Enzymatic saccharification of sugar cane bagasse by continuous xylanase and cellulase production from cellulomonas flavigena PR‐22

Cellulase (CMCase) and xylanase enzyme production and saccharification of sugar cane bagasse were coupled into two stages and named enzyme production and sugar cane bagasse saccharification. The performance of Cellulomonas flavigena (Cf) PR‐22 cultured in a bubble column reactor (BCR) was compared to that in a stirred tank reactor (STR). Cells cultured in the BCR presented higher yields and productivity of both CMCase and xylanase activities than those grown in the STR configuration. A continuous culture with Cf PR‐22 was run in the BCR using 1% alkali‐pretreated sugar cane bagasse and mineral media, at dilution rates ranging from 0.04 to 0.22 1/h. The highest enzymatic productivity values were found at 0.08 1/h with 1846.4 ± 126.4 and 101.6 ± 5.6 U/L·h for xylanase and CMCase, respectively. Effluent from the BCR in steady state was transferred to an enzymatic reactor operated in fed‐batch mode with an initial load of 75 g of pretreated sugar cane bagasse; saccharification was then performed in an STR at 55°C and 300 rpm for 90 h. The constant addition of fresh enzyme as well as the increase in time of contact with the substrate increased the total soluble sugar concentration 83% compared to the value obtained in a batch enzymatic reactor. This advantageous strategy may be used for industrial enzyme pretreatment and saccharification of lignocellulosic wastes to be used in bioethanol and chemicals production from lignocellulose. © 2016 American Institute of Chemical Engineers Biotechnol. Prog., 32:321–326, 2016     

Hydrolysis and large scale ultrafiltration study of alfalfa protein concentrate enzymatic hydrolysate

Batch enzymatic hydrolysis of insoluble Alfalfa Protein Concentrate by Delvolase was carried out at laboratory and at pilot-plant scale coupled to an ultrafiltration reactor with a mineral tubular membrane. Parametric studies were carried out on the batch system to determine the biochemical and hydrodynamical optimum conditions. The hydrolysis conditions selected were 40 degrees C, pH 9.5, initial substrate level 3 g protein/100 g and the enzyme substrate ratio 152 U/g protein. After 5 h of hydrolysis, 96% of the total amount of initial nitrogen was solubilized. The ultrafiltration conditions selected were a 10 000 Nominal Molecular Weight Cut-Off, a transmembrane pressure of 1.5 bar, a flux velocity of 0.8 m/s. Fifty percent of the initial nitrogen appeared in the permeate.     

Continuous enzymatic liquefaction of starch for saccharification

A process was explored for continuous enzymatic liquefaction of corn starch at high concentration and subsequently saccharification to glucose. The process appears to be quite efficient for conversion of starch to glucose and enzymatic liquefaction and should be readily adaptable to industrial fermentation processes. Preliminary work indicated that milled corn or other cereal grains also can be suitably converted by such a process. Essentially, the process involved incorporation of a thermostable, bacterial alpha-amylase for liquefaction and, subsequently, of a glucoamylase into the continuous mixer under conditions conductive to rapid enzymatic hydrolyses. Also studied was the effect on substrate liquefaction of variable such as starch concentration (40-70 degrees ), level of alpha-amylase (0.14-0.4%, dry starch basis), temperature (70-100 degrees C), pH (5.8-7.1), and residence time (6 and 12 min). The degree of liquefaction was assessed by determining (1) the Brookfield viscosity, (2) the amount of reducing groups, and (3) the rate and extent of glucose formed after glucoamylase treatment. Best liquefaction process conditions were achieved by using 50-60% starch concentration, at 95 degrees C, with 0.4% alpha-amylase, and a 6-min residence period in the mixture. Under these conditions, rate and extents of glucose obtained after glucoamylase treatment approached those obtained in longer laboratory batch liquefactions. The amount of glucose formed in 24h with the use of 0.4% glucoamylase was 86% of theory after a 6-min continuous liquefaction, compared to 90% for a 30-min laboratory batch liquefaction (95 degrees C, 0.4% alpha-amylase).     

