Calorimetric control of fed-batch cultures of Saccharomyces cerevisiae

Calorimetry has been used to control the glucose feeding in fed-batch cultures of S. cerevisiae in order to avoid ethanol formation and maintain a fully respiratory metabolism. Comparisons between batch and fed-batch cultivations showed that the former had a much lower growth yield. The growth yields for fed-batch cultivations were more than 30% higher than for batch cultures. However, energy balance calculations showed that a large part of the increase could be explained by the evaporation of ethanol during batch cultivations. When the growth yields obtained from the batch cultures were corrected for the evaporation of ethanol, the increase in growth yield for fed-batch cultures was about 10%.     

On-line monitoring of recombinant bacterial cultures using multi-wavelength fluorescence spectroscopy

Multi-wavelength fluorescence spectroscopy was evaluated as a tool for on-line monitoring of recombinant Escherichia coli cultivations expressing human basic fibroblast growth factor (hFGF-2). The data sets for the various combinations of the excitation and emission spectra from batch cultivations were analyzed using principal component analysis. Chemometric models (the partial least squares method) were developed for correlating the fluorescence data and the experimentally measured variables such as the biomass and glucose concentrations as well as the carbon dioxide production rate. Excellent correlations were obtained for these variables for the calibration cultivations. The predictability of these models was further tested in batch and fed-batch cultivations. The batch cultivations were well predicted by the PLS models for biomass, glucose concentrations and carbon dioxide production rate (RMSEPs were respectively 5%, 7%, 9%). However, when tested for biomass concentrations in fed-batch cultivations (with final biomass three times higher than the highest calibration data) the models had good predictability at high growth rates (RMSEPs were 3% and 4%, respectively for uninduced and induced fed-batch cultivations), which was as good as for the batch cultivations used for developing the models (RMSEPs were 3% and 5%, respectively for uninduced and induced batch cultivations). The fed-batch cultivations performed at low growth rates exhibited much higher fluorescence for fluorophores such as flavin and NAD(P)H as compared to fed-batch cultivations at high growth rate. Therefore, the PLS models tended to over-predict the biomass concentrations at low growth rates. Obviously the cells changed their concentration of biogenic fluorophores depending on the growth rate. Although multi-wavelength fluorescence spectroscopy is a valuable tool for on-line monitoring of bioprocess, care must be taken to re-calibrate the PLS models at different growth rates to improve the accuracy of predictions.     

Controlled pilot development unit-scale fed-batch cultivation of yeast on spruce hydrolysates

Yeast production on hydrolysate is a likely process solution in large-scale ethanol production from lignocellulose. The hydrolysate will be available on site, and the yeast has furthermore been shown to acquire an increased inhibitor tolerance when cultivated on hydrolysate. However, due to over-flow metabolism and inhibition, efficient yeast production on hydrolysate can only be achieved by well-controlled substrate addition. In the present work, a method was developed for controlled addition of hydrolysate to PDU (process development unit)-scale aerobic fed-batch cultivations of Saccharomyces cerevisiae TMB 3000. A feed rate control strategy, which maintains the ethanol concentration at a low constant level, was adapted to process-like conditions. The ethanol concentration was obtained from on-line measurements of the ethanol mole fraction in the exhaust gas. A computer model of the system was developed to optimize control performance. Productivities, biomass yields, and byproduct formation were evaluated. The feed rate control worked satisfactorily and maintained the ethanol concentration close to the setpoint during the cultivations. Biomass yields of 0.45 g/g were obtained on added hexoses during cultivation on hydrolysate and of 0.49 g/g during cultivation on a synthetic medium with glucose as the carbon source. Exponential growth was achieved with a specific growth rate of 0.18 h-1 during cultivation on hydrolysate and 0.22 h-1 during cultivation on glucose.     

Growth and energy metabolism in aerobic fed-batch cultures of Saccharomyces cerevisiae: simulation and model verification

A kinetic model of overflow metabolism in Saccharomyces cerevisiae was used for simulation of aerobic fed-batch cultivations. An inhibitory effect of ethanol on the maximum respiration of the yeast was observed in the experiments and included in the model. The model predicts respiration, biomass, and ethanol formation and the subsequent ethanol consumption, and was experimentally validated in fed-batch cultivations. Oscillating sugar feed with resulting oscillating carbon dioxide production did not influence the maximum respiration rate, which indicates that the pyruvate dehydrogenase complex is not involved as a bottleneck causing aerobic ethanol formation.     

