Biotransformation of 2-phenylethanol to phenylacetaldehyde in a two-phase fed-batch system

Phenylacetaldehyde (PA) can be produced by the oxidation of 2-phenylethanol (PE) through biotransformation. In order to prevent substrate and product inhibitions and the transformation of the PA to phenylacetic acid (PAA), utilization of a two-phase system is very attractive. Gluconobacter oxydans B-72 was used as the microorganism and iso-octane as the solvent. The effect of initial substrate concentration on the PA production was investigated in single- and two-phase systems. In the single-phase system, substrate inhibition occurred above 5 g/l, and in the two-phase system, above 7.5 g/l. Substrate inhibition kinetics were also studied in the two-phase system and kinetic constants were determined as r_max=0.64 g/l min, K_M=8.15 g/l, K_PA=2.5 g/l. Because it was observed that two-phase system is insufficient to remove the substrate inhibition effect, fed-batch operation was utilised in this study. For 7.5 g/l of PE, 1.65, 3.85, and 7.35 g/l of PA were obtained in the single-phase, two-phase, and two-phase three fed-batch systems, respectively. Effect of biotransformation time, initial substrate concentration, agitation speed, and fed-batch number on the PA production was investigated in a two-phase fed-batch system by the response surface methodology (RSM). The optimum values were found as 3 fed-batch number, 2.75 g/l initial substrate concentration, 150 rpm agitation speed, and 65 min of one batch biotransformation time. In order to verify these results, an experiment was performed at these optimum conditions and 7.10 g/l of PA concentration was obtained.     

Performance evaluation of various bioreactors for the removal of Cr(VI) and organic matter from industrial effluent

Performances of various bioreactors under different operating conditions were evaluated with respect to hexavalent chromium (Cr(VI)) reduction and COD removal. Continuous reactor studies were carried out with (i) aerobic suspended growth system, (ii) aerobic attached growth system, and (iii) anoxic attached growth system, using both synthetic and actual industrial wastewater. Arthrobacter rhombi-RE (MTCC7048), a Cr(VI) reducing strain enriched and isolated from chromium contaminated soil, was used in all the bioreactors for Cr(VI) biotransformation and COD removal. Aerobic and anoxic batch experiments were conducted to evaluate the bio-kinetic parameters. The bio-kinetic parameters for aerobic system were: μ_max = 2.34/d, K_s = 190 mg/L (as COD), K_i = 3.8 mg/L of Cr(VI), and Y_T = 0.377. These parameters for anoxic conditions were: μ_max = 0.57/d, K_s = 710 mg/L (as COD), K_i = 8.77 mg/L of Cr(VI), and Y_T = 0.13. Aerobic attached growth system, operated at a hydraulic retention time (HRT) of 24 h and an organic loading rate (OLR) of 3 kg/m³/d, performed better than aerobic suspended and the anoxic attached growth systems operated under identical conditions, while treating synthetic wastewater as well as industrial effluent.     

Enhanced activity of immobilized pepsin nanoparticles coated on solid substrates compared to free pepsin

In the present work nanoparticles (NPs) of pepsin were generated in an aqueous solution using high-intensity ultrasound, and were subsequently immobilized on low-density polyethylene (PE) films, or on polycarbonate (PC) plates, or on microscope glass slides. The pepsin NPs coated on the solid surfaces have been characterized by HRSEM, TEM, FTIR, XPS and DLS. The amount of enzyme introduced on the substrates, the leaching properties, and the catalytic activity of the immobilized enzyme on the three surfaces are compared. Catalytic activities of pepsin deposited onto the three solid surfaces as well as free pepsin, without sonication, and free pepsin NPs were compared at various pH levels and temperatures using a hemoglobin assay. Compared to native pepsin, pepsin coated onto PE showed the best catalytic activity in all the examined parameters. Pepsin immobilized on glass exhibited better activity than the native enzyme, especially at high temperatures. Enzyme activity of pepsin immobilized on PC was no better than native enzyme activity at all temperatures at pH 2, and only over a narrow pH range at 37 °C was the activity improved over the native enzyme. A remarkable observation is that immobilized pepsin on all the surfaces was still active to some extent even at pH 7, while free pepsin was completely inactive. The kinetic parameters, K_m and V_max were also calculated and compared for all the samples. Relative to the free enzyme, pepsin coated PE showed the greatest improvement in kinetic parameters (K_m = 15 g/L, V_max = 719 U/mg versus K_m = 12.6 g/L and V_max = 787 U/mg, respectively), whereas pepsin coated on PC exhibited the most unfavorable kinetic parameters (K_m = 18 g/L, V_max = 685 U/mg). The values for the anchored enzyme-glass were K_m = 19 g/L, V_max = 763 U/mg.     

