Death rate in a small air-lift loop reactor of vero cells grown on solid microcarriers and in macroporous microcarriers

The death rate of Vero cells grown on Cytodex-3 microcarrierswas studied as a function of the gas flow rate in a smallair-lift loop reactor. The death rate may be described byfirst-order death-rate kinetics. The first-order death-rateconstant as calculated from the decrease in viable cells, theincrease in dead cells and the increase in LDH activity islinear proportional to the gas flow rate, with a specifichypothetical killing volume in which all cells are killed ofabout 2.10(-3)m(3) liquid per m(3) of air bubbles.In addition, an experiment was conducted in the sameair-lift reactor with Vero cells grown inside porous Asahimicrocarriers. The specific hypothetical killing volumecalculated from this experiment has a value of 3.10(-4)m(3) liquid per m(3) of air bubbles, which shows thatthe porous microcarriers were at least in part able to protectthe cells against the detrimental hydrodynamic forcesgenerated by the bubbles.     

Effect of serum concentration on hybridoma viable cell density and production of monoclonal antibodies in CSTRs and on shear sensitivity in air-lift loop reactors

The death rate of hybridoma cells, grown in a continuous culture, has been studied in a small air-lift loop reactor as a function of reactor height and injected gas flow rate. The first-order death-rate constant was found to be proportional to the reciprocal height and to the gas flow rate, in accordance with the hypothetical killing volume model for insect cells in bubble columns. Furthermore, the effect of the serum concentration on viable cell concentration and cell productivity has been investigated in a continuous culture. A serum component became growth limiting when the serum concentration was decreased from 2% to 1%. No effect of the serum concentration on specific cell productivity could be measured. Samples from this culture were also studied in the air-lift loop reactor to determine the effect of serum concentration on the shear sensitivity. The cells' shear sensitivity increased with decreasing serum concentration. The protective effect of serum was found to be physical as well as physiological.     

Death rate in a small air-lift loop reactor of vero cells grown on solid microcarriers and in macroporous microcarriers

The death rate of Vero cells grown on Cytodex-3 microcarriers was studied as a function of the gas flow rate in a small air-lift loop reactor. The death rate may be described by first-order death-rate kinetics. The first-order death-rate constant as calculated from the decrease in viable cells, the increase in dead cells and the increase in LDH activity is linear proportional to the gas flow rate, with a specific hypothetical killing volume in which all cells are killed of about 2·10^–3 m³ liquid per m³ of air bubbles. In addition, an experiment was conducted in the same air-lift reactor with Vero cells grown inside porous Asahi microcarriers. The specific hypothetical killing volume calculated from this experiment has a value of 3·10^–4 m³ liquid per m³ of air bubbles, which shows that the porous microcarriers were at least in part able to protect the cells against the detrimental hydrodynamic forces generated by the bubbles.     

Promotion of oxygen transfer in three-phase fluidized-bed bioreactors by floating bubble breakers

The objective of the present study was to investigate a method to enhance the volumetric rate of oxygen transfer in three-phase fluidized-bed bioreactors. The rates of oxygen transfer from air bubbles to viscous liquid media were promoted by floating bubble breakers in three-phase fluidized beds operated in the bubble coalescing regime. The liquid-phase volumetric oxygen transfer coefficient has been recovered by fitting the axial dispersion model to the resultant data, and its dependence on the experimental variables, such as the gas and liquid flow rates, particle size, concentration of bubble breakers, and liquid viscosity, has been examined. The results indicate that the liquid-phase volumetric oxygen transfer coefficient can be enhanced up to 20-25%. The coefficient exhibits a maximum with respect to the volume ratio of the floating bubble breakers to the fluidized solid particles; it increases with increases in the gas and liquid flow rates and size of fluidized particles, while it decreases with an increase in the liquid viscosity. An expression has been developed to correlate the liquid-phase volumetric oxygen transfer coefficient with the experimental variables.     

