Process optimization of a continuous airlift tower-loop reactor

Based on the experimental investigations with H. polymorpha and Methylomonas M 15 in bench-scale airlift tower-loop reactors, a general distributed parameter model was developed and used to simulate to cultivation process in a 40-m-high production reactor. This general model was simplified with regard to the gas phase and loop balances and was employed to optimize cell productivity and/or profit in a 20-m-high pilot-plant airlift tower-loop reactor. Maximum cell productivity always occurs in the oxygen-transfer-limited growth range. In case of a high "penalty factor" for nonconsumed substrate, maximum profit is attained at the boundary between substrate and oxygen-transfer-limited growth. Oxygen-transfer limitation exists in the lower half of the tower, whereas in the upper half, substrate limitation prevails. The longitudinal dissolved oxygen concentration passes a minimum in this case as has been determined experimentally in the bench-scale column. The simulation results agree fairly well with the data measured in the pilot plant.     

Dynamic simulation of cyclic batch anaerobic digestion of cattle manure

Cyclic batch reactors with periodical feeds and extractions, are often used in cattle manure anaerobic digestion. The dynamic behavior of this type of reactor was simulated in this study. The kinetic model developed by I. Angelidaki et al. [Biotechnol. Bioeng. 42 (1993) 159], together with microbial growth kinetics, conventional material balances for an ideally cyclic batch reactor, liquid-gas interactions, and liquid phase equilibrium chemistry were used in this study. The model showed good agreement with the experimental data of R.I. Mackie and M.P. Bryant [Appl. Microbiol. Biotechnol. 43 (1995) 346], and R. Borja et al. [Chem. Eng. J. 54 (1994) B9]. The effects of hydraulic retention time (HRT), organic loading rate, reactant concentrations, feeding interval, and initial conditions such as pH and ammonia concentration on process performance can be evaluated by the dynamic model. Also simulation results show that the equilibrium conditions can be considered for CO2 distribution between liquid and gas phases, especially for processes with long retention times.     

Steady state characteristics of acclimated hydrogenotrophic methanogens on inorganic substrate in continuous chemostat reactors

A Monod model has been used to describe the steady state characteristics of the acclimated mesophilic hydrogenotrophic methanogens in experimental chemostat reactors. The bacteria were fed with mineral salts and specific trace metals and a H(2)/CO(2) supply was used as a single limited substrate. Under steady state conditions, the growth yield ( [Formula: see text] ) reached 11.66 g cells per mmol of H(2)/CO(2) consumed. The daily cells generation average was 5.67 x 10(11), 5.25 x 10(11), 4.2 x 10(11) and 2.1 x 10(11) cells/l-culture for the dilutions 0.071/d, 0.083/d, 0.1/d and 0.125/d, respectively. The maximum specific growth rate (mu(max)) and the Monod half-saturation coefficient (K(S)) were 0.15/d and 0.82 g/L, respectively. Using these results, the reactor performance was simulated. During the steady state, the simulation predicts the dependence of the H(2)/CO(2) concentration (S) and the cell concentration (X) on the dilution rate. The model fitted the experimental data well and was able to yield a maximum methanogenic activity of 0.24 L CH(4)/g VSS.d. The dilution rate was estimated to be 0.1/d. At the dilution rate of 0.14/d, the exponential cells washout was achieved.     

Anaerobic digestion model no. 1-based distributed parameter model of an anaerobic reactor: I. Model development

This work presents a distributed parameter model of the anaerobic digestion process. The model is based on the Anaerobic digestion model no. 1 (ADM1) and was developed to simulate anaerobic digestion process in high-rate reactors with significant axial dispersion, such as in upflow anaerobic sludge bed (UASB) reactors. The model, which was named ADM1d, combines ADM1's kinetics of biomass growth and substrate transformation with axial dispersion material balances. ADM1d uses a hyperbolic tangent function to describe biomass distribution within a one compartment model. A comparison of this approach with a two-compartment, sludge bed - liquid above the bed, model showed similar simulation results while the one-compartment model had less equations. A comparison of orthogonal collocation and finite difference algorithms for numerical solution of ADM1d showed better stability of the finite difference algorithm.     

Quantitative screening method for hydrolases in microplates using pH indicators: determination of kinetic parameters by dynamic pH monitoring.

