Hydrodynamic and kinetic study of cellulase production by Trichoderma reesei with pellet morphology

Numerical simulations and experimental validation were performed to understand the effects of hydrodynamics on pellet formation and cellulase production by filamentous T. reesei. The constructed model combined a steady-state multiple reference frame (MRF) approach describing mechanical mixing, oxygen mass transfer, and non-Newtonian flow field with a transient sliding mesh approach and kinetics of oxygen consumption, pellet formation, and enzyme production. The model was experimentally validated at various agitation speeds in a two-impeller Rushton turbine fermentor. Results from simulation and experimentation showed that higher agitation speeds led to increases in the pellet diameter and the proportion of pelletized (vs. filamentous) forms of the biomass. It also led to increase in dissolved oxygen mass transfer rate in shear-thinning fluid and cellulase productivity. The extent of these increases varied considerably among agitation speeds. Pellet formation and morphology were presumably affected within a viscosity-dependent shear-rate range. Cellulase activity and cell viability were shown to be sensitive to impeller shear. A maximum cellulase activity of 3.5 IU/mL was obtained at 400 rpm, representing a twofold increase over that at 100 rpm.     

Pellet morphology, culture rheology and lovastatin production in cultures of Aspergillus terreus

Pellet growth of Aspergillus terreus ATCC 20542 in submerged batch fermentations in stirred bioreactors was used to examine the effects of agitation (impeller tip speed u(t) of 1.01-2.71 ms(-1)) and aeration regimens (air or an oxygen-enriched mixture containing 80% oxygen and 20% nitrogen by volume) on the fungal pellet morphology, broth rheology and lovastatin production. The agitation speed and aeration methods used did not affect the biomass production profiles, but significantly influenced pellet morphology, broth rheology and the lovastatin titers. Pellets of approximately 1200 microm initial diameter were reduced to a final stable size of approximately 900 microm when the agitation intensity was >/=600 rpm (u(t)>/=2.03 ms(-1)). A stable pellet diameter of approximately 2500 microm could be attained in less intensely agitated cultures. These large fluffy pellets produced high lovastatin titers when aerated with oxygen-enriched gas but not with air. Much smaller pellets obtained under highly agitated conditions did not attain high lovastatin productivity even in an oxygen-enriched atmosphere. This suggests that both an upper limit on agitation intensity and a high level of dissolved oxygen are essential for attaining high titers of lovastatin. Pellet size in the bioreactor correlated equally well with the specific energy dissipation rate and the energy dissipation circulation function. The latter took into account the frequency of passage of the pellets through the high shear regions of the impellers. Pellets that gave high lovastatin titers produced highly shear thinning cultivation broths.     

Culture of photomixotrophic soybean and pine in a modified fermentor using a novel impeller

Photomixotrophic suspensions of Glycine max (soybean) and Pinus elliottii (slash pine) have been successfully cultured in a hybrid stirred tank photobioreactor using a novel cell-lift impeller. A cell-lift impeller exhibited cell viabilities over 90% and an average cell aggregate size of 1.0 mm or less. Flat-bladed turbines produced equivalent biomass to the cell-lift impeller, but cell viability was reduced (85%) and cell aggregate size increased (3-5 mm diameter). Maximum fresh weights of 82 g L(-1) (soybean) and 52 g L(-1) (slash pine) were achieved in 15 days using continuous lighting (90-100 muE m(-2) s(-1)) and supplemental 2% CO(2) inlet gas. Maximum biomass was achieved using an impeller speed of 60 rpm with air-flow rate of 0.2 vvm for the cell-lift impeller and the pair of flat bladed turbines. The lag and early exponential phases were characterized by (1) rapid hydrolysis of sucrose followed by preferential use of glucose and (2) a reduction in chlorophyll levels. Carbon dioxide (2%-5%) was an essential nutrient for photomixotrophic cell culture in the bioreactors.     

