Periodic operation of bioreactors for autocatalytic reactions with Michaelis-Menten kinetics

The performance of an isothermal tubular bioreactor carrying out autocatalytic reactions obeying Michaelis-Menten Kinetics is analyzed for improvement in the average yield of product B. Under steady-state condition, the reactor is shown to exhibit input multiplicities in the yield of B with the mean residence time. Simulation results show that a significant improvement in the average yield of B is obtained under feed substrate concentration cycling. The two values of mean residence time giving identical yield under conventional steady-state operation is shown to give distinctly different behaviour under periodic operation. The lower value of the residence time gives improved average yield of B. The performances of the reactor with power law kinetics and that with the Michaelis-Menten kinetics show distinct average yield under periodic operation even though steady-state operation gives identical yield.     

Nonlinear control of bioreactors with input multiplicities—an experimental work

The phrase input multiplicities means that an input variable with more than one value produces the same output value as if there were a single input–single output process. With input multiplicities, the value of the process gain changes as the manipulated variable changes, and beyond a certain input value, the sign of the gain also changes. A conventional PI controller for processes with input multiplicities may give unstable, less economical, or oscillatory responses. In the present work, control problems of a continuous bioreactor exhibiting two input multiplicities in the dilution rate on productivity were experimentally analyzed. A regulatory problem for the evaluation of controllers was taken up, i.e. a step change was made in the feed substrate concentration from 20 to 25 g/l at steady state conduction at lower (0.09386 h⁻¹) and higher (0.2278 h⁻¹) dilution rates for the same productivity of 2.9 g/l h. The nonlinear PI controller gave a more stable and fast response at both input dilution rates. The linear PI controller designed for a lower input dilution rate was stable, with some oscillations at the lower dilution rate, but the response was unstable at a higher dilution rate due to the input multiplicity behaviour of the process. Thus, nonlinear PI controller performance was found to be superior to that of the linear controller, and earlier reported theoretical results have been validated by the present experimental work.     

Gas–liquid mass transfer in an up-flow cocurrent packed-bed biofilm reactor

Gas–liquid mass transfer was investigated in an up-flow cocurrent packed-bed biofilm reactor. In aerobic processes gas–liquid mass transfer can be considered as a key operational parameter as well as in reactor scale-up. The present paper investigates the influence of the liquid phase mixing in the determination of the volumetric gas–liquid mass transfer coefficient (k_La) coefficient. Residence time distribution (RTD) experiments were performed in the reactor to determine the flow pattern of the liquid phase and to model mathematically the liquid phase mixing. The mathematical model derived from RTD experiments was used to evaluate the influence of the liquid mixing on the experimental estimation of the (k_La) in this reactor type. The methods used to estimate the k_La coefficient were: (i) dynamic gassing-out, (ii) sulphite method, and (iii) in-process estimation through biological conversion obtained in the reactor. The use of standard chemical engineering correlations to determine the k_La in this type of bioreactors is assessed. Experimental and modelling results show how relevant can be to take into consideration the liquid phase mixing in the calculations of the most-used methods for the estimation of k_La coefficient. k_La coefficient was found to be strongly heterogeneous along the reactor vertical axis. The value of the k_La coefficient for the packed-bed section ranged 0.01–0.12 s⁻¹. A preliminary correlation was established for up-flow cocurrent packed-bed biofilm reactors as a function of gas superficial velocity.     

Comparative studies on immobilized laccase behaviour in packed-bed and batch reactors

