Physiological effects of the presence and absence of gas vacuoles in the blue-green alga,Microcystis aeruginosa Kuetz. emend. Elenkin

Physiological evidence was obtained for a light shielding role for gas vacuoles inMicrocystis aeruginosa Kuetz. emend. Elenkin, by comparing photosynthetic oxygen evolution, growth behaviour and pigment composition of cells with intact or collapsed gas vacuoles. The oxygen evolution rates were strongly dependent on cell concentration, a maximum rate for cells with intact gas vacuoles occurring at about 1.4×10⁹ cells/ml and for cells with collapsed gas vacuoles at about 2.5×10⁹ cells/ml. By using light saturation curves for oxygen evolution, it was estimated that at low light intensities up to 30% of the photosynthetically useable light was shielded at a cell concentration of 6×10⁸ cells/ml. Collapsing the gas vacuoles twice daily did not alter the initial growth rate of the cultures, but enabled them to reach a higher final cell density. Collapsing of gas vacuoles during growth for about four generations resulted in a lower level of all acetone soluble pigments with a greater relative reduction in carotenoids than in chlorophyll a. Collapse of the gas vacuoles does not alter the cell volume. Various optical interactions which could account for light shielding are discussed.     

Growth and nutrient uptake of Newport bluegrass as affected by soil oxygen

Summary An oxygen diffusion rate of 20×10^–8 g cm^–2 min^–1 is required for root growth of Newport bluegrass. The optimum O.D.R. is in a range above 40.During the first growth period, the vegetative growth was not greatly affected by oxygen treatment except during the <1% treatment which did not permit root growth. After clipping, the growth increased with increasing oxygen to a maximum at the 10% treatment and then exhibited a lower growth under the 21% treatment. The plants survived through all oxygen treatments.The concentration of N, P, and K in the leaves generally increased with increased oxygen supply. Na accumulated to a high concentration under the lowest oxygen treatment.Paper No. 1489, Citrus Research Center, Agricultural Experiment Station, Riverside, California.     

Effect of oxygen on substrate utilization for nitrogen fixation and growth in Frankia spp.

Frankia, the actinomycete partner in the nitrogenfixing symbiosis of certain woody non-legumes, has been shown to fix nitrogen in pure culture under aerobic conditions. The sensitivity of in vivo nitrogen-fixation (acetylene reduction) to oxygen tension in the gas phase was measured in short-term assays with two Frankia isolates designated ARI3 and CcI3. The carbon source utilized had an effect on the optimum O₂ concentration for acetylene reduction. Cells utilizing an organic acid, e.g., propionate or pyruvate had maximum nitrogenase activity at an oxygen concentration of 15 to 20%. In contrast, cells respiring a sugar, e.g., trehalose or glucose, or endogenous reserves (glycogen or trehalose) had maximum acetylene reduction activity at 5 to 10% in the gas phase. Oxygen uptake kinetics showed that respiration in vesicle-containing cells utilizing trehalose had a biphasic response to oxygen concentration with a diffusion limited component at oxygen concentrations of 20 M to more than 300 M. These results suggested that trehalose was oxidized in the vesicles as well as in the vegetative hyphae. Oxygen concentration also had an effect on the trehalose-supported growth of cells (non nitrogenfixing, [⁺NH₄Cl]). Cells grown with 5–10% O₂ in the gas phase had a doubling time approximately half those grown with 20% O₂ (atmospheric). Propionate-grown cells showed similar growth rates at the two oxygen tensions, and grew faster (almost 2x) than the trehalose cells at 5–10% O₂. Trehalose also supported approximately 40% lower rates of oxygen uptake than propionate in vesicle-containing cells.     

Batch culture of Alcaligenes eutrophus ATCC 17697T using recycled gas closed circuit culture system

Batch culture of Alcaligenes eutrophus ATCC 17697^T using the recycled gas closed circuit culture system was done with the intention of developing a practical fermentation system for industrial culture of autotrophs. The gas phase of the culture system consisted of substrate gas so that gases in this culture system could be recycled forever as long as the amount of the gas consumed would be refilled. All gasses supplied into this system could be completely used without any loss as exhaust. Thus, this system assures high gas usage efficiency as well as operation safety. Studies on the effect of oxygen concentration showed the high oxygen concentration in substrate gas mixture suppressed the specific growth rate while a low oxygen concentration promoted the growth rate. This introduced the possibility of development of an explosion-free fermentation system with a high growth rate if appropriate system design and fermentation conditions were given. Since this system is closed, material balance and elementary analysis provide the ultimately accurate stoichiometry of the autotrophic culture of this bacterium.     

