Two-stage culture process for improved production of ganoderic acid by liquid fermentation of higher fungus Ganoderma lucidum

Investigations on the impact of pellet size on the cellular oxygen uptake and accumulation of ganoderic acid (GA) suggested the favorable effect of oxygen limitation on GA formation by the higher fungus Ganoderma lucidum. A two-stage fermentation process was thus proposed for enhanced GA production by combining conventional shake-flask fermentation with static culture. A high cell density of 20.9 g of DW/L (DW = dry cell weight) was achieved through a 4-day shake-flask fermentation followed by a 12-day static culture. A change in the cell morphology and a decrease in the sugar consumption rate were observed during the static culture. The GA production in the new two-stage process was considerably enhanced with its content increased from 1.36 (control) to 3.19 mg/100 mg of DW, which was much higher than previously observed.     

Scale-up of centrifugal impeller bioreactor for hyperproduction of ginseng saponin and polysaccharide by high-density cultivation of panax notoginseng cells

Scale-up of a novel centrifugal impeller bioreactor (CIB) was demonstrated for production of valuable plant-specific secondary metabolites by high-density cell cultures. Initial kLa was identified to be a key factor affecting cell growth and production of ginseng saponin and polysaccharide by high-density cultivation of Panax notoginseng cells in a 3-L CIB. A high level of ginseng saponin and polysaccharide production was obtained at an initial kLa value of 30.2 h(-1). A maximum dry cell weight (DW) and production titer of ginseng saponin and polysaccharide reached 22.0 +/- 0.3, 1.5 +/- 0.1, and 2.7 +/- 0.2 g/L on day 15 with their corresponding productivity of 1140 +/- 42, 81 +/- 8, and 150 +/- 17 mg/(L.d), respectively. Based on initial kLa level, the CIB high-cell-density cultivation process was successfully scaled up from 3 L to 30 L. A maximum DW and production titer of ginseng saponin and polysaccharide in a 30-L CIB reached 25.5 +/- 0.5, 1.7 +/- 0.1, and 2.9 +/- 0.1 g/L (on day 15) at an initial kLa value of 28.7 h(-1), respectively, and their corresponding productivity was 1340 +/- 56, 91 +/- 9, and 164 +/- 15 mg/(L.d). Furthermore, by adopting a fed-batch cultivation strategy, a maximum DW and concentrations of total saponin and polysaccharide in the 30-L CIB were enhanced to 30.3 +/- 1.0, 2.1 +/- 0.1, and 3.5 +/- 0.2 g/L with their corresponding productivity of 1467 +/- 87, 102 +/- 13, and 179 +/- 18 mg/(L.d), respectively. The work suggests that the CIB may have great potential in large-scale high-density plant cell cultures for efficient production of useful secondary metabolites.     

Development of a helical-ribbon impeller bioreactor for high-density plant cell suspension culture

A double helical-ribbon impeller (HRI) bioreactor with a 11-L working volume was developed to grow high-density Catharanthus roseus cell suspensions. The rheological behavior of this suspension was found to be shear-thinning for concentrations higher than 12 to 15 g DW . L(-1). A granulated agar suspension of similar rheological properties was used as a model fluid for these suspensions. Mixing studies revealed that surface baffling and bottom profiling of the bioreactor and impeller speeds of 60 to 150 rpm ensured uniform mixing of suspensions. The HRI power requirement was found to increase singnificantly for agar suspensions higher than 13 g DW . L(-1), in conjunction with the effective viscosity increase. Oxygen transfer studies showed high apparent surface oxygen transfer coefficients (k(L)a approximately 4 to 45 h(-1)) from agar suspensions of 30 g DW . L(-1) to water and for mixing speeds ranging from 120 to 150 rpm. These high surface k(I)a values were ascribed to the flow pattern of this bioreactor configuration combined with surface bubble generation and entrainment in the liquid phase caused by the presence of the surface baffles. High-density C. roseus cell suspension cultures were successfully grown in this bioreactor without gas sparging. Up to 70% oxygen enrichment of the head space was required to ensure sufficient oxygen supply to the cultures so that dissolved oxygen concentration would remain above the critical level (>/=10% air saturation). The best mixing speed was 120 rpm. These cultures grew at the same rate ( approximately 0.4 d(-1)) and attained the same high biomass concentrations ( approximately 25 to 27 g DW . L(-1), 450 to 500 g filtered wet biomass . L(-1), and 92% to 100% settled wet biomass volume) as shake flask cultures. The scale-up potential of this bioreactor configuration is discussed.     