Effects of pellet morphology on broth rheology in fermentations of Aspergillus terreus

Effects of pellet morphology on broth rheology are reported for pelleted submerged cultures of the lovastatin producing filamentous fungus Aspergillus terreus, growing in fluidized bed and stirred tank bioreactors. The pellet diameter and compactness were affected by the agitation intensity of the broth; however, the total biomass productivity was not affected. In fluidized beds and stirred tanks with agitation intensity of up to 300 rpm (impeller tip speed of 1.02 m s⁻¹), the fungal pellets were stable at diameters of up to about 2300 μm. In more intensely agitated stirred tanks (≥600 rpm; impeller tip speed of ≥2.03 m s⁻¹), the stable pellet size was only about ≤900 μm. The biomass concentration and the pellet diameter were the main factors that influenced the flow index and the consistency index of the power-law broths. Because the biomass productivity was the same in all experiments in a given type of reactor and the oxygen concentration was kept at ∼400% of air saturation, the pellet size and morphology were not influenced by oxygen mass transfer effects. Pellets were always dense in the core region and no necrosis of the biomass occurred.     

Effect of various process parameters on morphology, rheology, and polygalacturonase production by Aspergillus sojae in a batch bioreactor

The effects of pH, agitation speed, and dissolved oxygen tension (DOT), significant in common fungal fermentations, on the production of polygalacturonase (PG) enzyme and their relation to morphology and broth rheology were investigated using Aspergillus sojae in a batch bioreactor. All three factors were effective on the response parameters under study. An uncontrolled pH increased biomass and PG activity by 27% and 38%, respectively, compared to controlled pH (pH 6) with an average pellet size of 1.69 +/- 0.48 mm. pH did not significantly affect the broth rheology but created an impact on the pellet morphology. Similarly, at constant agitation speed the maximum biomass obtained at 500 rpm and at 30 h was 3.27 and 3.67 times more than at 200 and 350 rpm, respectively, with an average pellet size of 1.08 +/- 0.42 mm. The maximum enzyme productivity of 0.149 U mL-1 h-1 was obtained at 200 rpm with an average pellet size of 0.71 +/- 0.35 mm. Non-Newtonian and pseudoplastic broth rheology was observed at 500 rpm agitation speed, broth rheology exhibited dilatant behavior at the lower agitation rate (200 rpm), and at the medium agitation speed (350 rpm) the broth was close to Newtonian. Furthermore, a DOT range of 30-50% was essential for maximum biomass formation, whereas only 10% DOT was required for maximum PG synthesis. Non-Newtonian shear thickening behavior (n > 1.0) was depicted at DOT levels of 10% and 30%, whereas non-Newtonian shear thinning behavior (n < 1.0) was dominant at 50% DOT. The overall fermentation duration (50-70 h) was considerably shorter compared to common fungal fermentations, revealing the economic feasibility of this particular process. As a result this study not only introduced a new strain with a potential of producing a highly commercially significant enzyme but also provided certain parameters significant in the design and mathematical modeling of fungal bioprocesses.     

Comparison of O transfer characteristics between a new centrifugal impeller and a flat-bladed turbine impeller

The efficiency of O transfer by a novel centrifugal impeller was higher than that of a conventional flat-bladed turbine impeller at an agitation speed lower than 300 rpm. In addition, at the same agitation speed (200 and 300 rpm), the centrifugal impeller possessed smaller shear stress than the flat-bladed turbine impeller as evaluated by the changes in size distribution of granulated agar particles which were sheared with those two types of impeller.     

