Break-up, coalescence and catastrophic phase inversion in turbulent contactors

When a low concentration of immiscible phase is dispersed, break-up in the impeller region controls the drop size. The traditional application of Kolmogoroff's theory of local isotropic turbulence has been moderately successful in relating equilibrium drop sizes to the physical properties and the turbulent flow, with low power number impellers giving smaller drops at equal mean specific energy dissipation rates, [Formula: see text] However, to explain the reduction in drop size at equal [Formula: see text] on scale-up, the concept of intermittency must be introduced leading to a scale-up rule close to constant tip speed. With increasing concentration, coalescence generally becomes important and drop sizes increase. Modelling of coalescence involves collision frequency and coalescence efficiency. The latter is dependent on the type of drop interface, the establishment of which type for a particular system being difficult. The difficulty is compounded since in clean systems, at concentrations of the aqueous phase > approximately 20% by volume, droplets of oil appear in the aqueous drops whilst the converse is not found. At sufficiently high concentrations, where the concept of collision frequency is questionable, catastrophic phase inversion (CPI) occurs because coalescence becomes so high. Anything that enhances coalescence, e.g. surfactants, particles that bridge interfaces, wettable surfaces, bulk flow patterns, encourages CPI to occur at lower concentrations of dispersed phase. Satisfactory models for CPI are not available.

Oil/water and pre-emulsified oil/water (PIT) dispersions in a stirred vessel: Implications for fermentations

This study examines dispersions of rapeseed oil (RSO) in water by mechanical agitation under conditions mimicking those found in certain antibiotic fermentations; for example, in the presence of air, antifoam, and finely divided CaCO(3) particles. A problem with residual oil has been reported for such fermentations, and it has been suggested that the use of pre-emulsified oil can reduce this problem. Hence, the dispersion of a pre-emulsified oil produced by the "phase inversion temperature (PIT) method" has been evaluated. In both cases, the volume fraction of oil was 2%. For the RSO systems, a relatively high agitation speed was required to disperse the oil, especially in the presence of the particles and, when the agitation was stopped, separation occurred rapidly. The Sauter mean drop diameters depended on the system, being at an average energy dissipation rate of approximately 0.9 W kg(-1), 180 microm for RSO/water, 130 microm for RSO/water(antifoam)/air, 580 microm for RSO/water/CaCO(3), and 850 microm for RSO/water(antifoam)/air/CaCO(3). For the same four systems, the PIT emulsion, once dispersed, was very stable and the drop size was essentially independent of the operating conditions, with a Sauter mean diameter of approximately 0.3 microm. The implications of these findings for fermentations in which oil is used as a carbon source are assessed.

Measurement of strain-dependent toxicity in the indene bioconversion using multiparameter flow cytometry

The bionconversion of indene to cis-(1S,2R)-indandiol, a potential key intermediate in the synthesis of Merck's HIV protease inhibitor, CRIXIVAN trade mark, can be achieved using Rhodococcus, Pseudomonas putida, and Escherichia coli strains. This study reports on the application of multiparameter flow cytometry for the measurement of cytoplasmic membrane integrity and membrane depolarization as indicators of toxic effects of the substrate, product, and by-products using each of these strains. Measurements of oxygen uptake rate (OUR) and optical density (OD) as indicators of metabolic activity and biomass growth, respectively, were also made. Measurements of the cytoplasmic membrane potential, cell viability, and respiratory activity provided a sensitive set of parameters to assess toxicity in the indene bioconversion and provided the basis for process improvements and strain selection. The toxic concentrations of the substrate, product, and by-products for each strain have been determined. The results show that it is possible to accumulate cis-(1S,2R)-indandiol and cis-1-amino-2-indanol up to 20 g/L without significant negative effects on cell physiology using any of the strains tested. The Gram-negative P. putida (421-5 and GM 730) and E. coli strains were more resistant to indene and the isolated chemicals of the biotransformation than the Gram-positive Rhodoccoccus I24 strain, possibly due to the presence of the outer membrane and efflux pump mechanisms. P. putida GM 730 and the E. coli TDO 123 strains responded similarly to toxic effects, and the E. coli TDO 123 strain was more resistant than the P. putida 421-5 strain. In addition to the recommendations for strain selection, the identified targets for bioprocess improvement include a combination of genetic as well as process engineering approaches.

