Effects of external diffusion and design geometry on the performance of immobilized glucose isomerase reactor system

Using immobilized glucose isomerase, the effects of superficial velocity of the reaction solution flowing through a packed-bed reactor on the apparent kinetic constants of reversible reaction system were studied. The results showed that the apparent kinetic constants, both V_m″ and K_m″, of the forward reaction varied significantly as the superficial velocity is changed, whereas those of the reverse reaction varied only slightly. Using the kinetic data determined experimentally, computer simulation of the enzyme reactor performance was carried out, and the importance of the external mass transfer in the proximity of immobilized-enzyme particles was recognized. The reactor performance, expressed in terms of productivity, was examined as a function of the reactor height-to-diameter ratio, H/D. The productivity of the reactor system goes through a maximum value at a H/D ratio of about 1.6. and decreases as the H/D ratio increases. Theoretical analysis of the reaction kinetics of immobilized-enzyme system that has reversible reaction kinetics is also presented. The experimental results showed good agreement with the results found from the theoretical analysis and the computer simulation studies. Based on the principles of the methods and the results presented in this paper, it is anticipated that one can predict the optimal design and operating conditions for the glucose isomerase reactor system and that application of the results could be extended to other enzyme systems with reversible reaction kinetics.     

Kinetic modeling of a multiple immobilized enzyme system. I. Development and testing of the model

A kinetic model for the reaction sequence catalyzed by coimmobilized invertase and glucose oxidase with a sucrose substrate in a tubular reactor has been developed. The computerized mathematical model employs and orthogonal collection technique for solving oxidase were coimmobilized in poly(2-hydroxyethlmethacrylate) gels and used in a continuous flow packed-bed tubular reactor system. In addition to describing the development of the kinetic model, this article compares experimentally determined reactor effluent concentrations for various sucrose feed solutions to those predicted by the model. Variations between experimental and predicted reactor effluent concentrations were found to be on the micromolar level for sucrose feed concentrations as low as 1.38mM.     

Wastewater nitrification kinetics using reciprocating jet bioreactor

Kinetic investigations on growth parameters of nitrifying and COD oxidizing bacteria were carried out with recourse to a three stage reciprocating jet bioreactor system using real life wastewater. The system employed in this investigation essentially consisted of separate aerobic oxidation stage along with nitrification stage and anaerobic denitrification stage with facility for biomass recirculation whenever necessary. Steady-state COD oxidation reactor performance was assessed for various values of residence time. Yield coefficient and decay coefficient of COD oxidizing biomass were obtained as 0.3329 kg BM/kg COD and 0.0032 (1/h) respectively.It was observed that COD oxidizing bacteria co-existed with nitrifying bacteria during nitrification process due to the nature of wastewater used. Steady-state nitrification reactor performance was also assessed for various residence time values. Exact concentration of nitrifying and COD oxidizing biomass in the nitrification reactor was then estimated with the help of kinetic growth parameters of COD oxidizing biomass and extent of COD oxidation achieved in nitrification reactor. This further enabled evaluation of corrected kinetic growth parameters estimated as 0.4272 kg BM/kg NH ₄ ⁺ -N and 0.00626 (1/h) for nitrifier biomass yield coefficient and decay coefficient respectively.     

Application of the enzyme thermistor to the direct estimation of intrinsic kinetics using the saccharose-immobilized invertase system.

The possibility of using the enzyme thermistor (ET) for the direct determination of kinetic parameters (Km, Ki, Vm) of immobilized enzyme (IME) was evaluated using different preparations of invertase conjugated to bead celluloses. Two different ET columns packed with IME were operated in the mode of a differential enzyme reactor (short length, low substrate conversion). Kinetic parameters of the above IME reactor were computed by a nonlinear curve-fitting procedure. The obtained kinetic parameters were superverified by means of an independent differential reactor (DR) system. This system utilized an indirect postcolumn analytical method based on determination of glucose concentration in the stirred reservoir. Best agreement between the data acquired by direct (ET) and indirect (DR) methods was obtained if the ET column was operated at flow rates within the range of 1.0-1.5 ml min-1 using invertase-cellulose chlorotriazine conjugate. Influence of heat loss and flow nonideality is discussed. The proposed ET method offers a rapid, convenient, and general approach to determination of kinetic constants of IME preparations by omitting postcolumn analytical methods.     

