以摇瓶所得摄氧率为基准进行发酵放大

通过设计特殊摇瓶,用亚硫酸盐法测出摇瓶口纱布层氧通透率的基础上,在实际发酵情况下通过测定瓶内气、液相氧的变化得出其发酵过程中的摄氧率(OUR)及氧传递系数(K_La)。以特制摇瓶取得的菌体CUR为基准进行发酵过程和发酵罐的放大。通过质谱仪在线检测及采样分析,研究了3种不同供气流量及搅拌转速下的放大结果。摇瓶与发酵罐在菌体OUR、菌体产量方面吻合很好,而在整个放大过程中,发现摇瓶与发酵罐内的氧传递系数(K_La)、溶解氧(C_L)差异较大。     

Influence of oxygen adsorption on the dynamic K(L)a measurement in three-phase slurry reactors

To check for possible mass transfer limitations of oxygen and/or carbon dioxide in kinetic experiments on microbial desulphurization of coal, it is important to properly measure the volumetric mass transfer coefficient (k(L)a) especially at high slurry densities. Volumetric mass transfer coefficients of oxygen, at different solid hold-up values (epsilon(s) = 0 to 0.28) of coal slurries (d(par) < 100 * 10(-6) m), were measured in a lab scale fermentor and in a lab scale pachuca tank, using the dynamic gas-liquid absorption method. It was shown that serious errors could occur due to oxygen adsorption at the coal surface. Using the data of an independently measured adsorption isotherm, the real k(L)a could be calculated from the measured apparent k(L)a. The results show a k(L)a decrease of 40% to 50% at a volumetric solid hold-up of 28%. Estimation of the oxygen and carbon dioxide transfer rates, from the measured mass transfer coefficients, indicates that the stirred fermentor is suitable for kinetic experiments at high slurry densities, whereas the pachuca tank and shake flask are not. (c) 1992 John Wiley & Sons, Inc.     

Integrated optical sensing of dissolved oxygen in microtiter plates: a novel tool for microbial cultivation

Microtiter plates with integrated optical sensing of dissolved oxygen were developed by immobilization of two fluorophores at the bottom of 96-well polystyrene microtiter plates. The oxygen-sensitive fluorophore responded to dissolved oxygen concentration, whereas the oxygen-insensitive one served as an internal reference. The sensor measured dissolved oxygen accurately in optically well-defined media. Oxygen transfer coefficients, k(L)a, were determined by a dynamic method in a commercial microtiter plate reader with an integrated shaker. For this purpose, the dissolved oxygen was initially depleted by the addition of sodium dithionite and, by oxygen transfer from air, it increased again after complete oxidation of dithionite. k(L)a values in one commercial reader were about 10 to 40 h(-1). k(L)a values were inversely proportional to the filling volume and increased with increasing shaking intensity. Dissolved oxygen was monitored during cultivation of Corynebacterium glutamicum in another reader that allowed much higher shaking intensity. Growth rates determined from optical density measurement were identical to those observed in shaking flasks and in a stirred fermentor. Oxygen uptake rates measured in the stirred fermentor and dissolved oxygen concentrations measured during cultivation in the microtiter plate were used to estimate k(L)a values in a 96-well microtiter plate. The resulting values were about 130 h(-1), which is in the lower range of typical stirred fermentors. The resulting maximum oxygen transfer rate was 26 mM h(-1). Simulations showed that the errors caused by the intermittent measurement method were insignificant under the prevailing conditions.     

Kojic acid production byAspergillus flavus using gelatinized and hydrolyzed sago starch as carbon sources

Direct conversion of gelatinized sago starch into kojic acid byAspergillus flavus strain having amylolytic enzymes was carried out at two different scales of submerged batch fermentation in a 250-mL shake flask and in a 50-L stirred-tank fermentor. For comparison, fermentations were also carried out using glucose and glucose hydrolyzate from enzymic hydrolysis of sago starch as carbon sources. During kojic acid fermentation of starch, starch was first hydrolyzed to glucose by the action of α-amylase and glucoamylase during active growth phase. The glucose remaining during the production phase (non-growing phase) was then converted to kojic acid. Kojic acid production (23.5g/L) using 100 g/L sago starch in a shake flask was comparable to fermentation of glucose (31.5 g/L) and glucose hydrolyzate (27.9 g/L) but in the 50-L fermentor was greatly reduced due to non-optimal aeration conditions. Kojic acid production using glucose was higher in the 50-L fermentor than in the shake flask.     

