About: Slug flow is a(n) research topic. Over the lifetime, 3758 publication(s) have been published within this topic receiving 71157 citation(s).
01 Jan 1976-Aiche Journal
Abstract: Models are presented for determining flow regime transitions in two-phase gas-liquid flow. The mechanisms for transition are based on physical concepts and are fully predictive in that no flow regime transitions are used in their development. A generalized flow regime map based on this theory is presented.
01 May 1980-Aiche Journal
Abstract: Models for predicting flow pattern transitions during steady gas-liquid flow in vertical tubes are developed, based on physical mechanisms suggested for each transition. These models incorporate the effect of fluid properties and pipe size and thus are largely free of the limitations of empirically based transition maps or correlations.
Milton S. Plesset1•Institutions (1)
01 Sep 1949-Journal of Applied Mechanics
Abstract: Three regimes of liquid flow over a body are defined, namely: (a) noncavitating flow; (b) cavitating flow with a relatively small number of cavitation bubbles in the field of flow; and (c) cavitating flow with a single large cavity about the body. The assumption is made that, for the second regime of flow, the pressure coefficient in the flow field is no different from that in the noncavitating flow. On this basis, the equation of motion for the growth and collapse of a cavitation bubble containing vapor is derived and applied to experimental observations on such bubbles. The limitations of this equation of motion are pointed out, and include the effect of the finite rate of evaporation and condensation, and compressibility of vapor and liquid. A brief discussion of the role of "nuclei" in the liquid in the rate of formation of cavitation bubbles is also given.
19 Jun 1973-Journal of Fluid Mechanics
Abstract: Conditionally sampled hot-wire measurements were taken in a pipe at Reynolds numbers corresponding to the onset of turbulence. The pipe was smooth and carefully aligned so that turbulent slugs appeared naturally at Re > 5 × 104. Transition could be initiated at lower Re by introducing disturbances into the inlet. For smooth or only slightly disturbed inlets, transition occurs as a result of instabilities in the boundary layer long before the flow becomes fully developed in the pipe. This type of transition gives rise to turbulent slugs which occupy the entire cross-section of the pipe, and they grow in length as they proceed downstream. The leading and trailing ‘fronts’ of a turbulent slug are clearly defined. A unique relation seems to exist between the velocity of the interface and the velocity of the fluid by which relaminarization of turbulent fluid is prevented. The length of slugs is of the same order of magnitude as the length of the pipe, although the lengths of individual slugs differ at the same flow conditions. The structure of the flow in the interior of a slug is identical to that in a fully developed turbulent pipe flow. Near the interfaces, where the mean motion changes from a laminar to a turbulent state, the velocity profiles develop inflexions. The total turbulent intensity near the interfaces is very high and it may reach 15% of the velocity at the centre of the pipe. A turbulent energy balance was made for the flow near the interfaces. All of the terms contributing to the energy balance must vanish identically somewhere on the interface if that portion of the interface does not entrain non-turbulent fluid. It appears that diffusion which also includes pressure transport is the most likely mechanism by which turbulent energy can be transferred to non-turbulent fluid. The dissipation term at the interface is negligible and increases with increasing turbulent energy towards the interior of the slug.Mixed laminar and turbulent flows were observed far downstream for \[ 2000 < Re < 2700 \] when a large disturbance was introduced into the inlet. The flow in the vicinity of the inlet, however, was turbulent at much lower Re. The turbulent regions which are convected downstream at a velocity which is slightly smaller than the average velocity in the pipe we shall henceforth call puffs. The leading front of a puff does not have a clearly defined interface and the trailing front is clearly defined only in the vicinity of the centre-line. The length and structure of the puff is independent of the character of the obstruction which created it, provided that the latter is big enough to produce turbulent flow at the inlet. The puff will be discussed in more detail later.
01 Nov 1975-Industrial & Engineering Chemistry Fundamentals
Abstract: Kase, S.. J. Appl. Polym. Sci., 18, 3279 (1974). Matovich. M. A,, Pearson, J. R. A,. Ind. Eng. Chem., Fundam., 8, 512 (1969). Miller, J. C., S.P.E. Trans., 3, 134 (1963). Nickell, R. E., Tanner, R. I., Caswell. E., J. FIMMech., 65, 189 (1974). Pearson. J. R. A,, Matovich. M. A,. Ind. Eng. Chem., Fundam., 8, 605 (1969). Pearson, J. R. A,, Shah, Y. T., Trans. SOC. Rheol., 16, 519 (1972). Pearson, J. R. A., Shah, Y. T.. Ind. Eng. Chem., Fundam., 13, 134 (1974). Shah, Y. T., Pearson, J. R. A.. Ind. Eng. Chem., Fundam.. 11, 150 (1972). Trouton, F. T.. Proc. Roy. SOC. Ser. A, 77, 426 (1906). Weinberger, C. B., Ph.D. Dissertation, University of Michigan, 1970 Weinberger, C. B., Goddard, J. D., Int. J. Multiphase Now, 1, 465 (1974).
Topics: Slug flow (79%)