Application of multi-parameter flow cytometry using fluorescent probes to study substrate toxicity in the indene bioconversion

The bioconversion of indene to cis-(1S,2R) indandiol, a potential key intermediate in the synthesis of Merck's HIV protease inhibitor, CRIXIVAN trade mark, can be achieved using a Rhodococcus strain. This study using Rhodococcus I24 reports on the application of multiparameter flow cytometry for the measurement of cell physiological properties based on cytoplasmic membrane (CM) integrity and membrane depolarization as indicators of toxic effects of the substrate, indene. Quantification of intact polarized CM, intact depolarized CM and permeabilized CM of a large population of bacterial cells has been conducted using specific intracellular and membrane-binding fluorescent stains. Measurements of oxygen uptake rate (OUR) and optical density (OD) as indicators of metabolic activity and biomass growth, respectively, were also made. Indene concentrations of up to 0.25 g/L (0.037 g indene/g dry cell weight) did not significantly (<5% compared to control) affect cell light-scattering properties, intact CM, membrane polarization, respiratory activity, or biomass growth. Between this value and 1.5 g/L (0.221 g indene/g dry cell weight), the changes in intact CM, respiratory activity and biomass growth were relatively insignificant (<5% compared to control), although dissipation of the membrane potential of a significant proportion of the cell population occurred at 0.50 g/L (0.074 g indene/g dry cell weight). At 2.5 g/L (0.368 g indene/g dry cell weight) there was a significant increase in the dead cell population, accompanied by changes in the extracellular cationic concentrations and substantial decrease in respiratory activity. The primary effect of indene toxicity was the disruption of the proton motive force across the cytoplasmic membrane which drives the formation of ATP. The disruption of the proton motive force may have been due to the measured changes in proton permeability across the membrane. In addition, indene may have directly inhibited the membrane-bound enzymes related to respiratory activity. The overall consequence of this was reduced respiratory activity and biomass growth. The cell physiological properties measured via flow cytometry are important for understanding the effects of toxicity at the cellular level which neither measurements of biomass growth or indandiol formation rates can provide since both are cell averaged measurements. The technique described here can also be used as a generic tool for measuring cell membrane properties in response to toxicity of other indene-resistant strains that may be possible to use as recombinant hosts to perform the biotransformation of indene. This study has demonstrated that flow cytometry is a powerful tool for the measurement of cell physiological properties to assess solvent toxicity on whole cell biocatalysts.

Dependence of morphology on agitation intensity in fed-batch cultures of Aspergillus oryzae and its implications for recombinant protein production

We previously reported that, although agitation conditions strongly affected mycelial morphology, such changes did not lead to different levels of recombinant protein production in chemostat cultures of Aspergillus oryzae (Amanullah et al., 1999). To extend this finding to another set of operating conditions, fed-batch fermentations of A. oryzae were conducted at biomass concentrations up to 34 g dry cell weight/L and three agitation speeds (525, 675, and 825 rpm) to give specific power inputs between 1 and 5 kWm(-3). Gas blending was used to control the dissolved oxygen level at 50% of air saturation except at the lowest speed where it fell below 40% after 60-65 h. The effects of agitation intensity on growth, mycelial morphology, hyphal tip activity, and recombinant protein (amyloglucosidase) production in fed-batch cultures were investigated. In the batch phase of the fermentations, biomass concentration, and AMG secretion increased with increasing agitation intensity. If in a run, dissolved oxygen fell below approximately 40% because of inadequate oxygen transfer associated with enhanced viscosity, AMG production ceased. As with the chemostat cultures, even though mycelial morphology was significantly affected by changes in agitation intensity, enzyme titers (AGU/L) under conditions of substrate limited growth and controlled dissolved oxygen of >50% did not follow these changes. Although the measurement of active tips within mycelial clumps was not considered, a dependency of the specific AMG productivity (AGU/g biomass/h) on the percentage of extending tips was found, suggesting that protein secretion may be a bottle-neck in this strain during fed-batch fermentations.