心室辅助径流泵的设计方法

我们正在研制一种心室辅助径流泵,可在体外循环中代替血泵使用,也可作为心衰病人短期心脏辅助泵使用。此种无密封件的径流的泵的轴尖支承结构由一根据氧化铝陶瓷制成的叶轮轴和两只氧化锆陶瓷制成的轴尖轴承组成。叶轮的外径为７２毫米,进流处直径为２４毫米。位于叶轮上表面的六个叶片的进流侧高度为５．５毫米。出流侧高度为３毫米。     

Shear stress effects on cell growth and <Emphasis Type="SmallCaps">L</Emphasis>-DOPA production by suspension culture of <Emphasis Type="Italic">Stizolobium hassjoo</Emphasis> cells in an agitated bioreactor

Suspension cultures of Stizolobium hassjoo cells were cultivated in a 7l bioreactor. The growth rate and intracellular L-DOPA content of the cells using two different turbine impellers were compared. There were distinct differences in growth behavior and L-DOPA productivity in the range of 100 to 500 rpm for flat-blade turbine impeller. Disk turbine retarded significantly the cell growth but not so significantly for L-DOPA production in the range of 200 to 300 rpm. The shear force intensity of the two impellers at various rotational rates was compared with shear force index (SFI), and power input per unit mass and eddy length scale. There was good consistency among the three indexes for shear force intensity. Thus with SFI the shear force intensity of bioreactor can be indirectly estimated. A critical shear stress that may cause sublytic effect in cells was identified for flat-blade turbine operated at 400 rpm. The common effect between the shear stress and the proton elicitation in the bioreactor was elucidated with a hypothesis of signal transduction by second messenger, H⁺. Our results suggested that H⁺ transduced the signal to protoplast when S. hassjoo cells were stimulated by shear stress. This resulted in an increase of H⁺ which triggered a similar reaction to the pH control of culture broth and enhanced the L-DOPA production.     

Effects of agitation intensity on mycelial morphology and protein production in chemostat cultures of recombinant Aspergillus oryzae

The effects of agitation on fragmentation of a recombinant strain of Aspergillus oryzae and its consequential effects on protein production have been investigated. Constant mass, 5.3-L chemostat cultures at a dilution rate of 0.05 h-1 and a dissolved oxygen level of 75% air saturation, have been conducted at 550, 700, and 1000 rpm. These agitation speeds were chosen to cover a range of specific power inputs (2.2 to 12 kW m-3) from realistic industrial levels to much higher values. The use of a constant mass chemostat linked to a gas blender allowed variation of agitation speed and hence gas hold-up without affecting the dilution rate or the concentration of dissolved oxygen. The morphology of both the freely dispersed mycelia and clumps was characterized using image analysis. Statistical analysis showed that it was possible to obtain steady states with respect to morphology. The mean projected area at each steady state under growing conditions correlated well with the 'energy dissipation/circulation" function, [P/(kD3tc)], where P is the power input, D the impeller diameter, tc the mean circulation time, and k is a geometric constant for a given impeller. Rapid transients of morphological parameters in response to a speed change from 1000 to 550 rpm probably resulted from aggregation. Protein production (alpha-amylase and amyloglucosidase) was found to be independent of agitation speed in the range 550 to 1000 rpm (P/V = 2.2 and 12.6 kW m-3, respectively), although significant changes in mycelial morphology could be measured for similar changes in agitation conditions. This suggests that mycelial morphology does not directly affect protein production (at a constant dilution rate and, therefore, specific growth rate). An understanding of how agitation affects mycelial morphology and productivity would be valuable in optimizing the design and operation of large-scale fungal fermentations for the production of recombinant proteins. Copyright 1999 John Wiley & Sons, Inc.     

Impact of pellet size on growth and lignin peroxidase activity of Phanerochaete chrysosporium

We investigated the influence of pellet size on the growth and lignin peroxidase (LiP) productivity of Phanerochaete chrysosporium. Different pellet sizes were obtained by varying the vessel diameter under constant shaking conditions. Under these varying conditions the pellet size was in the range of 2–18 mm, while the number of pellets in a single vessel varied from around 1,200 in the Erlenmeyer flask to around 6 in the narrowest vessel. A correlation between the final pellet size and the shear rate was obtained, demonstrating that the pellet size is mainly affected by hydrodynamics. The growth of large pellets was described by a cubic growth model. Despite different pellet sizes, LiP activity appeared in all vessels, but the onset of LiP activity showed a delay based upon the pellet size, while maximal LiP activities varied by only 15%, being around 850 U/l.     

