Mass transfer effects on the reaction rate for heterogeneously distributed immobilized yeast cells

Here we examine the efficiency of different immobilized cell gradients applied to immobilized Saccharomyces cerevisiae fermenting glucose to ethanol. We developed a simulation model to fully study the competing effects of mass transfer hindrance and kinetics. It is based on a diffusion-reaction model and can be used to analyze the different cell concentration profiles inside an immobilized gel bead, in terms of effectiveness factors, productivity, and mass flux. The internal diffusion coefficient, which varies with the local cell concentration, as well as the external mass transfer, is taken into account when describing the efficiency. Although the diffusion hindrance is greater at higher cell concentrations, high cell concentration is still advantageous in the present case because the increase in reaction rate outweighs the diffusion hindrance. Thus, high cell concentrations contribute to increased productivity. The influence of the cell concentration gradient on the efficiency of the beads is negligible. Within the range of cell profiles studied it has been established that the location of the cells within the bead is of lesser importance. However, a steep cell gradient increases the importance of the external mass transfer.     

Ethanol production from whey permeate by immobilized yeast cells

The ability of two yeast strains to utilize the lactose in whey permeate has been studied. Kluyveromyces marxianus NCYC 179 completely utilized the lactose (9.8%), whereas Saccharomyces cerevisiae NCYC 240 displayed an inability to metabolize whey lactose for ethanol production. Of the two gel matrices tested for immobilizing K. marxianus NCYC 179 cells, sodium alginate at 2% (w/v) concentration proved to be the optimum gel for entrapping the yeast cells effectively. The data on optimization of physiological conditions of fermentation (temperature, pH, ethanol concentration and substrate concentration) showed similar effects on immobilized and free cell suspensions of K. marxianus NCYC 179, in batch fermentation. A maximum yield of 42.6 g ethanol l^?1 (82% of theoretical) was obtained from 98 g lactose l^?1 when fermentation was carried at pH 5.5 and 30°C using 120 g dry weight l^?1 cell load of yeast cells. These results suggest that whey lactose can be metabolized effectively for ethanol production using immobilized K. marxianus NCYC 179 cells.     

Mass Transfer Characteristics of Immobilized Cells Used in Fermentation Processes

ABSTRACT:?

There is great commercial interest in using immobilized cells for fermented beverage processes. The process advantages offered by immobilized cells are numerous, but an understanding of the mass transfer characteristics of a given system is needed in order to achieve efficient processes and high quality products. This is especially important in the food and beverage industry where fermentation products contribute to the flavor and aroma of the final product. The fundamental principles of mass transfer in immobilized cell systems are covered in this review. An overview of the current research efforts focused on external and internal mass transfer characteristics of immobilized cells used in fermentation processes is presented. Methods for measuring substrate diffusivities within immobilization matrices and areas requiring further research are discussed.     

Liquid-phase mass transfer in fixed-bed of polyurethane foam matrices containing immobilized anaerobic sludge

This paper reports on the results of liquid-phase mass transfer experiments carried-out in a bed of immobilized anaerobic sludge. The liquid superficial velocity (v_s) was found to deeply affect the liquid-phase volumetric mass transfer coefficient (k_sa) in the v_s range of 0.007 to 0.075 cm.s^–1. Moreover, k_sa increased exponentially with v_s in that range, due to the decrease of the external mass transfer resistance.     

Diffusion in gels containing immobilized cells: a critical review

Eleven experimental investigation of diffusion in gels containing immobilized cells are reviewed. The experimental data, which quantitatively express the diffusion coefficient as a function of the cell concentration, are compared with a number of well-known equations developed for mass transfer in heterogeneous media. Based on this comparison, a procedure for the theoretical prediction of effective diffusion coefficients in cell-containing gels is recommended.     

Analysis of mass transfer for immobilized cells in an extractive lactic acid fermentation

The use of immobilization in extractive lactic acid fermentation by Lactobacillus delbrueckii is preferred. In this article, the mathematical simulations to examine the influences of substrate and product transport were performed to assess the overall performance. The simulations showed that transport of the substrate in k-carrageenan beads was not a rate limiting factor. However, the model observed significant buildup of inhibitory product in large beads. The model was validated through comparisons with the experimental results. Finally, the model was used to predict the performance of the extractive fermentation under different operating strategies.     