Kinetics of nitrification using a fluidized sand bed reactor with attached growth

The oxidation of ammonium ion to nitrite and nitrate ion (nitrification) has been studied in a laboratory scale fluidized sand bed reactor with attached microbial growth. The undefined population of Nitrobacteracea organisms were immobilized on the sand particles by natural attachment after 2–3 months of adaptation. General balance equations have been formulated for a recycle reactor and oxygenation tank system. Kinetic experiments in the reactor and in a microrespirometer have been analyzed in terms of double Michaelis–Menten rate expression for the nitrogenous reactants and dissolved oxygen. Dynamic simulation of the batch integral reactor system was used to establish the error in the kinetic constant which arose due to assuming differential behavior. Design guidelines have been developed for the oxygen requirements in terms of oxygen transfer coefficients, oxygen enrichment, and liquid recycle rate.     

Determination of kinetic constants for a two-stage anaerobic upflow packed-bed reactor for dairy wastewater

A two-stage upflow packed-bed (reactors in series) system was used for the treatment of dairy wastewater. Nylon pads were used as supporting media for the biomass. This investigation aimed at the determination of various kinetic constants for substrate, biomass and biogas based on various models. The maximum loadings that could be applied to reactor I and reactor II were 14·29 and 5·0 kg of chemical oxygen demand (COD) per m³ per day, respectively. The maximum COD removal efficiencies at various loading rates were in the ranges of 93·8–98·5% and 72·5–84% for the two reactor systems, respectively. The combined biogas yield was between 0·196 and 0·386 m³ gas/kg COD_a.     

Effect of wall growth on the kinetic modeling of nitrite oxidation in a CSTR

A simple kinetic model was developed for describing nitrite oxidation by autotrophic aerobic nitrifiers in a continuous stirred tank reactor (CSTR), in which mixed (suspended and attached) growth conditions prevail. The CSTR system was operated under conditions of constant nitrite feed concentration and varying volumetric flow rates. Experimental data from steady-state conditions in the CSTR system and from batch experiments were used for the determination of the model's kinetic parameters. Model predictions were verified against experimental data obtained under transient operating conditions, when volumetric flow rate and nitrite feed concentration disturbances were imposed on the CSTR. The presented kinetic modeling procedure is quite simple and general and therefore can also be applied to other mixed growth biological systems.     

Glucoamylase and glucose oxidase preparations and their combined application for conversion of maltose to gluconic acid

The kinetic behavior of a system of multiple enzyme in solution has been studied in a variable volume batch reactor at pH 5, controlled dissolved oxygen concentration, and T = 30°C. The enzymes used were glucoamylase (R. delemar), glucose oxidase (A. niger), and gluconolactonase (A. niger), all of which are important commercial biocatalysts, and a disaccharide was employed as the starting substrate. This study includes the basic kinetic properties of individual enzymes and interactions between components of the reaction mixture. Classical Michaelis–Menten single substrate or two substrate kinetic with parameters based on initial rate data predict correctly the batch time course of the sequential reaction network.     

Noninvasive tool for optical online monitoring of individual biomass concentrations in a defined coculture

Cocultures bear great potential in the conversion of complex substrates and process intensification, as well as, in the formation of unique components only available due to inter-species interactions. Dynamic data of coculture composition is necessary for understanding and optimizing coculture systems. However, most standard online determined parameters measure the sum of all species in the reactor system. The kinetic behavior of the individual species remains unknown. Up to now, different offline methods are available to determine the culture composition, as well as the online measurement of fluorescence of genetically modified organisms. To avoid any genetic modification, a noninvasive online monitoring tool based on the scattered light spectrum was developed for microtiter plate cultivations. To demonstrate the potential, a coculture consisting of the bacterium Lactococcus lactis and the yeast Kluyveromyces marxianus was cultivated. Via partial least squares regression of scattered light spectra, the online determination of the individual biomass concentrations without further sampling and analyses is possible. The results were successfully validated by a Coulter counter-analysis, taking advantage of the different cell sizes of both organisms. The findings prove the applicability of the new method to follow in detail the dynamics of a coculture.     

Evaluation of droplet-based microfluidic platforms as a convenient tool for lipases and esterases assays

Abstract

The accurate estimation of kinetic parameters is of fundamental importance for biochemical studies for research and industry. In this paper, we demonstrate the application of a modular microfluidic system for execution of enzyme assays that allow determining the kinetic parameters of the enzymatic reactions such as V_max – the maximum rate of reaction and K_M – the Michaelis constant. For experiments, the fluorogenic carbonate as a probe for a rapid determination of the kinetic parameters of hydrolases, such as lipases and esterases, was used. The microfluidic system together with the method described yields the kinetic constants calculated from the concentration of enzymatic product changes via a Michaelis–Menten model using the Lambert function W(x). This modular microfluidic system was validated on three selected enzymes (hydrolases).     