Immobilized antibody-based flow type enzyme immunosensor for determination of human serum albumin

A flow-type enzyme immunosensor was prepared for the electrochemical determination of human serum albumin (HSA). The immunosensor was constructed from the immobilized antibody (anti-HSA IgG) reactor and an oxygen electrode. The immunochemical reaction of catalase-labelled antibody with HSA was completed with 30 min. After the immunochemical reaction, hydrogen peroxide solution was injected into the system and a peak current was obtained within 2 min. A linear relationship was observed between the current increase and the logarithm of HSA concentration in the range 10⁻⁸-10⁻⁶ g ml⁻¹. The minimum measurable concentration was 10⁻⁸ g ml⁻¹. The current increase was reproducible with 10% of the relative errors when a sample solution containing 10⁻⁷ g ml⁻¹ of HSA was used. The minimum measurable concentration increased to 10⁻⁹ g ml⁻¹ when hydrogen peroxide was recycled for 5 min in the reactor system. The immobilized antibody reactor could be reused. HSA in human serum was determined by the system proposed.     

High cell density suspension culture of mammalian anchorage independent cells: Oxygen transfer by gas sparging and defoaming with a hydrophobic net

Gas sparging directly into the culture-broth is not done in cell culture, except when the gas flow rate is very small, because much foaming occurs.During screening of defoaming methods, foam was observed to be broken up effectively when it made contact with a net fabricated from hydrophobic materials. Providing a highly efficient oxygen supply to suspension culture was tried using the new defoaming method. In a 5 1 reactor equipped with the foam-eliminating net fabricated with polysiloxane, oxygen was transferred at 21 mmole/l·h equivalent to an about forty-fold higher rate than in conventional surface aeration. This was equivalent to a consumption rate of 1×10⁸ cells/ml, even at a low oxygen gas flow rate of 0.1 cm/s corresponding to a fourth of the gas flow rate when foam leaked through the net.Perfusion culture of rat ascites hepatoma cell JTC-1 was successfully carried out in the 51 scale culture system with the net and a hydrophobic membrane for cell filtration. The viable cell concentration reached 2.7×10⁷ cells/ml after twenty-seven days, in spite of the nutrient-deficient condition of the lower medium exchange rate, that is, a working volume a day, and viability was maintained at more than 90%. In a 1.21 scale culture of mouse-mouse hybridoma cell STK-1, viable cell concentration reached 4×10⁷ cells/ml. These results showed that oxygen transfer by gas sparging with defoaming was useful for high density suspension culture. A foam-breaking mechanism was proposed.Abbreviations Eagle's MEM Eagle's minimal essential medium - Dulbecco's modified Eagle MEM Dulbecco's modified Eagle minimal essential medium     

The growth of <Emphasis Type="Italic">Chlorella sorokiniana</Emphasis> as influenced by CO<Subscript>2</Subscript>, light,and flue gases