Copper removal by algae Gelidium, agar extraction algal waste and granulated algal waste: kinetics and equilibrium

Biosorption of copper ions by an industrial algal waste, from agar extraction industry has been studied in a batch system. This biosorbent was compared with the algae Gelidium itself, which is the raw material for agar extraction, and the industrial waste immobilized with polyacrylonitrile (composite material). The effects of contact time, pH, ionic strength (IS) and temperature on the biosorption process have been studied. Equilibrium data follow both Langmuir and Langmuir-Freundlich models. The parameters of Langmuir equilibrium model were: q(max)=33.0mgg(-1), K(L)=0.015mgl(-1); q(max)=16.7mgg(-1), K(L)=0.028mgl(-1) and q(max)=10.3mgg(-1), K(L)=0.160mgl(-1) respectively for Gelidium, algal waste and composite material at pH=5.3, T=20 degrees C and IS=0.001M. Increasing the pH, the number of deprotonated active sites increases and so the uptake capacity of copper ions. In the case of high ionic strengths, the contribution of the electrostatic component to the overall binding decreases, and so the uptake capacity. The temperature has little influence on the uptake capacity principally for low equilibrium copper concentrations. Changes in standard enthalpy, Gibbs energy and entropy during biosorption were determined. Kinetic data at different solution pH (3, 4 and 5.3) were fitted to pseudo-first-order and pseudo-second-order models. The adsorptive behaviour of biosorbent particles was modelled using a batch reactor mass transfer kinetic model, which successfully predicts Cu(II) concentration profiles.     

Kinetics of total enzymatic hydrolysis of acetylcholine and acetylthiocholine

Kinetics and the mechanism of total in vitro hydrolyses (i.e. up to the exhaustion of substrate) of acetylcholine and acetylthiocholine by acetylcholinesterase and butyrylcholinesterase were studied in vitro in a batch reactor at 25 degrees C, pH 8 and ionic strength of 0.11 M. Every hydrolysis was monitored by 2-3 independent analytical methods. All studied types of enzymatic hydrolyses fulfilled the Michaelis-Menten reaction scheme with the irreversible second step. A table of obtained average values of rate constants and estimations of initial molar enzyme concentrations, and discussion of the results are presented.     

Deposition of lignin droplets produced during dilute acid pretreatment of maize stems retards enzymatic hydrolysis of cellulose

Electron microscopy of lignocellulosic biomass following high-temperature pretreatment revealed the presence of spherical formations on the surface of the residual biomass. The hypothesis that these droplet formations are composed of lignins and possible lignin carbohydrate complexes is being explored. Experiments were conducted to better understand the formation of these "lignin" droplets and the possible implications they might have on the enzymatic saccharification of pretreated biomass. It was demonstrated that these droplets are produced from corn stover during pretreatment under neutral and acidic pH at and above 130 degrees C, and that they can deposit back onto the surface of residual biomass. The deposition of droplets produced under certain pretreatment conditions (acidic pH; T > 150 degrees C) and captured onto pure cellulose was shown to have a negative effect (5-20%) on the enzymatic saccharification of this substrate. It was noted that droplet density (per unit area) was greater and droplet size more variable under conditions where the greatest impact on enzymatic cellulose conversion was observed. These results indicate that this phenomenon has the potential to adversely affect the efficiency of enzymatic conversion in a lignocellulosic biorefinery.     