Microbial biomass production from rice straw hydrolysate in airlift bioreactors

Rice straw is a by-product of rice production, and a great bioresource as raw biomass material for manufacturing value-adding protein for animal feedstock, which has been paid more and more attention. In the present work, utilizing rice straw hydrolysate as a substrate for microbial biomass production in 11.5L external-loop airlift bioreactors was investigated. Rice straw hydrolysate obtained through acid-hydrolyzing rice straw was used for the culture of yeast Candida arborea AS1.257. The influences of gas flow rate, initial liquid volume, hole diameter of gas sparger and numbers of sieve plates on microbial biomass production were examined. The best results in the external-loop airlift bioreactor were obtained under 9.0 L initial liquid volume, 1.1 (v/v)/min gas flow rate during culture time of 0-24 h and 1.4 (v/v)/min gas flow rate of 24-48 h at 29+/-1 degrees C. The addition of the sieve plates in the riser of the external-loop airlift bioreactor increased productivity. After 48 h, under optimized operation conditions, crude protein productivity with one sieve and two sieves were 13.6 mg/mL and 13.7 mg/mL, respectively, comparing 12.7 mg/mL without sieves in the airlift bioreactor and 11.7 mg/mL in the in the 10-L mechanically stirred tank bioreactor. It is feasible to operate the external-loop airlift bioreactors and possible to reduce the production cost for microbial biomass production from the rice straw hydrolysate.     

Effect of mycelial morphology on ergothioneine production during liquid fermentation of Lentinula edodes

The morphological type of a microorganism generally influences its metabolite production. In the present study, we investigated the effects of the mycelial morphology of shiitake (Lentinula edodes) on the production of 2-mercaptohistidine trimethylbetaine (ergothioneine, ESH) during liquid fermentation. Analyses of the distribution of ESH in mycelial cells of different morphological types revealed that the ESH content of pellets obtained from the liquid fermentation media was much greater than the content in the free mycelia and clumps. The concentration of ESH in pellets on day 15 of liquid fermentation reached 0.79 mg/g dry weight (DW), which is approximately three times the concentration found in mycelia clumps (0.28 mg/g DW) and free mycelia (0.31 mg/g DW). Macroscopic image analysis of the development and morphological changes of the pellets during a liquid fermentation period of up to 25 days indicated that pellet growth showed a highly positive correlation with the increase in ESH concentration (r ² = 0.9851). A reduced agitation rate of 50 rpm for the culture medium was suitable for pellet formation and size enlargement. The results obtained in this work would be helpful in guiding the intentional manipulation of the distribution and enrichment of ESH in L. edodes through changes in liquid fermentation conditions.     

Investigation of acid proteinase biosynthesis by the fungus Humicola lutea 120-5 in an airlift bioreactor

Acid proteinase production using filamentous fungus Humicola lutea 120-5 was studied under batch and continuous fermentation conditions in an airlift bioreactor. A comparison with proteinase production by fungal cells, cultivated in stirred tank bioreactor was made. The process performance in both fermentation devices was similar with respect to substrate utilization, biomass, and enzyme concentration. Continuous acid proteinase production was achieved for 14 days at an optimal dilution rate of 0.05/h with maximum specific activity of 90 U/mg DW of mycelia and yield of 38 U/mg glucose. The volumetric productivity (50 U/ml. h) was approximately 3 times higher than this of the batch system. All continuous experiments were carried out without any bacterial contamination, due to the low pH (3.0-3.5) during the process. The "pellet" type growth of the fungus in the airlift reactor prevented the system from plugging with filaments.     