Rotating drum fermentor for plant cell suspension cultures

A rotating drum fermentor designed for plant cell suspension cultures was constructed and tested. The oxygen transfer coefficient (k(L)a) and power requirements in the fermentor were determined with the water system under various conditions and the relationship between them in the fermentor was clarified. Also, the relationship between k(L)a and the apparent viscosity in the fermentor was investigated in the cell suspension system. The rotating drum fermentor was found to be superior to the mechanically agitated fermentor in the capacity of oxygen supply under high viscosity and low hydrodynamic stress conditions. This finding was also confirmed by the experiments with plant cell suspension cultures.     

溶氧对Blakeslea trispora分批发酵生产β-胡萝卜素的影响

在摇瓶和5 L发酵罐中研究了溶氧 (DO) 对Blakeslea trispora分批发酵生产β-胡萝卜素的影响,总结了5 L发酵罐中β-胡萝卜素发酵过程中溶氧的变化规律.结果表明,当500 mL摇瓶装液量为50 mL,转速为240 r/min条件下发酵生产β-胡萝卜素产量最大,达到3.416 g/L; 5 L发酵罐中,在搅拌转速为1 000 r/min,通气量为1.5 vvm的条件下,β-胡萝卜素的产量可达到3.712 g/L,略高于摇瓶,这可能是由于5 L发酵罐中的气液传递和混合状况好于摇瓶,促进了产物的合成.     

Online medium-throughput respirometry-based OTR measurements in magnetically stirred cultures

Intensified bioprocess development requires parallelized medium- to high-throughput experimentation with high on- and offline data density across all early scales of the development trajectory from microtiter plate via shake flask to lab-scale reactor. We developed a widespread measurement principle for intermediate scales, respirometry, into a parallelized oxygen transfer rate measurement device that could accurately record common process development-relevant effects such as acetate formation, diauxic growth, and nutrient limitations. The device was further equipped with dissolved oxygen measurement capability and sampling ports that allowed repetitive monoseptic sample withdrawal without disturbing the cultivation. Optimization of the operating parameters lead to k(L) a values of up to 160 h(-1) and corresponding oxygen transfer rates of 1 g L(-1) h(-1) for cultivation volumes of 50 mL.     

Scale-up from shake flasks to fermenters in batch and continuous mode with Corynebacterium glutamicum on lactic acid based on oxygen transfer and pH

Scale-up from shake flasks to fermenters has been hampered by the lack of knowledge concerning the influence of operating conditions on mass transfer, hydromechanics, and power input. However, in recent years the properties of shake flasks have been described with empirical models. A practical scale-up strategy for everyday use is introduced for the scale-up of aerobic cultures from shake flasks to fermenters in batch and continuous mode. The strategy is based on empirical correlations of the volumetric mass transfer coefficient (k(L) a) and the pH. The accuracy of the empirical k(L) a correlations and the assumptions required to use these correlations for an arbitrary biological medium are discussed. To determine the optimal pH of the culture medium a simple laboratory method based on titration curves of the medium and a mechanistic pH model, which is solely based on the medium composition, is applied. The effectiveness of the scale-up strategy is demonstrated by comparing the behavior of Corynebacterium glutamicum on lactic acid in shake flasks and fermenters in batch and continuous mode. The maximum growth rate (micro(max) = 0.32 h(-1)) and the oxygen substrate coefficient (Y O2 /S= 0.0174 mol/l) of C. glutamicum on lactic acid were equal for shake flask, fermenter, batch, and continuous cultures. The biomass substrate yield was independent of the scale, but was lower in batch cultures (Y(X/S) = 0.36 g/g) than in continuous cultures (Y(X/S) = 0.45 g/g). The experimental data (biomass, respiration, pH) could be described with a simple biological model combined with a mechanistic pH model.     