Monitoring and control of Gluconacetobacter xylinus fed-batch cultures using in situ mid-IR spectroscopy

A partial least-squares calibration model, relating mid-infrared spectral features with fructose, ethanol, acetate, gluconacetan, phosphate and ammonium concentrations has been designed to monitor and control cultivations of Gluconacetobacter xylinus and production of gluconacetan, a food grade exopolysaccharide (EPS). Only synthetic solutions containing a mixture of the major components of culture media have been used to calibrate the spectrometer. A factorial design has been applied to determine the composition and concentration in the calibration matrix. This approach guarantees a complete and intelligent scan of the calibration space using only 55 standards. This calibration model allowed standard errors of validation (SEV) for fructose, ethanol, acetate, gluconacetan, ammonium and phosphate concentrations of 1.16 g/l, 0.36 g/l, 0.22 g/l, 1.54 g/l, 0.24 g/l and 0.18 g/l, respectively. With G. xylinus, ethanol is directly oxidized to acetate, which is subsequently metabolized to form biomass. However, residual ethanol in the culture medium prevents bacterial growth. On-line spectroscopic data were implemented in a closed-loop control strategy for fed-batch fermentation. Acetate concentration was controlled at a constant value by feeding ethanol into the bioreactor. The designed fed-batch process allowed biomass production on ethanol. This was not possible in a batch process due to ethanol inhibition of bacterial growth. In this way, the productivity of gluconacetan was increased from 1.8 x 10(-3) [C-mol/C-mol substrate/h] in the batch process to 2.9 x 10(-3) [C-mol/C-mol substrate/h] in the fed-batch process described in this study.     

Experience in using an ethanol sensor to control molasses feed-rates in baker's yeast production

An ethanol sensor has been tested for feed-rate control of baker's yeast prouction. The yeast was grown on molasses in an 8 dm³ fed-batch reactor up to a cell concentration of 60–70 kg/m³. Studies were made on three levels: reliability of the sensor system, characterisation of the control problem, and evaluation of ethanol-controlled cultivations in terms of yield and production rate. Arguments are given for the conceptual advantages of ethanol control compared to other methods of substrate control. It is also shown that ethanol control allows for a simple regulator structure. In fact, a PID regulator, with constant parameters, was used around an exponential dosage scheme. Tuning of the regulator parameters was performed by using simulation on a simplified model of the process. Several cultivations have been carried out. Results from four comparable cultivations are given in detail, and the experience from many others is summarized.     

Fed-batch cultivation of <Emphasis Type="Italic">Saccharomyces cerevisiae</Emphasis> on lignocellulosic hydrolyzate

Saccharomyces cerevisiae grows very poorly in dilute acid lignocellulosic hydrolyzate during the anaerobic fermentation for fuel ethanol production. However, yeast cells grown aerobically on the hydrolyzate have increased tolerance for the hydrolyzate. Cultivation of yeast on part of the hydrolyzate has therefore the potential of enabling increased ethanol productivity in the fermentation of the hydrolyzate. To evaluate the ability of the yeast to grow in the hydrolyzate, fed-batch cultivations were run using the ethanol concentration as input variable to control the feed-rate. The yeast then grew in an undetoxified hydrolyzate with a specific growth rate of 0.19 h⁻¹ by controlling the ethanol concentration at a low level during the cultivation. However, the biomass yield was lower for the cultivation on hydrolyzate compared to synthetic media: with an ethanol set-point of 0.25 g/l the yield was 0.46 g/g on the hydrolyzate, compared to 0.52 g/g for synthetic media. The main reason for the difference was not the ethanol production per se, but a significant production of glycerol at a high specific growth rate. The glycerol production may be attributed to an insufficient respiratory capacity.     

Simulation of penicillin production in fed-batch cultivations using a morphologically structured model

A mathematical model is formulated to describe trends in biomass and penicillin formation as well as substrate consumption for fed-batch cultivations. The biomass is structured into three morphological compartments, and glucose and corn steep liquor are considered as substrates for growth. Penicillin formation is assumed to take place in the subapical compartment and in the growing region of the hyphal compartment. Furthermore, it is inhibited by glucose. Model parameters are estimated using an evolutionary algorithm and fitting the model to a standard fed-batch cultivation. The model is validated on experimental data from three different fed-batch cultivations, including two repeated fed-batch cultivations. The model predictions show good agreement with the measurements of biomass and pencillin concentrations for all fed-batch cultivations. (c) 1997 John Wiley & Sons, Inc. Biotechnol Bioeng 56: 593-604, 1997.     

A morphologically structured model for penicillin production.