In order to achieve recognition as environmentally friendly production, flue gases should be used as a CO₂ source for growing the microalgae Chlorella sorokiniana when used for hydrogen production. Flue gases from a waste incinerator and from a silicomanganese smelter were used. Before testing the flue gases, the algae were grown in a laboratory at 0.04, 1.3, 5.9, and 11.0 % (v/v) pure CO₂ gas mixed with fresh air. After 5 days of growth, the dry biomass per liter algal culture reached its maximum at 6.1 % CO₂. A second experiment was conducted in the laboratory at 6.2 % CO₂ at photon flux densities (PFD) of 100, 230, and 320 μmol photons m^?2 s^?1. After 4 days of growth, increasing the PFD increased the biomass production by 67 and 108 % at the two highest PFD levels, as compared with the lowest PFD. A bioreactor system containing nine daylight-exposed tubes and nine artificial light-exposed tubes was installed on the roof of the waste incinerator. The effect of undiluted flue gas (10.7 % CO₂, 35.8 ppm NO _x , and 38.6 ppm SO₂), flue gas diluted with fresh air to give 4.2 % CO₂ concentration, and 5.0 % pure CO₂ gas was studied in daylight (21.4?±?9.6 mol photons m^?2 day^?1 PAR, day length 12.0 h) and at 135 μmol photons m^?2 s^?1 artificial light given 24 h day^?1 (11.7?±?0.0 mol photons m^?2 day^?1 PAR). After 4 days’ growth, the biomass production was the same in the two flue gas concentrations and the 5 % pure CO₂ gas control. The biomass production was also the same in daylight and artificial light, which meant that, in artificial light, the light use efficiency was about twice that of daylight. The starch concentration of the algae was unaffected by the light level and CO₂ concentration in the laboratory experiments (2.5–4.0 % of the dry weight). The flue gas concentration had no effect on starch concentration, while the starch concentration increased from about 1.5 % to about 6.0 % when the light source changed from artificial light to daylight. The flue gas from the silicomanganese smelter was characterized by a high CO₂ concentration (about 17 % v/v), low oxygen concentration (about 4 %), about 100 ppm NO _x , and 1 ppm SO₂. The biomass production using flue gas significantly increased as compared with about 5 % pure CO₂ gas, which was similar to the biomass produced at a CO₂ concentration of 10–20 % mixed with N₂. Thus, the enhanced biomass production seemed to be related to the low oxygen concentration rather than to the very high CO₂ concentration.     

Design of a bubble-swawm bioreactor for animal cell culture

A stationary bubble-swarm has been used to aerate a mammalian cell culture bioreactor with an extremely low gas flow rate. Prolonging the residence time of the gas bubbles within the medium improved the efficiency of the gas transfer into the liquid phase and suppressed foam formation. An appropriate field of speed gradients prevented the bubbles from rising to the surface. This aeration method achieves an almost 90% transfer of oxygen supplied by the bubbles. Consequently, it is able to supply cells with oxygen even at high cell densities, while sparging with a gas flow of only 0.22·10^–3–1.45·10^–3 vvm (30–200 ml/h).The reactor design, the oxygen transfer rates and the high efficiency of the system are presented. Two repeated batch cultures of a rat-mouse hybridoma cell line are compared with a surface-aerated spinner culture. The used cell culture medium was serum-free, either with or without BSA and did not contain surfactants or other cell protecting agents. One batch is discussed in detail for oxygen supply, amino acid consumption and specific antibody production.     

Influence of aeration–homogenization system in stirred tank bioreactors,dissolved oxygen concentration and pH control mode on BHK-21 cell growth and metabolism

This work focused on determining the effect of dissolved oxygen concentration (DO) on growth and metabolism of BHK-21 cell line (host cell for recombinant proteins manufacturing and viral vaccines) cultured in two stirred tank bioreactors with different aeration-homogenization systems, as well as pH control mode. BHK-21 cell line adapted to single-cell suspension was cultured in Celligen without aeration cage (rotating gas-sparger) and Bioflo 110, at 10, 30 and 50 % air saturation (impeller for gas dispersion from sparger-ring). The pH was controlled at 7.2 as far as it was possible with gas mixtures. In other runs, at 30 and 50 % (DO) in Bioflo 110, the cells grew at pH controlled with CO₂ and NaHCO₃ solution. Glucose, lactate, glutamine, and ammonium were quantified by enzymatic methods. Cell concentration, size and specific oxygen consumption were also determined. When NaHCO₃ solution was not used, the optimal DOs were 10 and 50 % air saturation for Celligen and Bioflo 110, respectively. In this condition maximum cell concentrations were higher than 4 × 10⁶ cell/mL. An increase in maximum cell concentration of 36 % was observed in batch carried out at 30 % air saturation in a classical stirred tank bioreactor (Bioflo 110) with base solution addition. The optimal parameters defined in this work allow for bioprocess developing of viral vaccines, transient protein expression and viral vector for gene therapy based on BHK-21 cell line in two stirred tank bioreactors with different agitation–aeration systems.     