Scale-up of biopesticide production processes using wastewater sludge as a raw material

Studies were conducted on the production of Bacillus thuringiensis (Bt)-based biopesticides to ascertain the performance of the process in shake flasks, and in two geometrically similar fermentors (15 and 150 l) utilizing wastewater sludge as a raw material. The results showed that it was possible to achieve better oxygen transfer in the larger capacity fermentor. Viable cell counts increased by 38–55% in the bioreactor compared to shake flasks. As for spore counts, an increase of 25% was observed when changing from shake flask to fermentor experiments. Spore counts were unchanged in bench (15 l) and pilot scale (5.3–5.5 e⁺⁰⁸ cfu/ml; 150 l). An improvement of 30% in the entomotoxicity potential was obtained at pilot scale. Protease activity increased by two to four times at bench and pilot scale, respectively, compared to the maximum activity obtained in shake flasks. The maximum protease activity (4.1 IU/ml) was obtained in pilot scale due to better oxygen transfer. The Bt fermentation process using sludge as raw material was successfully scaled up and resulted in high productivity for toxin protein yield and a high protease activity.     

Noninvasive measurement of dissolved oxygen in shake flasks

Shake flasks are ubiquitous in cell culture and fermentation. However, conventional devices for measuring oxygen concentrations are impractical in these systems. Thus, there is no definitive information on the oxygen supply of growing cells. Here we report the noninvasive, nonintrusive monitoring of dissolved oxygen (DO) in shake flasks using a low-cost optical sensor. The oxygen-sensitive element is a thin, luminescent patch affixed to the inside bottom of the flask. The sensitivity and accuracy of this device is maximal up to 60% DO, within the range that is critical to cell culture applications. By measuring actual oxygen levels every 1 or 5 min throughout the course of yeast and E. coli fermentations, we found that a modest increase in shaker speed and a decrease in culture volume slowed the onset of oxygen limitation and reduced its duration. This is the first time that in situ oxygen limitation is reported in shake flasks. The same data is unattainable with a Clark type electrode because the presence of the intrusive probe itself changes the actual conditions. Available fiber optic oxygen sensors require cumbersome external connections and recalibration when autoclaved.     

Closure effects on oxygen transfer and aerobic growth in shake flasks

Oxygen mass transfer in shake flasks is an important aspect limiting the culture of aerobic microorganisms. In this work, mass transfer of oxygen through a closure and headspace of shake flasks is investigated. New equations for prediction of kGa in shake flasks with closures are introduced. Using Pseudomonas putida, microbial growth on glucose (fast metabolism) and phenol (slow metabolism) in shake flasks with closures were studied, considering both substrate and oxygen restrictions. A combined model for oxygen mass transfer and microbial growth is shown to accurately predict experimental oxygen concentrations and oxygen yield factors during growth experiments more accurately than previous models.     

Combined dissolved oxygen tension and online viscosity measurements in shake flask cultivations via infrared fluorescent oxygen-sensitive nanoparticles

Oxygen supply is one of the most critical process parameters in aerobic cultivations. To assure sufficient oxygen supply, shake flasks are usually used in combination with orbital shaking machines. In this study, a measurement technique for the dissolved oxygen tension (DOT) in shake flask cultures with viscosity changes is presented. The movement of the shaker table is monitored by means of a Hall effect sensor. For DOT measurements, infrared fluorescent oxygen-sensitive nanoparticles are added to the culture broth. The position of the rotating bulk liquid needs to be determined to assure measurements inside the liquid. The leading edge of the bulk liquid is detected based on the fluorescence signal intensity of the oxygen-sensitive nanoparticles. Furthermore, online information about the viscosity of the culture broth is acquired due to the detection of the position of the leading edge of the bulk liquid relative to the direction of the centrifugal force, as described by Sieben et al. (2019. Sci. Rep., 9, 8335). The DOT measurement is combined with a respiration activity monitoring system which allows for the determination of the oxygen transfer rate (OTR) in eight parallel shake flasks. Based on DOT and OTR, the volumetric oxygen transfer coefficient (k_La) is calculated during cultivation. The new system was successfully applied in cultivations of Escherichia coli, Bacillus licheniformis, and Xanthomonas campestris.     

