Twenty-four-well plate miniature bioreactor high-throughput system: assessment for microbial cultivations

High-throughput (HT) miniature bioreactor (MBR) systems are becoming increasingly important to rapidly perform clonal selection, strain improvement screening, and culture media and process optimization. This study documents the initial assessment of a 24-well plate MBR system, Micro (micro)-24, for Saccharomyces cerevisiae, Escherichia coli, and Pichia pastoris cultivations. MBR batch cultivations for S. cerevisiae demonstrated comparable growth to a 20-L stirred tank bioreactor fermentation by off-line metabolite and biomass analyses. High inter-well reproducibility was observed for process parameters such as on-line temperature, pH and dissolved oxygen. E. coli and P. pastoris strains were also tested in this MBR system under conditions of rapidly increasing oxygen uptake rates (OUR) and at high cell densities, thus requiring the utilization of gas blending for dissolved oxygen and pH control. The E. coli batch fermentations challenged the dissolved oxygen and pH control loop as demonstrated by process excursions below the control set-point during the exponential growth phase on dextrose. For P. pastoris fermentations, the micro-24 was capable of controlling dissolved oxygen, pH, and temperature under batch and fed-batch conditions with subsequent substrate shot feeds and supported biomass levels of 278 g/L wet cell weight (wcw). The average oxygen mass transfer coefficient per non-sparged well were measured at 32.6 +/- 2.4, 46.5 +/- 4.6, 51.6 +/- 3.7, and 56.1 +/- 1.6 h(-1) at the operating conditions of 500, 600, 700, and 800 rpm shaking speed, respectively. The mixing times measured for the agitation settings 500 and 800 rpm were below 5 and 1 s, respectively.     

Membrane-aerated microbioreactor for high-throughput bioprocessing

A microbioreactor with a volume of microliters is fabricated out of poly(dimethylsiloxane) (PDMS) and glass. Aeration of microbial cultures is through a gas-permeable PDMS membrane. Sensors are integrated for on-line measurement of optical density (OD), dissolved oxygen (DO), and pH. All three parameter measurements are based on optical methods. Optical density is monitored via transmittance measurements through the well of the microbioreactor while dissolved oxygen and pH are measured using fluorescence lifetime-based sensors incorporated into the body of the microbioreactor. Bacterial fermentations carried out in the microbioreactor under well-defined conditions are compared to results obtained in a 500-mL bench-scale bioreactor. It is shown that the behavior of the bacteria in the microbioreactor is similar to that in the larger bioreactor. This similarity includes growth kinetics, dissolved oxygen profile within the vessel over time, pH profile over time, final number of cells, and cell morphology. Results from off-line analysis of the medium to examine organic acid production and substrate utilization are presented. By changing the gaseous environmental conditions, it is demonstrated that oxygen levels within the microbioreactor can be manipulated. Furthermore, it is demonstrated that the sensitivity and reproducibility of the microbioreactor system are such that statistically significant differences in the time evolution of the OD, DO, and pH can be used to distinguish between different physiological states. Finally, modeling of the transient oxygen transfer within the microbioreactor based on observed and predicted growth kinetics is used to quantitatively characterize oxygen depletion in the system.     

Characterization and application of a miniature 10 mL stirred-tank bioreactor, showing scale-down equivalence with a conventional 7 L reactor