Continuous enzymatic transformation in an enzyme membrane reactor with simultaneous NAD(H) regeneration

Multienzyme reaction systems with simultaneous coenzyme regeneration have been investigated in a continuously operated membrane reactor at bench scale. NAD(H) covalently bound to polyethylene glycol with a molecular weight of 10⁴ [PEG-10,000-NAD(H)] was used as coenzyme. It could be retained in the membrane reactor together with the enzymes. L -leucine dehydrogenase (LEUDH) was used as catalyze for the reductive amination of α-ketoisocaproate (2-oxo-4-methylpentanoic acid) to L -leucine. Format dehydrogenease (FDH) was used for the regeneration of NADH. Kinetic experiments were carried out to obtain data which could be used in a kinetic model in order to predict the performance of an enzyme membrane reactor for the continuous production of L -leucine. The kinetic constants V_max and K_m of enzymes are all in the same range regardless of whether native NAD(H) or PEG-10,000-NAD(H) is used as coenzyme. L -leucine was produced continuously out of α-ketoisocaproate for 48 days; a maximal conversion of 99.7% was reached. The space-time yield was 324 mmol/L day (or 42.5 g/L day).     

Acetate conversion in anaerobic biogas reactors: Traditional and molecular tools for studying this important group of anaerobic microorganisms

Different methods were applied to study the role of aceticlastic methanogens in biogas reactors treating solid waste and wastewater. We used traditional microbiological methods, immunological and 16S rRNA ribosomal probesfor detection of the methanogens. Using this approach we identified themethanogenic spp. and their activity. In biofilm system, such as the UASBreactors the presence of the two aceticlastic methanogens could be correlatedto the difference in the kinetic properties of the two species. In biogas reactor treating solid wastes, such as manure or mixture of manure and organic industrial waste, only Methanosarcina spp. were identified. Methanosarcina spp. isolated from different plants had different kinetics depending on their origin. Relating the reactor performance data to measurement of the activity by conventional microbiological methods gave a good indication of the microbial status of specific trophic groups. 16S rRNA probing confirmed these observation and gave a more detailed picture of the microbial groups present.     

Fast determination of operational stability of the soluble acetylacetone-cleaving enzyme Dke1 in an enzyme membrane reactor

The main aim of this study was the determination of the operational stability of soluble Dke1 (EC 1.13.11.50) in an enzyme membrane reactor. In order to calculate the half-life of soluble Dke1, the K _M of oxygen must be known. The determination of this constant was done using progress curve analysis (K _M=260 μmol l⁻¹). In a next step, the reactor system was studied by building a mathematical model for calculation of the reactor system, using Berkeley Madonna ver. 8.0.1 software. After that, the determination of the half-life of Dke1 under operational conditions at different temperatures (5, 10, 15, 25, 30, 35°C) was performed. The quantitative criterion for stability was the value of the first-order rate constant of monomolecular inactivation. The experiments showed that soluble Dke1 is poorly stable. The half-life ranged from 308 min at 5°C to 9 min at 35°C. This method for determining the half-life is quite applicable for enzymes which are poorly stable. In addition, both the storage stability and the operational stability can be determined.     

Uptake of lactose and continuous lactic acid fermentation by entrapped non-growing Lactobacillus helveticus in whey permeate

 Continuous production of lactic acid from lactose has been carried out in a stirred-tank reactor with non-growing Lactobacillus helveticus entrapped in calcium alginate beads. A considerably longer operation half-life was obtained in a continuously operated reactor than in a batch-operated reactor. It is possible to simulate the action of entrapped non-growing cells on the basis of information from diffusion and kinetic experiments with suspended free cells. The simulation fit the experimental data over a broad range of substrate concentrations if the specific lactic acid production rate, q _P, was used as a variable parameter in the model. The dynamic mathematical model used is divided into three parts: the reactor model, which describes the mass balance in a continuously operated stirred-tank reactor with immobilized biomass, the mass-transfer model including both external diffusion and internal mass transfer, and the kinetic model for uptake of substrate on the basis of a Michaelis-Menten-type mechanism. From kinetic data obtained for free biomass experiments it was found, with the use of non-linear parameter estimation techniques, that the conversion rate of lactose by L. helveticus followed a Michaelis-Menten-type mechanism with K _S at half-saturation=0.22±0.01 g/l. The maximum specific lactose uptake rate for growing cells, q _S,max, varied between 4.32±0.02 g lactose g cells^-1 h^-1 and 4.89 ±0.02 g lactose g cells^-1 h^-1. The initial specific lactose uptake rate for non-growing cells, q _S,0, was found to be approximately 40% of the maximum specific lactose uptake rate for growing cells. Received: 4 October 1995/Received last revision: 23 April 1996/Accepted: 29 April 1996     

Estimation of the fraction of biologically active methyl <Emphasis Type="Italic">tert</Emphasis>-butyl ether degraders in a heterogeneous biomass sample

The fraction of biologically active methyl tert-butyl ether degraders in reactors is just as important for prediction of removal rates as knowledge of the kinetic parameters. The fraction of biologically active methyl tert-butyl ether degraders in a heterogeneous biomass sample, taken from a packed bed reactor, was determined using a batch kinetic based approach. The procedure involved modeling of methyl tert-butyl ether removal rates from batch experiments followed by parameter estimations. It was estimated to be 5–14% (w/w) of the measured volatile suspended solids concentration in the reactor.     

