are supplied with oxygen only by diffusion.List of symbols c substrate or product concentration mmol l–1 - c0 substrate or product concentration in the feed mmol l–1 - cGlc glucose concentration mmol l–1 - cGln glutamine concentration mmol l–1 - cAmm ammonia concentration mmol l–1 - cLac lactate concentration mmol l–1 - cFAB concentration of Fab# 10 antibody fragment g l–1 - cMAb monoclonal antibody concentration mg l–1 - D dilution rate d–1 - q cell-specific substrate uptake or metabolite production rate mmol cell–1 h–1 - qGlc cell-specific glucose uptake rate mmol cell–1 h–1 - qGln cell-specific glutamine uptake rate mmol cell–1 h–1 - qMAb cell-specific MAb production rate mg cell–1 h–1 - q* volume-specific substrate uptake or metabolite production rate mmol l–1 h–1 - q*FB volume-specific substrate uptake or metabolite production rate related to the fixed bed volume mmol lFB –1 h–1 - q*FB,Glc volume-specific glucose uptake rate related to the fixed bed volume mmol lFB –1 h–1 - q*FB,Gln volume-specific glutamine uptake rate related to the fixed volume mmol lFB –1 h–1 - q*FB,MAb volume-specific MAb production rate related to the fixed volume mg lFB –1 h–1 - q*FB,02 volume-specific oxygen uptake rate related to the fixed bed volume mmol lFB –1 h–1 - t time h - U superficial flow velocity mm s–1 - V medium volume in the conditioning vessel of the fixed bed reactor l - VFB volume of the fixed bed l - xv viable cell concentration cells ml–1 - yAmm,Gln yield of Ammonia from glutamine - yLac,Glc yield of lactate from glucose - specific growth rate h–1 - d specific death rate h–1  相似文献   

5.
Simultaneous nitrification and denitrification using a mixed methanotrophic culture was investigated. When both NO3 -N (108 mg l–1) and NH3-N (59 mg l–1) were added into batch reactors, nitrate removal was complete within 10 h at the rate of 47 mg NO3 -N g VSS–1 day–1 when dissolved oxygen (DO) concentration was maintained at 2 mg DO l–1. Ammonia removal started simultaneously with nitrate removal at a slower rate of 14 NH3-N g VSS–1 day–1. No significant accumulation of nitrite or nitrate during ammonia utilization suggested the occurrence of simultaneous nitrification and denitrification.  相似文献   

6.
Summary Submerged batch cultivation under controlled environmental conditions of pH 3.8, temperature 30°C, and KLa200 h–1 (above 180 mMO2 l –1 h–1 oxygen supply rate) produced a maximum (12.0 g·l –1) SCP (Candida utilis) yield on the deseeded nopal fruit juice medium containing C/N ratio of 7.0 (initial sugar concentration 25 g·l –1) with a yield coefficient of 0.52 g cells/g sugar. In continuous cultivation, 19.9 g·l –1 cell mass could be obtained at a dilution rate (D) of 0.36 h–1 under identical environmental conditions, showing a productivity of 7.2 g·l –1·h–1. This corresponded to a gain of 9.0 in productivity in continuous culture over batch culture. Starting with steady state values of state variables, cell mass (CX–19.9 g·l –1), limiting nutrient concentration (Cln–2.5 g·l –1) and sugar concentration (CS–1.5 g·l –1) at control variable conditions of pH 3.8, 30°C, and KLa 200 h–1 keeping D=0.36 h–1 as reference, transient response studies by step changes of these control variables also showed that this pH, temperature and KLa conditions are most suitable for SCP cultivation on nopal fruit juice. Kinetic equations obtained from experimental data were analysed and kinetic parameters determined graphically. Results of SCP production from nopal fruit juice are described.Nomenclature Cln concentration of ammonium sulfate (g·l –1) - CS concentration of total sugar (g·l –1) - CX cell concentration (g·l –1) - D dilution rate (h–1) - Kln Monod's constant (g·l –1) - m maintenance coefficient (g ammonium sulfate cell–1 h–1) - m(S) maintenance coefficient (g sugar g cell–1 h–1) - t time, h - Y yield coefficient (g cells/g ammonium sulfate) - Ym maximum of Y - YS yield coefficient based on sugar consumed (g cells · g sugar–1) - YS(m) maximum value of YS - µm maximum specific growth rate constant (h–1)  相似文献   