Glucose uptake rate as a tool to estimate hybridoma growth in a packed bed bioreactor

The immobilisation of cells in a perfusion culture allows to obtain a high cell concentration and an efficient removal of the catabolites without cell loss. A disadvantage of this system is that the cell density cannot be directly monitored. The cellular metabolism is just followed by online measurements of pH and dissolved oxygen (DO) and off-line determinations of residual metabolites. In this article, we report a high cell density achieved by the cultivation of a hybridoma in a bubble-column bioreactor filled with hollow glass cylinders. The parameters monitored during the cultivation were pH, temperature, DO, glucose, lactate and monoclonal antibody. The glucose uptake rate was used to estimate the cell concentration along the time. The maximum cell concentration calculated for the considered cultivation time was 2.7?×?10⁷ cell?·?ml^?1. The glucose concentration in the media decreased stepwise twice, causing a decrease on the specific growth rate, while maintaining high antibody productivity levels. Maximum monoclonal antibody productivity was 503?μg?·?l^?1?·?day^?1 and specific productivity, considering calculated cell density, was 0.019?ng?·?cell^?1?·?day^?1.     

A novel method for characterisation of microbial growth kinetics on volatile organic compounds

A novel method for the determination of microbial growth kinetics on hydrophobic volatile organic compounds (VOC) has been developed. A stirred tank reactor was operated as a fed-batch system to which the VOC was continuously fed via the gas phase, assuring a constant VOC concentration in the mineral medium. A flow of air was saturated with the VOC, and then mixed with a further flow of air, to obtain a predetermined VOC concentration. Thus, different VOC concentrations in the mineral medium could be obtained by altering the VOC concentration in the feed gas. The growth kinetics of Xanthobacter autotrophicus GJ10 on 1,2-dichloroethane (DCE) and of Pseudomonas sp. strain JS150 on MonoChloroBenzene (MCB) were assessed using this method. The growth of strain JS150 was strongly inhibited at MCB concentrations higher than 160 mg l⁻¹, and the results were fitted using a piecewise function. The growth kinetics of strain GJ10 were described by the Luong model where maximum growth rate μ_max = 0.12 h⁻¹, substrate saturation constant K _S = 7.8 mg l⁻¹, and maximum substrate concentration S _m (above which growth is completely inhibited) = 1080 mg l⁻¹. Varying nitrogen and oxygen flows enabled the effect of oxygen concentration on the growth kinetics of Pseudomonas JS150 to be determined. Received: 30 November 1998 / Received revision: 19 March 1999 / Accepted: 20 March 1999     

Effects of peptone on hybridoma growth and monoclonal antibody formation

Hybridoma WuT3 secreting a monoclonal antibody against T lymphocytes was grown in RPMI 1640 medium supplemented with 1% human serum. The effect of the concentration of peptone, as an additive, was investigated on cell growth, monoclonal antibody formation, and cell metabolism over 0–10 g l^–1 range. It was found that 1–5 g l^–1 peptone can significantly promote the growth of cells and increase the formation of monoclonal antibody, especially at 3–5 g l^–1, when both the accumulating level and secretion rate of monoclonal antibody are higher than that at other peptone concentrations. Based on glucose, lactate and ammonia analysis data, the efficiency of glycolysis was assessed and the utilization of amino acids was more efficient at 3–5 g l^–1 peptone. The cell growth and monoclonal antibody formation were inhibited at higher peptone concentrations, e.g. 10 g l^–1.     

Tepidibacillus fermentans gen. nov., sp. nov.: a moderately thermophilic anaerobic and microaerophilic bacterium from an underground gas storage

