Unsteady elastico-viscous flow in a curved pipe

Summary An analysis is presented of the flow of an elasticoviscous liquid in a pipe of circular cross-section, coiled in a circle oflarge radiusR, under the influence of a pressure gradient oscillating (about a zero mean) with frequencyn. Of particular interest is the secondary flow set up in the cross-section of the pipe due to centrifugal effects. For sufficiently small values ofn, it is found that the flow pattern approaches that which would be produced by a steady pressure gradient having the same instantaneous value (Thomas andWalters 1963), and of the type that one would be led to expect by centrifugal effects. For large values ofn, the flow in the interior of the pipe, away from the wall, is spectacularly reversed, flow now being directed towards the centre of curvature, elasticity having the effect of reducing the critical (high) frequencyn = n _c which onsets flow reversal.

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Zusammenfassung Eine Analyse der Strömung einer elasto-viskosen Flüssigkeit in einer Röhre von rundem Querschnitt, die in einem Kreis mit einemgroßen RadiusR gewunden ist, wird unter dem Einfluß eines Druckgradienten, der mit der Frequenzn oszilliert (um einen Nulldurchschnitt), dargestellt. Von besonderem Interesse ist die Sekundärströmung, die in dem Querschnitt der Röhre unter dem Einfluß der Zentrifugalwirkungen entsteht. Für genügend kleine Werte vonn wird herausgefunden, daß das Strömungsbild sich demjenigen annähert, das von einem stationären Druckgradienten erzeugt werden würde, der denselben augenblicklichen Wert besitzt (Thomas andWalters 1963) und dem Typus angehört, den man aufgrund der Zentrifugalwirkungen erwarten würde. Für große Werte vonn wird die Strömung im Inneren der Röhre, d. h. von den Rändern entfernt, in spektakulärer Weise umgekehrt; jetzt wird die Strömung zum Krümmungsmittelpunkt hin gerichtet, und die Elastizität hat die Wirkung, die kritische (hohe) Frequenzn = n _c zu reduzieren, bei der die Strömungsumkehr beginnt.

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With 2 figures     

Unsteady elastico-viscous flow in a rotating pipe

Summary An analysis is presented of incompressible flow in a straight pipe of circular cross-section, rotating about an axis perpendicular to its length, under the influence of a periodic pressure gradient. It is shown that the secondary axial velocity along the pipe is comprised of a steady part and an unsteady part oscillating at twice the frequency of the applied pressure gradient. Of particular interest is the steady component of velocity for which it is shown that, at high frequencies, a reversal of drift in certain regions can be induced.

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Zusammenfassung Es wird eine Analyse der inkompressiblen Strömung in einem geraden Rohr mit rundem Querschnitt, das um eine senkrecht zu seiner Länge verlaufende Achse rotiert, unter dem Einfluß eines periodischen Druckgradienten gegeben. Dabei wird gezeigt, daß die sekundäre axiale Anströmungsgeschwindigkeit in der Röhre aus einem stationären Anteil und aus einem nichtstationären Anteil besteht. Der letztere oszilliert mit einer Frequenz, die doppelt so groß ist wie die des wirkenden Druckgradienten. Von besonderem Interesse ist der stationäre Anteil der Angströmgeschwindigkeit, für den gezeigt wird, daß bei hohen Frequenzen in gewissen Bereichen eine Umkehr der Strömungsrichtung herbeigeführt werden kann.

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With 3 figures     

Hierarchical structures in a turbulent pipe flow

A hierarchical structure (HS) analysis (β-test and γ-test) is applied to a fully developed turbulent pipe flow. Velocity signals are measured at two cross sections in the pipe and at a series of radial locations from the pipe wall. Particular attention is paid to the variation of turbulent statistics at wall units 10<y⁺<3000. It is shown that at all locations the velocity fluctuations satisfy the She–Leveque hierarchical symmetry (Phys. Rev. Lett. 72 (1994) 336). The measured HS parameters, β and γ, are interpreted in terms of the variation of fluid structures. Intense anisotropic fluid structures generated near the wall appear to be more singular than the most intermittent structures in isotropic turbulence and appear to be more outstanding compared to the background fluctuations; this yields a more intermittent velocity signal with smaller γ and β. As turbulence migrates into the logarithmic region, small-scale motions are generated by an energy cascade and large-scale organized structures emerge which are also less singular than the most intermittent structures of isotropic turbulence. At the center, turbulence is nearly isotropic, and β and γ are close to the 1994 She–Leveque predictions. A transition is observed from the logarithmic region to the center in which γ drops and the large-scale organized structures break down. We speculate that it is due to the growing eddy viscosity effects of widely spread turbulent fluctuations in a similar way as in the breakdown of the Taylor vortices in a turbulent Couette–Taylor flow at high Reynolds numbers.     