Operational optimization of a turbine blade reactor using macroporous support and its application to rice callus regeneration

Optimal operation condition was investigated for immobilized rice callus culture using a turbine blade reactor (TBR²) with polyurethane foam supports. By using polyurethane foam block as immobilization support, the inhibition of cell growth at a high agitation speed was avoided because the hydrodynamic stress against immobilized cell was probably reduced. Experimental results in each operational condition were assessed by means of rice callus growth, immobilization ratio in TBR and those regeneration frequencies in regeneration culture using solid medium. Concerning with pore size of polyurethane foam and support size, three-millimeter cube support of polyurethane foam with an average pore size of 1.3 mm was the most suitable support. The maximum immobilization ratio was 50% under 5% support volume by volume of growth medium. For improving the immobilization ratio of rice callus in the TBR, the optimum TBR operation and modification were investigated further. By repeating a periodic operation 3 times (agitating at 300 rpm for 5 min and then 50 rpm for 2 min, and then 200 rpm of constant agitation speed during the remaining time), almost all supports could entrap rice callus and homogeneous immobilization was attained. The immobilization ratio was improved as compared with that using a constant operation at 200 rpm. Next, the TBR was modified by setting an air sparger inside the stainless mesh cylinder. In the modified TBR, the floating support by air bubbles was reduced, and the immobilization ratio increased further and reached 86.3% when we increased the support volume to 15% under periodic operation on a daily basis. The regeneration frequency of immobilized callus was also slightly increased by periodic operation and modification of the TBR.     

The Effect of the Chopper on Granules from Wet High-Shear Granulation Using a PMA-1 Granulator

Chopper presence and then chopper speed was varied during wet high shear granulation of a placebo formulation using a PMA-1 granulator while also varying the impeller speed. The granules were extensively analyzed for differences due to the chopper. The effect of the chopper on the granules varied with impeller speed from no effect at a low impeller speed of 300 rpm to flow interruptions at an impeller speed of 700 rpm to minimal impact at very high impeller speeds as caking at the bowl perimeter obscured the effect of the chopper on the flow pattern. Differences in the granule flowability were minimal. However, it was concluded that the largest fraction of optimal granules would be obtained at an impeller speed of 700 rpm with the chopper at 1,000 rpm allowing balances between flow establishment, segregation, and centrifugal forces.     

Impeller types and feeding modes influence the morphology and protein expression in the submerged culture of<Emphasis Type="Italic">Aspergillus oryzae</Emphasis>

The influences of impeller types on morphology and protein expression were investigated in a submerged culture ofAspergillus oryzae. The impeller types strongly affected mycelial morphology and protein production in batch and fed-batch fermentations. Cells that were cultured by propeller agitation grew in the form of a pellet, whereas cells that were cultured by turbine agitation grew in a freely dispersed-hyphal manner and in a clumped form. Pellet-grown cells showed high levels of protein production for both the intracellular heterologous protein (β-glucuronidase) and the extracellularly homologous protein (α-amylase). The feeding mode of the carbon source also influenced the morphological distribution and protein expression in fed-batch fermentation ofA. oryzae. Pulsed-feeding mainly showed high protein expression and homogeneous distribution of pellet whereas continuous feeding resulted in less protein expression and heterogeneous distribution with pellet and dispersed-hyphae. The pellet growth with propeller agitation paralleling with the pulsed-feeding of carbon source showed a high level of protein production in the submerged fed-batch fermentation of recombinantA. oryzae.     

