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Liquid flow region

At still higher temperatures, the rubbery flow and liquid flow regions are encountered, regions 4 and 5. In the former, flow is hindered by physical entanglements. At higher temperatures molecular motion is sufficiently rapid that molecules behave more nearly independently. [Pg.23]

Molecular flow, which occurs in the rubbery flow and liquid flow regions (regions 4 and 5 in Figure 1.12). [Pg.29]

A liquid flow region where the rheology follows a quasi-Newtonian regime. [Pg.707]

Region V (e-f) in Figure 1.19 is the liquid flow region which is reached at still higher temperatures where the increased kinetic energy of the chains permits them wri le out through entanglements rapidly... [Pg.54]

Glaser and Litt (G4) have proposed, in an extension of the above study, a model for gas-liquid flow through a b d of porous particles. The bed is assumed to consist of two basic structures which influence the fluid flow patterns (1) Void channels external to the packing, with which are associated dead-ended pockets that can hold stagnant pools of liquid and (2) pore channels and pockets, i.e., continuous and dead-ended pockets in the interior of the particles. On this basis, a theoretical model of liquid-phase dispersion in mixed-phase flow is developed. The model uses three bed parameters for the description of axial dispersion (1) Dispersion due to the mixing of streams from various channels of different residence times (2) dispersion from axial diffusion in the void channels and (3) dispersion from diffusion into the pores. The model is not applicable to turbulent flow nor to such low flow rates that molecular diffusion is comparable to Taylor diffusion. The latter region is unlikely to be of practical interest. The model predicts that the reciprocal Peclet number should be directly proportional to nominal liquid velocity, a prediction that has been confirmed by a few determinations of residence-time distribution for a wax desulfurization pilot reactor of 1-in. diameter packed with 10-14 mesh particles. [Pg.99]

NPei and NRtt are based on the equivalent sphere diameters and on the nominal velocities ug and which in turn are based on the holdup of gas and liquid. The Schmidt number is included in the correlation partly because the range of variables covers part of the laminar-flow region (NRei < 1) and the transition region (1 < NRtl < 100) where molecular diffusion may contribute to axial mixing, and partly because the kinematic viscosity (changes of which were found to have no effect on axial mixing) is thereby eliminated from the correlation. [Pg.107]

Fig. 3.18 Schematic of the near-wall and cavity regions for liquid flow over a superhydrophobic surface exhibiting micro-rib structures and flow perpendicular to the ribs... Fig. 3.18 Schematic of the near-wall and cavity regions for liquid flow over a superhydrophobic surface exhibiting micro-rib structures and flow perpendicular to the ribs...
Figure 5.6 Flow pattern map for a gas/liquid flow regime in micro channels. Annular flow wavy annular flow (WA) wavy annular-dry flow (WAD) slug flow bubbly flow annular-dry flow (AD). Transition lines for nitrogen/acetonitrile flows in a triangular channel (224 pm) (solid line). Transition lines for air/water flows in triangular channels (1.097 mm) (dashed lines). Region 2 presents flow conditions in the dual-channel reactor ( ), with the acetonitrile/nitrogen system between the limits of channeling (I) and partially dried walls (III). Flow conditions in rectangular channels for a 32-channel reactor (150 pm) (T) and singlechannel reactor (500 pm) (A) [13]. Figure 5.6 Flow pattern map for a gas/liquid flow regime in micro channels. Annular flow wavy annular flow (WA) wavy annular-dry flow (WAD) slug flow bubbly flow annular-dry flow (AD). Transition lines for nitrogen/acetonitrile flows in a triangular channel (224 pm) (solid line). Transition lines for air/water flows in triangular channels (1.097 mm) (dashed lines). Region 2 presents flow conditions in the dual-channel reactor ( ), with the acetonitrile/nitrogen system between the limits of channeling (I) and partially dried walls (III). Flow conditions in rectangular channels for a 32-channel reactor (150 pm) (T) and singlechannel reactor (500 pm) (A) [13].

See other pages where Liquid flow region is mentioned: [Pg.7]    [Pg.149]    [Pg.94]    [Pg.322]    [Pg.38]    [Pg.360]    [Pg.360]    [Pg.361]    [Pg.125]    [Pg.126]    [Pg.346]    [Pg.79]    [Pg.222]    [Pg.257]    [Pg.374]    [Pg.7]    [Pg.149]    [Pg.94]    [Pg.322]    [Pg.38]    [Pg.360]    [Pg.360]    [Pg.361]    [Pg.125]    [Pg.126]    [Pg.346]    [Pg.79]    [Pg.222]    [Pg.257]    [Pg.374]    [Pg.2531]    [Pg.664]    [Pg.607]    [Pg.202]    [Pg.282]    [Pg.426]    [Pg.1345]    [Pg.97]    [Pg.110]    [Pg.111]    [Pg.111]    [Pg.112]    [Pg.130]    [Pg.209]    [Pg.361]    [Pg.139]    [Pg.236]    [Pg.352]    [Pg.396]    [Pg.607]    [Pg.585]    [Pg.621]    [Pg.14]    [Pg.810]    [Pg.131]    [Pg.543]   
See also in sourсe #XX -- [ Pg.10 , Pg.27 , Pg.29 , Pg.56 ]

See also in sourсe #XX -- [ Pg.360 ]




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