Intensification of gas–liquid mass transfer using a rotating bed of porous packings for application to an E. coli batch fermentation process

Boodhoo, Kamelia; Vićević, Marija; Cartwright, Craig David; Ndlovu, T.M.; Toogood, EC

doi:10.1016/j.cej.2007.06.011

Cited by 18 publications

(8 citation statements)

References 26 publications

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“…The results were plotted in relation to their calculated power requirements and compared with other reactor types in Figure 6. (Arjunwadkar et al, 1998; Boodhoo et al, 2008; Bredwell et al, 1999; Garcia-Ochoa and Gomez, 2009; Gourich et al, 2006; Kraakman et al, 2011; Kreutzer et al, 2005; Linek et al, 2005; Markopoulos et al, 2007; Pirouzi et al, 2014) All results for k L a app generated experimentally are for CO. They were changed into mass transfer coefficients for O 2 for proper comparison using a ratio of the square root of the diffusivities according to penetration theory (Danckwerts, 1951).…”

Section: Resultsmentioning

confidence: 99%

“…Although the biocomposite absorbed $2-fold more CO, it produces the same amount of secreted products. With (Arjunwadkar et al, 1998;Boodhoo et al, 2008;Bredwell et al, 1999;Garcia-Ochoa and Gomez, 2009), open circle-bubble column (Linek et al, 2005), closed diamond-trickle bed reactor (Bredwell et al, 1999;Kraakman et al, 2011), closed circle-airlift reactor (Bredwell et al, 1999;Gourich et al, 2006;Loubiere et al, 2009;Pirouzi et al, 2014), cross hatch-monolith or microchannel (Kraakman et al, 2011;Kreutzer et al, 2005), black squares-3MM paper biocomposites. Inverted filled triangle is test case to confirm power calculations.…”

Section: Resultsmentioning

confidence: 99%

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A high gas fraction, reduced power, syngas bioprocessing method demonstrated with a Clostridium ljungdahlii OTA1 paper biocomposite

Schulte

Wiltgen

Ritter

et al. 2016

Biotech & Bioengineering

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We propose a novel approach to continuous bioprocessing of gases. A miniaturized coated-paper high gas fraction biocomposite absorber has been developed using slowly shaken horizontal anaerobic tubes with concentrated Clostridium ljungdahlii OTA1 absorbing syngas as a model system. These gas absorbers demonstrate elevated CO mass transfer with low power input, reduced liquid requirements, elevated substrate consumption, and increased product secretion compared to shaken suspended cells. We concentrate OTA1 in a cell paste which was coated by extrusion onto chromatography paper. Cell adhesion was by adsorption to the cellulose fibers; visualized by SEM. The C. ljungdahlii OTA1 coated paper mounted above the liquid level absorbs CO and H2 from a model syngas producing acetate with minimal ethanol. At 100 rpm shaking speed (7.7 W m−3) the optimal cell loading is 6.5 gDCW m−2 to maintain high CO absorbing reactivity without the cells coming off of the paper into the liquid phase. Reducing the medium volume from 10 mL to 4 mL (15% of tube volume) did not decrease CO reactivity. The reduced liquid volume increased secreted product concentration by 80%. The specific CO consumption by paper biocomposites was higher at all shaking frequencies <100 rpm than suspended cells under identical incubation conditions. At 25 rpm the biocomposite outperforms suspended cells for CO absorption by 2.5 fold, with a power reduction of 97% over the power input at 100 rpm. The estimated minimum apparent kLa for these biocomposite gas-absorbers is ~100 h−1, a 10 to 104 less power input than other syngas fermentation systems at similar kLa. Specific consumption rates in a biocomposite were measured as ~14 mmol gDCW−1 h−1. This work intensified CO absorption and reactivity by 14 fold to 94 mmol CO m−2 h−1 over previous C. ljungdahlii OTA1 work by our group. Specific acetate production rates were 23 mM h−1 or 46 mmol m−2 h−1. The specific rates and apparent kLa were shown to scale linearly with biocomposite coating area. These proof of concept results will be used to engineer a continuous biocomposite gas absorber bioreactor.