Kinetics of cellulose hydrolysis by halostable cellulase from a marine Aspergillus niger at different salinities

Kinetics of cellulose hydrolysis with halostable cellulase from a marine Aspergillus niger was analyzed at different salinities. Cellulase activity in 8% NaCl solution was 1.43 folds higher than that in NaCl free solution. Half saturation constant, K_m (15.6260 g/L) and the rate constant of deactivation, K_de (0.3369 g/L h) in 8% NaCl solution was lower than that (18.6364 g/L), 0.3754 (g/L h) in NaCl free solution. The maximum initial hydrolysis velocity, V_max (25.5295 g/L h), in 8% NaCl solution was higher than that in NaCl free solution (25.0153 g/L h). High salinity increased affinity to the cellulase to the substrate and thermostability. Halostable cellulase from a marine Aspergillus niger was valuable for cellulose hydrolysis under high salinity conditions.     

Fast conversion of glycerol to 1,3-propanediol by a new strain of Klebsiella pneumoniae

Five bacterial strains screened from a batch of 39 samples could convert glycerol anaerobically to 1,3-propanediol (1,3-PD). One of the strains, XJ-Li, which could synthesize 1,3-PD with a higher concentration, was identified and characterized. Phylogenetic analysis of the strain XJ-Li included the study of morphology, physiological and biochemical characteristics. In addition, 16SrDNA sequences were created. The results indicated that this strain is a member of Klebsiella pneumoniae. The optimal cultivation parameters for pH and temperature were determined as 8.0 and 40 °C, respectively. The optimized nitrogen source and carbon source were 6.0 g/L of (NH₄)₂SO₄ and 20 g/L of glycerol, respectively. After 8 h in batch fermentation, both the 1,3-PD concentration and glycerol consumption reached the maximum, with 12.2 g/L of 1,3-PD and 1.53 g/L h of productivity, and a molar yield of 1,3-PD to glycerol of 0.75. Fed-batch fermentation also indicated a higher molar yield of 0.70, and the concentration of 1,3-PD reached 38.1 g/L after 66.4 g/L of glycerol consumption. The results of batch and fed-batch fermentations demonstrated that K. pneumoniae XJ-Li would be an excellent 1,3-PD producer.     

Anaerobic treatment of saline wastewater by Halanaerobium lacusrosei

An upflow anaerobic packed bed reactor was operated continuously with synthetic saline wastewater at different initial COD concentrations (COD₀ = 1900–6300 mg/L), salt concentrations (0–5%, w/v) and hydraulic retention times (θ_H = 11–30 h) to investigate the effect of those operating parameters on COD removal from saline synthetic wastewater. Anaerobic salt tolerant bacteria, Halanaerobium lacusrosei, were used as dominant microbial culture in the process. The percent COD removal reached up to 94% at COD₀ = 1900 mg/L, 19 h hydraulic retention time and 3% salt concentration. No substrate inhibition effect was observed at high feed CODs. Increasing hydraulic retention time from 11 h to 30 h resulted in a substantial improvement in the COD removal from 60% to 84% at around COD₀ = 3400 mg/L and 3% salt concentration. Salt inhibition effect on COD utilization was observed at above 3% salt concentration. Modified Stover–Kincannon model was applied to the experimental data to determine the biokinetic coefficients. Saturation value constant, and maximum utilization rate constant of Stover–Kincannon model for COD were determined as K_B = 5.3 g/L day, U_max = 7.05 g/L day, respectively.     