A novel centrifugal impeller bioreactor. II. Oxygen transfer and power consumption

The effects of the impeller configuration, aeration rate, and agitation speed on oxygen transfer coefficient K(L)a were studied in a newly designed centrifugal impeller bioreactor (5-L). The oxygen transfer rates in the novel bioreactor were also compared with those in a cell-lift bioreactor with comparable dimensions. The cell-lift impeller produced much higher surface oxygen transfer rates than the centrifugal one at an agitation speed over 200 rpm. This result was in good agreement with our observation that the cell-lift impeller produced much higher unfavorable turbulence. In addition, the experiments using granulated agar particles as pseudo plant cells indicated that the K(L)a value decreased steadily with an increase in agar particle concentration, and the centrifugal impeller still demonstrated a larger K(L)a than the cell lift up to a high pseudo cell concentration of 19.5 g dry weight (DW)/L (under 150 rpm and 0.20 vvm) or 22.3 g DW/L (under 200 rpm and 0.20 vvm). Furthermore, the correlation between power number and impeller Reynolds number for both the centrifugal and the cell-lift impellers was successfully obtained, which could be used for predicting the power input required by each impeller. From the results obtained, the centrifugal impeller bioreactor is expected to have great potential in its application to shear-sensitive biological systems.     

Production of glomus intraradices propagules, an arbuscular mycorrhizal fungus, in an airlift bioreactor

This work addresses the symbiotic culture of the arbuscular mycorrhizal (AM) fungus Glomus intraradices with Daucus carota hairy roots transformed by Agrobacterium rhizogenes, in two submerged culture systems: Petri dish and airlift bioreactor. AM fungi play an active role in plant nutrition and protection against plant pathogens. These fungi are obligate biotrophs as they depend on a host plant for their needs in carbohydrates. The effect of the mycorrhizal roots inoculum-to-medium volume ratio on the growth of both symbionts was studied. A critical inoculating condition was observed at approximately 0.6 g dry biomass (DW). L-1 medium, above which root growth was significantly reduced when using a low-salt minimal (M) liquid medium previously developed for hairy root-AM fungi co-culture. Below critical inoculum conditions the maximum specific root growth and specific G. intraradices spore production rates of 0.021 and 0.035 d-1, respectively, were observed for Petri dish cultures. Maximum spore production in the airlift bioreactor was ten times lower than that of Petri dish cultures and obtained with the lowest inoculum assessed (0.13 g DW. L-1 medium) with 1.82 x 10(5) +/- 4.05 x 10(4) (SEM) spores (g DW inoculum)-1 (L medium)-1 in 107 d. This work proposes a second-generation bioprocess for AM fungi propagule production in bioreactors. Copyright 1999 John Wiley & Sons, Inc.     

Monoterpenoid oxindole alkaloid production by Uncaria tomentosa (Willd) D.C. cell suspension cultures in a stirred tank bioreactor

Cell growth, monoterpenoid oxindole alkaloid (MOA) production, and morphological properties of Uncaria tomentosa cell suspension cultures in a 2-L stirred tank bioreactor were investigated. U. tomentosa (cell line green Uth-3) was able to grow in a stirred tank at an impeller tip speed of 95 cm/s (agitation speed of 400 rpm), showing a maximum biomass yield of 11.9 +/- 0.6 g DW/L and a specific growth rate of 0.102 d(-1). U. tomentosa cells growing in a stirred tank achieved maximum volumetric and specific MOA concentration (467.7 +/- 40.0 microg/L, 44.6 +/- 5.2 microg/g DW) at 16 days of culture. MOA chemical profile of cell suspension cultures growing in a stirred tank resembled that of the plant. Depending on culture time, from the total MOA produced, 37-100% was found in the medium in the bioreactor culture. MOA concentration achieved in a stirred tank was up to 10-fold higher than that obtained in Erlenmeyer flasks (agitated at 110 rpm). In a stirred tank, average area of the single cells of U. tomentosa increased up to 4-fold, and elliptical form factor increased from 1.40 to 2.55, indicating enlargement of U. tomentosa single cells. This work presents the first report of U. tomentosa green cell suspension cultures that grow and produce MOA in a stirred tank bioreactor.     