The presented pH-dyn assay serves as a versatile tool for screening enzymatically catalyzed reactions consuming or producing acids. The method is based on material balances of substrates and products. Ion balances relate concentrations of acids and bases to pH. pH-changes caused by the enzymatically catalyzed reaction in a well-defined buffer system are recorded by light-absorption measurements of a pH-indicator. Kinetic parameters are estimated by fitting the modeled pH changes to the experimentally observed ones. The enzymatically catalyzed hydrolysis of 4-nitrophenol is used as a model system. A pH indicator, bromothymol blue, is used to monitor the reaction progress. The reaction is monitored until the limiting substrate is completely consumed. This allows the estimation of the parameters of the Michaelis-Menten kinetics, K(M) and k(cat), in a single run. The results agree well with conventional spectrophotometric experiments and values reported in literature. Around pH 7, environmental CO(2) influences pH. Carbon dioxide influence was included in the model. Thus it was possible to estimate initial CO(2) concentrations as a model parameter, and therefore automatic correction for the CO(2) disturbances was achieved. This was important to detect low conversions at low buffer concentrations.     

Photobioreactor design: Mixing, carbon utilization, and oxygen accumulation

Photobioreactor design and operation are discussed in terms of mixing, carbon utilization, and the accumulation of photosynthetically produced oxygen. The open raceway pond is the primary type of reactor considered; however small diameter (1-5 cm) horizontal glass tubular reactors are compared to ponds in several respects. These are representative of the diversity in photobioreactor design: low capital cost, open systems and high capital cost, closed systems. Two 100-m(2) raceways were operated to provide input data and to validate analytical results. With a planktonic Chlorella sp., no significant difference in productivity was noted between one pond mixed at 30 cm/s and another mixed from 1 to 30 cm/s. Thus, power consumption or CO(2) outgassing limits maximal mixing velocities. Mixing power inputs measured in 100-m(2) ponds agreed fairly well with those calculated by the use of Manning's equation. A typically configured tubular reactor flowing full (1 cm diameter, 30 cm/s) consumes 10 times as much energy as a typical pond (20 cm deep flowing at 20 cm/s). Tubular reactors that flow only partially full would be limited by large hydraulic head losses to very short sections (as little as 2 m length at 30 cm/s flow) or very low flow velocities. Open ponds have greater CO(2) storage capacity than tubular reactors because of their greater culture volume per square meter (100-300 L/m(2) vs. 8-40 L/m(2) for 1-5-cm tubes). However, after recarbonation, open ponds tend to desorb CO(2) to the atmosphere. Thus ponds must be operated at higher pH and lower alkalinity than would be possible with tubular reactors if cost of carbon is a constraint. The mass transfer coefficient, K(L), for CO(2) release through the surface of a 100-m(2) pond was determined to be 0.10 m/h. Oxygen buildup would be a serious problem with any enclosed reactor, especially small-diameter tubes. At maximal rates of photosynthesis, a 1-cm tubular reactor would accumulate 8-10 mg O(2)/L/min. This may result in concentrations of oxygen reaching 100 mg/L, even with very frequent gas exchange. In an open pond, dissolved oxygen rises much more slowly as a consequence of the much greater volume per unit surface area and the outgassing of oxygen to the atmosphere. The maximum concentration of dissolved oxygen is typically 25-40 mg/L. The major advantage of enclosed reactors lies in the potential for aseptic operation, a product value which justifies the expense. For most products of algal mass cultivation, open ponds are the only feasible photobioreactor design capable of meeting the economic and operating requirements of such systems, provided desirable species can be maintained.     

Cultivation of E. coli in single- and ten-stage tower-loop reactors

E. Coli was cultivated in batch and continuous operations in the presence of an antifoam agent in stirred-tank and in single- and ten-stage airlift tower reactors with an outer loop. The maximum specific growth rate, mu(m), the substrate yield coefficient, Y(x/s), the respiratory quotient, RQ, substrate conversion, U(s), the volumetric mass transfer coefficient, K(L)a, the specific interfacial area, a, and the specific power input, P/V(L), were measured and compared. If a medium is used with a concentration of complex substrates (extracts) 2.5 times higher than that of glucose, a spectrum of C sources is available and cell regulation influences reactor performance. Both mu(m) and Y(X/S), which were evaluated in batch reactors, cannot be used for continuous reactors or, when measured in stirred-tank reactors, cannot be employed for tower-loop reactors: mu(m) is higher in the stirred-tank batch than in the tower-loop batch reactor, mu(m) and Y(x/s) are higher in the continuous reactor than in the batch single-stage tower-loop reactor. The performance of the single-stage is better than that of the ten-stage reactor due to the inefficient trays employed. A reduction of the medium recirculation rate reduces OTR, U(s), Pr, and Y(X/S) and causes cell sedimentation and flocculation. The volumetric mass transfer coefficient is reduced with increasing cultivation time; the Sauter bubble diameter, d(s), remains constant and does not depend on operational conditions. An increase in the medium recirculation rate reduces k(L)a. The specific power input, P/V(L), for the single-stage tower loop is much lower with the same k(L)a value than for a stirred tank. The relationship k(L)a vs. P/V(L) evaluated for model media in stirred tanks, can also be used for cultivations in these reactors.     