The impact of fluid-dynamic-generated stresses on chDNA and pDNA stability during alkaline cell lysis for gene therapy products

Extensive tests have been carried out to assess the impact of fluid-dynamic-generated stress during alkaline lysis of Escherichia coli cells (host strain DH1 containing the plasmid pTX 0161) to produce a plasmid DNA (pDNA) solution for gene therapy. Both a concentric cylinder rheometer and two stirred reactors have been used, and both the alkaline addition and neutralization stages of lysis have been studied. Using a range of shear rates in the rheometer, stirrer speeds in the reactors, and different periods of exposure, their impact on chromosomal DNA (chDNA) and pDNA was assessed using agarose gel electrophoresis, a Qiagen Maxiprep with a polymerase chain reaction (PCR) assay, and a Qiagen Miniprep purification with a UV spectrophotometer. Comparison has been made with unstressed material subjected to similar holding times. These tests essentially show that under all these conditions, <2% chDNA was present in the pDNA solution, the pDNA itself was not fragmented, and a yield of 1 mg/g cell was obtained. These results, together with studies of rheological properties, have led to the design of a 60-L, stirred lysis reactor and the production of high-quality pDNA solution with <1% chDNA after further purification.

Scale-down model to simulate spatial pH variations in large-scale bioreactors

For the first time a laboratory-scale two-compartment system was used to investigate the effects of pH fluctuations consequent to large scales of operation on microorganisms. pH fluctuations can develop in production-scale fermenters as a consequence of the combined effects of poor mixing and adding concentrated reagents at the liquid surface for control of the bulk pH. Bacillus subtilis was used as a model culture since in addition to its sensitivity to dissolved oxygen levels, the production of the metabolites, acetoin and 2,3-butanediol, is sensitive to pH values between 6.5 and 7.2. The scale-down model consisted of a stirred tank reactor (STR) and a recycle loop containing a plug flow reactor (PFR), with the pH in the stirred tank being maintained at 6.5 by addition of alkali in the loop. Different residence times in the loop simulated the exposure time of fluid elements to high values of pH in the vicinity of the addition point in large bioreactors and tracer experiments were performed to characterise the residence time distribution in it. Since the culture was sensitive to dissolved oxygen, for each experiment with pH control by adding base into the PFR, equivalent experiments were conducted with pH control by addition of base into the STR, thus ensuring that any dissolved oxygen effects were common to both types of experiments. The present study indicates that although biomass concentration remained unaffected by pH variations, product formation was influenced by residence times in the PFR of 60 sec or longer. These changes in metabolism are thought to be linked to both the sensitivity of the acetoin and 2,3-butanediol-forming enzymes to pH and to the inducing effects of dissociated acetate on the acetolactate synthase enzyme.

Studies related to the scale-up of high-cell-density E. coli fed-batch fermentations using multiparameter flow cytometry: effect of a changing microenvironment with respect to glucose and dissolved oxygen concentration

Multiparameter flow cytometric techniques developed in our laboratories have been used for the "at-line" study of fed-batch bacterial fermentations. These fermentations were done at two scales, production (20 m(3)) and bench (5 x 10(-3) m(3)). In addition, at the bench scale, experiments were undertaken where the difficulty of achieving good mixing (broth homogeneity), similar to that found at the production scale, was simulated by using a two-compartment model. Flow cytometric analysis of cells in broth samples, based on a dual-staining protocol, has revealed, for the first time, that a progressive change in cell physiological state generally occurs throughout the course of such fermentations. The technique has demonstrated that a changing microenvironment with respect to substrate concentration (glucose and dissolved oxygen tension [DOT]) has a profound effect on cell physiology and hence on viable biomass yield. The relatively poorly mixed conditions in the large-scale fermentor were found to lead to a low biomass yield, but, surprisingly, were associated with a high cell viability (with respect to cytoplasmic membrane permeability) throughout the fermentation. The small-scale fermentation that most clearly mimicked the large-scale heterogeneity (i.e., a region of high glucose concentration and low DOT analogous to a feed zone) gave similar results. On the other hand, the small-scale well-mixed fermentation gave the highest biomass yield, but again, surprisingly, the lowest cell viability. The scaled-down simulations with high DOT throughout and locally low or high glucose gave biomass and viabilities between. Reasons for these results are examined in terms of environmental stress associated with an ever-increasing glucose limitation in the well-mixed case. On the other hand, at the large scale, and to differing degrees in scale-down simulations, cells periodically encounter regions of relatively higher glucose concentration.