Swirling turbulent flow through a curved pipe

An experimental study of a swirling turbulent flow through a curved pipe with a pipe-to-mean-bend radius ratio of 0.077 and a flow Reynolds number based on pipe diameter and mean bulk velocity of 50,000 has been carried out. A rotating section, six pipe diameters long, is set up at six diameters upstream of the curved bend entrance. The rotating section is designed to provide a solid-body rotation to the flow. At the entrance of the rotating section, a fully-developed turbulent pipe flow is established. This study reports on the flow characteristics for the case where the swirl number, defined as the ratio of the pipe circumferential velocity to mean bulk velocity, is one. Wall static pressures, mean velocities, Reynolds stresses and wall shear distribution around the pipe are measured using pressure transducers, rotating-wires and surface hot-film gauges. The measurements are used to analyze the competing effects of swirl and bend curvature on curved-pipe flows, particularly their influence on the secondary flow pattern in the crossstream plane of the curved pipe. At this swirl number, all measured data indicate that, besides the decaying combined free and forced vortex, there are no secondary cells present in the cross-stream plane of the curved pipe. Consequently, the flow displays characteristics of axial symmetry and the turbulent normal stress distributions are more uniform across the pipe compared to fully-developed pipe flows.List of symbols B calibration constant - e bridge voltage - e ₀ bridge voltage at zero flow - C _f total skin friction coefficient, = 2 _w/ W ₀ ² - D pipe diameter, = 7.62 cm - De Dean number, = ^1/2 Re - M angular momentum - n calibration constant - N _s swirl number, = D/2 W ₀ - r radial coordinate - R mean bend radius of curvature, = 49.5 cm - Re pipe Reynolds number, = DW ₀/ - S axial coordinate along the upstream (measured negative) and downstream (measured positive) tangent - U, V, W mean velocities along the radial, tangential and axial directions, respectively - u, v, w mean fluctuating velocities along the radial, tangential and axial directions, respectively - u, v, w root mean square normal stress along the radial, tangential and axial directions, respectively - v ^{ov2}, u^{ov2} normal stress along the tangential and radial direction, respectively - W ₀ mean bulk velocity, 10 m/s - W _c W measured at pipe axis - W total wall friction velocity, - total wall friction velocity measured at S/D = -18 - ,v vw, w7#x016B; turbulent shear stresses - pipe-to-mean-bend radius ratio, = D/2 R = 0.077 - axial coordinate measured from bend entrance - fluid kinematic viscosity - fluid density - _w mean total wall shear stress - instantaneous total wall shear - azimuthal coordinate measured zero from pipe hori zontal diameter near outer bend - angular speed of the rotating section     

Swirling turbulent flow through a curved pipe

An experimental study of swirling turbulent flow through a curved bend and its downstream tangent has been carried out. This study reports on the recovery from swirl and bend curvature and relies on measurements obtained in the downstream tangent and data reported in Part 1 to assess the recovery. Unlike the nonswirling flow case, the present measurements show that the cross-stream secondary flow is dominated by the decay of the solid-body rotation and the total wall shear stress measured at the inner and outer bend (furthest away from the bend center of curvature) is approximately equal. The shear distribution is fairly uniform, even at 1 D downstream of the bend exit. At 49D downstream of the bend exit, the mean axial velocity has recovered to its measured profile at 18D upstream of the bend entrance. Furthermore, the mean tangential velocity is close to zero everywhere and the turbulent shear and normal stresses take another 15D to approximately approach their stationary straight pipe values. Therefore, complete flow recovery from swirl and bend curvature takes a total length of about 85D from the bend entrance. This compares with a recovery length of about 78D for bend curvature alone. The recovery length is substantially shorter than that measured previously in swirling flow through straight pipes and is a consequence of the angular momentum decreasing by approximately 74% across the curved bend. Consequently, the effect of bend curvature is to accelerate swirl decay in a pipe flow.List of symbols C _f total skin friction coefficient, = 2 _w / w ₀ ² - D pipe diameter, = 7.62 cm - De Dean number, = ^1/2 Re = 13,874 - M angular momentum - N _s swirl number, = D/2 W ₀ = 1 - r radial coordinate - R mean bend radius of curvature, = 49.5 cm - Re pipe Reynolds number, = DW ₀ /v= 50,000 - S axial coordinate along the upstream (measured negative) and downstream (measured positive) tangent - U, V, W mean velocities along the radial, tangential and axial directions, respectively - u, v, w mean fluctuating velocities along the radial, tangential and axial directions, respectively - u, v, w root mean square normal stress along the radial, tangential and axial directions, respectively - W ₀ mean bulk velocity, 10 m/s - w total wall friction velocity, = _w / - (w ) _s total wall friction velocity measured as S/D = -18 - turbulent shear stresses - pipe-to-bend radius ratio, = D/2R = 0.077 - axial coordinate measured from bend entrance - fluid kinetic viscosity - fluid density - _w total wall shear stress - azimuthal coordinate measured zero from pipe horizontal diameter near outer bend - angular speed of the rotating section     