Packed- and fluidized-bed biofilm reactor performance for anaerobic wastewater treatment

Anaerobic degradation performance of a laboratory-scale packed-bed reactor (PBR) was compared with two fluidized-bed biofilm reactors (FBRs) on molasses and whey feeds. The reactors were operated under constant pH (7) and temperature (35 degrees C) conditions and were well mixed with high recirculation rates. The measured variables were chemical oxygen demand (COD), individual organic acids, gas composition, and gas rates. As carrier, sand of 0.3-0.5 mm diameter was used in the FBR, and porous clay spheres of 6 mm diameter were used in the PBR. Startup of the PBR was achieved with 1-5 day residence times. Start-up of the FBR was only successful if liquid residence times were held low at 2-3 h. COD degradations of 86% with molasses (90% was biodegradable) were reached in both the FBR and PBR at 6 h residence time and loadings of 10 g COD/L day. At higher loadings the FBR gave the best performance; even at 40-45 g COD/L day, with 6 h residence times, 70% COD was degraded. The PBR could not be operated above 20 g COD/L day without clogging. A comparison of the reaction rates show that the PBR and FBR per formed similarly at low concentrations in the reactors up to 1 g COD/L, while above 3 g COD/L the rates were 17.4 g COD/L day for the PBR and 38.4 g COD/L day for the FBR. This difference is probably due to diffusion limitations and a less active biomass content of the PBR compared with the fluidized bed.The results of dynamic step change experiments, in which residence times and feed concentrations were changed hanged at constant loading, demonstrated the rapid response of the reactors. Thus, the response times for an increase in gas rate or an increase in organic acids due to an increase in feed concentration were less than 1 day and could be explained by substrate limitation. Other slower responses were observed in which the reactor culture adapted over periods of 5-10 days; these were apparently growth related. An increase in loading of over 100% always resulted in large increases inorganic acids, especially acetic and propionic, as well as large increases in the CO(2) gas content. In general, the CO(2) content of the gas was very low, due to the large amount of dissolved CO(2) that exited with the liquid phase at low residence times. The performance of the FBR with whey was comparable to its performance with molasses, and switching of molasses to whey feed resulted in immediate good performance without adaptation.     

Oxygen and carbon dioxide mass transfer and the aerobic, autotrophic cultivation of moderate and extreme thermophiles: a case study related to the microbial desulfurization of coal

Mass transfers of O(2), CO(2), and water vapor are among the key processes in the aerobic, autotrophic cultivation of moderate and extreme thermophiles. The dynamics and kinetics of these processes are, in addition to the obvious microbial kinetics, of crucial importance for the industrial desulfurization of high-pyritic coal by such thermophiles. To evaluate the role of the temperature on the gas mass transfer, k(L)a measurements have been used to supplement the existing published data. Oxygen mass transfer from gas (air) to liquid (5 mM H(2)SO(4) in water) phase as a function of the temperature has been studied in a laboratory-scale fermentor. At 15, 30, 45, and 70 degrees C, (k(L)a)(o) values (for oxygen) were determined under three different energy input conditions by the dynamic gassing in/out method. The (k(L)a)(o) was shown to increase under these conditions with increasing temperature, and straight lines were obtained when the logarithm of (k(L)a)(o) was plotted against the temperature. By multiplying the equilibrium concentration of O(2) in water with (k(L)a)(o) maximal, O(2) transfer capacities were calculated. It appeared that in finite of a decreased solubility of O(2) at elevated temperature in mechanically mixed fermentors the calculated transfer capacities showed only minor changes for the range between 15 and 70 degrees C. However, in an air-mixed fermentor the transfer capacity of O(2) decreased slowly but steadily.Carbon dioxide mass transfer was predicted by calculations on the basis of the data for oxygen transfer. The maximal CO(2) transfer capacity, calculated as the product of the equilibrium CO(2) concentration times (k(L)a)(c), decreased slowly as the temperature increased over the range 15-70 degrees C under all three energy input conditions. Subsequent process design calculations showed that for aerobic, autotrophic cultures, CO(2) limitation is more likely to occur than O(2) limitation.     

