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Abstract

Bacteriophages, viruses that can infect bacteria, are promising alternatives for antibiotic treatment caused by antibiotic-resistant bacteria strains. For that reason, the production of bacteriophages is extensively studied. Mathematical modelling can lead to the improvement of bioprocess by identification of critical process parameters and their impact on the demanded product. Dynamic modelling considers a system (i.e. bioreactor or bioprocess) as a dynamic object focusing on changes in the initial and final parameters (such as biomass concentration and product formation) in time, so-called signals and treats the studied system as a “black box” that processes signals. This work aimed to develop a mathematical model that describes bacteriophage production process. As result, we created a dynamic model that can estimate the number of bacteriophages released from cells as plaque-forming units at specific time points based on the changes in the bacteria host-cell concentration. Moreover, the proposed model allowed us to analyze the impact of the initial virus concentration given by multiplicity of infection (MOI) on the amount of produced bacteriophages.
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Authors and Affiliations

Maciej Konopacki
1 2
ORCID: ORCID
Bartłomiej Grygorcewicz
1 2
ORCID: ORCID
Marta Gliźniewicz
2
ORCID: ORCID
Dominika Miłek
2
ORCID: ORCID
Marian Kordas
1
ORCID: ORCID
Rafał Rakoczy
1
ORCID: ORCID

  1. West Pomeranian University of Technology in Szczecin, Faculty of Chemical Technology and Engineering, Department of Chemical and Process Engineering, al. Piastów 42, 71-065 Szczecin, Poland
  2. Pomeranian Medical University in Szczecin, Chair of Microbiology, Immunology and Laboratory Medicine, Department of Laboratory Medicine, al. Powstanców Wielkopolskich 72, 70-111 Szczecin, Poland
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Abstract

Flow patterns generated by two ChemShear impellers, CS2 and CS4 have been measured and flow numbers calculated; Fl = 0.04 for both impellers. Transient and equilibrium drop sizes, d32 μm. of 3 different viscosity silicone oils agitated by a high-shear Rushton turbine, RT, a low-shear, high-flow HE3 impeller and the two ChemShears were determined. The equilibrium d32 are correlated by d_32=1300〖(ε_T)〗_(max.sv)^(-0.58) v^0.14 with an R2 = 0.94. However, the time to reach steady state and the equilibrium size at the same specific power do not match the above descriptors of each impeller’s characteristics. In other literature, these descriptors are also misleading. In the case of mixing time, a high shear RT of the same size as a high flow HE3 requires the same time at the same specific power in vessels of H/T = 1. In bioprocessing, where concern for damage to cells is always present, free suspension animal cell culture with high shear RTs and low-shear impellers is equally effective; and with mycelial fermentations, damage to mycelia is greater with low shear than high. The problems with these descriptors have been known for some time but mixer manufacturers and ill-informed users and researchers continue to employ them.

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Bibliography

Arai K., Konno M., Matumagata Y., Saito S., 1977. The effect of dispersed phase viscosity on the maximum stable drop size in turbulent flow. J. Chem. Eng. Jpn., 10, 325–330. DOI: 10.1252/jcej.10.325.

Baldyga J., Bourne J.R., Pacek A.W., Amanullah A., Nienow A.W., 2001. Effects of agitation and scale-up on drop size in turbulent dispersions: Allowance for intermittency. Chem. Eng. Sci., 56, 3377–3385. DOI: 10.1016/s0009-2509(01)00027-6.

Chapman C.M., Nienow A.W., Cooke M., Middleton J.C., 1983. Particle-gas-liquid mixing in stirred vessels: Part 2 – gas-liquid mixing. Chem. Eng. Res. Des., 61, 82–95.

Costariol E.,Rotondi M.C., Amini A., Hewitt C.J., NienowA.W., Heathman T.R.J., Rafiq Q.A., 2020. Demonstrating the manufacture of human CAR-T cells in an automated stirred-tank bioreactor. Biotechnol. J., 15, 2000177. DOI: 10.1002/biot.202000177.

Davies J.T., 1985. Droplet sizes of emulsions related to turbulent energy dissipation rates. Chem.Eng. Sci., 40, 839–842. DOI: 10.1016/0009-2509(85)85036-3.

Dyster K.N., Koutsakos E., Jaworski Z., Nienow A.W., 1993. An LDA study of the radial discharge velocities generated by a Rushton turbine: Newtonian fluids, Re ≥ 5. Chem. Eng. Res. Des., 71, 11–23.

Fondy P.L., Bates R.L., 1963.Agitation of liquid systems requiring a high shear characteristic. AIChE J., 9, 338–342. DOI: 10.1002/aic.690090312.

