Gas holdup, power consumption, and oxygen absorption coefficient in a stirred-tank fermentor under foam control

For a laboratory stirred-tank fermentor (STF) with foaming system of 0.5M sulfite solution containing an anionic soft detergent, the performing of a foam-breaking apparatus with a rotating disk (FARD)fitted to the STF was evaluated. The gas holdup in a mechanical foam-control system (MFS), i.e., the stirred-tank fermentor with the rotating disk foambreaker, was confirmed to be larger than that in a nonfoaming system (NS), i.e., the STF with an antifoam agent added. The agitation power in the mechanical foam control system was found to be smaller compared with the agitation power in the nonfoaming system, due to the increased gas holdup. Comparison of the oxygen absorption coefficient between the mechanical foam control system and the nonfoaming system in terms of the specific power input also demonstrated the superiority of the mechanical foam control system, not only in oxygen transfer performance but also in power input economy.     

Scale-up on basis of structured mixing models: A new concept

A new scale-up concept based upon mixing models for bioreactors equipped with Rushton turbines using the tanks-in-series concept is presented. The physical mixing model includes four adjustable parameters, i.e., radial and axial circulation time, number of ideally mixed elements in one cascade, and the volume of the ideally mixed turbine region. The values of the model parameters were adjusted with the application of a modified Monte-Carlo optimization method, which fitted the simulated response function to the experimental curve. The number of cascade elements turned out to be constant (N = 4). The model parameter radial circulation time is in good agreement with the one obtained by the pumping capacity. In case of remaining parameters a first or second order formal equation was developed, including four operational parameters (stirring and aeration intensity, scale, viscosity). This concept can be extended to several other types of bioreactors as well, and it seems to be a suitable tool to compare the bioprocess performance of different types of bioreactors. (c) 1994 John Wiley & Sons, Inc.     

Lipase-catalyzed selective synthesis of monolauroyl maltose using continuous stirred tank reactor

Monolauroyl maltose was synthesized by an immobilized lipase that catalyzed condensation of maltose and lauric acid in acetone using a batch reactor or a continuous stirred tank reactor. Mono- and di-lauroyl maltoses were identified by FT-IR, ¹H NMR, ¹³C NMR and MS. Monolauroyl maltose was selectively synthesized in a continuous stirred tank reactor and no diester was detected. The highest concentration of monolauroyl maltose at 28 mmol/l was obtained in 250 ml acetone when maltose was added at 4 g/d and the molar ratio of lauric acid to maltose was fixed at 4:1 at a flow rate of 0.15 ml/min for both influx and effluent without supplement of fresh molecular sieve.     

Optimization of exopolysaccharide production from Armillaria mellea in submerged cultures

Aims: To study the optimization of submerged culture conditions for exopolysaccharide (EPS) production by Armillaria mellea in shake‐flask cultures and also to evaluate the performance of an optimized culture medium in a 5‐l stirred tank fermenter. Methods and Results: Shake flask cultures for EPS optimal nutritional production contained having the following composition (in g l^?1): glucose 40, yeast extract 3, KH₂PO₄ 4 and MgSO₄ 2 at an optimal temperature of 22°C and an initial of pH 4·0. The optimal culture medium was then cultivated in a 5‐l stirred tank fermenter at 1 vvm (volume of aeration per volume of bioreactor per min) aeration rate, 150 rev min^?1 agitation speed, controlled pH 4·0 and 22°C. In the optimal culture medium, the maximum EPS production in a 5‐l stirred tank fermenter was 588 mg l^?1, c. twice as great as that in the basal medium. The maximum productivity for EPS (Q_p) and product yield (Y_P/S) were 42·02 mg l^?1 d^?1 and 26·89 mg g^?1, respectively. Conclusions: The optimal culture conditions we proposed in this study enhanced the EPS production of A. mellea from submerged cultures. Significance and Impact of the Study: The optimal culturing conditions we have found will be a suitable starting point for a scale‐up of the fermentation process, helping to develop the production of related medicines and health foods from A. mellea.     

Fermentation pH in stirred tank and air-lift bioreactors affects phytase secretion by Aspergillus japonicus differently but not the particle size

Abstract

Phytases are mainly produced by filamentous fungi and have great potential for biotechnological use in animal feed treatment, because this enzyme hydrolyzes ester bonds of the phytic acid releasing inositol and inorganic phosphate. The aim of this work was to evaluate the effect of pH on the production of phytase by Aspergillus japonicus in two different bioreactors, known to have different mixing patterns—stirred tank and air-lift bioreactors. The maximum phytase production—53 U/mL—was obtained at 120 h in the stirred tank while in the air-lift the maximum value was 41 U/mL, observed at 144 h. In fermentations evaluated at controlled pH values (3.5, 6.0, and 7.5), the stirred tank was more efficient for production of phytase than the air-lift. Under these conditions, the highest value was measured at 24 h and pH 3.5. These results were not closely related to fungi particle size, because hyphae with a similar diameter (0.51–0.63 mm) and sphericity (0.78–0.87 mm) secreted different amounts of phytase under the conditions studied.     