Study of drop and bubble sizes in a simulated mycelial fermentation broth of up to four phases

The mean sizes and size distributions of air bubbles and viscous castor oil drops were studied in a salt-rich aqueous solution (medium), first separately, and then simultaneously as a three-phase system. The dispersion was created in a 150-mm-diameter stirred tank equipped with a Rushton turbine, and the sizes were measured using an advanced video technique. Trichoderma harzianum biomass was added in some experiments to study the effect of a solid phase under unaerated and aerated conditions to give either three-or four-phase systems. In all cases, the different dispersed phases could be clearly seen. Such photoimages have never been obtained previously. For the three phases, air-oil-medium, aeration caused a drastic increase in Sauter mean drop diameter, which was greater than could be accounted for by the reduction in energy dissipation on aeration. Also, as in the unaerated case, larger drops were observed as the oil content increased. On the other hand, mean bubble sizes were significantly reduced with increasing oil phase up to 15% with bubbles inside many of the viscous drops. With the introduction of fungal biomass of increasing concentration (0.5 to 5 g L(-1)) under unaerated conditions, the Sauter mean drop diameter decreased. Finally, in the four-phase system (oil [10%]-medium-air-biomass) as found in many fermentations, all the phases (plus bubbles in drops) could clearly be seen and, as the biomass increased, a decrease in both the bubble and the drop mean diameters was found. The reduction in size of bubbles (and therefore increase in interfacial area) as the oil and bio- mass concentration increased provides a possible explanation as to why the addition of an oil phase has been reported to enhance oxygen transfer during many fermentations.

Control of pH in large-scale, free suspension animal cell bioreactors: alkali addition and pH excursions

It is likely that, in the future, animal cell cultures of a higher cell density and/or cell lines with higher specific oxygen demands will be available. Such developments will lead to the need for improved homogeneity in the bioreactor and a greater supply of nutrients. The accompanying significant increase in CO(2) production and accumulation and the resulting reduction in pH are also important implications for process engineering. Such pH reduction is typically controlled by the addition of sodium carbonate. Previous studies using flow visualization mimicking the operating conditions in a typical plant-scale reactor showed potentially cell-damaging regions within it due to pH excursions. This paper confirms the existence of these excursions by pH measurements in the alkali addition zone. It also identifies the accumulation of alkali in a region of poor local liquid homogenization as a serious scale-up problem and shows how a change in the addition point significantly reduces it.

The use of multi-parameter flow cytometry to compare the physiological response of Escherichia coli W3110 to glucose limitation during batch, fed-batch and continuous culture cultivations

Multi-parameter flow cytometric techniques have been developed for the 'at-line' study of bacterial cultivations. Using a mixture of specific fluorescent stains it is possible to resolve an individual cells physiological state beyond culturability, based on the presence or absence of an intact polarised cytoplasmic membrane, enabling assessment of population heterogeneity. It has been shown that during the latter stages of small-scale (5 l), well mixed fed-batch cultivations there is a considerable drop in cell viability, about 17%, as characterised by cytoplasmic membrane depolarisation and permeability. These phenomena are thought to be due to the severe and steadily increasing stress associated with glucose limitation at high cell densities, during the fed-batch process. Such effects were not found in either batch or continuous culture cultivations. The possibility of using these findings for improved process control using 'on-line' flow cytometry are discussed.