Fed-batch culture of recombinant Saccharomyces cerevisiae for glucose 6-phosphate dehydrogenase production

We examined glucose 6-phosphate dehydrogenase (G6PD) production by fed-batch cultivation, using a recombinant strain of Saccharomyces cerevisiae W303-181 overexpressing this enzyme. The cultivations were carried out in a 3 L fermenter at pH 5.7, 30 °C, 2.0 vvm aeration, 200 rpm agitation and an inoculum concentration of 1.0 g/L. The volume of the culture medium in the fed-batch process varied from 1.333 to 2.0 L, due to the addition of 15.0 g/L glucose solution during 5 h. Different feeding rates were studied (exponentially increasing and decreasing feeding rates), and the feeding profile was determined by values of the parameter K (time constant), namely: 0.2, 0.5 and 0.8 h⁻¹. The best enzyme production (847 U/L) was obtained with an exponentially increasing feeding rate and K = 0.2 h⁻¹. The results attained also showed that this process is promising for G6PD production.     

Secretory expression of functional barley limit dextrinase by Pichia pastoris using high cell-density fermentation

Heterologous production of large multidomain proteins from higher plants is often cumbersome. Barley limit dextrinase (LD), a 98 kDa multidomain starch and α-limit dextrin debranching enzyme, plays a major role in starch mobilization during seed germination and is possibly involved in starch biosynthesis by trimming of intermediate branched α-glucan structures. Highly active barley LD is obtained by secretory expression during high cell-density fermentation of Pichia pastoris. The LD encoding gene fragment without signal peptide was subcloned in-frame with the Saccharomyces cerevisiae α-factor secretion signal of the P. pastoris vector pPIC9K under control of the alcohol oxidase 1 promoter. Optimization of a fed-batch fermentation procedure enabled efficient production of LD in a 5-L bioreactor, which combined with affinity chromatography on β-cyclodextrin–Sepharose followed by Hiload Superdex 200 gel filtration yielded 34 mg homogenous LD (84% recovery). The identity of the recombinant LD was verified by N-terminal sequencing and by mass spectrometric peptide mapping. A molecular mass of 98 kDa was estimated by SDS–PAGE in excellent agreement with the theoretical value of 97419 Da. Kinetic constants of LD catalyzed pullulan hydrolysis were found to K_m,app = 0.16 ± 0.02 mg/mL and k_cat,app = 79 ± 10 s^?1 by fitting the uncompetitive substrate inhibition Michaelis–Menten equation, which reflects significant substrate inhibition and/or transglycosylation. The resulting catalytic coefficient, k_cat,app/K_m,app = 488 ± 23 mL/(mg s) is 3.5-fold higher than for barley malt LD. Surface plasmon resonance analysis showed α-, β-, and γ-cyclodextrin binding to LD with K_d of 27.2, 0.70, and 34.7 μM, respectively.     

Kinetic modeling and implementation of superior process strategies for β-galactosidase production during submerged fermentation in a stirred tank bioreactor

