Models a r e defined for various mixing conditions, in continuous flow systems. Differential equations a r e derived which take into acrount an effective volume of mixing, possillle short-circuiting, holcl-up time of the system, partial displacement or piston flow.The values of the different factors contained in the integrated equations can be determined experimentally by the particular response of a given system to a sudden change in composition of the feed.A correlation of the effective volume of mixing and the agitator r.p.m. is presented.
Irrevereible first-and eieeond-order reactions are studied for combinations of tubular and CST reactors when endothermal or exothermal adiabatic conditions prevail.Typical results presented for itf T and, Tr)i models show the variation of either the conversion or the relative residence time as a function of the mixing level of the system.
The performance of an adiabatic MT reactor has been studied under various experimental conditions, using the reaction between hydrogen peroxide and sodium thiosulphate. Following the M‐section, consisting of a CSTR, the T‐section was made up of a large number of small stirred tanks in series.
The same general condition for optimizing the MT model, that the reaction rate in the M‐section be a maximum, is shown to apply when maximizing the conversion for a given residence time as it was shown previously to apply when minimizing the residence time for a given conversion.
Very good agreement is shown between theoretical and experimental results, confirming the superior results often obtained with an MT combination as compared with those given by a stirred tank or a tubular reactor under similar conditions. Bi‐stable steady states of conversion have been achieved and their effect shown on the performance of the combined reactor.
Chemical flow reactors studied include models in which partial mixing and piston flow are present and others which involve partial mixing and short‐circuit. Mixing levels considered extend all the way between the extreme cases of tubular and continuous‐stirred tank reactors. Various orders of reaction are taken into account.
The curves presented, obtained through analytical methods, show either the variation of conversion with mixing level at given values of residence time, or relative residence times for a given conversion. Graphical methods of solution are proposed. They involve, in part, a means of computation whereby the overall conversion for a number of reactors in series is obtained from the individual conversions.
While isothermal conditions only have been considered, more interesting results are expected when other conditions are applicable, whether isothermal or not.
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