Dependence of penicillium chrysogenum growth, morphology, vacuolation, and productivity in fed-batch fermentations on impeller type and agitation intensity

The influence of the agitation conditions on the growth, morphology, vacuolation, and productivity of Penicillium chrysogenum has been examined in 6 L fed-batch fermentations. A standard Rushton turbine, a four-bladed paddle, and a six-bladed pitched blade impeller were compared. Power inputs per unit volume of liquid, P/VL, ranged from 0.35 to 7.4 kW/m3. The same fermentation protocol was used in each fermentation, including holding the dissolved oxygen concentration above 40% air saturation by gas blending. The mean projected area (for all dispersed types, including clumps) and the clump roughness were used to characterize the morphology. Consideration of clumps was vital as these were the predominant morphological form. For a given impeller, the batch-phase specific growth rates and the overall biomass concentrations increased with agitation intensity. Higher fragmentation at higher speeds was assumed to have promoted growth through increased formation of new growing tips. The mean projected area increased during the rapid growth phase followed by a sharp decrease to a relatively constant value dependent on the agitation conditions. The higher the speed, the lower the projected area for a given impeller type. The proportion by volume of hyphal vacuoles and empty regions decreased with speed, possibly due to fragmentation in the vacuolated regions. The specific penicillin production rate was generally higher with lower impeller speed for a given impeller type. The highest value of penicillin production as well as its rate was obtained using the Rushton turbine impeller at the lowest speed. At given P/VL, changes in morphology, specific growth rate, and specific penicillin production rate depended on impeller geometry. The morphological data could be correlated with either tip speed or the "energy dissipation/circulation function," but a reasonable correlation of the specific growth rate and specific production rate was only possible with the latter. Copyright 1998 John Wiley & Sons, Inc.     

In situ filtration of Anchusa officinalis culture in a cell-retention stirred tank bioreactor

Summary The effect of agitation and aeration on filtration of Anchusa officinalis culture in a stirred tank bioreactor integrated with an internal filter unit was investigated. Increases in suction head of the pump that drove the filtration process were measured at impeller speeds of 100 and 200 rpm. Surprisingly, suction head attained at 200 rpm was about 40% higher than at 100 rpm. Direct observation of the cake deposition process in the reactor using a dilute cell suspension revealed that the filter cake formed at 100 rpm was thicker, but less compact. Aeration at 0.4 vvm was shown to have little effect on the filtration rate, since the bulk fluid flow was dominated by the impeller hydrodynamics. The initial flux can be recovered by filter backwashing with compressed air at a flow rate of 0.6 vvm for a duration of 5 minutes.     

Production of manganese peroxidase by pellet culture of the lignin-degrading basidiomycete, Pleurotus ostreatus

Pleurotus ostreatus No. 42 produced the ligninolytic enzymes, manganese peroxidase (MnP) and laccase, in agitation culture in glucose/peptone/wheat-bran medium. Formation of mycelial pellets 1-2 mm in diameter was essential for the production of MnP; and the concentration of dissolved oxygen in the culture medium greatly influenced the production of MnP, a concentration over 5 ppm being necessary for MnP production. The maximal activity of MnP was obtained on days 7-9 of culture, after the consumption of nutrient glucose. Introduction of oxygen from the start of the cultivation caused large pellet formation, which resulted in a low MnP activity level. P. ostreatus No. 42 produced two MnP isozymes in agitation culture. The major isozyme, F-2, was 36.4 kDa and had a pI of 3.95. The MnP characteristics, Km values, dependence on Mn2+ and optimum pH showed the similarity between this isozyme and MnP 3, which was produced under different culture conditions. Analysis of the N-terminal amino acid sequence indicated the close similarity of F-2 to MnP 3.     

Scale-up synthesis of lipase-catalyzed palm esters in stirred-tank reactor

Lipase-catalyzed production of palm esters by alcoholysis of palm oil with oleyl alcohol in n-hexane was performed in 2L stirred-tank reactor (STR). Investigation on the performance of reactor operation was carried out in batch mode STR with single impeller mounted on the centrally located shaft. Rushton turbine (RT) impellers provide the highest reaction yield (95.8%) at lower agitation speed as compared to AL-hydrofoil (AL-H) and 2-bladed elephant ear (EE) impellers. Homogenous enzyme particles suspension was obtained at 250 rpm by using RT impeller. At higher impeller speed, the shear effect on the enzyme particles caused by agitation has decreased the reaction performance. Palm esters reaction mixture in STR follows Newtons' law due to the linear relation between the shear stress (tau) and shear rate (dupsilon/dy). High stability of Lipozyme RM IM was observed as shown by its ability to be repeatedly used to give high percentage yield (79%) of palm esters even after 15 cycles of reaction. The process was successfully scale-up to 75 L STR (50 L working volume) based on a constant impeller tip speed approach, which gave the yield of 97.2% after 5h reaction time.     