This paper reports development and implementation of superior fermentation strategies for β-galactosidase production by Lactobacillus acidophilus in a stirred-tank bioreactor. Process parameters (aeration and agitation) were optimized for the process by application of Central Composite Design. Aeration rate of 0.5 vvm and agitation speed of 250 rpm were most suitable for β-galactosidase production (2001.2 U/L). Further improvement of the operation in pH controlled environment resulted in 2135 U/L of β-galactosidase with productivity of 142.39 U/L h. Kinetic modeling for biomass and enzyme production and substrate utilization were carried out at the aforementioned pH controlled conditions. The logistic regression model (X₀ = 0.01 g/L; X_max = 2.948 g/L; μ_max = 0.59/h; R² = 0.97) was used for mathematical interpretation of biomass production. Mercier's model proved to be better than Luedeking–Piret model in describing β-galactosidase production (P₀ = 0.7942 U/L; P_max = 2169.3 U/L; P_r = 0.696/h; R² = 0.99) whereas the latter was more efficient in mathematical illustration of lactose utilization (m = 0.187 g/g h; Y_x/s = 0.301 g/L; R² = 0.98) among the two used in this study. Strategies like fed-batch fermentation (3694.6 U/L) and semi-continuous fermentation (5551.9 U/L) further enhanced β-galactosidase production by 1.8 and 2.8 fold respectively.     

Repeated fed-batch cultivation of Arthrospira (Spirulina) platensis using urea as nitrogen source

Arthrospira (Spirulina) platensis (Nordstedt) Gomont was autotrophically cultivated for biomass production in repeated fed-batch process using urea as nitrogen source, with the aim of making large-scale production easier, increasing cell productivity and then reducing the production costs. It was investigated the influence of the ratio of renewed volume to total volume (R), the urea feeding time (t_f) and the number of successive repeated fed-batch cycles on the maximum cell concentration (X_m), cell productivity (P_x), nitrogen-to-cell conversion yield (Y_x/n), maximum specific growth rate (μ_m) and protein content of dry biomass. The experimental results demonstrated that R = 0.80 and t_f = 6 d were the best cultivation conditions, being able to simultaneously ensure, throughout the three fed-batch cycles, the highest average values of three of the five responses (X_m = 2101 ± 113 mg L^?1, P_x = 219 ± 13 mg L^?1 d^?1 and Y_x/n = 10.3 ± 0.8 g g^?1).     

Operation of a fixed-bed bioreactor in batch and fed-batch modes for production of inulinase by solid-state fermentation

This work is focused on the inulinase production by solid-state fermentation (SSF) in a fixed-bed reactor (34 cm diameter and 50 cm height) with working capacity of 2-kg of dry substrate operated in batch and fed-batch modes. It was investigated different strategies for feeding the inlet air in the bioreactor (saturated and unsaturated air) as alternative to remove the metabolic heat generated during the microbial growth by evaporative cooling. The kinetic evaluation of the process carried out in batch mode using unsaturated air showed that the evaporative cooling decreasing the mean temperature of the solid-bed, although the enzyme production was lower than that obtained using saturated air. Results showed that maximum enzyme activity (586 ± 63 U gds⁻¹) was obtained in the fed-batch mode using saturated air after 24 h of fermentation. The enzymatic extract obtained by fed-batch mode was characterized and presented optimum temperature and pH in the range of 52–57 °C and 4.8–5.2, respectively. For a temperature range from 40 to 70 °C the enzyme presented decimal reduction time, D-value, ranging from 5748 to 47 h, respectively. For a pH range from 3.5 to 5.5 the enzyme showed good stability, presenting D-values higher than 2622 h. In terms of Michaelis–Mentem parameters were demonstrated that the crude inulinase activity presented higher affinity for substrate sucrose compared to inulin.     