Production of Trichoderma micropropagules as a biocontrol agent in static liquid culture conditions by using an integrated bioreactor system

ABSTRACT

In this study, we optimised the conditions for the production of micropropagules of Trichoderma harzianum EGE-K38 in static liquid culture in Modified Czapec Medium (MCM) containing 8?g/L glucose in an integrated tray bioreactor system designed by our research group. Incubation temperature, air flow rate, inoculum spore concentration, inoculation size, medium volume and the use of spores or agar plugs containing mycelia as inoculum were individually studied as one factor at a time. The maximum micropropagule count was 5.2?±?0.2?×?10^9?cfu/mL and dry cell weight was 17?±?2?g/L. For the subsequent drying processes, the maximum drying yield percentage ((viable micropropagule counts after drying/viable cells before drying)*100) after drying of micropropagules was 23.30% (cfu/cfu). Results obtained from our integrated tray bioreactor system showed that static liquid culture fermentation offers potential for industrial scale fungal BCAs production.     

Batch kinetics of Pseudomonas sp. growth on benzene. Modeling of product and substrate inhibitions

Batch tests of benzene degradation were performed in liquid phase at 30 degrees C, pH 6.8 +/- 0.2, and 200 rpm in two 3-L stirred tank bioreactors, using the benzene-degrading bacterium Pseudomonas sp. NCIMB 9688. A relatively high starting biomass level (220-270 mg(X)/L) and starting benzene concentration ranging from 20 to 200 mg(S)/L were selected as conditions to investigate possible inhibition phenomena. Volumetric as well as specific rates of biomass formation and substrate consumption were calculated from experimental data of both growth and benzene degradation and used to propose and check a new overall kinetic model for cell growth simultaneously accounting for both product and substrate inhibitions. The results of the present study evidenced the occurrence of a competitive-type product inhibition due to 2-hydroxymuconic semialdehyde (K(iP)' = 0.902 mg(S)/L), which was stronger than the uncompetitive-type inhibition exerted by substrate (K(iS) = 7.69 mg(S)/L).     

Adventitious root culture of <Emphasis Type="Italic">Polygonum multiflorum</Emphasis> for phenolic compounds and its pilot-scale production in 500 L-tank

Polygonum multiflorum Thunb. is an important medicinal plant that synthesizes an array of phenolic compounds. Its roots are used in a variety of pharmacological and cosmetic formulations, notably as hair dye. In the present study, the inoculum density (3–15 g/L) and culture period (1–7 weeks) were optimized in a 3 L bioreactor. High root biomass (14.18 g/L dry weight (DW)) was recorded with an inoculum of 7 g/L (p?≤?0.05), which is consistent with the results for 5 and 10 g/L. However, significantly higher yield of bioactive compounds (53.87 mg/g DW total phenolics and 27.96 mg/g DW total flavonoids) with high free radical scavenging activity was obtained in root samples from 5 g/L inoculum density. A 4 week culture period was sufficient for optimum root growth and metabolite production. The optimized conditions were used for large-scale (5 and 20 L) and pilot-scale (500 L) studies. Considering that the continuous aeration of root cultures may lead to oxidative stress, antioxidant enzyme activity and lipid peroxidation also were studied. The results revealed high catalase (CAT) and guaiacol peroxidase (G-POD) activities, and low malondialdehyde (MDA) production, with increasing culture scale (20 and 500 L), which may indicate low-level oxidative damage to the cultures. An optimal yield of 4.01 kg dry root biomass with 287.12 mg/L of total phenolic productivity was achieved in a 500 L pilot-scale bioreactor. This work can pave the way for commercial production of biomass and secondary metabolites at the industrial level, and meet the rising demand for natural ingredients, especially in the pharmaceutical and cosmetic industries.     