Bubble bed reactor: A reactor design to minimize the damage of bubble aeration on animal cells

A new bubble aeration system was designed to minimize cell killing and cellular damage due to sparging. The residence time of the bubbles in the developed bubble bed reactor was prolonged dramatically by floating them in a countercurrent produced by an impeller. The performance of the new reactor bubble aeration system, implemented in a laboratory reactor, was tested in dynamic aeration experiments with an without cells. An efficiency up to 95% in oxygen transfer could be achieved, which enables a much lower gas flow rate compared with conventional bubble aeration reactors. The low gas flow rate is important to keep cell damage by bubbles as low as possible. A laser light sheet technique used to find the optimal flow pattern in the reactor. The specific power dissipation of the impeller is a good measure to predict cell damage in a turbulent flow. Typical values for the power dissipation measured in the bubble bed reactor were in the range of 0.002 to 0.013 W/kg, which is far below the critical limit for animal cells. The growth of a hybridoma cell line was studied in cell cultivation experiments. A protein-free medium without supplements such as serum or Pluronic F68 was used to exclude any effect of cell-protecting factors, No difference in the specific growth rate and the yield of the antibodies was observed in cell grown in the bubble free surface aeration in the spinner flask. In contrast to the spinner flask, however, the bubble bed reactor design could be scaled up. (c) 1994 John Wiley & Sons, Inc.     

动物细胞在鼓泡式生物反应器中的死亡速率

通过实验测定,证明生物反应器中细胞死亡速率与气体鼓泡速率成正比而与反应器体积成反比。实验发现气泡大小对细胞死亡速率具有两种作用,一种作用在于影响气泡表面积生成速率;另一种作用则在于影响细胞在气泡表面的吸附程度,其最佳直径为5mm左右。血清和Pluronic F68能显著降低细胞死亡速率,当Pluronic F68浓度达到0．1％时,kd趋于零。所有这些实验结果均与前文提出的生物反应器设计模型具有很好的一致性。     

On-line estimation of viable cells in a hybridoma culture at various DO levels using ATP balancing and redox potential measurement

Two on-line methods for the estimation of viable cell number in hybridoma cultivation were investigated. One used an empirical correlation between redox potential and animal cell density. The other was based on an ATP balance with ATP steady-state assumption. Oxygen uptake rate measurement provided the amount of ATP which was produced by oxidation of NADH. Oxygen uptake rate was measured either by stationary liquid phase balance with surface aeration or by gas balance during bubble aeration with headspace flushing with an inert gas. The amount of ATP produced through the glycolysis was estimated based on the amount of lactate produced. In cultures, in which pH was controlled via manipulation of the gas phase composition, the flow of CO(2) was linearly correlated with the lactate concentration. At constant dissolved oxygen levels, the viable cell density was proportional to the estimated ATP production rate, during exponential growth and during later phases. The estimated specific ATP production rate, however, varied from 2.2 pmol cell(-1) h(-1) at 10% air saturation to 4.5 pmol cell(-1) h(-1) at 100% air saturation. Specific rates of glutamine, glucose, and lactate followed the shape of the specific ATP production rate, whereas the specific oxygen uptake rate was minimal at around 50% air saturation. (c) 1996 John Wiley & Sons, Inc.     

Enzyme recovery during gas/liquid two-phase flow microfiltration of enzyme/yeast mixtures

The effect of a gas/liquid two-phase flow on the recovery of an enzyme was evaluated and compared with standard crossflow operation when confronted with the microfiltration of a high-fouling yeast suspension. Ceramic tubular and flat sheet membranes were used. At constant feed concentration (permeate recycling) and transmembrane pressure, the results obtained with the tubular membrane were dependent on the two-phase flow pattern. In comparison with single-phase flow performances at the same liquid velocity, the enzyme transmission was maintained at a high level with a bubble flow pattern but it decreased by 70% with a slug flow, whatever the flow rate ratio. Identical results were obtained with flat sheet membranes: for the highest flow rate ratio, the enzyme transmission was reduced by 70% even though the permeate flux was improved by 240%. During diafiltration experiments with the tubular membrane, it was found that a bubble flow pattern led to a 13% higher enzyme recovery compared to single-phase flow conditions, whereas with a slug flow the enzyme recovery was strongly reduced. With bubble flow conditions, energy consumption was minimal, confirming that this flow pattern was the most suitable for enzyme recovery.     

Stochastic modelling of axial dispersion in external-loop airlift bioreactors

The paper presents a model of the motion of a particle subjected to several transport processes in connection with mixing in two phase flow. A residence time distribution technique coupled with a one-dimensional dispersion model was used to obtain the axial dispersion coefficient in the liquid phase, D_ax. The proposed model of D_ax for an external-loop airlift bioreactor is based on the stochastic analysis of the two-phase flow in a cocurrent bubble column and modified for the specific flow in the airlift reactor. The model takes into account the riser gas superficial velocity, the riser liquid superficial velocity, the Sauter bubble diameter, the riser gas hold-up, the downcomer-to-riser cross sectional area ratio. The proposed model can be applied with an average error of ᆨ.     