Ethanol production from alkaline peroxide pretreated enzymatically saccharified wheat straw

Wheat straw used in this study contained 44.24 +/- 0.28% cellulose and 25.23 +/- 0.11% hemicellulose. Alkaline H(2)O(2) pretreatment and enzymatic saccharification were evaluated for conversion of wheat straw cellulose and hemicellulose to fermentable sugars. The maximum yield of monomeric sugars from wheat straw (8.6%, w/v) by alkaline peroxide pretreatment (2.15% H(2)O(2), v/v; pH 11.5; 35 degrees C; 24 h) and enzymatic saccharification (45 degrees C, pH 5.0, 120 h) by three commercial enzyme preparations (cellulase, beta-glucosidase, and xylanase) using 0.16 mL of each enzyme preparation per g of straw was 672 +/- 4 mg/g (96.7% yield). During the pretreatment, no measurable quantities of furfural and hydroxymethyl furfural were produced. The concentration of ethanol (per L) from alkaline peroxide pretreated enzyme saccharified wheat straw (66.0 g) hydrolyzate by recombinant Escherichia coli strain FBR5 at pH 6.5 and 37 degrees C in 48 h was 18.9 +/- 0.9 g with a yield of 0.46 g per g of available sugars (0.29 g/g straw). The ethanol concentration (per L) was 15.1 +/- 0.1 g with a yield of 0.23 g/g of straw in the case of simultaneous saccharification and fermentation by the E. coli strain at pH 6.0 and 37 degrees C in 48 h.     

Hydrolysis of liquefied corn starch in a membrane reactor

The objective of this study was to develop a continuous hydrolysis process for the enzymatic saccharification of liquefied corn starch using a membrane reactor. A residence time distribution study confirmed that the membrane reactor could be modeled as a simple continuous stirred tank reactor (CSTR). Kinetic studies indicated that the continuous reactor operated in the first-order region with respect to substrate concentration at substrate concentrations greater than 200 g/L. At a residence time of 1 h and an enzyme concentration of 1 g/L, the maximum reaction velocity (V(m)) was 3.86 g glucose/L min and the apparent Michaelis constant (K(m) (')) was 562 g/L. The K(m) (') value for the continuous reactor was 2-7 times greater than that obtained in a batch reactor.Kinetic data were fit to a model based on the Michaelis-Menten rate expression and the design equation for a CSTR. Application of the model at low reactor space times was successful. At space times of 6 min or less, the model predicted the reactor's performance reasonably well. Additional work on the detection and quantitation of reversion products formed by glucoamylase is required. Isolation, detection, and quantitation of reversion products by HPLC was difficult. Detailed analysis on the formation of these reversion products could lead to better reactor designs in the future.     

Comparison of a batch, fed-batch and continuously operated stirred-tank reactor for the enzymatic synthesis of (R)-mandelonitrile by using a process model

The suitability of a batch, fed-batch and continuously operated stirred-tank reactor for the enzymatic production of (R)-mandelonitrile in an aqueous-organic biphasic system was investigated by using a process model. The considered biphasic system is 10-50% (v/v) 100 mM sodium citrate buffer of pH 5.5 dispersed in methyl tert-butyl ether. The constraints were that 750 moles of benzaldehyde per cubic meter should react towards (R)-mandelonitrile with an enantiomeric excess of 99% and a conversion of 98%. A continuously operated stirred-tank reactor could not meet the constraints, but the production in a batch or fed-batch reactor was feasible. The choice for a batch or fed-batch reactor is dependent on the influence of the costs for reactor operation and for the enzyme on the product costs. The choice for operating at a small or large aqueous-phase volume fraction is dependent on the costs and reusability of the enzyme. The volumetric productivity is maximal when operating as batch. The enzymatic productivity and turnover are maximal when operating as fed batch. In the fed-batch mode, the enzymatic productivity increased by 24-37%, the turnover increased by 50-60% and the volumetric productivity decreased by 33-71% as compared to a batch reactor. By enhancement of mass transfer both the volumetric and enzymatic productivity can be increased considerably, while the turnover is only slightly decreased.     

Depolymerization of chitosan by chinolytic complex from Bacillus sp. 739

Low-molecular-weight (3-6 kDa) water-soluble chitosan was obtained by enzymatic depolymerization. Hydrolysis of crab chitosan was induced by O-glycoside hydrolase (EC 3.2.1), an extracellular chitinolytic complex from Bacillus sp. 739. The optimum conditions for hydrolysis were found (sodium-acetate buffer, pH 5.2; 55 degrees C; an enzyme/substrate ratio 4 U/g chitosan; 1 h).     