7.
Summary Some environmental affects on cell aggregation described in the literature are briefly summarized. By means of a biomass recirculation culture (Contact system), using the yeast Torulopsis glabrata, the aggregation behavior of cells in static and in dynamic test systems is described. Sedimentation times required to obtain 50 g · l–1 yeast dry matter in static systems were always higher than in dynamic ones.In addition to, influencing the biomass yield, the specific growth rate of the yeast also affected cell aggregation. The specific growth rate and therefore the aggregation could be regulated by the biomass recirculation rate as well as by the sedimenter volume.Abbreviations fo Overflow flow rate (l·h–1) - fR Recycle flow rate (l·h–1) - ft0t Total flow rate through the fermenter (l·h–1) - g Gram - h Hour - DR Fermenter dilution rate due to recycle (h–1) - DS Fermeter dilution rate due to substrate (h–1) - Dtot Total fermenter dilution rate (h–1) - l Liter - Specific growth rate (h–1) - PF Fermenter productivity (g·l–1·h–1) - PFS Overall productivity (g·l–1·h–1) - RpM Rates per minute - RS Residual sugar content in the effluent with respect to the substrate concentration (%) - Y Yield of biomass with respect to sugar concentration (%) - Sed 50 Sedimentation time to reach a YDM of 50 g·l–1 (min) - V Volume (l) - VF Fermenter volume (l) - VSed Sedimenter volume (l) - VVM Volumes per volume and minute - XF YDM in the fermenter (g·l–1) - XF YDM in the recycle (g·l–1) - XS Yeast dry matter due to substrate concentration (g·l–1) - YDM Yeast dry matter (g·l–1)  相似文献   

8.
Summary Optimal growth conditions for Zymomonas mobilis have been established using continuous cultivation methods. Optimal substrate utilization efficiency occurs with 2.5 g l–1 yeast extract, 2.0 g l–1 ammonium sulfate and 6.0 g l–1 magnesium sulfate in the media. Catabolic activity is at its maximum with glucose uptake rates of 16–18 g l–1 h–1 and ethanol production rates of 8–9 g l–1 h–1, Qg values of 22–26 and Qp values between 11 and 13, which results in 40 g l–1 h–1 ethanol yields using a 100 g l–1 substrate feed. Any increase in these parameters goes on cost of substrate utilization efficiency. Calcium pantothenate can not substitute yeast extract.Abbreviations G Glucose (%) - Pant Calcium pantothenate (mg l–1) - D Dilution rate (h–1) - NH4 Ammonium sulfate (%) - Mg Magnesium sulfate (%) - S1 Residual glucose in the fermenter (g l–1) - S0 Glucose feed (g l–1) - Eth Ethanol concentration (g l–1) - GUR Glucose uptake rate (g l–1 h–1) - Qg Specific glucose uptake rate (g g–1 h–1) - Qp Specific ethanol production rate (g g–1 h–1) - EPR Ethanol production rate (g l–1 h–1) - Yg Yield coefficient for glucose (g g–1) - Yp Conversion efficiency (%) - C Biomass concentration (g l–1) Present address: (Until June 1982) Institut für Mikrobiologie, TH Darmstadt, 6100 Darmstdt, Federal Republic of Germany  相似文献   

9.
Pseudomonas sp. 42A2 when incubated for 36 h with oleic acid (20 g l–1) in a stirred bioreactor, accumulated 10-hydroxy-8E-octadecenoic acid. Production in a 2 l bioreactor with 1.4 l of working volume, was increased from 0.65 g l–1 to 7.4 g l–1 with K L a values ranging between 15 and 200 h–1. A linear relationship was found between volumetric productivity and oxygen transfer rates and an exponential relation between the specific rate of product formation and specific growth rate.  相似文献   