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Section: Resultsmentioning

confidence: 99%

Section: Resultsmentioning

confidence: 99%

A high gas fraction, reduced power, syngas bioprocessing method demonstrated with a Clostridium ljungdahlii OTA1 paper biocomposite

Schulte

Wiltgen

Ritter

et al. 2016

Biotech & Bioengineering

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show abstract

“…The effects of aeration rate and broth viscosity on gas holdup at three different impeller speeds of 600, 800, and 1000 rpm are depicted in Figures a and b, respectively. The three used viscosities (2, 4, and 6 mPa · s) were chosen to predict the behaviour of the medium . As can be seen, in this study both viscosity and aeration rate have a small, increasing effect on the gas holdup.…”

Section: Resultsmentioning

confidence: 99%

“…This breakage can lead to higher values for the energy dissipation rate, up to 10 4 W · kg −1 . High shear rates generated within this range of energy can damage cells . Therefore, to scale up the bioreactors from laboratory to industrial scale there is a need to keep a balance between increasing the k L a values and reducing the damaging effect of shear stress on cells inside the bioreactor.…”

Section: Resultsmentioning

confidence: 99%

Experiments and a three‐phase computational fluid dynamics (CFD) simulation coupled with population balance equations of a stirred tank bioreactor for high cell density cultivation

et al. 2015

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This research describes a three dimensional (3‐D) computational fluid dynamics (CFD) simulation coupled with population balance equations (PBE) to study hydrodynamics and biomass production in a laboratory‐scale stirred‐tank bioreactor. The gas‐liquid‐solid flow was modelled using a Eulerian multiphase and k−ϵ turbulence (RNG) model. The energy dissipation rates, gas holdup, flow patterns, Sauter mean bubble diameter, and volumetric mass transfer coefficient were investigated for three different types of impeller using a multiple reference frame (MRF) model within the whole multiphase bioreactor. The effects of aeration rate and impeller speed on gas holdup and volumetric mass transfer coefficient were investigated owing to oxygen limitation in high cell density cultivation (HCDC). As high viscosity puts a limit on the efficiency of the bioreactor, the influences of viscosity on Sauter mean diameter, gas holdup, and volumetric mass transfer coefficient were also assessed. To determine growth kinetics as well as gas holdup, a set of experiments was performed. The numerical results of gas holdup and kLa were compared with the experimental data. Obtained results suggest that the Scaba impeller results in higher values of volumetric mass transfer coefficient, and subsequently higher biomass concentrations. One of the greatest problems in HCDC is feed accumulation in particular places. As depletion of substrate occurs near the impeller, the best spot for feeding purposes is in the vicinity of the impeller. Current research gives insight into the determination of the optimal operating conditions of HCDC in stirred bioreactors.

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“…As part of these strategies, studies were carried out by Linnhoff March, of the energy savings made and data are given in Table 4. Immobilization of glucose isomerase (on an Obtaining adequate productivity, inorganic carrier) for production of high fructose improvements in activity, stability and (Drauz, 2012) corn syrup, penicillin G acylase(covalently selectivity attached to polyacrylate) for the production of semi-synthetic penicillins, lactase(on an ionexchange resin) for producing low-lactose milk, TL lipase (on silica) for fat modification Cells immobilization Beer fermentation using immobilised yeast cells High-productivity (Verbelen et al, 2010) Rotating bed of porous packings Using a rotating bed of porous packings for Intensification of gas-liquid mass transfer (Boodhoo et al, 2008) application to an E. coli batch fermentation process…”

Section: Energymentioning

confidence: 99%

Process Intensification for Production and Recovery of Biological Products

Vaghari¹,

Eskandari²,

Sobhani³

et al. 2015

American Journal of Biochemistry and Biotechnology

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Bioprocesses are important biological reactions which need several sophisticated methods and equipment to produce many novel and important compounds which some of them are traditionally produced by synthetic chemical reactions. In bioprocesses, the products are often produced in a dilute environment and finally they require a high purity. Because of that, downstream processes are usually included a large number of separation steps. Size and capital costs of the equipment are two main limitations of using bioprocesses at industrial scale. Bioprocess intensification by minimizing, substitution, moderation and simplification of the methods and equipment, drastically leads to sustainable processes. This study looks at intensification of the emerging equipment and operational methods and their advantages to lead smaller and cleaner bioprocess plants which in turn, increases production efficiency and quality and decreases byproducts formation, capital cost and energy consumption.

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Intensification of gas–liquid mass transfer using a rotating bed of porous packings for application to an E. coli batch fermentation process

Cited by 18 publications

References 26 publications

A high gas fraction, reduced power, syngas bioprocessing method demonstrated with a Clostridium ljungdahlii OTA1 paper biocomposite

A high gas fraction, reduced power, syngas bioprocessing method demonstrated with a Clostridium ljungdahlii OTA1 paper biocomposite

Experiments and a three‐phase computational fluid dynamics (CFD) simulation coupled with population balance equations of a stirred tank bioreactor for high cell density cultivation

Process Intensification for Production and Recovery of Biological Products

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