稀碱预处理棕榈残渣制备纤维乙醇

以棕榈残渣(Empty fruit bunch,EFB)为原料,通过预处理、酶解、发酵等过程制备纤维乙醇.首先对比了碱、碱/过氧化氢等预处理条件对棕榈残渣组成及酶解的影响,结果表明稀碱预处理效果较好.适宜的稀碱预处理条件为:NaOH浓度为1％,固液比为1∶10,在40℃浸泡24 h后于121℃下保温30 min,在该条件下,EFB的固体回收率为74.09％,纤维素、半纤维素和木质素的含量分别为44.08％、25.74％和13.89％.对该条件下预处理后的固体样品,以底物浓度5％、酶载量30 FPU/g底物酶解72 h,纤维素和半纤维素的酶解率分别达到84.44％和89.28％.进一步考察了酶载量和底物浓度对酶解的影响以及乙醇批式同步糖化发酵,当酶载量为30 FPU/g底物,底物浓度由5％增加至25％时,利用酿酒酵母Saccharomyces cerevisiae(接种量为5％,VIV)发酵72 h后乙醇的浓度分别为9.76 g/L和35.25 g/L,可分别达到理论得率的79.09％和56.96％.     

Immobilization of glucoamylase by adsorption on carbon supports and its application for heterogeneous hydrolysis of dextrin

Glucoamylase (GA) was immobilized by adsorption on carbon support: on Sibunit, on bulk catalytic filamentous carbon (bulk CFC) and on activated carbon (AC). This was used to prepare heterogeneous biocatalysts for the hydrolysis of starch dextrin. The effect of the texture characteristics and chemical properties of the support surface on the enhancement of the thermal stability of the immobilized enzyme was studied, and the rates of the biocatalyst's thermal inactivation at 65-80 degrees C were determined. The thermal stability of glucoamylase immobilized on different carbon supports was found to increase by 2-3 orders of magnitude in comparison with the soluble enzyme, and decrease in the following order: GA on Sibunit>GA on bulk CFC>GA on AC. The presence of the substrate (dextrin) was found to have a significant stabilizing effect. The thermal stability of the immobilized enzyme was found to increase linearly when the concentration of dextrin was increased from 10 wt/vol % to 50 wt/vol %. The total stabilization effect for glucoamylase immobilized on Sibunit in concentrated dextrin solutions was about 10(5) in comparison with the enzyme in a buffer solution. The developed biocatalyst, 'Glucoamylase on Sibunit' was found to have high operational stability during the continuous hydrolysis of 30-35 wt/vol % dextrin at 60 degrees C, its inactivation half-time (t1/2) exceeding 350 h. To improve the starch saccharification productivity, an immersed vortex reactor (IVR) was designed and tested in the heterogeneous process with the biocatalyst 'Glucoamylase on Sibunit'. The dextrin hydrolysis rate, as well as the process productivity in the vortex reactor, was found to increase by a factor of 1.2-1.5 in comparison with the packed-bed reactor.     

An ultrafiltration membrane bioreactor for the lipolysis of olive oil in reversed micellar media

The enzymatic hydrolysis of olive oil using Chromobacterium viscosum lipase B encapsulated in reversed micelles of dioctyl sodium sulfosuccinate (AOT) in isooctane was investigated in an ultrafiltration ceramic membrane reactor of tubular type, operating in a batch mode. Water concentration was found to be a critical parameter in the enzyme kinetics and hydrolysis yield of the reaction. The size of micelles, recirculation rate, and substrate concentration were found to be the major factors affecting the separation process. A correlation that enables the prediction of final conversion degrees in this bioreactor from the initial reaction conditions was established. (c) 1993 Wiley & Sons, Inc.     