10.
Summary A salicylate-hydroxylase-producing strain of Pseudomonas putida with an unusual capability to grow at toxic levels of salicylate up to 10 g l–1 has been isolated. It grew well under continuous culture conditions, with optimum growth at pH 6.5 and a temperature of 25° C. The use of an ammonium salt as a nitrogen source, instead of nitrate, resulted in a 30–40% increase in its biomass yield coefficient. Optimum growth under continuous culture conditions was achieved using 4 g l–1 salicylate at 25° C, pH 6.5 and 0.2 h–1 dilution rate. High salicylate hydroxylase enzyme activity [236 units (U) l–1] and productivity (424.8 U h–1) were obtained at a dilution rate of 0.45 h–1 using a mineral medium containing 4 g l–1 of salicylate. Operating under continuous culture conditions with oxygen limitation and a slight accumulation of residual salicylate (0.2 g l–1) resulted in a decrease in culture performance and enzyme productivity. Correspondence to: R. Marchant  相似文献   

11.
Organic sediments in freshwaters are regularly subject to low concentrations of oxygen. The ability of detritivores to sustain their feeding in such conditions should therefore be of importance for the decomposition process. In the present study, aquaria were used to determine processing rates of five lake-dwelling shredders at three different oxygen concentrations; normoxic (9 mg O2 l–1) and two levels of hypoxia (1 and 2 mg O2 l–1). Discs of alder leaves (Alnus glutinosa (L.)) were used as food. Four species of caddisfly larvae (Trichoptera Limnephilidae) and the isopod, Asellus aquaticus (L.) were compared in the experiments. Significant differences in processing rates per g animal biomass were found both at normoxia and 2 mg oxygen l–1. At l mg O2 l–1 none of the invertebrates fed on leaf discs. The caddisfly larvae Halesus radiatus (Curtis), being one of the two most efficient shredders at normoxia, did not feed at 2 mg oxygen l–1. The other species fed at rates 15–50 of that at normoxia. The least efficient shredder at normoxia, A. aquaticus was similar to two of the trichopterans at 2 mg O2 l–1. This study shows that the importance of specific shredder species may shift in case of hypoxia. Species-specific traits regarding oxygen sensitivity may also be influential for distribution patterns of shredder species both within and between lakes.  相似文献   

12.
Summary The production of L-asparaginase was investigated in Escherichia coli, growing under different conditions of aeration in a medium containing 2% or 6% corn steep. At both concentrations, excessive aeration decreased enzyme production. In the medium with 2% corn steep, L-asparaginase activity began to decline as soon as the oxygen absorption exceeded 0.22 mmol O2 l–1 min–1, and when the oxygen absorption rate was 1.26 mmol O2 l–1 min–1, enzyme activity reached only about 5% of maximum. In the medium with 6% corn steep, a decline of L-asperaginase activity did not appear until the oxygen absorption rate value exceeded 0.54 mmol O2 l–1 min–1, at the oxygen absorption rate of 1.26 mmol O2 l–1 min–1, the enzyme activity still reached about 50% of maximum.  相似文献   

13.
Acetone butanol ethanol (ABE) was produced in an integrated fed-batch fermentation-gas stripping product-recovery system using Clostridium beijerinckii BA101, with H2 and CO2 as the carrier gases. This technique was applied in order to eliminate the substrate and product inhibition that normally restricts ABE production and sugar utilization to less than 20 g l–1 and 60 g l–1, respectively. In the integrated fed-batch fermentation and product recovery system, solvent productivities were improved to 400% of the control batch fermentation productivities. In a control batch reactor, the culture used 45.4 g glucose l–1 and produced 17.6 g total solvents l–1 (yield 0.39 g g–1, productivity 0.29 g l–1 h–1). Using the integrated fermentation-gas stripping product-recovery system with CO2 and H2 as carrier gases, we carried out fed-batch fermentation experiments and measured various characteristics of the fermentation, including ABE production, selectivity, yield and productivity. The fed-batch reactor was operated for 201 h. At the end of the fermentation, an unusually high concentration of total acids (8.5 g l–1) was observed. A total of 500 g glucose was used to produce 232.8 g solvents (77.7 g acetone, 151.7 g butanol, 3.4 g ethanol) in 1 l culture broth. The average solvent yield and productivity were 0.47 g g–1 and 1.16 g l–1 h–1, respectively.  相似文献   