Improvement of ganoderic acid and Ganoderma polysaccharide biosynthesis by Ganoderma lucidum fermentation under the inducement of Cu2+

The cell growth and total accumulation of bioactive metabolites were significantly improved by Cu²⁺ addition during the submerged fermentation of medicinal mushroom Ganoderma lucidum. A mathematical model, constructed by response surface methodology combination with full factorial design, was applied to study the synergic effect of Cu²⁺ addition concentration and addition time. The optimal Cu²⁺ inducement strategy for the cell growth were different from those for the biosynthesis of ganoderic acid (GA) and Ganoderma polysaccharide. A multiple additions strategy of Cu²⁺ by adding each 1 mM Cu²⁺ on day 2, 6, 8 and 2 mM Cu²⁺ on day 4 was developed to enhance total accumulation of GA and extracellular polysaccharides. The highest GA content reached 3.0 ± 0.1 mg per 100 mg DW, which was increased by 76.5% and 33.9% compared with the control without Cu²⁺ addition and the peak value predicted by the constructed mathematical model, respectively. While, relatively higher addition concentration of Cu²⁺ (i.e., 5 mM) on the culture of day 4 led to higher content and total production of intracellular polysaccharides. © 2009 American Institute of Chemical Engineers Biotechnol. Prog., 2010     

Establishment of cultivating strategy for highly aggregated mycelia of Morchella esculenta in a stirred-tank bioreactor

Mycelia of Morchella esculenta were found to aggregate rapidly in a submerged culture, which caused the decrease in dispersed mycelia and the problem of diffusion limitation. The effect of different agitation schemes on the growth of mycelia was investigated in a stirred-tank bioreactor. At the constant speed of 100 or 300?rpm, rapid aggregation caused the biomass concentration to drop to zero in 30?h, which was even worse than achieved under static culture. Intermittent agitation maintained a higher mycelium fragment concentration for 48?h and enhanced the biomass concentration to 4.73?g/L at 120?h. The operation with a polytron connection disrupted effectively mycelium aggregation, thus increasing the specific growth rate, biomass concentration and maximum productivity to 0.0613 1/h, 7.73?g/L and 0.0878?g/L?h at 88?h, respectively. Moreover, logistic equations and genetic algorithm (GA) were used for the simulation of biomass growth and estimation of all kinetic coefficients. The operating strategy developed in this study could be used for the production of highly aggregated mycelia, which could also achieve a high cell-density culture in a stirred tank reactor.     

建立金线莲原球茎悬浮体系生产次生代谢产物

研究植物激素浓度和培养周期对金线莲原球茎悬浮培养生长及其代谢产物积累的影响,以增加金线莲悬浮培养的生长量,提高次生代谢产物的生产。结果表明,MS培养基添加S-3307 1.0mg/L,6-BA0.5mg/L和3%的蔗糖适合总生物量的生长(214.45g/L,FW和18.23g/L DW)。而MS培养基添加S-3307 1.0mg/L,6-BA 3.0mg/L和5%的蔗糖,总黄酮,总酚和多糖的干重(5.43mg/g,2.87mg/g和243.23mg/g)达到最大化。研究原球茎悬浮培养过程,发现经过7个星期培养就能获得最大的生物质总量(225.98 g/L的FW和18.53 g/L的DW)、总黄酮干重(5.09mg/g)和总酚干重(2.04mg/g),而多糖生产达到其峰值(229.36mg/g干重)是在培养后5个星期。     

Manipulation of ginsenoside heterogeneity of <Emphasis Type="Italic">Panax notoginseng</Emphasis> cells in flask and bioreactor cultivations with addition of phenobarbital

Structure-similar ginsenosides have different or even totally opposite biological activities, and manipulation of ginsenoside heterogeneity is interesting and significant to biotechnological application. In this work, addition of 1 mM phenobarbital to cell cultures of Panax notoginseng at a relatively high inoculation size of 7.6 g dry cell weight (DW)/L enhanced the production of protopanaxatriol-type (Rg₁ + Re) ginsenosides in both shake flask and airlift bioreactor (ALR, 1 L working volume). The content of Rg₁ + Re in the ALR was increased from 42.5 ± 4.0 mg per gram DW in untreated cell cultures (control) to 56.4 ± 4.6 mg per gram DW with addition of 1.0 mM phenobarbital. The maximum productivity of Rg₁ + Re in the ALR reached 5.66 ± 0.38 mg L⁻¹ d⁻¹, which was almost 3.3-fold that of control. The maximum ratio of the detectable ginsenosides protopanaxatriol:protopanaxadiol (Rb₁) was 7.6, which was about twofold that of control. The response of protopanaxadiol 6-hydroxylase (P6H) activity to phenobarbital addition coincided with the above-mentioned change of ginsenoside heterogeneity (distribution). Phenobarbital addition is considered as a useful strategy for manipulating the ginsenoside heterogeneity in bioreactor with enhanced biosynthesis of protopanaxatriol by P. notoginseng cells.     