Ghotli R.A., Raman A.A.A., Ibrahim S., Baroutian S., 2013. Liquid – liquid mixing in stirred vessels: A review. Chem. Eng. Comm., 200, 595–627. DOI: 10.1080/00986445.2012.717313.

Hanga M.P., Ali J., Moutsatsou P., de la Raga F.A., Hewitt C.J., NienowA.W,Wall I., 2020.

Bioprocess development for scalable production of cultivated meat. Biotech. Bioeng., 117, 3029–3039. DOI: 10.1002/bit.27469.

Hass V.C., Nienow A.W., 1989. A new axial pumping agitator for the dispersion of gas in liquids. Chem. Ing. Technik, 61, 152–154. DOI: 10.1002/cite.330610213.

Ibrahim S., Nienow A.W., 2004. Suspension of microcarriers for cell culture with axial flow impellers. Chem. Eng. Res. Des., 82, 1082–1088. DOI: 10.1205/cerd.82.9.1082.44161.

Indco, 2021. The difference between high shear and low shear mixing. Available at: https://www.indco.com/blog/indco/2020/03/05/the-difference-between-high-shear-and-low-shear-mixing.

Jaworski Z., Nienow A.W., Dyster K.N., 1996. An LDA study of the turbulent flow field in a baffled vessel agitated by an axial, down-pumping hydrofoil impeller. Can. J. Chem. Eng., 74, 3–15. DOI: 10.1002/cjce.5450740103.

Justen P., Paul G.C., Nienow A.W., Thomas C.R., 1996. Dependence of mycelial morphology on impeller type and agitation intensity. Biotech. Bioeng., 52, 672–684. DOI: 10.1002/(SICI)1097-0290(19961220)52:6672::AIDBIT5> 3.0.CO;2-L.

Langheinrich C., Nienow A.W., Eddleston T., Stevenson N.C., Emery A.N., Clayton T.M, Slater N.K.H., 1998.

Liquid homogenisation studies in animal cell bioreactors of up to 8m3 in volume. Food Bioprod. Process., 76, 107–116. DOI: 10.1205/096030898531873.

Leng D.E., Calabrese R.V., 2004. Immiscible liquid-liquid systems. In: Paul E.L., Atiemo-Obeng V.A., Kresta S.M. (Eds), Handbook of industrial mixing: Science and Practice, John Wiley, New York. 639–753. DOI: 10.1002/0471451452.ch12.

Leng D.E., Calabrese R.V., 2016. Immiscible liquid-liquid systems. In: Kresta S.M., Etchells III A.W., Dickey D.S., Atiemo-Obeng V.A. (Eds), Advances in industrial mixing: A companion to the handbook of industrial mixing. John Wiley, New York. 12, 457–464.

McManameyW.J., 1979. Sauter mean and maximum drop diameters of liquid-liquid dispersions in turbulent agitated vessel at low dispersed phase hold-up. Chem. Eng. Sci., 34, 432–434. DOI: 10.1016/0009-2509(79)85081-2.

Musgrove M., Ruszkowski S., 2000. Influence of impeller type,and agitation conditions on the drop size of immiscible liquid dispersions. Proceedings of the 10th European Conference on Mixing. Delft, the Netherlands, 2–5 July 2000, 165–172. DOI: 10.1016/b978-044450476-0/50022-4.

Nienow A.W., Coopman K., Heathman T.R.J., Rafiq Q.A., Hewitt C.J., 2016. Chapter 3 – Bioreactor engineering fundamentals for stem cell manufacturing. In: Cabral J.M.S. et al (Eds.) Stem Cell Manufacturing. Elsevier Science, Cambridge, USA. 43–75. DOI: 10.1016/B978-0-444-63265-4.00003-0.

Nienow A.W., Scott W.H., Hewitt C.J., Thomas C.R., Lewis G., Amanullah A., Kiss R., Meier S.J., 2013. Scaledown studies for assessing the impact of different stress parameters on growth and product quality during animal cell culture. Chem. Eng. Res. Des., 91, 2265–2274. DOI: 10.1016/j.cherd.2013.04.002.

Nienow A.W., 2021. The impact of fluid dynamic stress in stirred bioreactors-the scale of the biological entity: A personal view. Chem. Ing. Tech., 93, 17–30. DOI: 10.1002/cite.202000176.

Nienow A.W., 1997. On impeller circulation and mixing effectiveness in the turbulent flow regime. Chem. Eng. Sci., 52, 2557–2565. DOI: 10.1016/S0009-2509(97)00072-9.