Model for oxygen transfer in a shake flask

The shake flask is a very common and useful tool for the study of submerged fermentations on a small scale. However, the oxygen supply may easily become a limiting factor. A model for the aeration in shake flasks is presented that enables one to predict whether in the course of an experiment the oxygen supply is becoming a growth-limiting factor or not. The results of measurements of the transfer coefficient of a cotton plug and the oxygen mass-transfer coefficient k_la are also given.     

假丝酵母99-125脂肪酶的发酵工艺研究

对假丝酵母99-125脂肪酶的发酵工艺条件进行了一系列研究。选择了合适的培养基成分并进行优化 ,获得了最优的摇瓶培养基配方 (% ,W/V) :豆油 4.0 ,全脂豆粉 4.0 ,K₂HPO₄0.1,KH₂PO₄ 0.1。产酶水平能达到 5000IU/mL。在 30L发酵罐上进行初步放大实验 ,其产酶水平能达到 8100IU/mL。在1m³发酵罐上进行中试放大 ,产酶水平可达到 8000IU/mL。     

乳糖诱导重组尿酸酶基因在大肠杆菌中的表达

对用乳糖替代异丙基-β-D-硫代半乳糖苷(IPTG)诱导重组产朊假丝酵母尿酸酶基因在E.coli JM109(DE3)中表达进行了研究,拟建立一种高效低成本的生产重组尿酸酶的工艺路线。通过摇瓶试验对诱导所采用的乳糖浓度,诱导时机和诱导持续时间进行了优化,并考察在乳糖诱导下的目的产物表达动力学,随后在5 L发酵罐上进行扩大化培养以验证摇瓶优化的结果,进一步将乳糖作为诱导剂应用于高密度发酵过程。实验结果表明乳糖诱导的最佳浓度为5 g/L,最佳诱导时机是对数生长期中后期,诱导持续时间为9~10h;按照优化的条件在摇瓶和5 L发酵罐上进行分批培养,重组尿酸酶最大表达量可达菌体总蛋白的26%左右,可溶性蛋白的36%左右,略高于IPTG的诱导效果;高密度发酵过程菌体终密度达到OD600值40以上,尿酸酶表达量占菌体总蛋白25%左右。     

Oxygen transfer and mycelial growth in a tubular loop fermentor

A 22 m long. 20 liter tubular loop fermentor (TLF) has been tested for oxygen transfer characteristics and as a reactor for mycelial growth. Model calculations show that the flow pressure drop has an important influence on the axial oxygen profiles. A design model that accounts for this influence is presented. Using the model, K_L a values are calculated from the results of sulfite oxidation experiments. These are correlated with power consumption and aeration rates. The K_L a dependence on aeration rate was found to be less than found with tank reactors. The growth kinetics of three metabolite-producing mycelial organisms in the TLF are presented: a Streptomyces, a Fusarium, and a Acrophialophora. In order to determine the influence of reactor type on the growth and product formation, these cultures have been grown in tanks and shake flasks. The antibiotic, product spectrum of Streptomyces is compared on the basis of inhibition tests and it is shown that the distribution of products is reactor dependent. The Fusarium culture produced a previously unknown metabolite, whose concentration in the loop fermentor was four times higher than in a shake flask. The Acrophialophora culture grew twice as fast in the loop fermentor, but produced essentially none of the specific product. Power Consumptions of up to 8 kW/m³ in the tubular fermentor did not appear to harm the mycelia.     

Oxygen transfer phenomena in 48-well microtiter plates: determination by optical monitoring of sulfite oxidation and verification by real-time measurement during microbial growth

