• KSBB Journal
• /
• v.13 no.6
• /
• pp.700-705
• /
• 1998

Studies were made to investigate effects of the scale-up of stirred tank bioreactors on cell growth and alkaloids production for suspension cultures of Eschscholtzia californica. In the 1.5 L STR, cell lysis was observed at 110 rpm or higher agitation speed. The agitation speed of 30 L STR was 43.7 rpm to maintain the same shear stress developed in 1.5 L STR of 100 rpm. As a result of scale-up from 1.5 L to 30 L STR, the specific growth rate was decreased from 0.12 to 0.07 day-1. The alkaloids productivity was also decreased from 0.24 to 0.14 mg/L-day. Changes of mixing performance and oxygen transfer were studied to explain the decrease of cell growth and alkaloids production. Decreased oxygen transfer rate coefficient(KLa) and increased mixing time by the scale-up was observed at various aeration rates.

• Journal of Microbiology and Biotechnology
• /
• v.19 no.2
• /
• pp.167-171
• /
• 2009

The effects of culture conditions on succinic acid production and its possible scale-up have been studied. Mannheimia succiniciproducens LPK7, engineered for enhanced production of succinic acid and reduced by-product secretion, was used for the experiments. Mannheimia succiniciproducens LPK7 is a knock-out strain of wild type deficient in the ldhA, pflB, and pta-ackA genes, and is derived from Mannheimia succiniciproducens MBEL55E. Process optimization of factors including optimal temperature, pH, carbon source, and nitrogen source was performed to enhance the production of succinic acid in flasks. To observe scale-up effects, batch fermentation was carried out at various working volumes. At a working volume of 7.0 l, the final succinic acid concentration and yield were 15.4g/l and 0.86g/g. This result shows similar amount of succinic acid obtained in lab-scale fermentation, and it is possible to scale up to larger fermentors without major problems.

• Biotechnology and Bioprocess Engineering:BBE
• /
• v.8 no.5
• /
• pp.303-305
• /
• 2003

Scale-up of hirudin production from Saccharomyces cerevisiae from bench-scale to pilot-scale was carried out based on constant volumetric oxygen transfer coefficient (K$\sub$L/a). Fed-batch mode of cultivation using step-wise feeding strategy of galactose was employed for the production of hirudin in a 30-L and a 300-L pilot-scale fermentor. The final hirudin concentrations were achieved 390 mg/L and 286.1 mg/L, and the volumetric productivities were 80.4% and 90.7% with the 30-L and 300-L fermentors, respectively, compared to the productivity of the 5-L bench-scale fermentor.

• Journal of Plant Biotechnology
• /
• v.3 no.2
• /
• pp.59-66
• /
• 2001

Photoautotrophic micropropagation systems do not include sugar in the culture media. This characteristic provides advantages to scale up the micropropagation systems comparing photomixotrophic micropropagation systems. A closed, large-scale photoautotrophic micro-propagation for transplant production system has been developed at Chiba University, Japan. New concepts and technologies were adapted to produce high quality transplants at minimum usage of resources, and as scheduled. Newly developed software for production management was used to enhance the efficiency of the transplant production system. Currently, virus-free transplants of sweetpotato (Ipomoea batatas (L.) Lam.) are vegetatively propagated and produced under sterilized conditions in this system. This system can also be used for production of transplants of any other species including horticultural and woody plants with a minimum of modification.

• Journal of Microbiology and Biotechnology
• /
• v.15 no.1
• /
• pp.1-6
• /
• 2005

Optimal criterion for the scale-up production of schizophyllan, a fungal polysaccharide secreted by Schizophyllum commune, was investigated. For the production of the polysaccharide in a 150-l bioreactor, the culture conditions optimized in a 15-l bioreactor were applied to a 150-l bioreactor with scale-up process, by changing impeller speed and airflow rate. The optimized impeller speed in the 15-l bioreactor was 50 rpm in a technical medium based on barley. For establishment of the scale-up process, 3 kinds of criteria were used while the gas throughput number was kept constant, as follows; constant volume-related power input, constant tip speed of stirrer, and constant Reynolds number. In the 150-l bioreactor, the highest values for the maximum specific growth rate (1.17/day) and productivity (0.63 g/L${\cdot}$day) were achieved in the culture condition from constant volumerelated power input criterion.

• KSBB Journal
• /
• v.26 no.4
• /
• pp.357-364
• /
• 2011

This study was carried out to investigate the effects of agitation, aeration and scale-up on the mycelial growth, exo-polysaccharide (EPS) production, and mycelial morphology in the liquid culture of Ganoderma lucidum. A correlation between roughness and operating variables was also studied to scale-up the liquid culture of G. lucidum in a jar fermenter. When the agitation speed or aeration rate increased, the morphological form was changed from rough pellet to smooth pellet form. Increase of the agitation and aeration reduced the mycelial roughness. On the other hand, in the case of pellet size, it was not affected by aeration. The higher EPS production was obtained at approximately 17% of roughness and mycelial pellet size of 3~5 mm. The morphology at each fermenter was closely correlated with kLa value, and it was found that similarity of morphology would be used as a criteria of scale-up for liquid culture of G. lucidum.

