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• W210231787 abstract "The analysis of experiments conducted on binary beds of irregular-shaped solids, such as biomass granules (crushed olive pits) and sand, shows that a recent model devised for predicting the initial and final fluidization velocity of a twocomponent bed of spherical solids captures also the behaviour of mixtures of non-spherical particles. INTRODUCTION In a previous work (1), fluidization of two-solid beds has been subjected to fundamental analysis. This approach has led to the development of a model capable of interpreting the behaviour of binary-solid systems where segregation is driven by either size or density difference of their components. Based on a fundamental force balance, this model provides relationships for the velocity thresholds which encompass the fluidization process, namely the ‘‘initial’’ and the ‘‘final fluidization velocity’’ of the mixture, hereafter referred to as uif and uff, respectively. uif is predicted by means of a fully theoretical equation, whereas just one parameter is needed to calculate uff. Although not thoroughly predictive as for the evaluation of uff, the model equations have proved to be accurate in reproducing the dependence of either characteristic velocity on solid properties and mixture composition. A remarkable feature of the approach proposed is that of offering a unique interpretation frame of two-solid fluidization, overcoming the need for the separated analysis which characterizes previous literature works (36). More recently, the validity of the approach proposed has been successfully checked on beds of fully dissimilar solids (2), where both density and size differences are at work in promoting component separation. In this case, the simultaneous action of these two effects can give place to different segregation patterns. Like with particles that differ either in density or size, whenever these factors act synergistically (i.e when the larger particles are also denser), the progress of fluidization in an initially well-mixed system is accompanied by segregation mechanisms which determine the bed structure sketched in Fig.1a and described in detail elsewhere (1,2). This phenomenology has been termed “top fluidization”, since by increasing the gas velocity over uif the fluidized portion of the bed widens downward from the bed surface, while a static bed forms at the base. Conversely, with binary systems whose denser component is also the smaller, more than one fluidization patterns is possible. If the denser solid achieves fluidization first, the fluidization front may develop at the bottom of the bed (Fig. 1b) and the whole phenomenology is somewhat reversed, so that it can be referred to as ‘‘bottom fluidization’ (2).’ Fig. 1: Segregating fluidization patterns In both cases the bed can approximately be divided into three distinct layers as u varies from uif to uff: the fluidized layer, the packed layer and the residual mixed bed, whose heights are hF, hP and hm, respectively. However, the mechanism of fluidization changes their order along the bed height, with the upper layer constituted by the fluidized solid or by the packed one. This three-layer structure is a good approximation of the component distribution originating from the segregation mechanisms that take place along the fluidization velocity interval. In previous research, however, the analysis was limited to mixtures of spherical solids whereas systems of practical interest are often made of solids of irregular shape, like in operations such as coal or biomass gasification and combustion. Further investigation is therefore required to assess the model validity when nonspherical particles are involved, a goal that is pursued in the present contribution. THEORY The model tested in this work has been presented in previous papers (1,2), therefore only the basic equations are shown in this section. In its present application, however, the pressure drop is calculated by resorting to the Ergun’s equation rather than to Carman-Kozeny’s, in order to extend the analysis to particles with diameters larger than 1 mm. uif can be calculated by introducing the Sauter average diameter and the voidage of the homogeneous bed m:    g u d 75 . 1 u d 1 150 g av 2 if av 3 m g if 2 av 3 m m g            (1)" @default.
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• W210231787 date "2013-01-01" @default.
• W210231787 modified "2023-09-27" @default.
• W210231787 title "Modelling the Transition to the Fluidized State of Two-Solid Beds: Mixtures of Particles of Irregular Shape" @default.
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