Agitation,aeration and shear stress as key factors in inulinase production by Kluyveromyces marxianus

Factorial design and response surface analyses were used to optimize the production of inulinase (2,1-β-d-fructan fructanohydrolase, EC 3.2.1.7) by Kluyveromyces marxianus ATCC 16045, using sucrose as carbon source. Effects of aeration, agitation and type of impeller (disk turbine, marine, pitched blade) were studied in a batch stirred reactor. Two factorial designs 2² were carried out. Agitation speed varied from 50 to 550 rpm (revolution per minute), aeration rate from 0.5 to 2.0 vvm (air volume/broth volume·minute). It has been shown that the enzyme production was strongly influenced by mixing conditions, while aeration rate was shown to be less significant. Additionally, the increase in the agitation speed is limited by the death rate, which increases drastically at high speeds, lowering the enzyme production. Also, the impeller type has significant influence in the production, the disk impeller at 450 rpm and aeration at 1.0 vvm led to an activity of 121 UI/mL, while the pitched blade was shown to be the best impeller for this process, leading to the best production, 176 UI/mL, at 450 rpm and 1.0 vvm. The maximum shear stress for inulinase production was about 0.22 Pa, since higher values cause higher cell death rates, affecting the enzyme production. The same results were confirmed with another microorganism, which was also sensible to shear stress. Therefore, it has been concluded that in some cases, mainly when the microorganism is sensible to shear stress, the interaction between mass transfer and mechanical stress should be considered in scale up processes.     

A comprehensive comparison of mixing, mass transfer, Chinese hamster ovary cell growth, and antibody production using Rushton turbine and marine impellers

Large scale production of monoclonal antibodies has been accomplished using bioreactors with different length to diameter ratios, and diverse impeller and sparger designs. The differences in these physical attributes often result in dissimilar mass transfer, mechanical stresses due to turbulence and mixing inside the bioreactor that may lead to disparities in cell growth and antibody production. A rational analysis of impeller design parameters on cell growth, protein expression levels and subsequent antibody production is needed to understand such differences. The purpose of this study was to examine the impact of Rushton turbine and marine impeller designs on Chinese hamster ovary (CHO) cell growth and metabolism, and antibody production and quality. Experiments to evaluate mass transfer and mixing characteristics were conducted to determine if the nutrient requirements of the culture would be met. The analysis of mixing times indicated significant differences between marine and Rushton turbine impellers at the same power input per unit volume of liquid (P/V). However, no significant differences were observed between the two impellers at constant P/V with respect to oxygen and carbon dioxide mass transfer properties. Experiments were conducted with CHO cells to determine the impact of different flow patterns arising from the use of different impellers on cell growth, metabolism and antibody production. The analysis of cell culture data did not indicate any significant differences in any of the measured or calculated variables between marine and Rushton turbine impellers. More importantly, this study was able to demonstrate that the quality of the antibody was not altered with a change in the impeller geometry.     

The influence of preculture on the process performance of penicillin V production in a 100-l air-lift tower loop reactor

Summary The influence of stirrer speed in the third preculture on the performance of penicillin V production by Penicillium chrysogenum in complex medium in a 100-l air-lift tower loop reactor was investigated. The process performance in the main culture was improved by increasing the stirrer speed from 500 to 750 rpm: the pellet size was reduced to half, the cell growth was influenced only slightly, but the production phase was extended considerably, and the final penicillin concentration was increased from 5.1 g 1^-1 to 10.4 g 1^-1.