The aim of this study was to characterize the engineering environment of an instrumented 10 mL miniature stirred-tank bioreactor and evaluate its potential as a scale-down device for microbial fermentation processes. Miniature bioreactors such as the one detailed in this work have been developed by several research groups and companies and seek to address the current bottleneck at the screening stage of bioprocess development. The miniature bioreactor was characterized in terms of overall volumetric oxygen transfer coefficient and mixing time over a wide range of impeller speeds. Power input to the miniature bioreactor was directly measured, and from this the power number of each impeller was calculated and specific power input estimated, allowing the performance of the miniature bioreactor to be directly compared with that of a conventional 7 L bioreactor. The capability of the miniature bioreactor to carry out microbial fermentations was also investigated. Replicate batch fermentations of Escherichia coli DH5alpha producing plasmid DNA were performed at equal specific power input, under fully aerobic and oxygen-limiting conditions. The results showed a high degree of equivalence between the two scales with regard to growth and product kinetics. This was underlined by the equal maximum specific growth rate and equal specific DNA product yield on biomass obtained at the two scales of operation, demonstrating the feasibility of scaling down to 10 mL on the basis of equivalent specific power input.     

Proof-of-concept of a novel micro-bioreactor for fast development of industrial bioprocesses

The experimental performance of a novel micro-bioreactor envisaged for parallel screening and development of industrial bioprocesses has been tested in this work. The micro-bioreactor with an internal volume of 4.5 mL is operated under oscillatory flow mixing (OFM), where a controllable mixing and mass transfer rates are achieved under batch or continuous laminar flow conditions. Several batch fermentations with a flocculent Saccharomyces cerevisiae strain were carried out at initial glucose concentrations (S(0)) range of approximately 5-20 g/L and compared to yeast growth kinetics in a stirred tank (ST) bioreactor. Aerobic fermentations were monitored ex situ in terms of pH, DO, glucose consumption, and biomass and ethanol production (wherever applicable). An average biomass production increase of 83% was obtained in the micro-bioreactor when compared with the ST, with less 93.6% air requirements. It also corresponded to a 214% increase on biomass production when compared with growth in a shaken flask (SF) at S(0) = 20 g/L. Further anaerobic fermentations at the same initial glucose concentration ranges gave the opportunity to use state-of-the-art fiber optics technology for on-line and real-time monitoring of this bioprocess. Time profiles of biomass concentration (measured as optical density (OD)) were very similar in the ST bioreactor and in the micro-bioreactor, with a highly reproducible yeast growth in these two scale-down platforms.     

Quantification of power consumption and oxygen transfer characteristics of a stirred miniature bioreactor for predictive fermentation scale-up

Miniature parallel bioreactors are becoming increasingly important as tools to facilitate rapid bioprocess design. Once the most promising strain and culture conditions have been identified a suitable scale-up basis needs to be established in order that the cell growth rates and product yields achieved in small scale optimization studies are maintained at larger scales. Recently we have reported on the design of a miniature stirred bioreactor system capable of parallel operation [Gill et al. (2008); Biochem Eng J 39:164-176]. In order to enable the predictive scale-up of miniature bioreactor results the current study describes a more detailed investigation of the bioreactor mixing and oxygen mass transfer characteristics and the creation of predictive engineering correlations useful for scale-up studies. A Power number of 3.5 for the miniature turbine impeller was first established based on experimental ungassed power consumption measurements. The variation of the measured gassed to ungassed power ratio, P(g)/P(ug), was then shown to be adequately predicted by existing correlations proposed by Cui et al. [Cui et al. (1996); Chem Eng Sci 51:2631-2636] and Mockel et al. [Mockel et al. (1990); Acta Biotechnol 10:215-224]. A correlation relating the measured oxygen mass transfer coefficient, k(L)a, to the gassed power per unit volume and superficial gas velocity was also established for the miniature bioreactor. Based on these correlations a series of scale-up studies at matched k(L)a (0.06-0.11 s(-1)) and P(g)/V (657-2,960 W m(-3)) were performed for the batch growth of Escherichia coli TOP10 pQR239 using glycerol as a carbon source. Constant k(L)a was shown to be the most reliable basis for predictive scale-up of miniature bioreactor results to conventional laboratory scale. This gave good agreement in both cell growth and oxygen utilization kinetics over the range of k(L)a values investigated. The work described here thus gives further insight into the performance of the miniature bioreactor design and will aid its use as a tool for rapid fermentation process development.     