Mass transfer effects in solvent-free fat interesterification reactions: influences on catalyst design

The use of solvent-free systems in the oil and fats industry is commonplace. Initial studies on interesterification were carried out in solvent systems because the lipase was immobilized solely by adsorption onto particles of diatomaceous earth. In this study, the mass transfer characteristics associated with the continuous interesterification of olive oil in a solvent-free system have been examined, for lipase immobilized on the three ion-exchange materials: Duolite ES562, Duolite ES568, and Spheroil DEA. The process of immobilization is influenced by the internal structure of the material and this in turn influences the interesterification activity of the catalyst. Individually prepared catalysts for the three support materials have shown that external mass transfer limitations are unlikely even at low flowrates.In the case of Spherosil DEA, with a mean pore diameter of 1480 A, the wide pores would be expected to reduce internal mass transfer limitations; however, it is more likely that the reduction in activity with increased catalyst loading is due to the lipase molecules being immobilized in a tightly packed monolayer. In such a situation, some active sites of the lipase molecules would become inaccessible to substrate molecules leading to an observed reduction in activity. For Duolite ES568, the observed results are very similar to those seen for Spherosil DEA, however, the pore structure of this support material indicate that some internal mass transfer limitations may also be occurring. Yet the contribution of the individual effects cannot be determined. The results observed for the support Duolite ES562 are different than those observed for the other materials and reflect the heterogeneity of Duolite ES562. The large proportion of narrow pores in the support mean that, for the catalysts examined, immobilization is most likely to have occurred in the external pores of the particles, and as such no internal mass transfer limitation is observed.It is clear that for interesterification the material chosen for enzyme immobilization will have an important role in determining the catalyst efficiency. External mass transfer limitations are very minor and observed internal mass transfer limitations may be caused by both internal mass transfer and the manner in which the immobilization process occurs. (c) 1994 John Wiley & Sons, Inc.     

Importance of solute partitioning in biphasic oxidation of benzyl alcohol by free and immobilized whole cells of pichia pastoris

Using free and immobilized whole cells of Pichia pastoris, the biocatalytic oxidation of benzyl alcohol was investigated in different two-phase systems. This reaction was strongly influenced by both the substrate and product inhibitions, and the production rate of benzaldehyde in the aqueous system became maximum at the initial substrate concentration of ca. 29 g/L with the aldehyde formation less than 4 to 5 g/L even after a longer reaction period. The reaction rates in the two-liquid phase systems were predominantly determined by the partitioning behaviors of the substrate and product between the two phases rather than by enzyme deactivation by the organic solvents. In the two-liquid phase systems, consequently, the organic solvent acted as a reservior to reduce these inhibitory effects, and it was essential to select the organic solvent providing the optimal partitioning of the substrate into the aqueous phase as well as the preferential extraction of the product into the organic phase. The whole cells immobilized in a mixed matrix composed of silicone polymer [>50% (v/v)] and Ca alginate gel (<50%) worked well in the xylene and decane media, providing comparable activities with the free cells. The production rate of aldehyde was also influenced by the solute partitioning into the hydrophilic alginate phase where the cells existed. (c) 1994 John Wiley & Sons, Inc.     

Mass transfer and temperature effects on substrate utilization in brewery granules

Liquid film and diffusional resistances of brewery granules during acetate, propionate, and ethanol utilization were investigated. Substrate utilization rate increased with decreased granule size. Effectiveness factors for acetate, propionate, and ethanol were calculated by comparing the maximum rates of substrate utilization of whole granules (1.8 to 3.0 mm) and fine flocs (20 to 75 mum) derived by disrupting whole granules. For acetate, propionate, and ethanol, maximum specific substrate utilization rates (k(m') g/g VS . d) for the flocs, were 5.11, 6.25, and 5.49, respectively, and half-velocity coefficients (K(g') mM) were 0.45, 0.40, and 3.37, respectively. Calculated effectiveness factors were 0.32, 0.41, and 0.75 for acetate, propionate, and ethanol, respectively. The effect of temperature on substrate utilization was examined at 26 degrees C, 31 degrees C, and 37 degrees C using acetate as sole carbon source. Utilization rates increased with temperature. Flocs were most sensitive to temperature, and whole granules were least affected. The behavior of flocs was well described by the Van't Hoff-Arrhenius equation. Effectiveness factors for acetate utilization by the granules were 0.36, 0.35, and 0.32 at 26 degrees C, 31 degrees C, and 37 degrees C, respectively, indicating little effect of temperature. Based on these results, we conclude that both liquid film and diffusional resistances influenced the rate of substrate utilization in a UASB reactor with granular sludge. Temperature effects were much less important than diffusional limitations within the granules. (c) 1995 John Wiley & Sons, Inc.     