A novel moderately thermophilic bacterium, strain STGH^T, was isolated from Severo-Stavropolskoye underground gas storage (Russia). Cells of strain STGH^T were spore-forming motile straight rods 0.3 μm in diameter and 2.0–4.0 μm in length having a Gram-positive cell wall structure. The temperature range for growth was 36–65 °C, with an optimum at 50–52 °C. The pH range for growth was 5.5–8.0, with an optimum at pH 7.0–7.5. Growth of strain STGH^T was observed at NaCl concentrations ranging from 0 to 4.0 % (w/v) with an optimum at 1.0 % (w/v). Strain STGH^T grew anaerobically by reduction of nitrate, thiosulfate, S⁰ and AQDS using a number of complex proteinaceous compounds, organic acids and carbohydrates as electron donors. Nitrate was reduced to nitrite; thiosulfate and sulfur were reduced to sulfide. It also was able to ferment pyruvate, glucose, fructose, and maltose. The strain STGH^T did not grow under aerobic conditions during incubation with atmospheric concentration of oxygen but was able to microaerobic growth (up to 10 % of oxygen in gas phase). The G+C content of DNA of strain STGH^T was 34.8 mol%. 16S rRNA gene sequence analysis revealed that the isolated organism belongs to the class Bacilli. We propose to assign strain STGH^T to a new species of a novel genus Tepidibacillus fermentans gen. nov., sp.nov. The type strain is STGH^T (=DSM 23802^T, =VKM B-2671^T).     

Influence of dissolved oxygen concentration on growth,mitochondrial function and antibody production of hybridoma cells in batch culture

The effects of dissolved oxygen concentration on hybridoma cell growth, metabolism, and antibody production were studied. A mouse hybridoma cell line producing an IgG1 directed at a consensus -interferon was grown in batch cultures in a 5 dm³ stirred bioreactor at dissolved oxygen (DO) concentrations of 5, 30, 90 and 95% or air saturation. High oxygen tension (95% of air saturation) reduced specific growth rate without affecting cell viability. At lower dissolved oxygen levels, specific growth rates were approximately independent of DO, although changes in mitochondrial function and antibody production were observed. Flow cytometry assays of a fluorescent mitochondria-specific marker (Rhodamine 123) show significant single-cell heterogeneities during late exponential growth and greater average fluorescence in cultures grown at 95% DO. The quantity of cell-surface immunoglobulin, measured by an immunofluorescent flow cytometric technique, was the same at high (95%) and low (5%) dissolved oxygen concentrations. Myeloma cells of the type used in constructing the above hybridoma line were much less sensitive to dissolved oxygen level. Specific respiration rate, pyruvate utilization rate, cytochrome oxidase activity, and succinate-cytochrome c oxidoreductase activity were significantly greater (62–116%) for the hybridoma cells than for the myeloma cells in T-flask cultures.     

Production and scale‐up of a monoclonal antibody against 17‐hydroxyprogesterone

The hybridoma 192 was used to produce a monoclonal antibody (MAb) against 17‐hydroxyprogesterone (17‐OHP), for possible use in screening for congenital adrenal hyperplasia (CAH). The factors influencing the MAb production were screened and optimized in a 2 L stirred bioreactor. The production was then scaled up to a 20 L bioreactor. All of the screened factors (aeration rate, stirring speed, dissolved oxygen concentration, pH, and temperature) were found to significantly affect production. Optimization using the response surface methodology identified the following optimal production conditions: 36.8°C, pH 7.4, stirring speed of 100 rpm, 30% dissolved oxygen concentration, and an aeration rate of 0.09 vvm. Under these conditions, the maximum viable cell density achieved was 1.34 ± 0.21 × 10⁶ cells mL^?1 and the specific growth rate was 0.036 ± 0.004 h^?1. The maximum MAb titer was 11.94 ± 4.81 μg mL^?1 with an average specific MAb production rate of 0.273 ± 0.135 pg cell^?1 h^?1. A constant impeller tip speed criterion was used for the scale‐up. The specific growth rate (0.040 h^?1) and the maximum viable cell density (1.89 × 10⁶ cells mL^?1) at the larger scale were better than the values achieved at the small scale, but the MAb titer in the 20 L bioreactor was 18% lower than in the smaller bioreactor. A change in the culture environment from the static conditions of a T‐flask to the stirred bioreactor culture did not affect the specificity of the MAb toward its antigen (17‐OHP) and did not compromise the structural integrity of the MAb. © 2012 American Institute of Chemical Engineers Biotechnol. Prog., 2013     

Influence of temperature rise on kinetic parameters during batch propagation of Kluyveromyces fragilis in cheese whey under ambient conditions