Incorporating hydrodynamics into spatiotemporal metabolic models of bubble column gas fermentation

Gas fermentation has emerged as a technologically and economically attractive option for producing renewable fuels and chemicals from carbon monoxide (CO) rich waste streams. LanzaTech has developed a proprietary strain of the gas fermentating acetogen Clostridium autoethanogenum as a microbial platform for synthesizing ethanol, 2,3-butanediol, and other chemicals. Bubble column reactor technology is being developed for the large-scale production, motivating the investigation of multiphase reactor hydrodynamics. In this study, we combined hydrodynamics with a genome-scale reconstruction of C. autoethanogenum metabolism and multiphase convection–dispersion equations to compare the performance of bubble column reactors with and without liquid recycle. For both reactor configurations, hydrodynamics was predicted to diminish bubble column performance with respect to CO conversion, biomass production, and ethanol production when compared with bubble column models in which the gas phase was modeled as ideal plug flow plus axial dispersion. Liquid recycle was predicted to be advantageous by increasing CO conversion, biomass production, and ethanol and 2,3-butanediol production compared with the non-recycle reactor configuration. Parametric studies performed for the liquid recycle configuration with two-phase hydrodynamics showed that increased CO feed flow rates (more gas supply), smaller CO gas bubbles (more gas–liquid mass transfer), and shorter column heights (more gas per volume of liquid per time) favored ethanol production over acetate production. Our computational results demonstrate the power of combining cellular metabolic models and two-phase hydrodynamics for simulating and optimizing gas fermentation reactors.     

Cometabolic degradation of trichloroethylene in a bubble column bioscrubber

A bubble column bioreactor was used as bioscrubber to carry out a feasibility study for the cometabolic degradation of trichloroethylene (TCE). Phenol was used as cosubstrate and inducer. The bioreactor was operated like a conventional chemostat with regard to the cosubstrate and low dilution rates were used to minimize the liquid outflow. TCE degradation measurements were carried out using superficial gas velocities between 0.47and 4.07 cm s(-1) and TCE gas phase loads between 0.07 and 0.40 mg L(-1) Depending on the superficial gas velocity used, degrees of conversion between 30% and 80% were obtained. A simplified reactor model using plug flow for the gas phase, mixed flow for the liquid phase, and pseudo first order reaction kinetics for the conversionof TCE was established. The model is able to give a reasonable approximation of the experimental data. TCE degradation at the used experimental conditions is mainly limited by reaction rate rather than by mass transfer rate. The model can be used to calculate the reactor volume and the biomass concentration for a required conversion. (c) 1995 John Wiley & Sons Inc.     

Effects of bubble–liquid two‐phase turbulent hydrodynamics on cell damage in sparged bioreactor

According to recent experimental studies on sparged bioreactors, significant cell damage may occur at the gas inlet region near the sparger. Although shear stress was proposed to be one of the potential causes for cell damage, detailed hydrodynamic studies at the gas inlet region of gas–liquid bioreactors have not been performed to date. In this work, a second‐order moment (SOM) bubble–liquid two‐phase turbulent model based on the two‐fluid continuum approach is used to investigate the gas–liquid hydrodynamics in the bubble column reactor and their potential impacts on cell viability, especially at the gas inlet region. By establishing fluctuation velocity and bubble–liquid two‐phase fluctuation velocities correlation transport equations, the anisotropy of two‐phase stresses and the bubble–liquid interactions are fully considered. Simulation results from the SOM model indicate that shear and normal stresses, turbulent energy dissipation rate, and the turbulent kinetic energy are generally smaller at the gas inlet region when compared with those in the fully developed region. In comparison, a newly proposed correlation expression, stress‐induced turbulent energy production (STEP), is found to correlate well with the unusually high cell death rate at the gas inlet region. Therefore, STEP, which represents turbulent energy transfer to a controlled volume induced by a combination of shear and normal stresses, has the potential to provide better explanation for increased cell death at the sparger region. © 2013 American Institute of Chemical Engineers Biotechnol. Prog., 30:48–58, 2014     

Selective desorption of carbon dioxide from sewage sludge for in situ methane enrichment--part I: pilot-plant experiments