14.
The death of the hybridoma VO 208 in a continuous culture at pH 7 and 6.8 was investigated by measuring both the appearance of visible dead cells which do not exclude the trypan blue dye and the release of lactate dehydrogenase (LDH) in the culture medium. The intracellular LDH was found to be completely released either when live cells lysed or when they were transformed into visible dead cells. No significant lysis of blue dead cells could be observed at the two different pH. Using a LDH balance over the culture system, cell lysis was found negligible at pH 7, but accounted for 20% of the total cell death at pH 6.8. A methodology is proposed to evaluate the rate constants of hybridoma lysis and total death. For the investigated cell line in continuous culture, the calculated total cell death rate constant was found to increase from 0.002 h–1 to 0.01 h–1 when decreasing the pH from 7 to 6.8.Abbreviations D dilution rate (h–1) - kb specific trypan-blue dead cells appearance rate (h–1) - kL specific lysis rate of viable cells (h–1) - kd specific death rate (h-1) - LDH0 lactate dehydrogenase activity in the feed culture medium (IU.l–1) - LDH lactate dehydrogenase activity in the outlet culture medium (IU.l–1) - LDHi intracellular lactate dehydrogenase activity of viable cells (IU.10–9 cells) - rLDH total rate of LDH release (IU.h–1.L–1) - rb transformation rate of viable cells into blue dead cells (109 cells.h–1.L–1) - xv viable cell concentration (109 cells.l–1) - xb trypan-blue dead cell concentration (109 cells.l–1)  相似文献   

15.
Summary Batch and continuous two-stage cultures have been conducted in order to determine the effect of yeast extract (YE) on the homolactic fermentation of whey permeate byLactobacillus helveticus. Supplementation with YE had a significant effet on lactic acid concentration, volumetric productivity, and substrate conversion, but not on lactic acid yield. Volumetric productivity in the first stage increased from 2 to 9 g l–1 per hour by increasing the YE concentration from 1.5 to 25 g l–1 At the same time conversion improved from 22% to 93% at a dilution rate of 0.2 h–1. The second stage demonstrated the effect of YE at a lower dilution rate (0.14 h–1. A high system conversion (97%) and a high final lactic acid concentration (40 g l–1) were achieved with 10 g l–1 YE.  相似文献   

16.
Sequencing-batch reactors were used to develop an activated sludge enrichment culture capable of degrading 1-naphthylamine (1NA). Approximately 5 months acclimation with salicylic acid (1600 mg l–1) as the primary source of carbon were required to obtain an enrichment culture able to degrade even small quantities of 1NA. After an additional 4 months acclimation, during which the concentration of salicyclic acid was decreased to 50 mg l–1, a culture developed that degraded 1NA concentrations as high as 300 mg l–1. Kinetic determinations showed that 1NA degradation (in the presence of salicylate) followed Michaelis-Menten kinetics with K m and V m values of 32.5±2.2 mg l–1 and 375±18 ng 1NA mg–1 cells h–1, respectively. The same enrichement was able to degrade 1NA when present as the sole source of carbon and energy and to convert approximately 87% to CO2.  相似文献   