New application of single and mixed immobilized cells for furfural biodegradation

In this study, a new application of immobilized microbial cells for biodegradation of furfural in aqueous solution was investigated using spouted bed bioreactor. Pseudomonas sp., as a single type specie as well as activated sludge as mixed cultures were individually immobilized in 3 different bio-carrier matrices which were prepared by reinforcement of natural polysaccharides including sodium alginate, guar-gum and agar-agar with polyvinyl alcohol. The results demonstrated a complete removal (100%) of furfural from aqueous solutions using immobilized cells (IC) of Pseudomonas sp., and mixed cultures as well. Recycling of used IC for furfural removal in successive treatment cycles provided significant removal rates up to 96%. In general, results revealed that IC exhibited better performance compared to free cells in regard with the removal rate of furfural, duration of biodegradation process, as well as the ability for recycling and sustaining the high concentrations of furfural.     

Mass transfer studies on the reduction of Cr(VI) using calcium alginate immobilized Bacillus sp. in packed bed reactor

This study presents the external mass transfer effects on the reduction of hexavalent chromium (Cr(VI)) using calcium alginate immobilized Bacillus sp. in a re-circulated packed bed batch reactor (RPBR). The effect of flow rate on the reduction Cr(VI) was studied. Theoretically calculated rate constants for various flow rates were analyzed using external film diffusion models and compared with experimental values. The external mass transfer coefficients for the bioconversion of Cr(VI) were also investigated. The external mass transfer effect was correlated with a model of the type J_D = K Re⁻⁽¹⁻ⁿ⁾. The model was tested with various K values and the mass transfer correlation J_D = 5.7 Re^−0.70 was found to predict the experimental data accurately. The proposed model would be useful for the design of industrial reactor and scale up.     

Photoproduction of hydrogen, nitrogenase and hydrogenase activities of free and immobilized whole cells of Rhodobacter sphaeroides O.U. 001

Abstract Photoproduction of hydrogen, nitrogenase activity (acetylene reduction) and hydrogenase activity (methylene blue dye reduction) were studied in free and alginate immobilized whole cells of a purple non-sulfur photosynthetic bacterium Rhodobacter sphaeroides O.U. 001. Four-fold increase in hydrogen production, two-fold increase in nitrogenase activity and 1.2-fold increase in the hydrogenase activity were observed in immobilized cells compared to free cells. Effect of various inhibitors (CO and C₂H₂) and electron donor (H₂) on the above three functions by free and immobilized cells has also been studied.     

Mass transfer limitations in gel beads containing growing immobilized cells

Immobilized-cell aggregates have traditionally been approximated as effective continua within which the catalytic activity of the cells is homogeneously distributed. Chang & Park (1985), however, recently modelled the immobilized cells as discrete inclusions within a support matrix. With some modification, this theory is applicable to the analysis of microbial colonies growing within gel beads, and indicates that predictions obtained using the traditional approach may be significantly in error.     

Mass transfer limitations in solid-state digestion

The biodegradation of waste placed in layers was studied in 500-ml lysimeters, without leachate recycle. All four became methanogenic within 100 days but the steady-state biogas output only reached 0.09 l kg^–1 d^–1, whereas an earlier study on a mixed feedstock had yielded 1.8 l kg^–1 d^–1. A novel physical model of solid-state digestion is deduced, implying a crucial role for mass transfer processes, with successful operation only within a limited range of diffusion rates.     

Reaction and diffusion in a gel membrane reactor containing immobilized cells

To investigate the effect of diffusional limitations and heterogeneous cell distribution in a gel-immobilized cell system, a gel membrane reactor has been constructed. The reactor consists essentially of a gel layer with immobilized cells, flanked by two well-mixed chambers. Through one chamber substrate is pumped, and this chamber is the equivalent of the outside of a spherical gel bead. The second closed measuring chamber contains a small quantity of liquid that can equilibrate with the inside surface of the membrane, eventually after a long transient. Analysis of the liquid in this chamber can give direct information on substrate and product concentrations at the gel surface, and is and indication of the situation in the center of a gel bead. The gel membrane reactor appears to be an excellent tool to study diffusion and reaction in a gel-containing immobilized cells. A mathematical model with time- and position-dependent cell concentration and diffusion coefficient is described. Experimental data show the effective diffusion coefficient of glucose in an alginate gel to decrease with yeast cell concentration. Moreover, kinetic parameters could be determined, using the mathematical model. Microscopic analysis confirmed the proliferation of the gel-entrapped microorganisms in the outer layer of the matrix, as predicted by the model. Potentially, this type of reactor has a clear potential to study the physiology of gel-immobilized cells. (c) 1992 John Wiley & Sons, Inc.     