Extracellular laccase produced by the wood-rotting fungus Cerrena unicolor was immobilized covalently via glutaraldehyde to cellulose-based carrier Granocel. Laccase was partially purified by membrane concentration and diafiltration followed by precipitation with acetone. Five-fold increase in the measured activity of immobilized enzyme was obtained when six times purer laccase was used for immobilization. For the best preparation, with very high activity of 2053 U per 1 mL of the carrier, thermal- and pH-stability, and activity profiles were determined. Experiments carried out in a batch reactor showed that k_cat/K_m for immobilized enzyme (0.65) is three times lower than the value obtained for the native laccase (2.19) whereas k_cat/K_m estimated from continuous reactor (1.50) is notably closer to that for the native enzyme. Continuous process probably reflects more precisely kinetics of the reaction accompanied by simultaneous product precipitation on the carrier’s surface. Operational stability of immobilized laccase was tested in continuous mode operation with ABTS, guaiacol and trichlorophenol as substrates and showed that packed-bed reactor is unprofitable system for laccase immobilized on Granocel carrier due to the high bed compaction. However, excellent stability of the preparation was noted under 20 successive runs in the well mixed tank reactor and better ability towards trichlorophenol biotransformation was observed in the case of immobilized laccase.     

Simulation of glucose isomerase reactor: optimum operating temperature

A design equation for immobilized glucose isomerase (IGI) packed bed reactor is developed assuming enzyme deactivation and substrate protection. The developed equation is used to simulate the performance of the reactor at various temperatures (50–80 °C). Enzyme deactivation is significant at high temperature. Substrate protection showed to have significant effect in reducing enzyme deactivation and increasing the enzyme half-life. Factors affecting the optimum operating temperature are discussed. The optimum operating temperature is greatly influenced by the operating period and to a lesser extent with both initial glucose concentration and glucose conversion.Two modes of reactor operation are tested i.e., constant feed flow rate and constant conversion. Reactor operating at constant conversion is more productive than reactor operating at constant flow rate if the working temperature is higher than the optimum temperature. Although at lower temperatures than the optimum, the two modes of operation give the same result.List of Symbols a residual enzyme activity - E [mg/l] concentration of active enzyme - E _a [kJ/mole] activation energy - E ₀ [mg/l] initial concentration of active enzyme - k [Specific] kinetic parameter - k _d [h^–1] first order thermal deactivation rate constant - k _e equilibrium constant - k _m [mole/l] apparent Michaelis constant - k _p [mole/l] Michaelis constant for product - k _s [mole/l] Michaelis constant for substrate - k ₀ [Specific] pre-exponential factor - Q [1/h] volumetric flow rate - ¯Q [1/h] average volumetric flow rate - R [kJ/mol·k] ideal gas constant - s [mole/l] apparent substrate concentration - s [mole/l] substrate concentration - s _e [mole/l] substrate concentration at equilibrium - s ₀ [mole/l] substrate concentration at reactor inlet - p [mole/l] product concentration - p _e [mole/l] product concentration at equilibrium - P _r [mole fructose/l·h] reactor productivity - T [k] temperature - t [h] time - t _p [h] operating time - V [l] reactor volume - v [mole/l·h] reaction rate - v [mole/l] reaction rate under enzyme deactivation and substrate protection - v _m [mole/l·h] maximum apparent reaction rate - v _p [mole/l·h] maximum reaction rate for product - v _s [mole/l·h] maximum reaction rate for substrate - x substrate fractional conversion - x _e substrate fractional conversion at equilibrium Greek Symbols effectiveness factor - mean effectiveness factor - substrate protection factor - [h] residence time - [h] average residence time - ₀ [h] initial residence time     

kLa of stirred tank bioreactors revisited

By means of improved feedback control k_La measurements become possible at a precision and reproducibility that now allow a closer look at the influences of power input and aeration rate on the oxygen mass transfer. These measurements are performed online during running fermentations without a notable impact on the biochemical conversion processes. A closer inspection of the mass transfer during cultivations showed that at least the number of impellers influences mass transfer and mixing: On the laboratory scale, two hollow blade impellers clearly showed a larger k_La than the usually employed three impeller versions when operated at the same agitation power and aeration rate. Hollow blade impellers are preferable under most operational conditions because of their perfect gas handling capacity. Mixing time studies showed that these two impeller systems are also preferable with respect to mixing. Furthermore the widths of the baffle bars depict a significant influence on the k_La. All this clearly supports the fact that it is not only the integral power density that finally determines k_La.     