In situ methane enrichment in anaerobic digestion of sewage sludge has been investigated by experiments and by modeling. In this first part, the experimental work on the desorption of carbon dioxide and methane from sewage sludge is reported. The bubble column, had a diameter of 0.3 m and a variable height up to 1.8 m. At operation the dispersion height in the column was between 1 and 1.3 m. Outdoor air was used. The column was placed close to a full-scale sewage sludge digester, at a municipal wastewater treatment plant. The digester was operated at mesophilic conditions with a hydraulic retention time of about 20 days. The bubble column was operated to steady-state, at which carbon dioxide concentration and alkalinity were determined on the liquid side, and the concentration of carbon dioxide and methane on the gas side. Thirty-eight experiments were performed at various liquid and gas flow rates. The experimental results show that the desorption rates achieved for carbon dioxide ranges from 0.07 to 0.25 m(3) CO(2)/m(3) sludge per day, which is comparable to the rate of generation by the anaerobic digestion. With increasing liquid flow rate and decreasing gas flow rate the amount of methane desorbed per amount of carbon dioxide desorbed increases. The lowest methane loss achieved is approximately 2% of the estimated methane production in the digestion process.     

A molecular dynamics analysis of homogeneous bubble nucleation with a noncondensable gas in cryogenic cavitation inception

In this paper, homogeneous bubble nucleation in liquid oxygen (as one of the cryogenic fluids) with a noncondensable gas of nitrogen or that of helium was investigated using molecular dynamics method employing a fitted Lennard-Jones potential. We evaluated the influence of nitrogen gas and helium gas on the SATuration line (SAT) and the spinodal line as the thermodynamic limit of stability (TLS), and on the kinetic limit of stability (KLS) defined from a bubble nucleation rate. As a result, it was obtained that the influence of the noncondensable gases on the SAT and the TLS was negligible at molar fraction less than 1% although helium gas had several times stronger action to decrease the KLS compared with nitrogen gas. On the other hand, it was also indicated that the actual influence of both noncondensable gases on the cavitation inception in liquid oxygen might be negligible at least at standard conditions where the fluid starts to flow around or less than the atmospheric pressure.     

Mathematical model of gas bubble evolution in a straight tube.

Deep sea divers suffer from decompression sickness (DCS) when their rate of ascent to the surface is too rapid. When the ambient pressure drops, inert gas bubbles may form in blood vessels and tissues. The evolution of a gas bubble in a rigid tube filled with slowly moving fluid, intended to simulate a bubble in a blood vessel, is studied by solving a coupled system of fluid-flow and gas transport equations. The governing equations for the fluid motion are solved using two techniques: an analytical method appropriate for small nondeformable spherical bubbles, and the boundary element method for deformable bubbles of arbitrary size, given an applied steady flow rate. A steady convection-diffusion equation is then solved numerically to determine the concentration of gas. The bubble volume, or equivalently the gas mass inside the bubble for a constant bubble pressure, is adjusted over time according to the mass flux at the bubble surface. Using a quasi-steady approximation, the evolution of a gas bubble in a tube is obtained. Results show that convection increases the gas pressure gradient at the bubble surface, hence increasing the rate of bubble evolution. Comparing with the result for a single gas bubble in an infinite tissue, the rate of evolution in a tube is approximately twice as fast. Surface tension is also shown to have a significant effect. These findings may have important implications for our understanding of the mechanisms of inert gas bubbles in the circulation underlying decompression sickness.     

Investigation of the structure of two-phase flow fermentation model media in bubble-column bioreactors

Summary Electrical conductivity microprobes have been used to estimate the transverse variation of bubble size, local gas holdup and local specific gas/liquid interfacial area in bench scale bubble column bioreactors containing fermentation model media. Inserted O₂-electrodes and plane parallel windows alter the structure of the two phase flow. Even slight tilting of the column strongly influences the transverse profiles of the bubble size and local gas holdup. The larger bubbles are collected at the wall, where they can be redispersed. These observations open up new possibilities for the construction of bubble column bioreactors.     

Bubble splitting in bifurcating tubes: a model study of cardiovascular gas emboli transport.