Use of multi-staining flow cytometry to characterise the physiological state of Escherichia coli W3110 in high cell density fed-batch cultures

High cell density fed-batch fermentations of Escherichia coli W3110 have been carried out at specific growth rates of less than 0.3 h-1, to investigate the effect of glucose limitation on the physiological state of individual cells. After an initial exponential batch phase, the feed rate was held constant and a final dry cell weight of approximately 50 g per litre was achieved. The fermentations were monitored by mass spectrometry whilst measurements of pH, DOC, CFU/mL, TCN, OD500nm and residual glucose concentrations were made. Satisfactory and reproducible results were obtained. Flow cytometric analysis of cells in broth samples, based on either of two multi-staining protocols, revealed a progressive change in cell physiological state throughout the course of the fermentations. From these measurements it was concluded that the loss in reproductive viability towards the end of the fed-batch process is due to cell death and not due to the formation of a "viable but nonculturable state" as had previously been reported. Since the presence of a high proportion of dead or dying cells at any time during a fermentation has a detrimental effect on the synthesis of any desired product it is proposed that an on-line flow cytometric analysis and control strategy could be used as a means of increasing overall process efficiency.

Effects of agitation intensity on mycelial morphology and protein production in chemostat cultures of recombinant Aspergillus oryzae

The effects of agitation on fragmentation of a recombinant strain of Aspergillus oryzae and its consequential effects on protein production have been investigated. Constant mass, 5.3-L chemostat cultures at a dilution rate of 0.05 h-1 and a dissolved oxygen level of 75% air saturation, have been conducted at 550, 700, and 1000 rpm. These agitation speeds were chosen to cover a range of specific power inputs (2.2 to 12 kW m-3) from realistic industrial levels to much higher values. The use of a constant mass chemostat linked to a gas blender allowed variation of agitation speed and hence gas hold-up without affecting the dilution rate or the concentration of dissolved oxygen. The morphology of both the freely dispersed mycelia and clumps was characterized using image analysis. Statistical analysis showed that it was possible to obtain steady states with respect to morphology. The mean projected area at each steady state under growing conditions correlated well with the 'energy dissipation/circulation" function, [P/(kD3tc)], where P is the power input, D the impeller diameter, tc the mean circulation time, and k is a geometric constant for a given impeller. Rapid transients of morphological parameters in response to a speed change from 1000 to 550 rpm probably resulted from aggregation. Protein production (alpha-amylase and amyloglucosidase) was found to be independent of agitation speed in the range 550 to 1000 rpm (P/V = 2.2 and 12.6 kW m-3, respectively), although significant changes in mycelial morphology could be measured for similar changes in agitation conditions. This suggests that mycelial morphology does not directly affect protein production (at a constant dilution rate and, therefore, specific growth rate). An understanding of how agitation affects mycelial morphology and productivity would be valuable in optimizing the design and operation of large-scale fungal fermentations for the production of recombinant proteins. Copyright 1999 John Wiley & Sons, Inc.

Dependence of penicillium chrysogenum growth, morphology, vacuolation, and productivity in fed-batch fermentations on impeller type and agitation intensity

The influence of the agitation conditions on the growth, morphology, vacuolation, and productivity of Penicillium chrysogenum has been examined in 6 L fed-batch fermentations. A standard Rushton turbine, a four-bladed paddle, and a six-bladed pitched blade impeller were compared. Power inputs per unit volume of liquid, P/VL, ranged from 0.35 to 7.4 kW/m3. The same fermentation protocol was used in each fermentation, including holding the dissolved oxygen concentration above 40% air saturation by gas blending. The mean projected area (for all dispersed types, including clumps) and the clump roughness were used to characterize the morphology. Consideration of clumps was vital as these were the predominant morphological form. For a given impeller, the batch-phase specific growth rates and the overall biomass concentrations increased with agitation intensity. Higher fragmentation at higher speeds was assumed to have promoted growth through increased formation of new growing tips. The mean projected area increased during the rapid growth phase followed by a sharp decrease to a relatively constant value dependent on the agitation conditions. The higher the speed, the lower the projected area for a given impeller type. The proportion by volume of hyphal vacuoles and empty regions decreased with speed, possibly due to fragmentation in the vacuolated regions. The specific penicillin production rate was generally higher with lower impeller speed for a given impeller type. The highest value of penicillin production as well as its rate was obtained using the Rushton turbine impeller at the lowest speed. At given P/VL, changes in morphology, specific growth rate, and specific penicillin production rate depended on impeller geometry. The morphological data could be correlated with either tip speed or the "energy dissipation/circulation function," but a reasonable correlation of the specific growth rate and specific production rate was only possible with the latter. Copyright 1998 John Wiley & Sons, Inc.