Optimization of a cultivation process for recombinant protein production by Escherichia coli.

A single-stage fed-batch bioprocess for the production of a recombinant protein beta-galactosidase, by E. coli has been developed. The XL1-blue strain of E. coli which harbors a multi-number foreign plasmid PT was cultured in a reformulated medium. Critical medium components were selected and their respective concentrations were optimized with the Orthogonal Table method. An exponential substrate feeding schedule was used to maintain optimum conditions. Inhibition of growth and protein expression caused by excessive concentrations of glucose and acetate was investigated and subsequently minimized with an incremental nutrient feeding schedule which limited the specific growth rate of a culture. The program necessary to facilitate the control of substrate addition is fully described. This program has been used with a 2.5 l bioreactor and a commercially available software package for optimization without on-line or off-line measurement of optical density (OD), CO2, glucose or acetate. The optimized fed-batch process limited the acetate concentration to less than 20 mM; maintained an exponential growth phase for 50 h; and produced a cell density of 51 g l-1 dry cell weight (DCW) or 154 OD600 with a beta-galactosidase activity of 990 U ml-1.     

Development of a large-scale biocalorimeter to monitor and control bioprocesses

Calorimetry has shown real potential at bench-scale for chemical and biochemical processes. The aim of this work was therefore to scale-up the system by adaptation of a standard commercially available 300-L pilot-scale bioreactor. To achieve this, all heat flows entering or leaving the bioreactor were identified and the necessary instrumentation implemented to enable on-line monitoring and dynamic heat balance estimation. Providing that the signals are sufficiently precise, such a heat balance would enable calculation of the heat released or taken up during an operational (bio)process. Two electrical Wattmeters were developed, the first for determination of the power consumption by the stirrer motor and the second for determination of the power released by an internal calibration heater. Experiments were designed to optimize the temperature controller of the bioreactor such that it was sufficiently rapid so as to enable the heat accumulation terms to be neglected. Further calibration experiments were designed to correlate the measured stirring power to frictional heat losses of the stirrer into the reaction mass. This allows the quantitative measurement of all background heat flows and the on-line quantitative calculation of the (bio)process power. Three test fermentations were then performed with B. sphaericus 1593M, a spore-forming bacterium pathogenic to mosquitoes. A first batch culture was performed on a complex medium, to enable optimization of the calorimeter system. A second batch culture, on defined medium containing three carbon sources, was used to show the fast, accurate response of the heat signal and the ability to perfectly monitor the different growth phases associated with growth on mixed substrates, in particular when carbon sources became depleted. A maximum heat output of 1100 W was measured at the end of the log-phase. A fed-batch culture on the same defined medium was then carried out with the feed rate controlled as a function of the calorimeter signal. A maximum heat output of 2250 W was measured at the end of the first log-phase. This work demonstrates that real-time quantitative calorimetry is not only possible at pilot-scale, but could be readily applied at even larger scales. The technique requires simple, readily available devices for determination of the few necessary heat flows, making it a robust, cost-effective technique for process development and routine monitoring and control of production processes.     

Application of process mass spectroscopy to the detection of metabolic changes in plant tissue culture

There is a clear need in the area of plant cell culture for methods of on-line estimation of culture parameters. The introduction of plant cells into culture can result in a loss of their photoautotrophic character so that they are largely heterotrophic. As a result, fermentation off-gas analysis may not be confounded by photosynthetically-related O₂ production. In this study performance of a suspension culture of Syringa vulgaris, in a pneumatically agitated bioreactor of in-house design, was investigated. The effect of light on growth, carbohydrate metabolism and the respiratory quotient (RQ), determined by process mass spectroscopy, was studied. Yield coefficients for cells grown in the light and dark were similar although the patterns of carbohydrate uptake were quite different. Maximum biomass yields were higher in this bioreactor than normally observed in shake flasks. The RQ was dynamic during the course of the fermentation, peaking during the transition from the lag phase to the growth phase. It is suggested that the RQ may prove useful as an on-line parameter for monitoring transitions in cellular metabolism during plant cell culture fermentations.Abbreviations RQ respiratory quotient - v.v.m. volume of gas fed to fermenter per unit volume per minute - Y_X/S growth yield coefficient based on total carbohydrate     