The transport of long gas bubbles, suspended in liquid, through symmetric bifurcations, is investigated experimentally and theoretically as a model of cardiovascular gas bubble transport in air embolism and gas embolotherapy. The relevant dimensionless parameters in the models match the corresponding values for arteries and arterioles. The effects of roll angle (the angle the plane of the bifurcation makes with the horizontal), capillary number (a dimensionless indicator of flow), and bubble volume (or length) on the splitting of bubbles as they pass through the bifurcation are examined. Splitting is observed to be more homogenous at higher capillary numbers and lower roll angles. It is shown that, at nonzero roll angles, there is a critical value of the capillary number below which the bubbles do not split and are transported entirely into the upper branch. The value of the critical capillary number increases with roll angle and parent tube diameter. A unique bubble motion is observed at the critical capillary number and for slightly slower flows: the bubble begins to split, the meniscus in the lower branch then moves backward, and finally the entire bubble enters the upper branch. These findings suggest that, in large vessels, emboli tend to be transported upward unless flow is unusually strong but that a more homogeneous distribution of emboli occurs in smaller vessels. This corresponds to previous observations that air emboli tend to lodge in the upper regions of the lungs and suggests that relatively uniform infarction of tumors by gas embolotherapy may be possible.     

Gas–liquid dispersion in a fibrous fixed bed biofilm reactor at growth and non-growth conditions

There is limited data on gas dispersion characteristics of fixed bed biofilm reactors under growth and non-growth conditions. In this paper, the gas–liquid dispersion of a bubble bed packed with a fibrous structured packing for biofilm application is studied. The reactor is operated with Pseudomonas putida aimed at aniline degradation in wastewater. Gas hold-up and bubble size distribution are determined. Running gas–liquid reaction conditions as well as non-reactive flow gas hold-up and bubble size distribution in the presence of surface-active and viscous components were measured. The properties of the gas dispersion proved to be stabilized by the fibrous bed presence and showed improvement of the dispersion parameter by the packing. Gas hold-up was found to increase monotonously with the rise of gas superficial velocity and viscosity and with surface tension fall. Liquid superficial velocity showed marginal effect. Apart from showing high gas hold-up and low bubble size due to surface-active and viscous dissolved elements, the biochemical reaction did not pose any significant additional effect. In agreement with the expected lack of bubble coalescence and break-up in the highly ionic solution practiced, the population size distribution and average bubble size were found to vary with the major operation factors opposite to their gas hold-up contribution. Gas hold-up was correlated with the specific bubble-to-channel size ratio and further with the variables considered. An empirical equation is proposed that relates gas hold-up with all studied variables. Assuming geometric similarity of the prototype and the real vessels, the equation as well as its corresponding range of fluid velocities can be used for bioreactor design and scale-up. The results concerning the gas hold-up are shown to be comparable with previous studies of mesh wire packing.     

Hemolytic potential of hydrodynamic cavitation

The purpose of this study was to determine the hemolytic potentials of discrete bubble cavitation and attached cavitation. To generate controlled cavitation events, a venturigeometry hydrodynamic device, called a Cavitation Susceptibility Meter (CSM), was constructed. A comparison between the hemolytic potential of discrete bubble cavitation and attached cavitation was investigated with a single-pass flow apparatus and a recirculating flow apparatus, both utilizing the CSM. An analytical model, based on spherical bubble dynamics, was developed for predicting the hemolysis caused by discrete bubble cavitation. Experimentally, discrete bubble cavitation did not correlate with a measurable increase in plasma-free hemoglobin (PFHb), as predicted by the analytical model. However, attached cavitation did result in significant PFHb generation. The rate of PFHb generation scaled inversely with the Cavitation number at a constant flow rate, suggesting that the size of the attached cavity was the dominant hemolytic factor.     

Reactor heterogeneity with saccharopolyspora erythraea airlift fermentations

Bioreactor heterogeneity has been studied in a multiconfigurable pilot-scale airlift reactor (0.25 m3) which created different degrees of heterogeneity. The impact of the two sparger configurations, i.e. in the draft tube or the annulus, in conjunction with a marine propeller fitted at the base of the downcomer, on the physiology of Saccharopolyspora erythraea was studied. Cellular growth, morphology, and productivity were compared between airlift and stirred tank reactors. Dissolved oxygen tension heterogeneity caused by differences in dissolved oxygen tension around the vessel did not affect growth, but the reduction of heterogeneity improved the specific erythromycin production rate and final specific production. Erythromycin production was shown to be proportional to the energy dissipation rate. The enhancement of bubble coalescence with increasing apparent viscosity led to the reduction of the sectional gas holdups and the improvement of liquid mixing. The extent of the changes with increasing apparent viscosity was dependent on the broth morphology, reactor configurations, and operating conditions. Copyright 1998 John Wiley & Sons, Inc.