Oxygen limitation is one of the most frequent problems associated with the application of shaking bioreactors. The gas-liquid oxygen transfer properties of shaken 48-well microtiter plates (MTPs) were analyzed at different filling volumes, shaking diameters, and shaking frequencies. On the one hand, an optical method based on sulfite oxidation was used as a chemical model system to determine the maximum oxygen transfer capacity (OTR(max)). On the other hand, the Respiration Activity Monitoring System (RAMOS) was applied for online measurement of the oxygen transfer rate (OTR) during growth of the methylotropic yeast Hansenula polymorpha. A proportionality constant between the OTR(max) of the biological system and the OTR(max) of the chemical system were indicated from these data, offering the possibility to transform the whole set of chemical data to biologically relevant conditions. The results exposed "out of phase" shaking conditions at a shaking diameter of 1 mm, which were confirmed by theoretical consideration with the phase number (Ph). At larger shaking diameters (2-50 mm) the oxygen transfer rate in MTPs shaken at high frequencies reached values of up to 0.28 mol/L/h, corresponding to a volumetric mass transfer coefficient (k(L)a) of 1,600 1/h. The specific mass transfer area (a) increases exponentially with the shaking frequency up to values of 2,400 1/m. On the contrary, the mass transfer coefficient (k(L)) is constant at a level of about 0.15 m/h over a wide range of shaking frequencies and shaking diameters. However, at high shaking frequencies, when the complete liquid volume forms a thin film on the cylindric wall of the well, the mass transfer coefficient (k(L)) increases linearly to values of up to 0.76 m/h. Essentially, the present investigation demonstrates that the 48-well plate outperforms the 96-well MTP and shake flasks at widely used operating conditions with respect to oxygen supply. The 48-well plates emerge, therefore, as an excellent alternative for microbial cultivation and expression studies combining the advantages of both the high-throughput 96-well MTP and the classical shaken Erlenmeyer flask.     

Optimization of oxygen mass transfer in a multiphase bioreactor with perfluorodecalin as a second liquid phase

Oxygenation is an important parameter involved in the design and operation of mixing-sparging bioreactors and it can be analyzed by means of the oxygen mass transfer coefficient (k(L)a). The operational conditions of a stirred, submerged aerated 2-L bioreactor have been optimized by studying the influence of a second liquid phase with higher oxygen affinity (perfluorodecalin or olive oil) in the k(L)a. Using k(L)a measurements, the influence of the following parameters on the oxygen transfer rate was evaluated: the volume of working medium, the type of impellers and their position, the organic phase concentration, the aqueous phase composition, and the concentration of inactive biomass. This study shows that the best experimental conditions were achieved with a perfluorodecalin volume fraction of 0.20, mixing using two Rushton turbines with six vertical blades and in the presence of YPD medium as the aqueous phase, with a k(L)a value of 64.6 h(-1). The addition of 20% of perfluorodecalin in these conditions provided a k(L)a enhancement of 25% when pure water was the aqueous phase and a 230% enhancement when YPD medium was used in comparison to their respective controls (no perfluorodecalin). Furthermore it is shown that the presence of olive oil as a second liquid phase is not beneficial to the oxygen transfer rate enhancement, leading to a decrease in the k(L)a values for all the concentrations studied. It was also observed that the magnitude of the enhancement of the k(L)a values by perfluorodecalin depends on the biomass concentration present.     

Performance of Bacillus subtilis on fibrous biomass sugar hydrolysates in producing biosurfactants and techno-economic comparison

Bioprocess and Biosystems Engineering - Surfactin and fatty acetyl glutamate (FA-Glu) were produced by Bacillus subtilis in 5-L fermentor. In a previous 50-mL shake flask study, sugar hydrolysates...     

Effect of oxygen transfer on glycerol biosynthesis by an osmophilic yeast Candida magnoliae I(2)B

The influence of oxygen on glycerol production by an osmophilic yeast, Candida magnoliae I(2)B, was studied in a bioreactor. Oxygen transfer rates (OTRs) and volumetric oxygen transfer coefficients (k(L)a) were determined at different aeration and agitation rates. Cell growth as well as glycerol production was strongly affected by oxygen supply. Improvement in OTRs resulted in increased cell growth and glycerol yield. However, at high OTRs, there was a reduction in glucose uptake rate, indicating Pasteur Effect, and glycerol accumulation was also reduced at k(L)a of 253 h(-1). The availability of oxygen per unit of cell mass was found to be the most important factor that controlled cell growth, glucose uptake, and glycerol yield. The overall productivity and yield of glycerol could be related with k(L)a. The biosynthesis of glycerol was found to both growth- and non-growth-associated, although glycerol was mainly produced in post-exponential phase.