Effect of time delay in specific growth rate on the periodic operation of bioreactors with input multiplicities

The effect of time delay in specific growth rate () on the periodic operation of bioreactors with input multiplicities is theoretically analyzed for productivity improvement. A periodic rectangular pulse is applied either in feed substrate concentration (S_f) or in dilution rate (D). Periodic operation under feed substrate concentration cycling gives improvement in productivity at lower value of ¯S_f of the two steady-state multiplicities of S_f only when the time delay in is larger. Whereas the larger value of ¯S_f gives improvement in average productivity for all values of time delay. Dilution rate (D) cycling gives an improvement in average productivity particularly for larger time delay in . This improvement in average productivity is obtained only at smaller value of dilution rate out of the two steady-state input multiplicities of D.List of Symbols D 1/h dilution rate - F memory function - g dummy variable - K_i g/l substrate inhibition constant - K_m g/l substrate saturation constant - P g/l product concentration - P_m g/l product saturation constant - Q g/(hl) product cell produced per unit time - S g/l substrate concentration - S_f g/l feed substrate concentration - S_f,p g/l feed substrate concentration during fraction of a period - X g/l biomass concentration - Y_X/S g/g cell mass yield - w variable either S or Z - Z g/l weighted average of substrate concentration Greek Letters 1/h time delay parameter - ₁ , ₂ product yield parameters, g/g and 1/h - pulse width expressed as a fraction of a period - 1/h specific growth rate - _m 1/h maximum specific growth rate - h period of oscillation - – average value     

Studies on microbial glucose isomerase: 4. Characteristics of immobilized whole-cell glucose isomerase from Streptomyces spp.

Whole-cell glucose isomerase from a Streptomyces spp. was immobilized by entrapment in gelatin matrices crosslinked with glutaraldehyde. The resultant immobilized enzyme preparation had up to 40% recovery yield of the activity and showed relatively long stabilities during storage and the isomerizing reaction. The storage half-life of the preparation was 19 months at 5°C and the half-life of the enzyme during operation was 260 days in the presence of 1 mM Co²⁺ and 80 days in the absence of the metal ion. Optimum pH and temperature were 7.5 and 70–75°C, respectively. The K_m values for glucose and fructose were 0.29 and 0.46 m, respectively, with a maximum theoretical conversion yield of 56%. The simulation results based on the reversible one-substrate enzyme kinetic model agreed well with the experimental data obtained from a batch reactor. The continuous operation of packed bed reactors demonstrated that some effects of the external film diffusion resistance were apparent at low flow rates of the substrate feed solution, whereas the internal pore diffusion resistance was negligible up to the pellet size used in this work.     

Influence of dissolved oxygen on the nitrification kinetics in a circulating bed biofilm reactor

The influence of dissolved oxygen concentration on the nitrification kinetics was studied in the circulating bed reactor (CBR). The study was partly performed at laboratory scale with synthetic water, and partly at pilot scale with secondary effluent as feed water. The nitrification kinetics of the laboratory CBR as a function of the oxygen concentration can be described according to the half order and zero order rate equations of the diffusion-reaction model applied to porous catalysts. When oxygen was the rate limiting substrate, the nitrification rate was close to a half order function of the oxygen concentration. The average oxygen diffusion coefficient estimated by fitting the diffusion-reaction model to the experimental results was around 66% of the respective value in water. The experimental results showed that either the ammonia or the oxygen concentration could be limiting for the nitrification kinetics. The latter occurred for an oxygen to ammonia concentration ratio below 1.5–2 gO₂/gN-NH₄ ⁺ for both laboratory and pilot scale reactors. The volumetric oxygen mass transfer coefficient (k _L a) determined in the laboratory scale reactor was 0.017?s^?1 for a superficial air velocity of 0.02?m s^?1, and the one determined in the pilot scale reactor was 0.040?s^?1 for a superficial air velocity of 0.031?m?s^?1. The k _L a for the pilot scale reactor did not change significantly after biofilm development, compared to the value measured without biofilm.     