Anaerobic biodegradation tests and gas emissions from subsurface flow constructed wetlands

Anaerobic tests with gravel from horizontal subsurface flow constructed wetlands (SSF) used for the treatment of urban wastewater were developed in order to evaluate the anaerobic biodegradability of their effluents. Two types of assays were conducted. The reactors used for the first type were glass vials of 45 mL, that were used for only one measurement, requiring starting experiments with a number of reactors equal to the measurements to be made. For the second type of experiments multiple measurements were done in the same reactors, by using flasks of 2.2L. The COD of the SSF effluents used for the tests ranged from 60 to 130 mg/L. The evolution of CO(2) in the headspace of the reactors was used as indicator of anaerobic biodegradation rates. CO(2) mass emission rates ranged from 0.005 to 0.015 micromol/mL day. CH(4) generation was not detected in the tests in relation with the refractory properties of the effluent organic matter of the studied SSF. In situ measurement of CO(2) and CH(4) emissions from the gravel of the SSF ranged from 0.106 to 0.464 and from 0.039 to 0.107 mmol/m(2)h, respectively. Several CO(2) fluxes measured in the field were quite consistent with the emissions observed in the laboratory. The developed tests can help to understand the performance of SSF and improve their operation.     

Scaleup of ajmalicine production by plant cell cultures of Catharanthus roseus

The effect of scaleup on he production of ajmalicine by a Catharanthus roseus cell suspension culture in a selected induction medium were studied. In preliminary experiments it was observed that the culture turned brown and the production was inhibited upon transfer from a shake flask to a stirred bioreactor with forced aeration. Two factors were recognized as the potential origin of the differences between shake flask and bioreactor cultures: gas composition and mechanical shear forces. These factors were studied separately.By recirculating a large part of the exhaust gas, a comparable gas regime was obtained in a bioreactor as occurred in a shake flask cultures. This resulted in the absence of browning and a similar pattern of ajmalicine production as observed in shake flasks. The effect of shear forces could not be demonstrated. However, the experiments showed that the culture may be very sensitive to liquid phase concentrations of gaseous compounds. The effects of k(L)a, aeration rate, CO(2) production rate, and influent gas phase CO(2) concentration on the liquid phase CO(2) concentration are discussed. (c) 1993 John Wiley & Sons, Inc.     

Kinetic studies on (N-formyltryptophyl)cytochrome c.

The formylation of the ring nitrogen atom of the tryptophan residue in cytochrome c was carried out and consequent changes in the kinetic properties of the protein were investigated. The reduction of formylated cytochrome c by Cr2+ was studied by stopped-flow techniques. At pH 6.5 the reduction process shows the presence of two phases. One phase (k = 4 X 10(4) M-1-s-1) is dependent on Cr2+ concentration and one phase (k = 5.0 s-1) is not. A study of the temperature dependence of the two phases yields values for their activation energies of 38.6kJ-mol-1 and 42.4kJ-mol-1 respectively. The reaction of the reduced formylated cytochrome c with CO was followed by means of both stopped-flow techniques and flash photolysis. The combination with CO at pH 6.8 measured in stopped-flow experiments shows two phases, both dependent on the concentration of CO (k1 = 1.8 X 10(2) M-1-s-1). If CO was dissociated from the protein by photolysis and then allowed to recombine with it, it was found to do so in a simple manner, at a rate which depended on the concentration of CO (k = 1.9 X 10(2) M-1-s-1). A tentative model which can accommodate these findings is proposed. The reaction of the oxidized form of formylated cytochrome c with NO was followed by means of stopped-flow techniques. The reaction was found to be biphasic with one phase dependent on the concentration of NO (k = 2.8 X 10(3) M-1-s-1) and one phase (k = 0.2x-1) independent of the concentration of NO. This behaviour is compared with that of the native molecule. A comparison of these kinetic observations with those on other tryptophan-specific modifications leads to the conclusion that the main alteration in kinetic properties is due, not to the nature of the modifying group, but rather to the disruption of the normal environment of the haem.     