Three 5 l working volume fermenters were used to investigate the growth of the yeast Kluyveromyces fragilis in acid cheese whey under ambient temperature in order to assess the specific growth rate and yield, the lactose and oxygen uptake rates during the various phases of batch culture, the effect of increasing temperature on the various kinetic parameters, and the need for a cooling unit for single cell production batch systems. The initial dissolved oxygen in the medium was 5.5 mg l^–1 and the pH was maintained at 4.5. The observed lag phase, specific growth rate and maximum cell number were 4 h, 0.2 h^–1 and 8.4 × 10⁸ cells ml^–1, respectively. About 99% of the lactose in cheese whey was utilized within 20 h, 85% during the exponential growth phase. The specific lactose utilization rates by K. fragilis were 0.20 × 10^–12, 1.457 × 10^–12, 0.286 × 10^–12 and 0.00 g lactose cell^–1 h^–1, for the lag, exponential, stationary and death phases, respectively. The dissolved oxygen concentration in the medium decreased as the cell number increased. The lowest oxygen concentration of 1.2 mg l^–1 was observed during the stationary phase. The volumetric oxygen transfer coefficient was 0.41 h^–1 and the specific oxygen uptake rates were 0.32 × 10^–12, 2.14 × 10^–12, 0.51 × 10^–12 and 0.003 × 10^–12 mg O₂ cell^–1 h^–1, for the lag, exponential, stationary and death phases, respectively. The maximum temperature recorded for the medium was 33 °C, indicating that a cooling unit for batch production of single cell protein at ambient temperature is not needed for this type of bioreactor. The increase in medium temperature affected the cell growth and the lactose and oxygen uptake rates.     

CO2 in large-scale and high-density CHO cell perfusion culture

Productivity in a CHO perfusion culture reactor was maximized when pCO₂ was maintained in the range of 30–76 mm Hg. Higher levels of pCO₂ (> 150 mm Hg) resulted in CHO cell growth inhibition and dramatic reduction in productivity. We measured the oxygen utilization and CO₂ production rates for CHO cells in perfusion culture at 5.55×10^-17 mol cell^-1 sec^-1 and 5.36×10^-17 mol cell^-1 sec^-1 respectively. A simple method to directly measure the mass transfer coefficients for oxygen and carbon dioxide was also developed. For a 500 L bioreactor using pure oxygen sparge at 0.002 VVM from a microporous frit sparger, the overall apparent transfer rates (k_La+k_AA) for oxygen and carbon dioxide were 0.07264 min^-1 and 0.002962 min^-1 respectively. Thus, while a very low flow rate of pure oxygen microbubbles would be adequate to meet oxygen supply requirements for up to 2.1×10⁷ cells/mL, the low CO₂ removal efficiency would limit culture density to only 2.4×10⁶ cells/mL. An additional model was developed to predict the effect of bubble size on oxygen and CO₂ transfer rates. If pure oxygen is used in both the headspace and sparge, then the sparging rate can be minimized by the use of bubbles in the size range of 2–3 mm. For bubbles in this size range, the ratio of oxygen supply to carbon dioxide removal rates is matched to the ratio of metabolic oxygen utilization and carbon dioxide generation rates. Using this strategy in the 500 L reactor, we predict that dissolved oxygen and CO₂ levels can be maintained in the range to support maximum productivity (40% DO, 76 mm Hg pCO₂) for a culture at 10⁷ cells/mL, and with a minimum sparge rate of 0.006 vessel volumes per minute.A = volumetric agitated gas-liquid interfacial area at the top of the liquid, 1/mB = cell broth bleeding rate from the vessel, L/minCER = carbon dioxide evolution rate in the bioreactor, mol/min[CO₂] = dissolved CO₂ concentration in liquid, M[CO₂]^* = CO₂ concentration in equilibrium with sparger gas, M[CO₂]^** = CO₂ concentration in equilibrium with headspace gas, MCO₂(1) = dissolved carbon dioxide molecule in water[C_T] = total carbonic species concentration in bioreactor medium, M[C_T]_F = total carbonic species concentration in feed medium, MD = bioreactor diameter, mD_I = impeller diameter, mD_b = the initial delivered bubble diameter, mF = fresh medium feeding rate, L/minH_L = liquid height in the vessel, mk_A = carbon dioxide transfer coefficient at liquid surface, m/mink _infA ^supO = oxygen transfer coefficient at liquid surface, m/minNomenclature     