Nienow A.W., 2014. Stirring and stirred tank reactors. Chem. Ing Tech., 86, 2063–2074. DOI: 10.1002/cite.201400087.

Nienow A.W., Bujalski W., 2002. Recent studies on agitated three phase (gas-liquid-solid) systems in the turbulent regime. Chem. Eng. Res. Des., 80, 832–838. DOI: 10.1205/026387602321143363.

NOV Chemineer, 2021. Available at: https://www.chemineer.com/literature.html.

Oh S.K.W., Nienow A.W., Emery A.N., Al-Rubeai M., 1992. Further studies of the culture of mouse hybridomas in an agitated bioreactor with and without continuous sparging. J. Biotechnol., 22, 245–270. DOI: 10.1016/0168-1656(92)90144-X.

Oldshue J.Y., 1983. Fluid mixing technology and practice, McGraw Hill, New York.

Pacek A.W, Nienow A.W., 1995. A problem for the description of turbulent dispersed liquid-liquid systems. Int. J. Multiphase Flow, 21, 323–325. DOI: 10.1016/0301-9322(94)00068-u.

Pacek A.W, Nienow A.W., Moore I.P.T., 1994b. On the structure of turbulent liquid-liquid dispersed flows in an agitated vessel. Chem. Eng. Sci., 49, 3485–3498. DOI: 10.1016/s0009-2509(94)85027-5.

Pacek A.W., Chamsart S., NienowA.W., Bakker A., 1999. The influence of impeller type on mean drop size and drop size distribution in an agitated vessel. Chem. Eng. Sci., 54, 4211–4222. DOI: 10.1016/s0009-2509(99)00156-6.

Pacek A.W., Moore I.P.T., Calabrese R.V., Nienow A.W., 1993. Evolution of drop size distributions and average drop diameters in liquid-liquid dispersions before and after phase inversion. Chem. Eng. Res. Des., 71, 340–341.

Pacek A.W., Moore I.P.T., Nienow A.W., Calabrese R.V., 1994a. A video technique for the measurement of the dynamics of liquid-liquid dispersion during phase inversion. AIChE J., 40, 1940–1949. DOI: 10.1002/aic.690401203.

Padron D.A., Okonkwo D.A., 2018. Effect of impeller type on drop size of turbulent, non-coalescing liquid-lquid dispersions. 16th European Conference on Mixing, Toulouse, France, 9–12 September 2018.

Paterson G.K., Pauls E.L., Kresta S.M., Etchells A.W., 2015. Mixing and chemical reaction. In: Kresta S.M., Etchells III A.W., Dickey D.S, Atiemo-Obeng V.A. (Eds.), Advances in industrial mixing: A companion to the handbook of industrial mixing. John Wiley, New York. 465–478.

Rotondi M., Grace N., Betts J., Bargh N., Costariol E., Zoro B., Hewitt C.J., Nienow A.W., Rafiq Q.A., 2021. Design and development of a new ambr250r bioreactor vessel for improved cell and gene therapy applications. Biotechnol. Lett., 43, 1103–1116. DOI: 10.1007/s10529-021-03076-3.

Sandadi S., Pedersen H., Bowers J.S., Rendeiro D., 2011. A comprehensive comparison of mixing, mass transfer, Chinese hamster ovary cell growth, and antibody production using Rushton turbine and marine impellers. Bioprocess. Biosyst. Eng., 34, 819. DOI: 10.1007/s00449-011-0532-0.

Sepro Mixing and Pumping, 2021. Mixing basics: Shear and flow. Available at: https://mixing.seprosystems.com/mixing-basics-shear-and-flow/.

Simmons M.J.H., Zhu H, BujalskiW., Hewitt C.J., Nienow A.W., 2007. Mixing in bioreactors using agitators with a high solidity ratio and deep blades. Chem. Eng. Res. Des., 85, 551–559. DOI: 10.1205/cherd06157.

SPX Flow, 2021. Lightnin Mixers. General Overview.Available at: https://www.spxflow.com/assets/pdf/LGT_A400_B-937_US.pdf.

Wille M., Langer G., Werner U., 2001. The influence of macroscopic elongational flow on dispersion processes in agitated tanks. Chem. Eng. Technol., 24, 119–127. DOI: 10.1002/1521-4125(200102)24:2119::aidceat119>3.0.co;2-g.

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Authors and Affiliations

Andrzej W. Pacek
1
Alvin W. Nienow
1

  1. School of Chemical Engineering, University of Birmingham, Edgbaston, Birmingham, B15 2TT, UK

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