Galanthamine production by Leucojum aestivum L. shoot culture in a modified bubble column bioreactor with internal sections

Shoot culture of summer snowflake (Leucojum aestivum L.) was successfully cultivated in an advanced modified glass‐column bioreactor with internal sections for production of Amaryllidaceae alkaloids. The highest amounts of dry biomass (20.8 g/L) and galanthamine (1.7 mg/L) were achieved when shoots were cultured at 22°C and 18 L/(L·h) flow rate of inlet air. At these conditions, the L. aestivum shoot culture possessed mixotrophic‐type nutrition, synthesizing the highest amounts of chlorophyll (0.24 mg/g DW (dry weight) chlorophyll A and 0.13 mg/g DW chlorophyll B). The alkaloids extract of shoot biomass showed high acetylcholinesterase inhibitory activity (IC₅₀ = 4.6 mg). The gas chromatography–mass spectrometry (GC/MS) profiling of biosynthesized alkaloids revealed that galanthamine and related compounds were presented in higher extracellular proportions while lycorine and hemanthamine‐type compounds had higher intracellular proportions. The developed modified bubble‐column bioreactor with internal sections provided conditions ensuring the growth and galanthamine production by L. aestivum shoot culture.     

Biomass axial distribution in airlift bioreactor with yeast and plant cells

This study was aimed at determining the degree of biomass homogeneity in the various parts of an internal loop airlift bioreactor, thus verifying the assumption, often made in bioreactor studies, of a well-mixed liquid-biomass system. Following characterization of the hydrodynamics of the vessel with water, the axial biomass distribution in the riser and downcomer was determined for plant and yeast cell suspensions of 5.8, 8.5, and 12.5 g DW/L Phaseolus vulgaris and of 30 and 46 g DW/L Saccharomyces cerevisiae. The airlift bioreactor with a surface ratio A(D)/A(D) of 1.04 and aspect ratio of 4.95 was investigated under various aeration rates. The yeast cells were found to be distributed practically uniformly throughout the vessel at the aeration rates of 0.1-1.45 vvm. However, in the case of the denser and cluster-forming plant cells, a clear trend of a gradual bio-mass accumulation in the downcomer, a slightly lower but uniform biomass loading in the riser, and a slightly higher biomass concentration in the gas-liquid separator was observed at the lower aeration rates of 0.1-0.61 vvm. In the case of powderized calcium carbonate (55g/L) often used in fermentations of organic acids, a slight trend of a gradual accumulation of solids towards the bottom parts in both the downcomer and riser was observed. A better representative sampling location, in terms of solids and biomass loading, seems to be in the middle part of the vessel. It is suggested that airlift bioreactors with higher aspect ratios (>5) may be prone to a more significant inhomogeneity of solids (biomass and particles).     

气升式液体培养假褐云斑鹅膏菌丝及毒素检测分析

采集并组织分离到假褐云斑鹅膏Amanita pseudoporphyria的纯培养菌丝。培养发现其在琼脂培养基上生长形态与一般蕈菌有差别。摇瓶液体培养条件下,假褐云斑鹅膏菌丝体干重为0.626g/L,在气升式反应器内假褐云斑鹅膏菌丝体干重可达到1.629g/L。反应器培养的菌丝体毒素的HPLC分析表明菌丝体内含有鹅膏毒肽,而不含有鬼笔毒肽。结果表明可以通过液体培养鹅膏菌丝体来生产鹅膏毒素。