A morphologically structured model is proposed to describe penicillin production in fed-batch cultivations. The model accounts for the effects of dissolved oxygen on cell growth and penicillin production and variations in volume fractions of abiotic and biotic phases due to biomass formation. Penicillin production is considered to occur in the subapical hyphal cell compartment and to be affected by availability of glucose and oxygen. As it stands, the model provides a wide range of applicability in terms of operating conditions. The model has been tested for various conditions and has given satisfactory results. A series of glucose feeding profiles have been considered to demonstrate the capabilities of the proposed model. It is concluded that the model may be valuable for the interpretation of experimental data collected specifically for metabolic flux analysis during fed-batch cultivation because the elements of measured specific production rates are determined from measurements of the concentrations of the components and their mass balances. The proposed model may be further used for developing control strategies and model order reduction algorithms.     

Kalman filter based glucose control at small set points during fed-batch cultivation of Saccharomyces cerevisiae

A glucose control system is presented, which is able to control cultivations of Saccharomyces cerevisiae even at low glucose concentrations. Glucose concentrations are determined using a special flow injection analysis (FIA) system, which does not require a sampling module. An extended Kalman filter is employed for smoothing the glucose measurements as well as for the prediction of glucose and biomass concentration, the maximum specific growth rate, and the volume of the culture broth. The predicted values are utilized for feedforward/feedback control of the glucose concentration at set points of 0.08 and 0.05 g/L. The controller established well-defined conditions over several hours up to biomass concentrations of 13.5 and 20.7 g/L, respectively. The specific glucose uptake rates at both set points were 1.04 and 0.68 g/g/h, respectively. It is demonstrated that during fed-batch cultivation an overall pure oxidative metabolism of glucose is maintained at the lower set point and a specific ethanol production rate of 0.18 g/g/h at the higher set point.     

Intracellular pH-based controlled cultivation of yeast cells: II. cultivation methodology

Intracellular pH (pH(i)) was measured on-line in a bioreactor using a fluorescent pH(i) indicator, 9-aminoacridine, and controlled fed-batch cultivations of yeast cells based on pH(i) (FB-pH(i)) were performed. In FB-pH(i) cultivations, automated glucose additions were made to the culture in response to culture pH(i). The average ethanol (an-aerobic product) yield was significantly lower [0.12 g g(-1) glucose in fed-batch pH(i) cultivations with 100 ppm glucose additions (FB-pH(i)-100 cultivation) vs. 0.48 g g(-1) glucose in batch] and cell yield was higher (0.54 g g(-1) glucose in FB-pH(i)-100 cultivation vs. 0.3 g g(-1) glucose in batch) compared to batch cultivation. An expression has been derived to calculate changes in pH(i) from measured fluorescence values when the cell concentration increases during growth. Cultivations based on pH(i), performed with different magnitudes of glucose addition (100, 50, and 10 ppm additions), showed that lower magnitudes of glucose addition resulted in lower ethanol yields while cell yield remained unaffected. The ratio of specific oxygen uptake rate to specific glucose uptake rate (OUR/GUR) increased with decreased in magnitude of glucose additions in FB-pH(i) cultivations, suggesting that the culture aerobic state was higher when the magnitude of glucose addition was lower. The average cell productivity in FB-pH(i) cultivations was 29% higher than in batch cultivation. Cells were also cultivated at high OUR conditions, and the results are compared with other cultivations. (c) 1993 John Wiley & Sons, Inc.     

Fed-batch cultivation of the docosahexaenoic-acid-producing marine alga Crypthecodinium cohnii on ethanol

The heterotrophic marine microalga Crypthecodinium cohnii produces docosahexaenoic acid (DHA), a polyunsaturated fatty acid with food and pharmaceutical applications. So far, DHA production has been studied with glucose and acetic acid as carbon sources. This study investigates the potential of ethanol as an alternative carbon source for DHA production by C. cohnii. In shake-flask cultures, the alga was able to grow on ethanol. The specific growth rate was optimal with 5 g l(-1) ethanol and growth did not occur at 0 g l(-1) and above 15 g l(-1). By contrast, in fed-batch cultivations with a controlled feed of pure ethanol, cumulative ethanol addition could be much higher than 15 g l(-1), thus enabling a high final cell density and DHA production. In a representative fed-batch cultivation of C. cohnii with pure ethanol as feed, 83 g dry biomass l(-1), 35 g total lipid l(-1) and 11.7 g DHA l(-1) were produced in 220 h. The overall volumetric productivity of DHA was 53 mg l(-1 )h(-1), which is the highest value reported so far for this alga.     