The use of flow cytometry to study the impact of fluid mechanical stress on Escherichia coli W3110 during continuous cultivation in an agitated bioreactor

Continuous culture fermentations of Escherichia coli W3110 have been carried out at controlled dissolved oxygen levels of 40% and 10% of saturation. Satisfactory and reproducible results were obtained. Agitation speeds of 400 and 1200 rpm at an aeration rate of 1 vvm have been used as well as an aeration rate of 3 vvm at 400 rpm. The upper levels of these variables represent much higher agitation and aeration intensities than those normally used in practical fermentations. The fermentations were monitored by mass spectrometry and optical density, and cell samples were studied by flow cytometry, SEM, and TEM. Protocols were developed so the state of both cell membranes and cell size could be measured by flow cytometry. Under all the conditions of agitation and aeration, flow cytometric analysis indicated that both cell membranes were intact and that a cytoplasmic membrane potential existed; also the cell size did not change, results confirmed by SEM and TEM. There were no detectable changes in off-gas analysis or optical density during the continuous fermentation nor in the cell structure as revealed by SEM or TEM, except at the highest agitation intensity. Under the latter conditions, after 7 h, the outer polysaccharide layer on the cell was stripped away. It is concluded that any changes in biological performance of this E. coli cell line due to variations in agitation or aeration intensity or scale of operation cannot be attributed to fluid dynamic stresses associated with the turbulence generated by impellers or with bursting bubbles.

Agitator speed and dissolved oxygen effects in xanthan fermentations

Agitation speed affects both the extent of motion in Xanthan fermentation broths because of their rheological complexity and the rate of oxygen transfer. The combination of these two effects causes the dissolved oxygen concentration and its spatial uniformity also to change with agitator speed. Separating these complex interactions has been achieved in this study in the following way. First, the influence of agitation speeds of 500 and 1000 rpm has been investigated at a constant nonlimiting dissolved oxygen concentration of 20% of air saturation using gas blending. Under these controlled dissolved oxygen conditions, the results demonstrate that the biological performance of the culture was independent of agitation speed as long as broth homogeneity could be ensured. With the development of increasing rheological complexity lending to stagnant regions at Xanthan concentrations >20 g/L, it is shown that the superior bulk mixing achieved at 1000 rpm, compared with 500 rpm, leading to an increased proportion of the cells in the fermentor to be metabolically active and hence higher microbial oxygen uptake rates, was responsible for the enhanced performance. Second, the effects of varying dissolved oxygen are compared with a control in each case with an agitator speed of 1000 rpm to ensure full motion, but with a fixed, nonlimiting dissolved oxygen of 20% air saturation. The specific oxygen uptake rate of the culture in the exponential phase, determined using steady-state gas analysis data, was found to be independent of dissolved oxygen above 6% air saturation, whereas the specific growth rate of the culture was not influenced by dissolved oxygen, even at levels as low as 3%, although a decrease in Xanthan production rate could be measured. In the production phase, the critical oxygen level was determined to be 6% to 10%, so that, below this value, both specific Xanthan production rate as well as specific oxygen uptake rate decreased significantly. In addition, it is shown that the dynamic method of oxygen uptake determination is unsuitable even for moderately viscous Xanthan broths. Copyright 1998 John Wiley & Sons, Inc.

The influence of impeller type in pilot scale xanthan fermentations

The rheological complexity of Xanthan fermentations presents an interesting problem from a mixing viewpoint, because the phenomena of poor bulk blending and low oxygen mass transfer rates inherent in highly viscous fermentations (and their consequences) can be systematically investigated, even at the pilot plant scale. This study in a 150 L fermentor compares the physical and biological performance of four pairs of impellers: a standard Rushton turbine, a large diameter Rushton turbine, a Prochem Maxflo T, and a Scaba 6SRGT. Accurate in-fermentor power measurements, essential for the comparison of impellers in relation to operating costs are also reported. It is demonstrated that the agitator performance in Xanthan fermentations is very specific and the choice of which impeller to use in bioreactors to obtain enhanced performance is dependant on the applied criterion. None of the criterion favored the use of the standard Rushton turbine, therefore suggesting that there are strong grounds for retrofitting these impellers with either large diameter impellers of similar design or with novel agitators. In addition, fluid dynamic modeling of cavern formation has clearly highlighted the importance of a well mixed and oxygenated region for providing the capacity for high microbial oxygen uptake rates which govern Xanthan productivity and quality. Copyright 1998 John Wiley & Sons, Inc.