Structure of turbulent pipe flow

The problem of turbulent flow in a straight circular pipe is solved. We consider a system consisting of the equation of motion, the equation for the turbulence energy, the expression relating the turbulence coefficient with the turbulence scale, and the integral formula for determining the turbulence scale. A numerical solution is presented for this closed system of equations for turbulent flow. The results of calculations are compared with experimental data.     

Rotation effects on a fully-developed turbulent pipe flow

A fully-developed turbulent pipe flow is allowed to pass through a rotating pipe section, whose axis of rotation coincides with the pipe axis. At the exit end of the rotating section, the flow passes into a stationary pipe. As a result of the relaxation of surface rotation, the turbulent flow near the pipe wall is affected by extra turbulence production created by the large circumferential shear strain set up by the rapid decrease of the rotational velocity to zero at the wall. However, the flow in the most part of the pipe is absent of this extra turbulence production because the circumferential strain is zero as a result of the solid-body rotation imparted to the flow by the rotating pipe section. The combined effect of these two phenomena on the flow is investigated in detail using hot-wire anemometry techniques. Both mean and turbulence fields are measured, together with the wall shear and the turbulent burst behavior at the wall. A number of experiments at different rotational speeds are carried out. Therefore, the effects of rotation on the behavior of wall shear, turbulent burst at the wall, turbulence production and the near-wall flow can be documented and analysed in detail.     

Optimal transient growth in turbulent pipe flow

The optimal transient growth process of perturbations driven by the pressure gradient is studied in a turbulent pipe flow. A new computational method is proposed, based on the projection operators which project the governing equations onto the subspace spanned by the radial vorticity and radial velocity. The method is validated by comparing with the previous studies. Two peaks of the maximum transient growth amplification curve are found at different Reynolds numbers ranging from 20 000 to 250 000. The optimal flow structures are obtained and compared with the experiments and DNS results. The location of the outer peak is at the azimuthal wave number n=1, while the location of the inner peak is varying with the Reynolds number. It is observed that the velocity streaks in the buffer layer with a spacing of 100δ_v are the most amplified flow structures. Finally, we consider the optimal transient growth time and its dependence on the azimuthal wave length. It shows a self-similar behavior for perturbations of different scales in the optimal transient growth process.     

Nuclear magnetic resonance study of turbulent flow in a pipe

Results are given from an investigation of longitudinal turbulent diffusion by the nuclear magnetic tracer method, and a technique is described for determining the velocity distribution function of the fluid particles in the pipe cross section.Translated from Izvestiya Akademii Nauk SSSR, Mekhanika Zhidkosti i Gaza, No. 6, pp. 105–110, November–December, 1971.     

Particle behavior in a turbulent pipe flow with a flat bed

Particle behavior in a turbulent flow in a circular pipe with a bed height h = 0.5R is studied at Re_b = 40,000 and for two sizes of particles (5 μm and 50 μm) using large eddy simulation, one-way coupled with a Lagrangian particle tracking technique. Turbulent secondary flows are found within the pipe, with the curved upper wall affecting the secondary flow formation giving rise to a pair of large upper vortices above two smaller vortices close to the pipe floor. The behavior of the two sizes of particle is found to be quite different. The 50 μm particles deposit forming irregular elongated particle streaks close to the pipe floor, particularly at the center of the flow and the pipe corners due to the impact of the secondary flows. The deposition and resuspension rate of the 5 μm particles is high near the center of the floor and at the pipe corners, while values for the 50 μm particles are greatest near the corners. Near the curved upper wall of the pipe, the deposition rate of the 5 μm particles increases in moving from the wall center to the corners, and is greater than that for the larger particles due to the effects of the secondary flow. The maximum resuspension rate of the smaller particles occurs above the pipe corners, with the 50 μm particles showing their highest resuspension rate above and at the corners of the pipe.     