Effect of heating rate on pDNA production by E. coli

The effects of heating rate (HR) on the performance of two-phase (batch followed by fed-batch) high cell-density cultivations (HCDC) of E. coli DH5α for the production of plasmid DNA (pDNA) were investigated. Optimal temperatures for the HCDC, as selected from shake flask experiments at constant temperatures between 30 and 45 °C, were 35 °C for biomass accumulation in the batch phase and 42 °C for inducing pDNA replication during the fed-batch. In HCDC the temperature was increased at HR of 0.025, 0.05, 0.10 and 0.25 °C/min and the performance of the cultivations were compared to a HCDC run at constant temperature (35 °C). Compared to constant 35 °C, heat-induced HCDC accumulated up to 50% less biomass within the same cultivation time and acetate and glucose accumulated to high concentrations. The overall specific productivity (Q_P) and average pDNA yield (Y_p/x) in HCDC at 35 °C were 0.22 ± 0.02 mg/g h and 5.3 ± 0.00 mg/g, respectively. Such parameters were maximum at a HR of 0.05 °C/min, reaching 0.56 ± 0.06 mg/g h and 9.3 ± 0.6 mg/g, respectively. At HR above 0.5 °C/min, Y_p/x remained relatively constant, whereas Q_P tended to decrease. The supercoiled pDNA fraction remained around 80% at all HR. Bioreactors were equipped with a capacitance/conductivity probe. In all cases biomass concentration correlated closely with the capacitance signal and acetate and glucose accumulation was accompanied by an increase in the conductivity signal. Thus, it was possible to calculate acetate and biomass concentrations, as well as μ, from online capacitance and conductivity signals using estimators. Altogether, in this study it was shown that it is possible to maximize pDNA productivity by choosing an appropriate HR and that relevant parameters can be estimated by capacitance/conductivity signals, which are useful for better process control and development.     

Kinetic study on enzymatic esterification of tuna fish oil fatty acids with butanol

Docosahexaenoic acid (DHA) is an important polyunsatured fatty acid (PUFA) which can be purified from tuna fish oil fatty acids by selective enzymatic esterification. The present paper investigates the kinetic study for selective esterification of tuna fish oil fatty acids with butanol catalyzed by Rhizopus oryzae lipase (ROL) in biphasic solvent system. Under the most suitable reaction conditions, 76.2% esterification was achieved in 24 h. Different kinetic models for esterification given by Segel [1], Oliveira et al. [2], Gogoi et al. [3], and Kraai et al. [4] were tested for fitting the esterification data and the model given by Oliveira et al. [2] was found to be most suitable. The model given by Prazeres et al. [5] for hydrolysis was also tested for esterification and the model with second order product inhibition was found to provide better match between the predicted and experimental values than that of model by Oliveira et al. [2]. The kinetic model was fitted using MATLAB^® to determine the best kinetic parameters. The average value of kinetic constants using the model given by Prazeres et al. were estimated as K_m = 23.6 μmoles FFA/ml, K_i1 = 4.6 × 10⁻⁵ μmoles FFA/mg enzyme h, K_i2 = 0.0062 μmoles FFA/mg enzyme h and K₂ = 149.5 μmoles FFA/mg enzyme h.     

Single cell oil production from hydrolysates of inulin and extract of tubers of Jerusalem artichoke by Rhodotorula mucilaginosa TJY15a

In this study, we found that Rhodotorula mucilaginosa TJY15a could accumulate 48.8% (w/w) oil from hydrolysate of inulin and its cell dry weight reached 14.8 g/l during the batch cultivation while it could accumulate 48.6% (w/w) oil and 52.2% (w/w) oil from hydrolysate of extract of Jerusalem artichoke tubers and its cell dry weight reached 14.4 g/l and 19.5 g/l during the batch and fed-batch cultivations, respectively. At the end of the fed-batch cultivation, only 0.04% of reducing sugar and 0.08% of total sugar were left in the fermented medium. Over 87.6% of the fatty acids from the yeast strain TJY15a cultivated in the hydrolysate of extract of Jerusalem artichoke tubers was C_16:0, C_18:1 and C_18:2, especially C_18:1 (54.7%). Therefore, the results show that hydrolysates of inulin and extract of Jerusalem artichoke tubers were also the good materials for single cell oil production.     