On-line monitoring of ethanol,acetaldehyde and glycerol during industrial fermentations with Saccharomyces cerevisiae

Industrial fermentations carried out in a 500-1 bioreactor were monitored on-line by a prototype of a split-flow modified thermal biosensor. Acetaldehyde and glycerol in the extracellular broth were monitored over the first 48 h of fed-batch fermentations. The aim was to determine the usefulness of these secondary metabolites for on-line monitoring and control. When fermentation of the 13–16 g/l batch sugar was monitored, using immobilised aldehyde dehydrogenase, the acetaldehyde reached a peak value of 0.3 g/l. With immobilised alcohol oxidase a much larger peak of 3.5 g/l ethanol was seen immediately after the acetaldehyde peak. When glycerokinase was used a delayed peak of 1 g/l glycerol was monitored. Of the three metabolites monitored, the ethanol proved the most valuable indicator of suitable timing for the start of the feeding phase and later for controlling and preventing overfeed using the on-line biosensor system.     

Rheology of filamentous fermentations

The performance of a bioreactor containing a filamentous fermentation broth is greatly influenced by the rheological properties of the broth. These properties are determined mainly by the concentration of biomass, its growth rate and morphology. Included in the morphology are such factors as the geometry of hyphae (length, diameter, branching frequency), hyphal flexibility and hyphal-hyphal interactions, which can all be affected by the operational design of the reactor. Thus, correlations describing viscosity as a function of biomass only are of limited value. A better understanding of the relations between morphology and rheology may be achieved by a combination of rheological and morphological studies.Rheological properties are normally determined using off-line measurements in-spite of associated problems with sample treatment influencing the results. Equipment for dynamic, on-line, measurement of morphology and rheology is available, but little used in filamentous fermentations. Controlling the rheological properties of mycelial fermentations may be difficult because of the great number of factors influencing mycelial development and/or hyphal-hyphal interactions.Polymer solutions are often used to simulate flow behaviour of filamentous fermentations and scale-up and mass transfer considerations are based on these studies. Although much information has been gained this way, the predictions developed do not include the effect of an active biomass on the mass transfer and flow properties of the culture. It is important to carry out studies on the non-homogeneous fermentation fluids, and develop correlations based on these studies.     

A novel parallel shaken bioreactor system for continuous operation

A novel continuous bioreactor system was developed as a shaken culture vessel for the investigation of the growth kinetics and product formation of microorganisms in milliscale. The novel bioreactor system mainly consists of a specially designed 250-mL shake flask with two inlets, one for gas supply and one for medium supply, and one combined outlet on the side of flask for exhaust gas and culture liquid. As a result of the circulating motion of the fermentation broth in the shake flask, the maximum liquid height reaches the edge of the outlet and the fermentation broth is accelerated into the outlet by centrifugal force. Additionally, the excess fermentation broth leaving the culture vessel is continuously driven by the exhaust gas. Because of the small scale and the simple handling it is possible to operate many of these shaken bioreactor vessels simultaneously. By using parallel vessels operated at different dilution rates on the same shaker, the data for a complete biomass over dilution rate (X-D) diagram of a biological culture can be evaluated in an efficient manner, thus saving money, materials, and time. Continuous fermentations of the yeast Saccharomyces cerevisiae H1022 (ATCC 32167) in the shaken bioreactor system and in a conventional stirred tank fermentor showed very similar results.     

On-line biomass monitoring by capacitance measurement.

