Photolithotrophic cultivation of Laminaria saccharina gametophyte cells in a stirred-tank bioreactor

Filamentous cell cultures derived from female gametophytes of the temperate brown macroalga Laminaria saccharina were photolithotrophically cultivated in artificial seawater medium within an illuminated 1.3-L stirred-tank bioreactor at 13 degrees C using CO(2) in air as the carbon source. A Monod model adequately described light-saturated growth. The apparent half-saturation constant (K(o)) was 23 muE/m(2)-s, and maximum specific growth rate was 0.15 day(-1). At a constant inoculation cell density of 50 mg DCW/L, biomass productivity after 26 days of cultivation increased from 630 mg DCW/L at 18 muE/m(2)-s to 890 mg DCW/L at 228 muE/m(2)-s. At 98 muE/m(2)-s, 1.1 vvm aeration rate, and 250 rpm impeller speed, the CO(2) transfer rates (CO(2) TRs) and CO(2) consumption rates (r(co(2) )) were determined over the cultivation period. At peak CO(2) demand, the maximum CO(2) TR was 0.19 mmol CO(2)/L-h, but r(co(2) ) was only 0.15 mmol CO(2)/L-h, implying that the culture was not CO(2) transport limited. This is the first reported bioreactor cultivation study of cell cultures derived from a macrophytic marine alga. (c) 1995 John Wiley & Sons, Inc.     

Characterization of agitation environments in 250 ml spinner vessel, 3 L,and 20 L reactor vessels used for animal cell microcarrier culture

Three dimensional particle tracking velocimetry (3-D PTV) was used to characterize the flow fields in the impeller region of three microcarrier reactor vessels. Three typical cell culture bioreactors were chosen: 250 ml small-scale spinner vessels, 3 L bench-scale reactor, and 20 L medium-scale reactor. Conditions studied correspond to the actual operating conditions in industrial setting and were determined based on the current scale-up paradigm: the Kolmogorov eddy length criterion. In this paper we present characterization of hydrodynamics on the basis of flow structures produced because of agitation. Flow structures were determined from 3-D mean velocity results obtained using 3-D PTV. Although the impellers used in 3 L and 20 L reactors were almost identical, the flow structures produced in the two reactors differed considerably. Results indicate that near geometric scale up does not necessarily amount to scale-up of flow patterns and indicates that intensity as well as distribution of energy may vary considerably during such a scale-up.     

Replacement of immobilised cell bioreactors by smaller immobilised enzyme bioreactors: unique-outcome predictability for cytochromes P450 isoforms?

Both immobilized enzymes (IME) and immobilized cells (IMC) are acceptable as the biocatalysts essential for the attainment of rapid rates of bioconversion in bioreactors. IMC can display higher than expected cellular permeability whilst IME can exhibit high catalytic constant (k_cat/K_m) despite limitations on substrate utilisation due to an unstired diffusion layer of solvent. Scale-down switching from IMC to IME involves the replacement of high-volume biotechnology by low-volume biotechnology, sometimes using IME mimics in partially non-aqueous solvent systems. Highly purified IME systems covalently immobilised to particles of, for instance, microcrystalline cellulose or porous glass, can retain both the hydrophilic and hydrophobic intermediate products in situ of the chosen sequence of enzyme reactions. These bioconversions, therefore, are as efficient as those with IMC where enzymes are often particle- or membrane-bound so that even hydrophilic intermediates are not released rapidly into solution. This mimicry of in vivo biosynthetic pathways that are compartmentalised in vivo (e.g. of lysosomes, mitochondria and endoplasmic reticulum) can replace larger IMC by IME especially in application of up to 2700 cytochromes P450 isoforms in bioprocessing. In silico investigation of appropriate model IME systems, in comparison with IMC systems, will be needed to define the optimal bioreactor configuration and parameters of operation, such as pH, T and oxygen mass transfer rate (OTR). The application solely of hazop (applied hazard and operability concepts) may, nevertheless, not be recommended to replace fully the in silico and real-lab pilot-scale and scale studies. Here, food-safe bioprocessing has to be achieved without incorporation of recognised biohazards; especially in the form of unacceptable levels of toxic metals that promote a risk-analysis uncertainty.     