Conversion of cellobiose to glucose using immobilized β-glucosidase reactors

Cellobiose is an intermediate in the enzymatic hydrolysis of cellulose to glucose and acts as an inhibitor for the cellulase enzymes. The conversion of cellobiose to glucose was studied with β-glucosidase adsorbed on Amberlite DP-1, a cation-exchange resin. The best overall pH for adsorption and reactor operation was near 5.0. The K_m values increased with increasing enzyme loading due to competitive inhibition. The maximum practical enzyme loading was about 28 units/g resin. The immobilized enzyme was operated continously in both packed bed and fluidized bed reactors, giving half-lives between 200 and 375 h.     

The nitrite reductase activity of horse heart carboxymethylated-cytochrome <Emphasis Type="Italic">c</Emphasis> is modulated by cardiolipin

Horse heart carboxymethylated cytc (CM-cytc) displays myoglobin-like properties. Here, the effect of cardiolipin (CL) liposomes on the nitrite reductase activity of ferrous CM-cytc [CM-cytc-Fe(II)], in the presence of sodium dithionite, is reported between pH 5.5 and 7.6, at 20.0 °C. Cytc-Fe(II) displays a very low value of the apparent second-order rate constant for the NO₂ ^?-mediated conversion of cytc-Fe(II) to cytc-Fe(II)-NO [k _on = (7.3 ± 0.7) × 10^?2 M^?1 s^?1; at pH 7.4], whereas the value of k _on for NO₂ ^? reduction by CM-cytc-Fe(II) is 1.1 ± 0.2 M^?1 s^?1 (at pH 7.4). CL facilitates the NO₂ ^?-mediated nitrosylation of CM-cytc-Fe(II) in a dose-dependent manner, the value of k _on for the NO₂ ^?-mediated conversion of CL–CM-cytc-Fe(II) to CL–CM-cytc-Fe(II)-NO (5.6 ± 0.6 M^?1 s^?1; at pH 7.4) being slightly higher than that for the NO₂ ^?-mediated conversion of CL–cytc-Fe(II) to CL–cytc-Fe(II)-NO (2.6 ± 0.3 M^?1 s^?1; at pH 7.4). The apparent affinity of CL for CM-cytc-Fe(II) is essentially pH independent, the average value of B being (1.3 ± 0.3) × 10^?6 M. In the absence and presence of CL liposomes, the nitrite reductase activity of CM-cytc-Fe(II) increases linearly on lowering pH and the values of the slope of the linear fittings of Log k _on versus pH are ?1.05 ± 0.07 and ?1.03 ± 0.03, respectively, reflecting the involvement of one proton for the formation of the transient ferric form, NO, and OH^?. These results indicate that Met80 carboxymethylation and CL binding cooperate in the stabilization of the highly reactive heme-Fe atom of CL–CM-cytc.     

The effect of molybdate and tungstate ions on the metabolic rates and enzyme activities in methanol-grown Methylobacterium sp. RXM

Feed-switching experiments were carried out in steady-state methanol-excess chemostat Methylobacterium sp. RXM cultures at a fixed dilution rate, temperature and pH (0.10 h^–1, 30° C and 6.95, respectively). The removal of molybdate from the nutrient supply led to a metabolic energy deficiency reflected in the molar growth yield and biomass values. High carbon conversion efficiency was linked with high formate dehydrogenase (FDH) activity and observed only when either molybdate or tungstate was added to the feed medium. A constant coenzyme ratio NAD⁺/K-ferri-cyanide linked to FDH activity was found during the enzyme stimulation period following the feed-switching experiment with tungstate addition, which suggests that both activities belong to the same enzyme. Quantitative metabolic responses (carbon conversion efficiency, methanol and O₂ consumption rates, CO₂ production rate and respiratory quotient) were measured in between steady-states just after the shift in the nutrient supply composition. Correspondence to: F. M. Gírio     

Optimization of operating temperature for continuous glucose isomerase reactor system

The Optimal temperature control policy for an immobilized glucose isomerase reactor system was studied. This optimization study takes into consideration the enzyme deactivation during the continuous reactor operation. The Kinetic parameters including reduced Michaelis–Menten constant (K?_m), reduced maximum reaction rate (V?_m), equilibrium constant (K_e), and enzyme deactivation constant (k_d) and their functional relationships to temperature were determined experimentally. The optimization problem was formulated in terms of maximization of fructose productivity as the objective function. The optimization problem was solved by making use of a maximum principle and the control vector iteration method. Approximately optimal temperature control policy was employed as compared with the reactor operation at an optimum constant temperature.     