Production of pediocin SM-1 by Pediococcus pentosaceus Mees 1934 in fed-batch fermentation: Effects of sucrose concentration in a complex medium and process modeling

Production of pediocin SM-1 by Pediococcus pentosaceus Mees 1934 was investigated in semi-aerobic, pH-controlled, batch and fed-batch fermentations using a complex medium containing sucrose as the main source of carbon. The effects of sucrose concentration were studied in fed-batch fermentations in which a sucrose solution was added at stable feeding rates (5, 7, 9 and 10 g/l/h). The results showed that pediocin is produced as a product of the primary metabolism and its titer could be greatly improved by adjusting the sucrose feeding rate in fed-batch fermentation. The maximum titer of pediocin of 145 AU/ml was obtained in the fed-batch culture with 7 g/l/h feeding rate and that was 119% higher compared to the titer obtained in batch culture. Higher feeding rates (9 and 10 g/l/h) resulted in decreased pediocin yields while biomass levels appeared to be rather unaffected. The specific rate of pediocin formation was also sensitive to sucrose concentration levels. A mathematical model developed on the basis of well-known rate equations for batch and fed-batch cultures and growth associated production, described successfully cell growth, sucrose assimilation, lactate production and pediocin production in fed-batch culture.     

Purification,kinetic and thermodynamic characterization of soluble acid invertase from sugarcane (Saccharum officinarum L.)

We report for the first time kinetic and thermodynamic properties of soluble acid invertase (SAI) of sugarcane (Saccharum officinarum L.) salt sensitive local cultivar CP 77-400 (CP-77). The SAI was purified to apparent homogeneity on FPLC system. The crude enzyme was about 13 fold purified and recovery of SAI was 35%. The invertase was monomeric in nature and its native molecular mass on gel filtration and subunit mass on SDS-PAGE was 28 kDa. SAI was highly acidic having an optimum pH lower than 2. The acidic limb was missing. Proton transfer (donation and receiving) during catalysis was controlled by the basic limb having a pKa of 2.4. Carboxyl groups were involved in proton transfer during catalysis. The kinetic constants for sucrose hydrolysis by SAI were determined to be: k_m = 55 mg ml^?1, k_cat = 21 s^?1, k_cat/k_m = 0.38, while the thermodynamic parameters were: ΔH* = 52.6 kJ mol^?1, ΔG* = 71.2 kJ mol^?1, ΔS* = ?57 J mol^?1 K^?1, ΔG*_E–S = 10.8 kJ mol^?1 and ΔG*_E–T = 2.6 kJ mol^?1. The kinetics and thermodynamics of irreversible thermal denaturation at various temperatures 53–63 °C were also determined. The half -life of SAI at 53 and 63 °C was 112 and 10 min, respectively. At 55 °C, surprisingly the half -life increased to twice that at 53 °C. ΔG*, ΔH* and ΔS* of irreversible thermal stability of SAI at 55 °C were 107.7 kJ mol^?1, 276.04 kJ mol^?1 and 513 J mol^?1K^?1, respectively.     

The P170 expression system enhances hyaluronan molecular weight and production in metabolically-engineered Lactococcus lactis

Recombinant Lactococcus lactis strains based on the P170 expression system were developed for hyaluronan (HA) production, by incorporating genes from the has operon of Streptococcus zooepidemicus and compared with nisin-inducible recombinant L. lactis strains containing the hasABC and hasABD constructs. It was found across all batch and fed-batch experimental studies that HA concentration and molecular weight (MW) were higher for the P170 expression systems than the corresponding NICE-based strains. The highest hyaluronan MW was obtained for all constructs in batch studies at 60 g/L initial glucose concentration, the highest being 2.94 MDa for the P170 strains with hasABC construct (L. lactis APJ3). In fed-batch studies with constant feed rate, the L. lactis APJ3 gave better HA yield (0.03 g/g) than the NICE-based strain. A higher hyaluronan MW was obtained for all strains in pulse fed-batch compared to constant feed experiments, the highest being 2.52 MDa for L. lactis APJ3.     