On-line enzyme activity determination using the stopped-flow technique: application to laccase activity in pulp mill waste-water treatment

An automated system for on-line measurement of enzyme activity is proposed. The system uses a flow injection manifold in the stopped-flow mode to measure initial reaction rates. The time during which the flow is halted is selected in such a way as to optimise the enzyme/substrate ratio for the correct determination of activity values. The proposed system was used to determine the activity of laccase produced by the fungus Trametes versicolor immobilised on nylon in a fixed-bed reactor used for treating pulp mill waste water. Received: 17 February 1997 / Received revision: 23 April 1997 / Accepted: 27 April 1997     

Performance of the continuous glucose isomerase reactor system for the production of fructose syrup

Glucose isomerase in the form of heat-treated whole-cell enzyme prepared from Streptomyces phaeochromogenus follows the reversible single-substrate reaction kinetics in isomerization of glucose to fructose. Based on the Kinetic constants determined and the mathematical model of the reactor system developed, the preformance of a plug-flow-type continuous-enzyme reactor system was studied experimentally and also simulated with the aid of a computer for the ultimate objective of optimization of the glucose isomerase reactor system. The enzyme decay function for both the enzyme storage and during the use in the continuous reactor, was found to follow the first-order decay kinetics. When the enzyme decay function is taken into consideration, the ideal homogeneous enzyme reactor kinetics provided a satisfactory working model without further complicatin of the mathematical model, and the results of computer simulation were found to be in good agreement with the experimental results. Under a given set of constraints the performance of the continuous glucose isomerase reactor system can be predicted by using the computer simulation method described in this paper. The important parameters studied for the optimization of reactor operation were enzyme loading, mean space time of the reactor, substrate feed concentration, enzyme decay constants, and the fractional conversion, in addition to the kinetic constants. All these parameters have significant effect on the productivity. Some unique properties of the glucose isomerization reaction and its effects on the performance of the continuous glucose isomerase reactor system have been studied and discussed. The reaction kinetics of glucose isomerase and the effects of both the enzyme loading and the changes in reaction rate within a continuous reactor on the productivity are all found to be of particular importance to this enzyme reactor system.     

Electron transfer from cytochromeb 5 to cytochromec

The reaction of cytochromeb ₅ with cytochromec has become a very prominent system for investigating fundamental questions regarding interprotein electron transfer. One of the first computer modeling studies of electron transfer and protein/protein interaction was reported using this system. Subsequently, numerous studies focused on the experimental determination of the features which control protein/protein interactions. Kinetic measurements of the intracomplex electron transfer reaction have only appeared in the last 10 years. The current review will provide a summary of the kinetic measurements and a critical assessment of the interpretation of these experiments.     

Pilot-scale culture ofCoffea arabica in a novel loop fluidised bed reactor

A novel bubble free loop fluidized bed reactor for plant cell cultures was developed and tested usingCoffea arabica as a model cell line. The effects of main operational parameters like morphology and size of inoculum, oxygen supply as well as recirculation of sparingly soluble gases on cell growth and alkaloid production rates in this reactor were studied and the results were compared with standard shake flask experiments. By on-line monitoring of biomass and oxygen uptake rates the main kinetic parameters for cell growth and alkaloid production were evaluated. It was demonstrated that the novel reactor is easy to run and is particularly adequate for measuring kinetic parameters necessary for scale up.     

Potential of Thiobacillus ferrooxidans for waste gas purification. Part 2. Increase in continuous ferrous iron oxidation kinetics using immobilized cells

Thiobacillus ferrooxidans could be used to regenerate ferrous sulphate solution produced in a process to remove H₂S from waste gas if the reaction rate could be increased. The aim of the present study was to increase the volumetric productivity by using immobilized cells. Kinetic data of ferrous iron oxidation were determined in fixed-bed and fluidized-bed reactor configurations with different support materials in order to find the most practical system for scale-up. By using a fixed-bed reactor the iron oxidation rate can be increased to 3.6 g l^–1 h^–1, fivefold higher than suspended cells, and results in a bioreactor of reasonable size. With the kinetic data obtained, the biological reaction is no longer a limiting factor for industrial-scale application. Correspondence to: W. Schäfer-Treffenfeldt