A fedbatch strategy for optimal red pigment production by monascus ruber

According to the measurement of the pigment production and some material balance treatments, the monosodium glutamate (MSG), which represents a main substrate involved in the production of red pigment by Monascus ruber, is recovered on-line. Fedbatch operation then represents an alternative for increasing the production of pigment. A nonlinear quotient control scheme is expressed to regulate the monosodium glutamate substrate at an optimal value determined from batch studies.List of Symbols A absorbancy units (AU) - L lightness parameter - Pig red pigment quantity (Gmol) - vol fermentor active volume (1) - empirical coefficient - MW _pig red pigment molecular weight (g) - E elementary matrix - E ^# pseudo-inverse elementary matrix - r conversion rates vector (g· l^–1·h^–1) - E _m measured part of the elementary matrix - r _m measured conversion rates vector - E _c non-measured part of the elementary matrix - r _c non-measured conversion rates vector - v fictitious controller input - h fictitious controller output - u controller input - y controller output - y controller setpoint - k ₁ controller parameter - k ₂ controller parameter - k time iteration - MSG monosodium glutamate concentration (g·l^–1) - MSG _init monosodium glutamate initial quantity (g) - MSG _added total quantity of monosodium glutamate added (g) - MSG _cons total quantity of monosodium glutamate consumed (g) - MW _msg monosodium glutamate molecular weight (g)     

Kinetic Modeling of Acetophenone Reduction Catalyzed by Alcohol Dehydrogenase from <Emphasis Type="Italic">Thermoanaerobacter</Emphasis> sp.

NADPH-dependent alcohol dehydrogenase (ADH) from Thermoanaerobacter sp. was kinetically characterized using reduction of acetophenone as a model. To achieve 98% conversion of acetophenone, cofactor regeneration by oxidation of 2-propanol with the same enzyme was used. The enzyme was stable in the batch reactor. It was enantioselective towards (S)-1-phenylethanol (ee>99.5%). Due to its high deactivation in continuously operated stirred tank reactor (k_d=0.0141 min⁻¹) there was no way to keep high conversion of acetophenone at 98%. The deactivation occurred in the repetitive batch as well. A mathematical model for the acetophenone reduction with cofactor regeneration describing the behaviour in a batch, repetitive-batch and continuously stirred tank reactor was developed.     

Electron heat transport through the plasma-electrode boundary in weakly ionized plasma

The average electron thermal energies in the emission flux from the electrode into the plasma, ? ₁, and from the plasma toward the electrode, ? ₂, are determined for the cases of large and small values of the coefficient of kinetic reflection. It is shown that these energies vary within the ranges 0.5k _B T _c < ? ₁ < 2k _B T _c and 0.5k _B T _e < ? ₂ < 2k _B T _e , where T _c and T _e are the temperatures of the cathode and plasma electrons, respectively. The obtained values can be used to formulate the boundary conditions for the hydrodynamic equations at the electrode or a dielectric wall.     

Determination of protein complex stoichiometry through multisignal sedimentation velocity experiments

Determination of the stoichiometry of macromolecular assemblies is fundamental to an understanding of how they function. Many different biophysical methodologies may be used to determine stoichiometry. In the past, both sedimentation equilibrium and sedimentation velocity analytical ultracentrifugation have been employed to determine component stoichiometries. Recently, a method of globally analyzing multisignal sedimentation velocity data was introduced by Schuck and coworkers. This global analysis removes some of the experimental inconveniences and inaccuracies that could occur in the previously used strategies. This method uses spectral differences between the macromolecular components to decompose the well-known c(s) distribution into component distributions c_k(s); that is, each component k has its own c_k(s) distribution. Integration of these distributions allows the calculation of the populations of each component in cosedimenting complexes, yielding their stoichiometry. In our laboratories, we have used this method extensively to determine the component stoichiometries of several protein-protein complexes involved in cytoskeletal remodeling, sugar metabolism, and host-pathogen interactions. The overall method is described in detail in this work, as are experimental examples and caveats.     