Investigation on the properties and kinetics of glucose-fed aerobic granular sludge

Aerobic granulation is a process in which suspended biomass aggregate and form discrete well-defined granules in aerobic systems. To investigate the properties and kinetics of aerobic granular sludge, aerobic granules were cultivated with glucose synthetic wastewater in a series of sequencing batch reactors (SBR). The spherical shaped granules were observed on 8th day with the mean diameter of 0.1 mm. With the organic loading rate (OLR) being increased to 4.0 g COD L⁻¹ d⁻¹, aerobic granules grew matured with spherical shape. The size of granules ranged from 1.2 to 1.8 mm, and the corresponding settling velocity of individual granule was 24.2–36.4 m h⁻¹. The oxygen utilization rate (OUR) of mature granules was 41.90 g O₂ kg MLSS⁻¹ h⁻¹, which was two times higher than that of activated sludge (18.32 g O₂ kg MLSS⁻¹ h⁻¹). The experimental data indicated that the substrate utilization and biomass growth kinetics generally followed Monod's kinetics model. The corresponding kinetic coefficients of k (maximum specific substrate utilization rate), K_s (half velocity coefficient), Y (growth yield coefficient) and K_d (decay coefficient) were determined as follows, k_c = 23.65 d⁻¹, K_c = 3367.05 mg L⁻¹, K_N = 0.038 d⁻¹, K_N = 29.65 mg L⁻¹, Y = 0.1927–0.2022 mg MMLS (mg COD)⁻¹ and K_d = 0.00845–0.0135 d⁻¹, respectively. Those properties of aerobic granules made aerobic granules system had a short setup period, high substrate utilization rate and low sludge production.     

Purification and characterization of an exo-polygalacturonase produced by Penicillium viridicatum RFC3 in solid-state fermentation

The pectinolytic enzyme obtained from Penicillium viridicatum RFC by solid-state fermentation was purified to homogeneity by pretreatment with kaolin (40 mg mL⁻¹) and ultrafiltration, followed by chromatography on a Sephadex G50 column. The apparent molecular weight of the enzyme was 24 kDa. Maximal activity occurred at pH 6.0 and at 60 °C. The enzyme proved to be an exo-polygalacturonase, releasing galacturonic acid by hydrolysis of highly esterified pectin. The presence of 10 mM Ba²⁺ increased the enzyme activity by 96% and its thermal stability by 30%, besides increasing its stability at acid pH. The apparent K_m with apple pectin as substrate was 1.82 mg mL⁻¹ and the V_max was 81 μmol min⁻¹ mg⁻¹.     

Forming nanoparticles of α-amylase and embedding them into solid surfaces

In the current work nanoparticles (NPs) of α-amylase were generated in an aqueous solution using high-intensity ultrasound, and were subsequently immobilized on polyethylene (PE) films, or polycarbonate (PC) plates, or on microscope glass slides. The α-amylase NPs coated on the solid surfaces have been characterized by ESEM, TEM, FTIR, XPS and AFM. The substrates immobilized with α-amylase were used for hydrolyzing soluble potato starch to maltose. The amount of enzyme introduced in the substrates, leaching properties, and the catalytic activity of the immobilized enzyme were compared. The catalytic activity of the amylase deposited on the three solid surfaces was compared to that of the same amount of free enzyme at different pHs and temperatures. α-Amylase coated on PE showed the best catalytic activity in all the examined parameters when compared to native amylase, especially at high temperatures. When immobilized on glass, α-amylase showed better activity than the native enzyme over all pH and temperature values studied. However, the immobilization on PC did not improve the enzyme activity at any pH and any temperature compared to the free amylase. The kinetic parameters, K_m and V_max were also calculated. The amylase coated PE showed the most favorable kinetic parameters (K_m = 5 g L⁻¹ and V_max = 5E−07 mol mL⁻¹ min⁻¹). In contrast, the anchored enzyme-PC exhibited unfavorable kinetic parameters (K_m = 16 g L⁻¹, V_max = 4.2E−07 mol mL⁻¹ min⁻¹). The corresponding values for amylase-glass were K_m = 7 g L⁻¹, V_max = 1.8E−07 mol mL⁻¹ min⁻¹, relative to those obtained for the free enzyme (K_m = 6.6 g L⁻¹, V_max = 3.3E−07 mol mL⁻¹ min⁻¹).