• Journal of Microbiology and Biotechnology
• /
• v.20 no.4
• /
• pp.763-766
• /
• 2010

An efficient and simple fermentation process was developed for the production of ${\gamma}$-aminobutyric acid (GABA) by Lactobacillus sakei B2-16. When the L. sakei B2-16 was cultivated in the rice bran extracts medium containing 4% sucrose, 1% yeast extract, and 12% monosodium glutamate, the maximum GABA concentration reached 660.0 mM with 100% conversion yield, showing the 2.4- fold higher GABA concentration compared with the modified MRS medium without the rice bran extracts. The GABA production was scaled-up from a laboratory scale (5 l) to a pilot (300 l) and a plant (5,000 l) scale to investigate the application possibility of GABA production to industrial fields. The production yields at the pilot and plant scales were similar to the laboratory scale using rice bran extracts medium, which could be effective for the low-cost production of GABA.

• Journal of the Korean Society of Manufacturing Process Engineers
• /
• v.17 no.1
• /
• pp.48-56
• /
• 2018

Due to the growing concerns of energy resource depletion and environmental destruction, the mass production of microalgae has been studied. The scale-up of a photobioreactor (PBR) is required for the mass production of biomass. In this paper, the geometric parameters and oxygen transfer rate (OTR) are considered, to scale up a flat panel photobioreactor (FP PBR). The PBR is designed using the goal-driven optimization (GDO) method to accomplish the scale-up. The local sensitivity of each output parameter with respect to the input parameter is analyzed through the design of experiment (DOE), and the design candidates are evaluated with the screening sampling method. The volumetric mass transfer coefficient is measured by the dynamic method.

• Journal of Microbiology and Biotechnology
• /
• v.23 no.10
• /
• pp.1445-1453
• /
• 2013

The scale-up criterion of constant oxygen mass transfer coefficient ($k_La$) was applied for the production of itaconic acid (IA) in a 50 L pilot-scale fermentor by the fungal cells of Aspergillus terreus. Various operating conditions were examined to collect as many $k_La$ data as possible by adjusting the stirring speed and aeration rate in both 5 L and 50 L fermentor systems. In the fermentations performed with the 5 L fermentor, the highest IA production was obtained under the operating conditions of 200 rpm and 1.5 vvm. Accordingly, we intended to find out parallel agitation and aeration rates in the 50 L fermentor system, under which the $k_La$ value measured was almost identical to that ($0.02sec^{-1}$) of the 5 L system. The conditions of 180 rpm and 0.5 vvm in the 50 L system turned out to be optimal for providing almost the same volumetric amount of dissolved oxygen (DO) into the fermentor, without causing shear damage to the producing cells due to excessive agitation. Practically identical fermentation physiologies were observed in both fermentations performed under those respective operating conditions, as demonstrated by nearly the same values of volumetric ($Q_p$) and specific ($q_p$) IA production rates, IA production yield ($Y_{p/s}$), and specific growth rate (${\mu}$). Specifically, the negligible difference of the specific growth rate (${\mu}$) between the two cultures (i.e., $0.029h^{-1}$ vs. $0.031h^{-1}$) was notable, considering the fact that ${\mu}$ normally has a significant influence on $q_p$ in the biosynthesis of secondary metabolites such as itaconic acid.

• Journal of Microbiology and Biotechnology
• /
• v.21 no.6
• /
• pp.604-612
• /
• 2011

Beauveria bassiana SFB-205 supernatant can effectively control cotton aphid populations, which is closely associated with its chitinase activity. The present work extends to optimizing a culture medium to produce more efficacious supernatant in flask conditions, followed by scale-up in 7 L, 300 L and 1.2 KL fermentors with the parameter of chitinase. In flask conditions, a combination of soluble starch and yeast extract produced the greatest amount of chitinase (5.1 units/ml) and its supernatant had the highest aphicidal activity. An optimal quantitative combination of the two substrates, estimated by a response surface method, enabled the supernatant to have 15.7 units/ml of chitinase activity and 3.7 ml/l of median lethal concentration ($LC_{50}$) of toxicity against cotton aphid adults in laboratory conditions. In the scale-up conditions, overall supernatant had 25-28 units/ml of chitinase activity. Decrease in pH and limitation of dissolved oxygen (DO) during cultures were significantly related to the yield of chitinase. These results suggest that the substrate-dependent chitinase production can be background information for optimizing a culture medium, and pH and DO are critical factors in maximizing the production in scale-up conditions.