An in-situ, steam-sterilizable capacitance probe was used to follow the biomass concentration on-line, in bioreactors from 20 to 2000 l total volume. Microbial cultures of Saccharomyces cerevisiae, Pichia pastoris and Streptomyces virginiae were grown in batch and fed-batch culture in both defined and complex media in order to demonstrate the wide dynamic operating range of the instrument. A linear correlation was found between the on-line capacitance measurement and the off-line measurements (optical density, OD620; packed mycelial volume, PMV; biomass concentration X, and colony forming units, CFU ml-1) for biomass concentrations (dry cell weight) up to 30 g l-1 (St. virginiae), 106 g l-1 (S. cerevisiae) and 89 g l-1 (P. pastoris). The on-line capacitance measurement was slightly influenced by variations in agitation speed and strong extraneous radio frequencies. A specific capacitance constant (Cs) was defined for all microbial cells which was dependent on cell viability and cell size. The Cs was easy to calculate using the on-line capacitance measurement and an off-line estimation of biomass concentration. The Biomass Monitor proved suitable for precise on-line monitoring of both homogeneous (uni-cellular) and heterogeneous (mycelial) cultures in bioreactors.     

On-line growth measurements in bioreactors by titrating metabolic proton exchange

Recording the amount of titrant required to maintain constant pH in a bioreactor where cell metabolism causes acidity changes allows on-line determinations of growth kinetics in computer-controlled batch cultures. A system for making such measurements is described and its performance is investigated. Transient bicarbonate accumulation occurs if the culture produces CO₂ at high pH values and low gas transfer rates. We have developed a mathematical model for the titrant requirement as a function of the cell growth rate, the gas transfer properties of the bioreactor and the culture pH. According to this model, bicarbonate accumulation affects the stoichiometry between titrant and biomass but does not prevent determination of growth rate constants. These predictions are confirmed using model experiments and measurements during batch growth of microbial cultures.     

A predictive and feedback control algorithm maintains a constant glucose concentration in fed-batch fermentations.

A combined predictive and feedback control algorithm based on measurements of the concentration of glucose on-line has been developed to control fed-batch fermentations of Escherichia coli. The predictive control algorithm was based on the on-line calculation of glucose demand by the culture and plotting a linear regression to the next datum point to obtain a predicted glucose demand. This provided a predictive "coarse" control for the glucose-based nutrient feed. A direct feedback control using a proportional controller, based on glucose measurements every 2 min, fine-tuned the feed rate. These combined control schemes were used to maintain glucose concentrations in fed-batch fermentations as tight as 0.49 +/- 0.04 g/liter during growth of E. coli to high cell densities.     

A predictive and feedback control algorithm maintains a constant glucose concentration in fed-batch fermentations

A combined predictive and feedback control algorithm based on measurements of the concentration of glucose on-line has been developed to control fed-batch fermentations of Escherichia coli. The predictive control algorithm was based on the on-line calculation of glucose demand by the culture and plotting a linear regression to the next datum point to obtain a predicted glucose demand. This provided a predictive "coarse" control for the glucose-based nutrient feed. A direct feedback control using a proportional controller, based on glucose measurements every 2 min, fine-tuned the feed rate. These combined control schemes were used to maintain glucose concentrations in fed-batch fermentations as tight as 0.49 +/- 0.04 g/liter during growth of E. coli to high cell densities.     

Solid-state fermentation: a continuous process for fungal tannase production

Truly continuous solid-state fermentations with operating times of 2-3 weeks were conducted in a prototype bioreactor for the production of fungal (Penicillium glabrum) tannase from a tannin-containing model substrate. Substantial quantities of the enzyme were synthesized throughout the operating periods and (imperfect) steady-state conditions seemed to be achieved soon after start-up of the fermentations. This demonstrated for the first time the possibility of conducting solid-state fermentations in the continuous mode and with a constant noninoculated feed. The operating variables and fermentation conditions in the bioreactor were sufficiently well predicted for the basic reinoculation concept to succeed. However, an incomplete understanding of the microbial mechanisms, the experimental system, and their interaction indicated the need for more research in this novel area of solid-state fermentation.     