Production of optically pure L-alanine in batch and continuous stirred tank reactors using immobilized Pseudomonas sp.

A process to obtain optically pure l-alanine has been developed using batch and continuous stirred tank reactors with a new l-aminoacylase-producing bacterium Pseudomonas sp. BA2 immobilized in calcium alginate beads coated with glutaraldehyde. The maximum production of l-alanine in a continuous stirred tank reactor was 11.26 g after 2 days of operation which is higher than that previously reported.     

The Freter model: A simple model of biofilm formation

A simple, conceptual model of biofilm formation, due to R. Freter et al. (1983), is studied analytically and numerically in both CSTR and PFR. Two steady state regimes are identified, namely, the complete washout of the microbes from the reactor and the successful colonization of both the wall and bulk fluid. One of these is stable for any particular set of parameter values and sharp and explicit conditions are given for the stability of each. The effects of adding an anti-microbial agent to the CSTR are examined.Supported by NSF Grant DMS 0107439 and UTA Grant REP 14748717Supported by NSF Grant DMS 0107160     

Alkaloid production by plant cell cultures of Holarrhena antidysenterica: II. Effect of precursor feeding and cultivation in stirred tank bioreactor

Precursor feeding strategy for increasing the yield of conessine, a steroidal alkaloid of Holarrhena antidysenterica, was established in cell suspension culture. A total of 50 mg/L added cholesterol was converted into 43 mg/L of alkaloid, 90% of which constituted the conessine. By applying the precursor feeding policy to the cell suspension culture in modified Murashige and Skoog (MS) medium, a total of 143 mg/L of alkaloid was produced in 8 days. In this way the alkaloid content of the cells was increased more than six times compared to that obtained in the standard MS medium. The steps leading to biotransformation of cholesterol into alkaloids were unaffected by phosphate. The shake flask data were successfully transferred to a bench scale 6-L stirred tank bioreactor in which the specific biosynthetic rate of alkaloid production was 110 mg/100 g dry cell weight per day, about 160 times higher than that of whole plant.     

Performance Of A Membrane Bioreactor For Enzymatic Transesterification: Characterization And Comparison With A Batch Stirred Tank Reactor

A membrane bioreactor containing cutinase microencapsulated in reversed micelles of AOT/isooctane was used to perform the alcoholysis of butyl acetate with hexanol. The membrane used was a tubular ceramic membrane with a cut-off of 15, 000 Da. Membrane characterization involved two parts: structure definition and operational properties. The former included membrane imaging to define the average membrane pore size. With the values obtained, characterization proceeded through the prediction of permeability and number of pores. The separation properties of the membrane were evaluated with the determination of rejection coefficients, based on transmission experiments, for all system components, including the substrates, products and the biocatalyst. The performance of the membrane bioreactor (MBR) was compared with the results obtained in a batch stirred tank reactor (BSTR) using the normalized residence time concept. The MBR operated as a differential reactor as theoretical treatment of experimental data demonstrated.     

Studies on the Bacterial Formation of Peptide Antibiotic,Colistin

The biosynthetic mechanism of 6-methyloctanoic and isooctanoic acids, which are present in the amide linkage with the α-amino group of the terminal α, γ-diaminobutyric acid residue of colistin A and B, respectively was investigated. From the isotopic experiments using isoleucine-U-¹⁴C, valine-U-¹⁴C and acetic acid-2-¹⁴C, it was concluded that 6-methyloctanoic and isooctanoic acids were derived from isoleucine and valine, respectively.

Amino acids pooled in colistin-producing cells grown in the synthetic medium were abundant in isoleucine, valine and leucine, which were probable precursors of the abovedescribed fatty acid components of colistin and cellular fatty acids. On the other hand, 6-methyloctanoic and isooctanoic acids were not found in the cellular fatty acids, while C-15 and C-16 branched chain fatty acids usually found in Bacillus sp. were abundantly contained in the cells, indifferently of an improved capacity of colistin formation.     

A comparison of orbitally‐shaken and stirred‐tank bioreactors: pH modulation and bioreactor type affect CHO cell growth and protein glycosylation

Orbitally shaken bioreactors (OSRs) support the suspension cultivation of animal cells at volumetric scales up to 200 L and are a potential alternative to stirred‐tank bioreactors (STRs) due to their rapid and homogeneous mixing and high oxygen transfer rate. In this study, a Chinese hamster ovary cell line producing a recombinant antibody was cultivated in a 5 L OSR and a 3 L STR, both operated with or without pH control. Effects of bioreactor type and pH control on cell growth and metabolism and on recombinant protein production and glycosylation were determined. In pH‐controlled bioreactors, the glucose consumption and lactate production rates were higher relative to cultures grown in bioreactors without pH control. The cell density and viability were higher in the OSRs than in the STRs, either with or without pH control. Volumetric recombinant antibody yields were not affected by the process conditions, and a glycan analysis of the antibody by mass spectrometry did not reveal major process‐dependent differences in the galactosylation index. The results demonstrated that OSRs are suitable for recombinant protein production from suspension‐adapted animal cells. © 2016 American Institute of Chemical Engineers Biotechnol. Prog., 32:1174–1180, 2016