Simultaneous saccharification and fermentation of cellulose for lactic acid production

Lactic acid production from α-cellulose by simultaneous saccharification and fermentation (SSF) was studied. The cellulose was converted in a batch SSF using cellulase enzyme Cytolase CL to produce glucose sugar andLactobacillus delbrueckii to ferment the glucose to lactic acid. The effects of temperature, pH, yeast extract loading, and lactic acid inhibition were studied to determine the optimum conditions for the batch processing. Cellulose was converted efficiently to lactic acid, and enzymatic hydrolysis was the rate controlling step in the SSF. The highest conversion rate was obtained at 46°C and pH 5.0. The observed yield of lactic acid from α-cellulose was 0.90 at 72 hours. The optimum pH of the SSF was coincident with that of enzymatic hydrolysis. The optimum temperature of the SSF was chosen as the highest temperature the microorganism could withstand. The optimum yeast extract loading was found to be 2.5 g/L. Lactic acid was observed to be inhibitory to the microorganisms’ activity.     

Preparation of immobilized alpha-amylase covalently attached to granular polyacrylonitrile

In this report, alpha-Amylase originating from Bacillus subtilis (liquefying type) was immobilized on partially imidoesterized polyacrylonitrile (PAN) by covalent bonding. For the preparation of immobilized alpha-amylase, which has a high activity and high stability to repeated use, the optimum conditions for the preparation reaction were investigated. The optimum conditions for the preparation reaction were quantified on the basis of the enzymatic activity, the preservation of the activity during repeated use in batch process and the protein content on the support. Further-more, enzymatic properties of immobilized alpha-amylase prepared at optimum conditions were compared with the native enzyme. The optimum temperature and reaction time for the imidoes-terification reaction were 30 degrees c and 6 h, respectively, whereas those of the amidinatin reaction were 30-40 degrees C and more than 3 h, respectively; the optimum pH range was 9-10. Immobilized alpha-amylase prepared at the optimum conditions was very stable against the repeated use and had more than 90% of relative to activity of the first use after the tenth procedure. The initial reaction rate of immobilized alpha-amylase was lower than native alpha-amylase, but same amount of reducing sugars were produced after the reaction passed for more than 90 min. The immobilized alpha-amylase was less stabel at the high temperature and the more basic media. However, after long incubation time, immobilized alpha-amylase was more stable than the native enzyme in exposure to heat and a storng base.     

Purification and characteristic of endo-(1--4)-beta-xylanase from Geotrichum candidum 3C

A method of purification of endo-(1-->4)-beta-xylanase (endoxylanase; EC 3.2.1.8) from the culture liquid of Geotrichum candidum 3C, grown for three days, is described. The enzyme purified 23-fold had a specific activity of 32.6 U per mg protein (yield, 14.4%). Endoxylanase was shown to be homogeneous by SDS-PAGE (molecular weight, 60 to 67 kDa). With carboxymethyl xylan as substrate, the optimum activity (determined viscosimetrically) was recorded at pH 4.0 (pI 3.4). The enzyme retained stability at pH 3.0-4.5 and 30-45 degrees C for 1 h. With xylan from beach wood, the hydrolytic activity of the enzyme (ability to saccharify the substrate) was maximum at 50 degrees C. In 72 h of exposure to 0.2 mg/ml endoxylanase, the extent of saccharification of xylans from birch wood, rye grain, and wheat straw amounted to 10, 12, and 7.7%, respectively. At 0.4 mg/ml, the extent of saccharification of birch wood xylan was as high as 20%. In the case of birch wood xylan, the initial hydrolysis products were xylooligosaccharides with degrees of polymerization in excess of four; the end products were represented by xylobiose, xylotriose, xylose, and acid xylooligosaccharides.     

Sugar production from agricultural woody wastes by saccharification with Trichoderma viride cellulase.