Scale-down and parallel operation of the riboflavin production process with Bacillus subtilis

The establishment and the improvement of industrial bioprocesses calls for the selection of media compositions and process conditions in highly parallel experiments as well as for the intensified screening of new biocatalysts and improved production strains. This work presents for the first time the scale-down and the successful adaptation of an industrial riboflavin fed-batch production process with Bacillus subtilis to a fully automated setup with 48 parallel stirred bioreactors at a milliliter scale (10 mL). The feasibility of an intermittent feeding mode and a discontinuous at-line pH control for parallel cultivations over up to 53 h is demonstrated together with interlaced process analyses at a microliter scale for quasi-simultaneous at-line monitoring of biomass, substrate and product concentration. The discontinuous feeding mode necessitated an increased oxygen input, resulting in lower final biomass concentrations. However, the product yields and volumetric productivities in the milliliter setup were equivalent to the yields and productivities obtained during the reference cultivations at laboratory scale, which allows considering the automated system together with the developed schedule as a screening tool for high-throughput bioprocess design of the described production process.     

Simple fed-batch cultivation strategy for the enhanced production of a single-sugar glucuronic acid-based oligosaccharides by a cellulose-producing <Emphasis Type="Italic">Gluconacetobacter hansenii</Emphasis> strain

The production of water-soluble single-sugar glucuronic acid-based oligosaccharides (WSOS) by a cellulose producing strain Gluconacetobacter hansenii PJK was studied in a periodically recycled and fed-batch cultivations using glucose/ethanol or glucose only. Fermentations were carried out in a 2 L jar fermenter equipped with a turbine impeller with 6 flat blades. WSOS were produced constantly but the bacterial cellulose (BC) production stopped at 48 h of cultivation in a periodically recycled culture using the exhausted medium supplemented with glucose and ethanol. Tremendous quantities of WSOS were obtained in fed-batch cultivations using glucose/ethanol (35.6 g/L at 132 h of cultivation) or glucose only (86 g/L after 240 h of cultivation) as the nutritional source. However, the BC production yield under these nutritional conditions decreased significantly in comparison to previous studies about the BC production by the same strain. The overall results revealed that G. hansenii is capable of producing enormous quantities of WSOS compared to those reported previously for compounds of a related chemical nature. Moreover, the WSOS production was found to be dependent on the pH of the culture broth.     

Thermophilic,lignocellulolytic bacteria for ethanol production: current state and perspectives

Lignocellulosic biomass contains a variety of carbohydrates, and their conversion into ethanol by fermentation requires an efficient microbial platform to achieve high yield, productivity, and final titer of ethanol. In recent years, growing attention has been devoted to the development of cellulolytic and saccharolytic thermophilic bacteria for lignocellulosic ethanol production because of their unique properties. First of all, thermophilic bacteria possess unique cellulolytic and hemicellulolytic systems and are considered as potential sources of highly active and thermostable enzymes for efficient biomass hydrolysis. Secondly, thermophilic bacteria ferment a broad range of carbohydrates into ethanol, and some of them display potential for ethanologenic fermentation at high yield. Thirdly, the establishment of the genetic tools for thermophilic bacteria has allowed metabolic engineering, in particular with emphasis on improving ethanol yield, and this facilitates their employment for ethanol production. Finally, different processes for second-generation ethanol production based on thermophilic bacteria have been proposed with the aim to achieve cost-competitive processes. However, thermophilic bacteria exhibit an inherent low tolerance to ethanol and inhibitors in the pretreated biomass, and this is at present the greatest barrier to their industrial application. Further improvement of the properties of thermophilic bacteria, together with the optimization production processes, is equally important for achieving a realistic industrial ethanol production.     

Fermentative capacity in high-cell-density fed-batch cultures of baker's yeast

High-cell-density fed-batch processes for bakers' yeast production will involve a low-average-specific growth rate due to the limited oxygen-transfer capacity of industrial bioreactors. The relationship between specific growth rate and fermentative capacity was investigated in aerobic, sucrose-limited fed-batch cultures of an industrial bakers' yeast strain. Using a defined mineral medium, biomass concentrations of 130 g dry weight/L were reproducibly attained. After an initial exponential-feed phase (mu = 0.18 h(-1)), oxygen-transfer limitation necessitated a gradual decrease of the specific growth rate to ca. 0.01 h(-1). Throughout fed-batch cultivation, sugar metabolism was fully respiratory, with a biomass yield of 0.5 g biomass/g sucrose(-1). Fermentative capacity (assayed off-line as ethanol production rate under anaerobic conditions with excess glucose) showed a strong positive correlation with specific growth rate. The fermentative capacity observed at the end of the process (mu = 0.01 h(-1)) was only half that observed during the exponential-feed phase (mu = 0.18 h(-1)). During fed-batch cultivation, activities of glycolytic enzymes, pyruvate decarboxylase and alcohol dehydrogenase in cell extracts did not exhibit marked changes. This suggests that changes of fermentative capacity during fed-batch cultivation were not primarily caused by regulation of the synthesis of glycolytic enzymes.     