Optimization and modeling of lactose hydrolysis in a packed bed system using immobilized β-galactosidase from Aspergillus oryzae

This work studied the hydrolysis of lactose using β-galactosidase from Aspergillus oryzae immobilized with a combination of adsorption and glutaraldehyde cross-linking onto the ion exchange resin Duolite A568 as a carrier. A central composite design (CCD) was used to study the effects of lactose concentration and feed flow rate on the average hydrolysis reaction rate and lactose conversion in a fixed bed reactor operating continuously with an upflow at a temperature of 35 ± 1 °C. The optimal conditions for the average hydrolysis reaction rate and the lactose conversion included a lactose concentration of 50 g/L and a feed flow rate of 6 mL/min. The average reaction rate and conversion reached 2074 U and 65%, respectively. The immobilized enzyme activity was maintained during the 30 days of operation in a fixed bed reactor with a 0.3 mL/min feed flow rate of a 50 g/L lactose solution at room temperature. Feed flows ranging from 0.6 to 12 mL/min were used to determine the distribution of residence times and the kinetics of the fixed bed reactor. A non-ideal flow pattern with the formation of a bypass flow in the fixed bed reactor was identified. The conditions used for the kinetics study included a lactose solution concentration of 50 g/L at pH 4.5 and a temperature of 35 ± 1 °C. Kinetic models using a PFR and axial dispersion methods were used to describe the lactose hydrolysis in the fixed bed reactor, thus accounting for the competitive inhibition by galactose. To increase the lactose conversion, experiments were performed for two fixed bed reactors in series, operating in continuous duty with upflow, with the optimal conditions determined using the CCD for a fixed bed reactor. The total conversion for the two reactors in series was 82%.     

Reaction of cythchrome c with one-electron redox reagents. I. Reduction of ferricytochrome c by the hydrated electron produced by pulse radiolysis

Pulse radiolysis-kinetic spectrometry has been used to investigate the reaction of hydrated electrons with ferricytochrome c in dilute aqueous solution at pH 6.5–7.0. Time resolutions from 2·10^?7 to 1 s were employed. Transient spectra from 320 to 580 nm were characterized with a wavelength resolution of ±0.5 nm. 1 In neutral salt-free solution, k(ferricytochrome c+e^?_aq)=(6.0±0.9)·10¹⁰ M^?1·s^?1 and k(ferricytochrome c+H)=(1.2±0.2)·10¹⁰ M^?1·s^?1. The reaction of ferricytochrome c with hydrated electrons is sensitive to ionic strength; in 0.1 M NaClO₄, k(ferricytochrome c+e^?_aq)=(2.4±0.4)·10¹⁰ M^?1·s^?1. In contrast, k(ferricytochrome c+H) is insensitive to ionic strength. Time resolution of three spectral stages has been accomplished. The primary spectrum is the first observable spectrum detectable after irradiation and is formed in a second-order process. Its rate of formation is indisting-uishable from the rate of disappearance of the electron spectrum. The secondary spectrum is generated in a true first order intramolecular process, k(p→s)=(1.2±0.1)·10⁵ s^?1. The tertiary spectrum is also generated in a true first-order process, k(s→t)=(1.3±0.2)·10² s^?1. The specific rates of both transformations are independent of the wavelength of measurement. The tertiary spectrum, observable 50 ms after initial reaction and remaining unchanged thereafter for at least 1 s, shows that relaxed ferrocytochrome c is the only detectable product. This product is not autoxidizable, as expected for native reduced enzyme. It is more probable that the intramolecular changes responsible for the p→s and s→t spectral transformations involve the influence of conformational relaxation of ferrocytochrome c upon electronic energy states then that they are intramolecular transmission of reducing equivalents from primary sites of electron attachment.