Bioreactors comparison

Cultivation of NSO cells in an AcuSyst Jr hollow-fiber bioreactor comparison of two different operation strategies, designated basic and optimized strategy (Rodriguez et al., 2005). 

TABLE 12.1 Bioreactor Comparison with Relative Benefit (+) or Challenge (—)... 

Barradas OP, Jandt U, Phan LDM, Villanueva ME, Schaletzky M, Rath A, Freund S, Reichl U, Skerhutt E, Scholz S, Noll T, Sandig V, Portner R, Zeng A-P. (2012) Evaluation of criteria for bioreactor comparison and operation standardization for mammalian cell culture. Eng. Life Sci., 12(5) 1-11. 

Eigure 6 enables a comparison to be made of kj a values in stirred bioreactors and bubble columns (51). It can be seen that bubble columns are at least as energy-efficient as stirred bioreactors in coalescing systems and considerably more so when coalescence is repressed at low specific power inputs (gas velocities). 

Fig. 6. A comparison of k a values (51). Represented are 1, stirred bioreactor using water, = 0.02 m/s, kj a (eq. 16) 2, stirred bioreactor using water, t 3 = 0.04 m/s, kj a (eq. 16) 3, bubble column using water, kj a (eq. 18) 4, stirred bioreactor using salt water, = 0.02 m/s, kj a (eq. 17) 5, stirred bioreactor using salt water, = 0.04 m/s, kj a (eq. 17) and 6, bubble column using salt water (noncoalescing).

Clara M, Strenn B, Ausserleitner M, Kreuzinger N (2004) Comparison of the behaviour of selected micropollutants in a membrane bioreactor and a conventional wastewater treatment plant. Water Sci Technol 50 29-36... 

For basic studies it is very advantageous to use suitable model particle systems which are much better reproducible and can be performed in a much shorter time. The best comprehension can be derived from studies under technical flow conditions in real bioreactors and partial comparison with experiences with biological cultures. 

According to Eq. (14) the maximum velocity gradient at the wall is at y = D/2. It amounts to (du/dy) ju=C u/D. The stress derived from this with Eq. (1) has been used in a number of studies (see e.g. [8-11]) as a measure of stress. However, particles are only subjected to this maximum stress if they close to y = 0. As this cannot or can only temporarily be the case during flow through channels, such test results should be regarded with caution and only conditionally suitable for comparison with the results from other model apparatuses, not to mention bioreactors. 

The comparison of biological material systems and model particle systems in Fig. 2 shows that, under the operating conditions relevant for bioreactors, the... 

The comparison of the results obtained from model particle systems with experience of biological systems shows a similar tendency on many points. Therefore it proved to be very advantageous for the basic investigations, especially for the comparison of different reactor types, to use suitable model particle systems with similar properties to those of biological material systems. This permitted the performance of test series under technically relevant operating conditions, similar to those prevailing in bioreactors, in a relatively short time. The results are more reproducible than in biological systems and therefore permit faster and more exact optimization of reactors. 

Liu BB, Zhang F, Feng XX (2006) Thauera and Azoarcus as functionally important genera in a denitrifying quinoline-removal bioreactor as revealed by microbial community structure comparison. FEMS Microbiol Ecol 55 274—286... 

Park D, Leeb DS, Jounga JY, Park JM (2005) Comparison of different bioreactor systems for indirect H2S removal using iron-oxidizing bacteria. Process Biochem 40 1461-1467... 

Fig. 3.97. Comparison of ion-pair chromatography separations of RB5-H and metabolites by on-line and in situ sampling coupled to HPLC-DAD from bioreactor (A) 585 nm scanning wavelength, (B) 270 nm scanning wavelength. Peak identification TAHNDSDP1 = 7-amino-8-hydroxy-l,3-naph-toquinone-3,6-disulphonate-l,2-diamine TAHNDSDP2 = dihydroxynaphtoquinone-3,6-disulphonate-diimine p-Base = 2-(4-aminobenzenesulphonyl)ethanol. Reprinted with permission from A. Plum et al. [156],...

Performance comparisons with a Clark-type sensor demonstrated the applicability of the optical sensor in monitoring dissolved oxygen (DO) levels in a bioreactor.<73) Figure 13.11 shows the response profiles of the optical sensor and Clark-type electrode... 

Kunkel J.P., Jan D.C., Butler M., and Jamieson J.C. (2000), Comparisons of the glycosylation of a monoclonal antibody produced under nominally identical cell culture conditions in two different bioreactors, Biotechnol. Prog. 16, 462 -70. 