Liquid-to-Gas Mass Transfer in Anaerobic Processes: Inevitable Transfer Limitations of Methane and Hydrogen in the Biomethanation Process

Liquid-to-gas mass transfer in anaerobic processes was investigated theoretically and experimentally. By using the classical definition of k(L)a, the global volumetric mass transfer coefficient, theoretical development of mass balances in such processes demonstrates that the mass transfer of highly soluble gases is not limited in the usual conditions occurring in anaerobic fermentors (low-intensity mixing). Conversely, the limitation is important for poorly soluble gases, such as methane and hydrogen. The latter could be overconcentrated to as much as 80 times the value at thermodynamic equilibrium. Such overconcentrations bring into question the biological interpretations that have been deduced solely from gaseous measurements. Experimental results obtained in three different methanogenic reactors for a wide range of conditions of mixing and gas production confirmed the general existence of low mass transfer coefficients and consequently of large overconcentrations of dissolved methane and hydrogen (up to 12 and 70 times the equilibrium values, respectively). Hydrogen mass transfer coefficients were obtained from the direct measurements of dissolved and gaseous concentrations, while carbon dioxide coefficients were calculated from gas phase composition and calculation of related dissolved concentration. Methane transfer coefficients were based on calculations from the carbon dioxide coefficients. From mass balances performed on a gas bubble during its simulated growth and ascent to the surface of the liquid, the methane and carbon dioxide contents in the gas bubble appeared to be controlled by the bubble growth process, while the bubble ascent was largely responsible for a slight enrichment in hydrogen.     

Methane recovery from water hyacinth through whole-cell immobilization technology

The concepts of feed pretreatment, phase separation, and whole-cell immobilization technology have been incorporated in this investigation for the development of rational and cost-effective two- and three-stage methane recovery systems from water hyacinth (WH)Analyses of laboratory data reveal that a three-stage system could be designed with an alkali pretreatment stage [3.6% Na(2)CO(3) + 2.5% Ca(OH)(2) W/W, 24 h HRT] followed by an open acid reactor (2.1 days HRT) and closed immobilized methane reactor (12 h HRT), providing steady-state COD conversion of 62-65%, TVA conversion of 91-95%, and gas productivity of 4.08-5.36 L/L reactor volume/day with 82% methane. A gas yield of 50 L/kg WH/day (dry wt basis) at 35-37 degrees C is possible with this system. Insulation bricks, with particle size distribution of 500-3000 mum, were used as support material in the reactors at organic loading rate of 20 kg COD/m(3) day. The reactors matured in 15-18 weeksSubstantial reduction in retention time for the conversion of volatile acids in immobilized methane reactors prompted further research on the combined immobilized reactor to make possible an additional reduction in the cost of a WH-based biogas system. Evaluation of laboratory data reveals that a two-stage system could be designed with an open alkali pretreatment stage and a combined immobilized reactor (12 h HRT), providing steady-state COD conversion of 53% and gas productivity of 3.1 L/L reactor volume/day with 86% methane. A gas yield of 44 L/kg WH/day (dry wt basis) at 35-37 degrees C could be obtained from this system. Insulation bricks, with 500-1000 mum particle size distribution, was used as support material at an organic loading rate of 15 kg COD/m(3) day. Notwithstanding the fact that the technology in this study has been developed with water hyacinth as substrate, the implicit principles could be extended to any other organic substrate.     

Development of a process for efficient use of CO2 from flue gases in the production of photosynthetic microorganisms

A new methodology to use efficiently flue gases as CO(2) source in the production of photosynthetic microorganisms is proposed. The CO(2) is absorbed in an aqueous phase that is then regenerated by microalgae. Carbonated solutions could absorb up to 80% of the CO(2) from diluted gas reaching total inorganic carbon (TIC) concentrations up to 2.0 g/L. The pH of the solution was maintained at 8.0-10.0 by the bicarbonate/carbonate buffer, so it is compatible with biological regeneration. The absorption process was modeled and the kinetic parameters were determined. Anabaena sp. demonstrated to tolerate pH (8.0-10.0) and TIC (up to 2.0 g/L) conditions imposed by the absorption step. Experiments of regeneration of the liquid phase demonstrated the feasibility of the overall process, converting CO(2) into organic matter. The developed process avoids heating to regenerate the liquid whereas maximizing the efficiency of CO(2) use, which is relevant to achieve the commercial production of biofuels from microalgae.     