Alginate production by Azotobacter vinelandii DSM576 in batch fermentation

The kinetics of growth and alginate production from glucose in a nitrogen and phosphate-rich medium by Azotobacter vinelandii DSM576 were studied in a laboratory fermenter at pH 7 and 35°C. Batch fermentations were carried out both without control of dissolved oxygen concentration (DO) and at 1, 2, 5 and 10% DO. Although growth was faster at higher DO, maximum biomass concentration was lower. No alginate was produced at 10% DO. Alginate production was faster at 5 and 2% DO but higher alginate concentrations and yields were obtained without DO control. Alginate production was growth-associated at 5% DO, but significant amounts of alginate were produced after growth had stopped at lower DO values. In fermentations without DO control the molecular weight of the polymer reached a maximum (11–17.6 × 10⁴) when specific growth rate was between 0.02 and 0.04 h⁻¹ and residual concentration of ammoniacal nitrogen was between 0.01 and 0.02 g L⁻¹ and then sharply decreased. Received 15 August 1997/ Accepted in revised form 08 January 1998     

Evaluation of the effects and interactions of mixing and oxygen transfer on the production of Fab’ antibody fragments in Escherichia coli fermentation with gas blending

Fermentations carried out at 450-L and 20-L scale to produce Fab’ antibody fragments indicated a serious problem to control levels of dissolved oxygen in the broth due to the large oxygen demand at high cell densities. Dissolved oxygen tension (DOT) dropped to zero during the induction phase and it was hypothesised that this could limit product formation due to inadequate oxygen supply. A gas blending system at 20-L scale was employed to address this problem and a factorial 2² experimental design was executed to evaluate independently the effects and interaction of two main engineering factors: agitation rate and DOT level (both related to mixing and oxygen transfer in the broth) on Fab’ yields. By comparison to the non-gas blending system, results in the gas blending system at same scale showed an increase in the production of Fab’ by 77% independent of the DOT level when using an agitation rate of 500 rpm level and by 50% at an agitation rate of 1,000 rpm with 30% DOT. Product localisation in the cell periplasm of >90% was obtained in all fermentations. Results obtained encourage further studies at 450-L scale initially, to evaluate the potential of gas blending for the industrial production of Fab’ antibody fragments.     

Performance of an external loop air-lift bioreactor for the production of monoclonal antibodies by immobilized hybridoma cells

Summary The performance of an external loop air-lift bioreactor was investigated by assessing the inter-relationships between various hydrodynamic properties and mass transfer. The feasibility of using this bioreactor for the production of monoclonal antibodies by mouse hybridoma cells immobilized in calcium alginate gel beads and alginate/poly-l-lysine microcapsules was also examined. When the superficial gas velocity, V _g , in the 300 ml reactor was varied from 2 to 36 cm/min, the average liquid velocity increased from 3 to 14 cm/sec, the gas hold-up rose from 0.2 to 3.0%, and the oxygen mass transfer coefficient, k _L a, increased from 2.5 to 18.1 h^-1. A minimum liquid velocity of 4 cm/s was required to maintain alginate gel beads (1000 m diameter, occupying 3% of reactor volume) in suspension. Batch culture of hybridoma cells immobilized in alginate beads followed logarithmic growth, reaching a concentration of 4×10⁷ cells/ml beads after 11 days. Significant antibody production did not occur until day 9 into the culture, reaching a value of 100 g/ml of medium at day 11. On the other hand, bioreactor studies with encapsulated hybridoma cells gave monoclonal antibody concentrations of up to 800 g/ml capsules (the antibody being retained within the semipermeable capsule) and maximum cell densities of 2×10⁸ cells/ml capsule at day 11. The volumetric productivities of the alginate gel immobilized cell system and the encapsulated cell system were 9 and 3 g antibody per ml of reactor volume per day, respectively. The main advantage of the bioreactor system is its simple design, since no mechanical input is required to vary the hydrodynamic properties.