The tuning of a model-based estimator for the specific growth rate of Candida utilis

Control of microbial conversion processes is frequently inhibited by the infeasibility of measuring important process variables. In order to circumvent this lack of measurements, an accurate or valuable and conveniently measurable on-line hardware measurement can be combined with the balance equations describing the process to obtain estimates of less easily measurable variables. In this article the on-line estimation of the specific growth rate of Candida utilis is evaluated. The observer-based estimator requires a hardware measurement of the biomass during fermentations in conjuction with a model of the process; therefore the Biomass Monitor, giving an on-line measurement of viable biomass, is used in the bioreactor experiments described. The optimal tuning of the estimation for the experimental conditions is described and several alternative adaptations of the design of the estimator are presented. The influence of implemented time intervals for discretization of the estimator on the reliability of the estimated growth rate values is discussed. Additionally, the necessary choice of an initial value of the estimated specific growth rate has proven to be of great importance in practice.     

Solid-state fermentation in rotating drum bioreactors: operating variables affect performance through their effects on transport phenomena

Aspergillus oryzae ACM 4996 was grown on an artificial gel-based substrate and on steamed wheat bran during solid-state fermentations in 18.7 L rotating drum bioreactors. For gel fermentations fungal growth decreased as rotational speed increased, presumably due to increased shear. For wheat bran fermentations fungal growth improved under agitated compared to static culture conditions, due to superior heat and mass transfer. We conclude that the effects of operational variables on the performance of SSF bioreactors are mediated by their effects on transport phenomena such as mixing, shear, heat transfer, and mass transfer within the substrate bed. In addition, the substrate characteristics affect the need for and the rates of these transport processes. Different transport phenomena may be rate limiting with different substrates. This work improves understanding of the effects of bioreactor operation on SSF performance.     

Implementation of a thermal biosensor in a process environment: on-line monitoring of penicillin V in production-scale fermentations.

The production of penicillin V was monitored in 0.5 m3 and 160 m3 bioreactors. The thermal biosensor was an enzyme thermistor modified for split-flow analysis. The heat signal generated in the enzyme column was corrected for any nonspecific heat with the use of an identical but inactive reference column. The on-line monitoring was performed in the fermentation pilot plant and in a fermentation plant of Novo Nordisk A/S. Immobilized beta-lactamase was used to monitor three consecutive 0.5 m3 penicillin fermentations. Broth samples were continuously filtered through a tangential flow filtration unit in a sterile external loop. The on-line penicillin V values were 10% higher than those obtained by off-line HPLC analysis. Alternatively a polypropylene filtration probe was inserted into a 160 m3 bioreactor and samples were withdrawn at 0.5 ml/min. The same experiments were repeated with purified and immobilized penicillin V acylase. The on-line penicillin V values obtained with this enzyme correlated very well with those from HPLC analysis. The on-line monitoring was controlled and analysed by a software program written in Labtech Notebook.     

On-line monitoring of monoclonal antibodies in animal cell culture using a grating coupler

A grating coupler was used for the on-line determination of monoclonal antibodies produced in perfused animal cell bioreactor. The device was connected with the culture vessel via a flow-injection analysis (FIA) system, which was controlled automatically. Specific antimouse lgG antibodies were immobilized on the surface of the sensor-chip. After injection of the sample, the binding of mouse lgG was observed in real time. The regeneration of the binding sites of the immobilized antibodies using an acidic solution allowed the on-line detection of produced monoclonal antibodies in the range of 10 to 150 mug/mL. In contrast to other techniques coupled to bioprocesses, the developed method represents a regenerable direct immunosensor. Results were compared with standard ELISA techniques (off-line) and a competitive immunochemical assay using the grating coupler (off-line). (c) 1993 John Wiley & Sons, Inc.