Solubilization and concentration of carbon dioxide: novel spray reactors with immobilized carbonic anhydrase

Novel spray reactors are described that employ immobilized biocatalyst (carbonic anhydrase), enabling concentration and solubilization of emitted CO(2) by allowing catalytic contact with water spray. The reactors were fed with simulated emission gas. The performance of the reactors was investigated with respect to operation variable: emission flow rate; gas composition in the emission stream; water flow rate; area-to-volume ratio of immobilized reactor core; and the enzyme load within the core. The reactors were also investigated for pressure drop and extractability of CO(2) from the emission with single vs. multiple reactors (of combined equal volume). The biotechnological process of solubilization and concentration of CO(2) from emission exhausts or streams occurring in the spray reactors could be coupled for further biochemical/chemical conversion of the concentrated CO(2).     

全球变化条件下植物个体的生理生态学模型

天气模型中应用随机模拟方法,产生以天或小时为时间间隔的气温、降水、相对湿度、云量、太阳辐射等天气要素的动态变化时间序列。利用北京地区近30年天气资料进行了模拟验证,模拟结果与实际的天气变化进程相符。生理生态模型描述了净光合速率、气孔传导度、蒸腾速率、水分利用效率的变化机理。结合开顶式CO_2浓度倍增大豆(Glycine max(L.)Merr.)生长实验,分析了这些生理生态特性在全球变化下的动态响应机制,并进行了模拟预测。结果表明:CO_2浓度倍增情况下,净光合速率提高45％,其中光量子效率显著增加,而CO_2传导系数略有下降;气孔传导度、蒸腾速率下降约30％;水分利用效率随CO_2浓度增加几乎呈线性增长,倍增后提高近一倍。     

Ex situ bioremediation of pyrene contaminated soil in bio-slurry phase reactor operated in periodic discontinuous batch mode: Influence of bioaugmentation

Ex situ treatment of simulated pyrene-contaminated soil was studied in bio-slurry phase reactors operated in periodic discontinuous batch mode under anoxic–aerobic–anoxic–anoxic microenvironment. Experiments were performed in six different bio-slurry phase reactors (retention time of 120 h; soil loading rate of 20 kg soil/m³-day; operating temperature at 28±2 °C) by varying substrate concentration (substrate loading rate (SLR), 0.12, 0.24 and 0.36 g pyrene/kg soil-day) and bioaugmentation application (domestic sewage inoculum; CFU—2×10⁶). The performance of slurry phase reactors was found to be dependent on the applied SLR and application of bioaugmentation (domestic sewage as augmented inoculum). Control reactor (killed control) showed only 6% of pyrene degradation while the non-augmented reactor showed an efficiency of 34% (substrate degradation rate (SDR)—0.0165 g pyrene/kg soil-day). In the case of augmented reactors, the system operated with low SLR showed a pyrene degradation efficiency of almost 90% (SDR—0.04 g pyrene/kg soil-day) and the reactor with high SLR showed 50% (SDR—0.025 g pyrene/kg soil-day) of pyrene degradation indicating the dependence of performance on the substrate concentration. Colony forming units (CFUs) variation was in good agreement with the performance of the reactors with respect to pyrene degradation. On the whole, pyrene degradation rate was greater in the augmented reactors compared to non-augmented reactors.     

Optimization of oxygen mass transfer in a multiphase bioreactor with perfluorodecalin as a second liquid phase

Oxygenation is an important parameter involved in the design and operation of mixing-sparging bioreactors and it can be analyzed by means of the oxygen mass transfer coefficient (k(L)a). The operational conditions of a stirred, submerged aerated 2-L bioreactor have been optimized by studying the influence of a second liquid phase with higher oxygen affinity (perfluorodecalin or olive oil) in the k(L)a. Using k(L)a measurements, the influence of the following parameters on the oxygen transfer rate was evaluated: the volume of working medium, the type of impellers and their position, the organic phase concentration, the aqueous phase composition, and the concentration of inactive biomass. This study shows that the best experimental conditions were achieved with a perfluorodecalin volume fraction of 0.20, mixing using two Rushton turbines with six vertical blades and in the presence of YPD medium as the aqueous phase, with a k(L)a value of 64.6 h(-1). The addition of 20% of perfluorodecalin in these conditions provided a k(L)a enhancement of 25% when pure water was the aqueous phase and a 230% enhancement when YPD medium was used in comparison to their respective controls (no perfluorodecalin). Furthermore it is shown that the presence of olive oil as a second liquid phase is not beneficial to the oxygen transfer rate enhancement, leading to a decrease in the k(L)a values for all the concentrations studied. It was also observed that the magnitude of the enhancement of the k(L)a values by perfluorodecalin depends on the biomass concentration present.