Corrigendum to “Comparison between average shear rates in conventional bioreactor with Rushton and Elephant ear impellers” [Chem. Eng. Sci. 90 (2013) 92–100]

Bustamante, Maritza Catalina Condori; Cerri, Marcel O.; Badino, Alberto Colli

doi:10.1016/j.ces.2013.12.018

Cited by 5 publications

(5 citation statements)

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“…Comparable to the aforementioned studies, for the cases investigating impeller combinations including up‐pumping impellers, the reactor liquid volume ranges from V = 3–4 L , , over V = 35 L , up to V = 30 m 3 . The up‐pumping impellers are 3‐ and 4‐bladed hydrofoils (3‐HYDRO‐U, 4‐HYDRO‐U) and the aforementioned EEU while the down‐pumping axial flow impellers were the 3‐HYDRO or EED.…”

Section: Impellers Used In Cultivation Systemsmentioning

confidence: 84%

“…Tang et al actually showed the positive effect of three 3‐HYDRO‐U on the overall biological performance. While it is worth mentioning that the (top‐bottom) EEU‐EED combination showed the best performance in terms of k L a relative to power input , in three studies , , the combination EED‐EEU actually showed the best performance in terms of k L a itself. The overall good performance of the impeller combinations with axial flow impellers is mostly correlated to a more uniform flow field and a lower tendency of compartmentation.…”

Section: Impellers Used In Cultivation Systemsmentioning

confidence: 99%

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Multiphase Stirred Tank Bioreactors – New Geometrical Concepts and Scale‐up Approaches

Böhm

Hohl

Bliatsiou

et al. 2019

Chemie Ingenieur Technik

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Mainly with respect to biotechnological cases, current developments in the field of impeller geometries and findings for multistage configurations with a specific view on aerated stirred tanks are reviewed. Although often the first choice, in the given case the 6‐straight blade disc turbine is usually not the best option. Furthermore, quantities usable for scale‐up, specifically applicable in this field are discussed. Only quantities taking local conditions into account appear to be able to actually compare different stirrer types and scales.

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Section: Impellers Used In Cultivation Systemsmentioning

confidence: 84%

Section: Impellers Used In Cultivation Systemsmentioning

confidence: 99%

Multiphase Stirred Tank Bioreactors – New Geometrical Concepts and Scale‐up Approaches

Böhm

Hohl

Bliatsiou

et al. 2019

Chemie Ingenieur Technik

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show abstract

Section: Methodsmentioning

confidence: 99%

“…Scale‐up (1 L) : The run was carried out in a spinner flask (1.5 L) (see SI) with Elephant ear turbine impellers (DASGIP, Germany) in a volume of 1 L. The rationale for selecting the latter over standard impellers such as Rushton turbine impellers, was the lower associated shear rate. [30] The cell lysate – without any purification step – was used directly for the synthesis. For the preparation of the biocatalyst mix the following biomasses each from 200 mL cultivation, except for PPA which was 45 mL, were mixed: UDK, 3.46 g; UMPK/PPK3, 5.2 g; GALK, 5.54 g; GALU, 5.7 g; PPA, 1.7 g in 120 mL of 50 mM HEPES buffer (pH 8.1), 400 mM NaCl and 5 % glycerol.…”

Section: Methodsmentioning

confidence: 99%

Cell‐Free Multi‐Enzyme Synthesis and Purification of Uridine Diphosphate Galactose

et al. 2021

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High costs and low availability of UDP‐galactose hampers the enzymatic synthesis of valuable oligosaccharides such as human milk oligosaccharides. Here, we report the development of a platform for the scalable, biocatalytic synthesis and purification of UDP‐galactose. UDP‐galactose was produced with a titer of 48 mM (27.2 g/L) in a small‐scale batch process (200 μL) within 24 h using 0.02 genzyme/gproduct. Through in‐situ ATP regeneration, the amount of ATP (0.6 mM) supplemented was around 240‐fold lower than the stoichiometric equivalent required to achieve the final product yield. Chromatographic purification using porous graphic carbon adsorbent yielded UDP‐galactose with a purity of 92 %. The synthesis was transferred to 1 L preparative scale production in a stirred tank bioreactor. To further reduce the synthesis costs here, the supernatant of cell lysates was used bypassing expensive purification of enzymes. Here, 23.4 g/L UDP‐galactose were produced within 23 h with a synthesis yield of 71 % and a biocatalyst load of 0.05 gtotal_protein/gproduct. The costs for substrates per gram of UDP‐galactose synthesized were around 0.26 €/g.

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“…A pitched‐blade turbine was taken as an impeller with combined (both radial and axial) flow pattern, again, in down‐ (PBD) and up‐pumping (PBU) configuration. Pitched‐blade and hydrofoil impellers were included in this study because of their effective function in full‐scale apparatuses and low shear stresses .…”

Section: Methodsmentioning

confidence: 99%

Volumetric Mass Transfer Coefficient in Fermenters: Scale‐up Study in Viscous Liquids

et al. 2017

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In the design of mechanically agitated fermenters, the volumetric mass transfer coefficient k L a often becomes the key parameter. In case of viscous liquids, k L a prediction based on literature correlations suffers from a wide distribution. The aim is to provide reliable k L a correlations based on a large experimental data set obtained using the dynamic pressure method, the physical correctness of which was verified earlier. Multiple-impeller fermenters of two scales were used. The impeller tip speed, rather than the power input, revealed to be the proper term for prediction of k L a. When the impeller power number is used, k L a values for various impeller types can be predicted by a common correlation which, based on a wide range of operational conditions, can be applied in the design.

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Corrigendum to “Comparison between average shear rates in conventional bioreactor with Rushton and Elephant ear impellers” [Chem. Eng. Sci. 90 (2013) 92–100]

Cited by 5 publications

References 0 publications

Multiphase Stirred Tank Bioreactors – New Geometrical Concepts and Scale‐up Approaches

Multiphase Stirred Tank Bioreactors – New Geometrical Concepts and Scale‐up Approaches

Cell‐Free Multi‐Enzyme Synthesis and Purification of Uridine Diphosphate Galactose

Volumetric Mass Transfer Coefficient in Fermenters: Scale‐up Study in Viscous Liquids

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