Physiological and environmental factors affecting the growth of insect cells and infection with baculovirus

Insect cell growth can be significantly improved by close attention to the conditions used in the inoculum stages. Initial cell concentration, spent medium carry over and inoculum phase withdrawal significantly influenced the growth kinetics of Spodoptera frugiperda (Sf9) cells. The percentage of cells infected with wild and recombinant baculovirus AcNPV and (in the later case) the beta-galactosidase yield in fresh medium was appreciably affected by the stage of the growth curve that cells were in when infected and by the multiplicity of infection (MOI). However, the cell density at the time of infection and the medium condition showed little direct influence on infectivity. There may, however, be an indirect influence in that these factors determine the relative distribution of cells in the cell cycle. The infectivity is then in turn affected by the relative frequency of cells in the G1, S and G2/M phases. Insect cell specific oxygen uptake rates (1.3-3.4 x 10(-17) mol per cell per s) were essentially similar to or less than those measured for hybridoma cells. However, when Sf9 cells were infected with baculovirus, the specific oxygen uptake rate increased by up to 40%.

Further studies of the culture of mouse hybridomas in an agitated bioreactor with and without continuous sparging

TB/C3 mouse hybridoma cells have been grown at 2 controlled dO2 conditions by headspace and sparged oxygenation. Also a variety of sparging rates and sparger sizes and positions have been employed. Headspace oxygenation at dO2 levels from 5% to 100% of saturation give essentially the same performance as controls. Sparging is generally damaging to cells, the extent of damage decreasing with reduced sparging rate until at below about 0.02 vvm results equivalent to the unsparged conditions are obtained. Damage is clearly linked with bubble-cell interactions at the air-medium interface where bubbles bursting in clusters and of a size less than 5 mm appear to be the most lethal. When the interaction of air sparging with the agitator flow leads to an increase in the number of smaller bubbles and cluster bursts, cell damage is further increased. Pluronic F-68 reduces damage very significantly. Biological aspects are briefly discussed in the light of various biological tests. The practical implications of this work for large scale, free suspension cell culture are outlined.

Action of shear on enzymes: studies with alcohol dehydrogenase

Yeast alcohol dehydrogenase (ADH) solutions (approximately 1 mg/ml, pH 7) were sheared in a coaxial cylindrical viscometer. This was fitted with a lid sealing the contents from the atmosphere and preventing evaporation. At 30 degrees C after a total of 5 hr intermittent shearing at 683 sec-1 no losses of activity were observed. No losses were found after 5 hr continuous shearing and in a no-shear control. At 40 degrees C and 683 sec-1 there were only small activity losses in 5 hr. Shearing at 3440 sec-1 no measurable losses of activity were found with a 1.03 mg/ml solution in 5 hr at 30 degrees C, a 1.03 mg/ml solution in 8 hr at 5 degrees C, and with a 3.89 mg/ml solution in 3 hr at 5 degrees C. In all these cases, however, a white precipitate formed that was not observed in zero shear control experiments. The sheared 3.89 mg/ml solution was clarified by centrifugation. It was shown that there were no ADH aggregates in the supernatant and that the precipitate was less than 2% of the original protein. At 30 degrees C under adverse pH conditions (pH 8.8) there was no significant difference in activity losses of an approximately 1 mg/ml solution sheared at 65 and 744 sec-1. An approximately 0.5 mg/ml ADH solution, pH 7, was agitated in a small reactor with no free air-liquid interface. Peak shear rates near the impeller were estimated to be about 9000 sec-1. Only a small decrease in specific activity was observed until over 15 hr total running at 5 degrees C.