17.
The profundal zone of Lake Esrom, Denmark has a dense population of Chironomus anthracinus, which survives 2–4 months of oxygen depletion each summer during stratification. The metabolism of 3rd and 4th instar larvae was examined in regard to variation in biomass and temperature. Respiration at air saturation was described by a curvilinear multiple regression relating oxygen consumption to individual AFDW and temperature. At 10 °C and varying oxygen regimes the O2 consumption and CO2 production of 4th instar larvae were almost unaltered from saturation to about 3 mg O2 l–1, but decreased steeply below this level. The respiratory quotient increased from 0.82 at saturation to about 3.4 at oxygen concentrations near 0.5 mg O2 l–1. This implied a shift from aerobic to partially anaerobic metabolism. At 0.5 mg O2 l–1 the total energy production equalled 20% of the rate at saturation of which more than one third was accounted for by anaerobic degradation of glycogen. This corresponded to a daily loss of 12 µg mg AFDW–1 or approximately 5% of the body reserves. At unchanged metabolic rate the glycogen store would last three weeks, but long term oxygen deficiency causes a further suppression of the energy metabolism in C. anthracinus.  相似文献   

18.
A 20-l packed-bed reactor filled with foamed glass beads was tested for the treatment of acetonitrile HPLC wastes. Aeration was provided by recirculating a portion of the reactor liquid phase through an aeration tank, where the dissolved oxygen concentration was kept at 6 mg/l. At a feeding rate of 0.77 g acetonitrile l–1 reactor day–1, 99% of the acetonitrile was removed; and 86% of the nitrogen present in acetonitrile was released as NH3, confirming that acetonitrile volatilization was not significant. Increasing the acetonitrile loading resulted in lower removal efficiencies, but a maximum removal capacity of 1.0 g acetonitrile l–1 reactor day–1 was achieved at a feeding rate of 1.6 g acetonitrile l–1 reactor day–1. The removal capacity of the system was well correlated with the oxygenation capacity, showing that acetonitrile removal was likely to be limited by oxygen supply. Microbial characterization of the biofilm resulted in the isolation of a Comamonas sp. able to mineralize acetonitrile as sole carbon, nitrogen and energy source. This organism was closely related to C. testosteroni (91.2%) and might represent a new species in the Comamonas genus. This study confirms the potential of packed-bed reactors for the treatment of a concentrated mixture of volatile pollutants.  相似文献   

19.
When Euglena gracilis was grown in the heterotrophic condition with glucose and (NH4)2SO4 as the carbon and nitrogen source, a high cell yield (4.28–4.48 g l–1) was obtained and the culture pH decreased to 1.6–2. The biomass production in the heterotrophic culture was compared to those in the autotrophic and mixotrophic cultures. Autotrophic growth was 4.7–6.3% of the heterotrophic one, whereas about 15–19% higher growth was obtained in the mixotrophic culture. Moreover, good production of chlorophyll (39.4 mg l–1) and carotenoids (13.8 mg l–1) were attained in the mixotrophic culture, giving the highest fermenter productivity with respect to biomass as well as chlorophyll and carotenoids. Through an energetic analysis in the mixotrophic culture, it was estimated about 25–28% of the total ATP requirement is formed in the photochemical reactions. This resulted in an improved biomass production in the mixotrophic culture of E. gracilis.  相似文献   

20.
Chlorella sorokiniana was cultured in heterotrophic or mixotrophic mode in outdoor enclosed tubular photobioreactor. The culture temperature was maintained at 32–35 °C. At night, theChlorella culture grew heterotrophically, and 0.1 M glucose was completely consumed. The biomass growth yield of glucose was 0.35 ± 0.001 g-biomass g-glucose–1. During the day, the algal culture grew mixotrophically and the biomass growth yield was 0.49 g-biomass g-glucose–1 in low density culture (initial biomass concentration, Xo = 2 g l–1), 0.56 g-biomass g-glucose–1 in medium density culture (Xo = 4 g l–1) and 0.46 g-biomass g-glucose–1 in high density culture (Xo = 7 g l–1). The daily area productivity of the culture, with Xo = 4 g l–1 corresponded to 127 g-biomass m–2 d–1 during the day and 79 g-biomass m–2 d–1 during the night. In all the cultures, the dissolved O2 concentration increased in the morning, reached the maximum value at noon, and then decreased in the afternoon. The dissolved CO2 concentration remained at 3 mBar in the morning and increased in the afternoon. Glycolate was not found to accumulate in culture medium.  相似文献   

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