Integrated continuous winemaking process involving sequential alcoholic and malolactic fermentations with immobilized cells

An integrated winemaking process – including sequential alcoholic and malolactic fermentations operated continuously – was developed. For the continuous alcoholic fermentation, yeast cells (Saccharomyces cerevisiae) were immobilized either on grape stems or on grape skins, while bacterial cells (Oenococcus oeni) used for conducting continuous malolactic fermentation were immobilized on grape skins only. The produced wines were subjected to chemical analysis by HPLC (ethanol, glycerol, sugars and organic acids) and by gas chromatography (major and minor volatile compounds). The final proposed integrated continuous process permitted the production of 960 mL/d of a dry white wine, with an alcoholic strength of about 13 vol%, by using two 1.5 L tower bed reactors packed with 260 g of grape skins. The produced wines revealed a good physicochemical quality. Moreover, 67% of the malic acid concentration could be reduced in the second reactor. Both fermentative processes proved to be much more efficient than those conducted traditionally with free cells or even with immobilized cells, but in the batch mode of operation.     

Comparison of substrate utilization and growth kinetics between immobilized and suspended Pseudomonas cells

A methodology is described for measurement if immobilized and suspended cell growth and substrate utilization kinetics parameters. Substrate utilization and growth kinetics were compared between immobilized and suspended cells for toluene degrading Pseudomonas strains K3-2 and 2,4-dichlorophenoxyacetic acid (2,4-D) degrading strain DBO131(pR0101), respectively. Kinetic parameters were estimated using nonlinear parameter estimation methods and compared between the immobilized and suspended Pseudomonas cells to determine the effect of immobilization on cellular growth and substrate utilization. Factors influencing the experimental design included calculated oxygen flux rates, primary carbon substrate flux rates, and shear stresses on the immobilize cell. Statistical interpretation of the cellular reaction rate parameters indicates that only the growth kinetics of the toluene system were significantly altered upon immobilization. Substrate utilization kinetics remained unchanged upon immobilization. The substrate growth associated half-saturation constant (K(g)) for the toluene system increased by 30-fold and the maximum specific growth rate (mu(max)) decreased by 2-fold upon immobilization. Implication of these results for experimental determination of cellular kinetic parameters and for immobilization cell bioreactors design are discussed. (c) 1993 John Wiley & Sons, Inc.     

Continuous penicillin G hydrolysis in an electro-membrane reactor with immobilized penicillin G acylase

Penicillin G (2%, w/v in phosphate buffer, pH 8) was hydrolysed in a flow-through, miniature electro-membrane reactor with the penicillin G acylase immobilized in 5% (w/v) polyacrylamide (diam. 10 mm, thickness 2.6 mm, enzyme activity 24 U ml^–1). The conversion of penicillin G increased from 0.15 to almost 0.5 when the electric current applied to the reactor was changed from –600 to +600 A/m² with a substrate residency of 1 h. Symbols and abbreviations c _j ^p & concentration of component j in product stream (M) c _j ^s & concentration of component j in substrate stream (M) c _s ^o & substrate concentration at reactor inlet (M) C _j ^p=c _j ^p/c _S ⁰ & scaled concentration of component j in product stream C _j ^s=c _j ^s/c _S ⁰ & scaled concentration of component j in substrate stream i & electric current density (A/m²) j & reaction component, j P, Q or S P & main reaction product (6-aminopenicillanic acid) PGA & penicillin G acylase Q & side reaction product (phenylacetic acid) S & substrate (penicillin G) Y _s=C _P ^s+C _P ^p & substrate conversion & mean residence time of substrate and product streams in reactor (h) =C _Q ^s+C _Q ^p+C _S ^s+C _S ^s & check-sum of scaled concentrations =C _P ^p/(C _P ^s+C _P ^p) & separation factor of 6-aminopenicillanic acid (0 1)