The saccharification of agricultural woody wastes was studied using a commercial enzyme preparation, Cellulase onozuka, derived from Trichoderma viride or the solid culture extracts of the fungus. With the intention of producing sugar at low cost, a simple procedure of enzymatic saccharification of rice straw, bagasse, and sawdust was studied. Delignifying methods of these wastes were investigated using dilute sodium hydroxide solution and dilute peracetic acid. Rice straw and bagasse were effectively delignified by boiling in a 1% sodium hydroxide solution for 3 hr or by autoclaving at 120 degrees C in a 1% sodium hydroxide solution for 1 hr. The sawdust from a broad leaved tree (Machilus thunbergii) was delignified by autoclaving at 120 degrees C in a 1% sodium hydroxide solution for 1 hr and by subsequent boiling in diluted 1/5 peracetic acid for 1 hr. This type of sawdust was also delignified by boiling in 1/5 peracetic acid for 1 hr and by subsequent autoclaving at 120 degrees C in a 1% sodium hydroxide solution for 1 hr. The sawdust from a coniferous tree (Cryptomeria japonica) was delignified by boiling in 1/5 peracetic acid for 1 hr and by subsequent autoclaving at 120 degrees C in a 1% sodium hydroxide solution for 1 hr; however, the successive treatment by autoclaving with alkali solution and subsequent boiling with diluted peracetic acid failed to bring about the desired effect. The saccharification of delignified rice straw, bagasse, and sawdust was examined using Cellulase onozuka, wheat bran or rice straw solid culture at various substrate concentrations, resulting in the formation of 5 to 10% sugar solutions after incubation at pH 5.0, 45 degrees C for 48 hr. The optimum substrate concentration existed at around 10%. Reuse of cellulase solution and resaccharification of residual sawdust were considered to be inadequate.     

Factors influencing the production of a novel compound, 7,10-dihydroxy-8(E)-octadecenoic acid, by Pseudomonas aeruginosa PR3 (NRRL B-18602) in batch cultures

Pseudomonas aeruginosa PR3 (NRRL B-18602) converts oleic acid to a novel compound, 7,10-dihydroxy-8(E)-octadecenoic acid (DOD). Parameters that included medium volume, cell growth time, gyration speed, pH, substrate concentration, and dissolved oxygen concentration were evaluated for a scale-up production of DOD in batch cultures using Fernbach flasks and a bench-top bioreactor. Maximum production of about 2 g DOD (38% yield) was attained in Fernbach flasks containing 500 ml medium when cells were grown at 28 degrees C and 300 rpm for 16-20 h and the culture was adjusted to pH 7 prior to substrate addition. Increases of medium volume and substrate concentration failed to enhance yield. When batch cultures were initially conducted in a reactor, excessive foaming occurred that made the bioconversion process inoperable. This was overcome by a new aeration mechanism that provided adequate dissolved oxygen to the fermentation culture. Under the optimal conditions of 650 rpm, 28 degrees C, and 40-60% dissolved oxygen concentration, DOD production reached about 40 g (40% yield) in 4.5 L culture medium using a 7-L reactor vessel. This is the first report on a successful scale-up production of DOD.     

Immobilization of epoxide hydrolase from Aspergillus niger onto DEAE-cellulose: enzymatic properties and application for the enantioselective resolution of a racemic epoxide

Recombinant epoxide hydrolase (EH) from Aspergillus niger can be a very promising tool for the resolution of various racemic epoxides by enantioselective hydrolysis. The enzyme was successfully immobilized by ionic adsorption onto DEAE-cellulose (99% yield, 70% of retention activity). The temperature for maximal activity (40 °C) and the activation energy (38.8 kJ/mol) were similar for both the immobilized and free EHs, whereas the optimal pH was about one unit less for the immobilized enzyme. Thermal stability was also affected by immobilization; the immobilized enzyme appeared to be slightly less stable than the free one. However, a gram-scale resolution of racemic para-chlorostyrene oxide (pCSO) was successfully carried out in a repeated batch reactor, operated for seven cycles. Furthermore, using a very high substrate concentration of 2 M (306 g/L), i.e. biphasic conditions, the resolution of 3 g of pCSO was also achieved in a repeated batch reactor using approximately 300 mg of immobilized EH, corresponding to less than 3 mg of the enzymatic powder.