Oxygen gradients in animal-cell bioreactors

An estimation is made of oxygen gradients in animal-cell bioreactors, using straightforward engineering calculations. Three types of bioreactor are considered: stirred vessel, bubble column and air lift, of sizes between 0.01 and 10 m³. First, the gradient is estimated in the stagnant layer surrounding a cell (15 m), a microcarrier (185 m) with 300 cells attached to it, a macroporous support (1.25 mm) containing 185,00 cells and one (6 mm) containing 4.25 million cells. It is assumed that oxygen consumption is 10^–16 mole O₂·cell^–1·s^–1, while mass transfer coefficients are obtained from Sherwood relations. Circulation and liquid-retention times of the bioreactors are compared with the oxygen-exhaust times of suspensions with 10¹², 10¹³ and 10¹⁴ cells/m³ to estimate if oxygen gradients are likely to exist in the bulk-liquid phase. Finally, the gradient in the liquid film surrounding air bubbles is estimated using k _l A-values obtained from empirical correlations. It is clear from all these estimations that in many situations severe gradients can be expected. The question remains, however, whether gradients should be avoided as much as possible, or may be tolerated to a certain extent or even created on purpose because of possible beneficial effects.     

Strategies to overcome foaming and wall-growth during the cultivation of Morinda elliptica cell suspension culture in a stirred-tank bioreactor

Strategies to overcome foaming and wall-growth during the cultivation of Morinda elliptica (Rubiaceae) cell suspension cultures in a stirred-tank bioreactor are described. Of all the strategies applied, only bubble-free aeration was successful in eliminating foaming by 100%. Despite the foaming effect of around 40% in G medium strategy with 0.012% (v/v) antifoam, the maximum dry cell weight attained (19.2 g l^-1) and anthraquinone (AQ) content (4.0 mg g^-1 DW) was nearly three times higher than that achieved in cultivation using 0.025% (v/v) antifoam. For continuous cell growth, the effect of inoculum age should also be considered when anti-foam is to be added. P medium strategy, without antifoam addition, not only promoted both growth (18 g l^-1) and AQ production (9.8 mg g^-1 DW), but also resulted in lower foaming and wall-growth (below 30% level), and higher foaming reduction (30–40%). This revised version was published online in June 2006 with corrections to the Cover Date.     

Ajmalicine production by cell cultures of Catharanthus roseus: from shake flask to bioreactor

The productivity of a cell culture for the production of a secondary metabolite is defined by three factors: specific growth rate, specific product formation rate, and biomass concentration during production. The effect of scaling-up from shake flask to bioreactor on growth and production and the effect of increasing the biomass concentration were investigated for the production of ajmalicine by Catharanthus roseus cell suspensions. Growth of biomass was not affected by the type of culture vessel. Growth, carbohydrate storage, glucose and oxygen consumption, and the carbon dioxide production could be predicted rather well by a structured model with the internal phosphate and the external glucose concentration as the controlling factors. The production of ajmalicine on production medium in a shake flask was not reproduced in a bioreactor. The production could be restored by creating a gas regime in the bioreactor comparable to that in a shake flask. Increasing the biomass concentration both in a shake flask and in a stirred fermenter decreased the ajmalicine production rate. This effect could be removed partly by controlling the oxygen concentration in the more dense culture at 85% air saturation.     