A process for the production of human proinsulin in Saccharomyces cerevisiae

In order to develop a large-scale fermentation process for the production of human proinsulin in yeast, the intra-cellular expression of a human superoxide dismutase-human proinsulin fusion product (SOD-PI) has been studied. The expression of SOD-PI in Saccharomyces cerevisiae is regulated by a hybrid alcohol dehydrogenase 2/glyceraldehyde-3-phosphate dehydrogenase promoter. The promoter is repressed by glucose and derepressed by depletion of glucose. Although the genetic stability of the construction is shown to be poor under product-inducing conditions, it is demonstrated in shake flask experiments that a stable expression potential can be maintained in a complex medium for more than 60 generations by maintaining excess glucose throughout the cultivations. These results have been confirmed in continuous cultures in chemostat and turbidostat experiments. Addition of the glucose analogs glucosamine, 2-desoxyglucose, methylglucose, and thioglucose also leads to repression of SOD-PI formation. The analogs, however, are not suitable for improving genetic stability during propagation because of growth inhibition. In batch fermentation experiments in a complex medium at 30 degrees C, it has been demonstrated that initial glucose concentrations up to 50 g/L result in high specific SOD-PI yields giving an overall yield of up to 700 mg SOD-PI/L whereas higher glucose concentrations lead to both lower specific and overall yields due to depletion of critical medium components in the production period. In fed-batch experiments at 30 degrees C it has been possible to obtain high specific SOD-PI yields even at high biomass concentrations by feeding glucose at a constant rate of 1.5 g/L/h for 40 h followed by a feeding of ethanol at 1.0 g/L/h for 24 h, thus giving an overall yield of 1200 mg/L. Decreasing the temperature from 30 to 26 degrees C leads to improved yields in batch as well as fed-batch experiments. The optimized fed-batch fermentation process which is suitable to be scaled up to the cubic meter level has been tested in 200-L fermentations resulting in yields of more than 1500 mg/L of the fusion protein which conveniently can be used as a precursor in the production of recombinant human proinsulin.     

Improving cultivation processes for recombinant protein production

An new cascade control system is presented that reproducibly keeps the cultivation part of recombinant protein production processes on its predetermined track. While the system directly controls carbon dioxide production mass and carbon dioxide production rates along their setpoint profiles in fed-batch cultivation, it simultaneously keeps the specific biomass growth rates and the biomass profiles on their desired paths. The control scheme was designed and tuned using a virtual plant environment based on the industrial process control system SIMATIC PCS 7 (Siemens AG). It is shown by means of validation experiments that the simulations in this straightforward approach directly reflect the experimentally observed controller behaviour. Within the virtual plant environment, it was shown that the cascade control is considerably better than previously used control approaches. The controller significantly improved the batch-to-batch reproducibility of the fermentations. Experimental tests confirmed that it is particularly suited for cultivation processes suffering from long response times and delays. The performance of the new controller is demonstrated during its application in Escherichia coli fed-batch cultivations as well as in animal cell cultures with CHO cells. The technique is a simple and reliable alternative to more sophisticate model-supported controllers.     

Morphologically structured model for antitumoral retamycin production during batch and fed-batch cultivations of Streptomyces olindensis

A morphologically structured model is proposed to describe trends in biomass growth, substrate consumption, and antitumoral retamycin production during batch and fed-batch cultivations of Streptomyces olindensis. Filamentous biomass is structured into three morphological compartments (apical, subapical, and hyphal), and the production of retamycin, a secondary metabolite, is assumed to take place in the subapical cell compartment. Model accounts for the effect of glucose as well as complex nitrogen source on both the biomass growth and retamycin production. Laboratory data from bench-scale batch and fed-batch fermentations were used to estimate some model parameters by nonlinear regression. The predictive capability of the model was then tested for additional fed-batch and continuous experiments not used in the previous fitting procedure. The model predictions show fair agreement to the experimental data. The proposed model can be useful for further studies on process optimization and control.