Fig. 2. Diagrams of the processes with instrumentation, (a) Schematic diagram for wastewater digester. Two temperature sensors Ti and T2 were nsed for measnre-ments. Time series were acquired from Ti and T2 was nsed for corroborating no transfer heat to surroundings by comparison with TI measnrements. (b) Schematic for the liquid-liquid heat exchanger. Note that the Bioreactor-Exchanger interconnection involves recycle streams between two feedback controlled processes.

TABLE 1 Comparison of Projected Capital Costs for Major Bioreactor Components and of Operating Costs for Three Treatment Alternatives for Benzene-Contaminated Water (Costs in U.S. Dollars, 1995)... 

This chapter describes the different types of batch and continuous bioreactors. The basic reactor concepts are described as well as the respective basic bioreactors design equations. The comparison of enzyme reactors is performed taking into account the enzyme kinetics. The modelhng and design of real reactors is discussed based on the several factors which influence their performance the immobilized biocatalyst kinetics, the external and internal mass transfer effects, the axial dispersion effects, and the operational stabihty of the immobilized biocatalyst. 

This chapter shows how a biphasic medium can help in reducing loss of volatile compounds in a gaseous phase exiting from a bioreactor, in comparison with pure aqueous systems. It also emphasises the usefulness of solvents having low vapour pressure (heavy organic solvents or ionic liquids) in the reduction of the release of compounds into the environment. There are, from this point of view, common interests between engineering needs and environmental concerns in the flavouring industry. 

Defiance, L. and Jaffrin, M.Y. (1999) Comparison between filtrations at fixed transmembrane pressure and fixed permeate flux application to a membrane bioreactor used for wastewater treatment. Journal of Membrane Science, 152, 203-210. 

Le-Clech, P., Jefferson, B. and Judd, S.J. (2003) Impact of aeration, solids concentration and membrane characteristics on the hydraulic performance of a membrane bioreactor. Journal of Membrane Science, 218,117—129. Le-Clech, P., Jefferson, B. and Judd, S.J. (2005) Comparison of submerged and side-stream tubular membrane bioreactor configurations. Desalination, 173, 113-122. 

Bioenergetics Biomass, Bioengineering of Biomass Utilization, Limits of Bioreactors Catalysis, Industrial Coal Structure and Reactivity Combustion Energy Efficiency Comparisons Among Countries Energy Flows in Ecology... 

Merten O-W, Cruz PE, Rochette C, Geny-Fiamma C, Bouquet C, Gonsalves D, Danos O, Carrondo MJT (2001), Comparison of different bioreactor systems for the production of high titer retroviral vectors, Biotechnol. Prog. 17 326-335. 

A comparison between insect and mammalian cell culture technology shows various similarities and differences. Due to the fact that insect cell lines typically derive from specific organs or non-differentiated embryonic tissues, the same cell line can proliferate in suspension or in adherent manner (in monolayer). This versatility in growth mode, which contrasts with most mammalian cell lines, increases the choices of bioreactor types and culture strategies for production. Contact inhibition shown by various mammalian cell lines is low or absent for insect cells, and they tend to aggregate in suspension or in adherent cultures. 

Figure 9.19 shows typical cell concentrations reached in the main industrial bioreactors and a comparison of these values with those found in microbial fermentations. As can be observed, batch and fed-batch cultivations attain dry biomass values comparable to those of continuous cultures of microorganisms, so that mass and heat transfer capacities are not limited for these operation modes. However, high cell density cultivation in heterogeneous bioreactors, such as hollow-fiber devices, reaches dry biomass values similar to the maxima observed in microbial cultures. 

Table 9.3 Comparison of working parameters and typical productivities found for the main industrial bioreactors...

Moro AM, Rodrigues MTA, Gouveia MN, Silvestri MLZ, Kalil JE, Raw I (1994), Multi-parametric analyses of hybridoma growth on glass cylinders in a packed-bed bioreactor system with internal aeration. Serum-supplemented and serum-free media comparison for MAb production, J. Immunol. Methods 176 67-77. 

The FundaLux system, for instance, aspirates a liquid aliquot with a Teflon piston into an external glass cell, allows a (selectable) time (typically 2 min) to degas, measures transmission in comparison to an air blank, and releases the aliquot back to the reactor an interesting feature - specific to this instrument -is the repetitive cleaning of the optical window by the moving Teflon piston. Some problems with infections have been communicated with this device since the measuring cell is external to the bioreactor and the sensor is probably insufficiently sterilized in situ. 

A comparison between the performance of conventional biological waste-water treatment basins and the reciprocating bioreactor is given in Table XXVI. As shown, the conversion rate in the reciprocating reactor can be as high as more than four times that obtained in a conventional bioreactor. 

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