Scale-up of a pan-coating process

The purpose of this work was to develop a practical scale-up model for a solvent-based pan-coating process. Practical scale-up rules to determine the key parameters (pan load, pan speed, spray rate, air flow) required to control the process are proposed. The proposed scale-up rules are based on a macroscopic evaluation of the coating process. Implementation of these rules does not require complex experimentation or prediction of model parameters. The proposed scale-up rules were tested by conducting coating scale-up and scale-down experiments on 24-inch and 52-inch Vector Hi-coaters. The data demonstrate that using these rules led to similar cumulative drug release profiles (f2≫50; and P Analysis of Variance [P _ANOVA]≫0.05 for cumulative percentage of drug released after 12 hours [Cum 12] from tablets made at 24- and 52-inch scales. Membrane characteristics such as opacity and roughness were also similar across the 2 scales. The effects of the key process variables on coat weight uniformity and membrane characteristics were also studied. Pan speed was found to be the most significant factor related to coating uniformity. Spray droplet size was found to affect the membrane roughness significantly, whereas opacity was affected by the drying capacity.     

Comparative evaluation of modified bioreactors for enhancement of growth and secondary metabolite biosynthesis usingPanax ginseng hairy roots

Hairy root cultures have demonstrated great promise in terms of their biosynthetic capability toward the production of secondary metabolites, but continue to constitute a major challenge with regard to large-scale cultures. In order to assess the possibility of conducting mass production of biomass, and the extraction of useful metabolites fromPanax ginseng. P. ginseng hairy roots, transformed byRhizobium rhizogenes KCTC 2744, were used in bioreactors of different types and sizes. The most effective mass production of hairy roots was achieved in several differently sized air bubble bioreactors compared to all other bioreactor types. Hairy root growth was enhanced by aeration, and the production increased with increasing aeration rate in a 1 L bioreactor culture. It was determined that the hairy root growth rate could be substantially enhanced by increases in the aeration rate upto 0.5 wm, but at aeration rates above 0.5 wm, only slight promotions in growth rates were observed. In 20 L air bubble bioreactors, with a variety of inoculum sizes, the hairy roots exhibited the most robust growth rates with an inoculum size of 0.1% (w/v), within the range 0.1 to 0.7% (w/v). The specific growth rates of the hairy roots decreased with increases in the inoculum size.     

A scalable membrane gradostat reactor for enzyme production using Phanerochaete chrysosporium

This is the first demonstration of process scale-up of a membrane gradostat reactor for continuous enzyme production using Phanerochaete chrysosporium ME446. The fungus was immobilised by reverse filtration on to externally unskinned, ultrafiltration capillary membranes and then nutrient gradients were induced across the biofilm. A 10-fold scale-up from a single capillary bioreactor to a 2.4 l multi-capillary unit resulted in a 7-fold increase in enzyme productivity with a peak at 209 U l^–1 d^–1. Subsequent scale effects on the spore distribution, continuous manganese peroxidase production profile and biofilm development are discussed.     

利用DNS法快速分析及优化柚皮苷的酶解过程

【目的】建立采用3,5-二硝基水杨酸(DNS)法快速测定柚皮苷水解率的方法,并利用该方法对柚苷酶催化水解柚皮苷生成柚皮素的反应过程进行优化研究。【方法】利用棘孢曲霉JMUdb058发酵得到的柚苷酶催化水解柚皮苷,采用DNS法对柚皮苷酶解过程中还原糖的生成量进行分析,经过换算得到柚皮苷的水解率,并在此基础上通过单因素实验优化柚皮苷的酶解过程。【结果】在柚皮苷的水解过程中,还原糖的生成量与柚皮苷的水解量及柚皮素的生成量均呈现出良好的线性关系,因此可利用DNS法测定体系中还原糖的生成量,并通过换算得到柚皮素的生成量。利用该方法优化柚皮苷的酶解过程得到柚苷酶转化柚皮苷的最适温度为50°C、pH为5.0、酶用量为8 U/mL、底物浓度为0.2 g/100 mL。在此条件下,柚皮苷酶解150 min后可达到平衡,此时其水解率为85%。通过Lineweaver-Burk双倒数作图法测得Km为