Skin Friction following BLADE manipulation in a turbulent pipe flow

This study attempts to analyze the measured wall shear stress distribution downstream of single and tandem BLADEs in fully developed pipe flow. Previous works have indicated the adverse effect of overall drag increase with the single BLADE in both channel and pipe flows, and an even larger drag increase with the tandem BLADES. This is contrary to that observed for external boundary layer flow. Extensive comparisons are then made to the wall shear stress distribution following BLADEs in boundary layer flow, leading to the conclusion of little or no potential in the application of BLADEs alone to pipe flow.     

Deposition of inertial particles from a turbulent pipe flow

An explicit formula is derived for the rate of deposition of large particles (droplets) on a tube wall in two-phase turbulent flow. Moscow. Translated from Izvestiya Rossiiskoi Akademii Nauk, Mekhanika Zhidkosti i Gaza, No. 2, pp. 68–75, March–April, 1998. The work was financially supported by the International scientific foundation INTAS (grant No. 94-4348) and by the Russian Foundation for Fundamental Research (project No. 97-01-00398).     

Unsteady separated and reattaching turbulent flow over a two-dimensional square rib

The spatio-temporal characteristics of the separated and reattaching turbulent flow over a two-dimensional square rib were studied experimentally. Synchronized measurements of wall-pressure fluctuations and velocity fluctuations were made using a microphone array and a split-fiber film, respectively. Profiles of time-averaged streamwise velocity and wall-pressure fluctuations showed that the shear layer separated from the leading edge of the rib sweeps past the rib and directly reattaches on the bottom wall (x/H=9.75) downstream of the rib. A thin region of reverse flow was formed above the rib. The shedding large-scale vortical structures (fH/U₀=0.03) and the flapping separation bubble (fH/U₀=0.0075) could be discerned in the wall-pressure spectra. A multi-resolution analysis based on the maximum overlap discrete wavelet transform (MODWT) was performed to extract the intermittent events associated with the shedding large-scale vortical structures and the flapping separation bubble. The convective dynamics of the large-scale vortical structures were analyzed in terms of the autocorrelation of the continuous wavelet-transformed wall pressure, cross-correlation of the wall-pressure fluctuations, and the cross-correlation between the wall pressure at the time-averaged reattachment point and the streamwise velocity field. The convection speeds of the large-scale vortical structures before and after the reattachment point were U_c=0.35U₀ and 0.45U₀, respectively. The flapping motion of the separation bubble was analyzed in terms of the conditionally averaged reverse-flow intermittency near the wall region. The instantaneous reattachment point in response to the flapping motion was obtained; these findings established that the reattachment zone was a 1.2H-long region centered at x/H=9.75. The reverse-flow intermittency in one period of the flapping motion demonstrated that the thin reverse flow above the rib is influenced by the flapping motion of the separation bubble behind the rib.     

Mixing of mutually soluble liquids in turbulent flow in a pipe

The problem concerned with mixing of mutually soluble liquids in turbulent flow in a pipe [1–11] is considered. To describe the distribution of concentration in the region of mixture, taken average across the section of the pipe, we use a model based on a one-dimensional model of the type of heat-conduction equation with an effective coefficient which, as tests show, is different from the coefficients of molecular and turbulent transfer. The dimensionless value of this coefficient depends on a number of parameters, such as the Reynolds number calculated for one of the liquids, roughness, ratio of the densities and viscosities of the liquids, as well as on the concentration, gradients of concentration, etc. These relationships can be established either by means of tests or on the basis of theoretical consideration of the mixing phenomenon. In this paper we theoretically derive a dispersion model with an effective diffusion coefficient which depends on Reynolds and Schmidt numbers, as well as on roughness.Translated from Zhurnal Prikladnoi Mekhaniki i Tekhnicheskoi Fiziki, No. 5, pp. 96–102, September–October, 1971.     

Unsteady hydromagnetic pipe flow at small Hartmann number

Summary In this paper we have studied the problem of the unsteady flow of an electrically conducting incompressible viscous fluid through a circular pipe under the influence of a uniform applied transverse magnetic field when the walls are non-conducting. It has been assumed that the velocity vanishes on the non-conducting walls and initially the fluid is at rest. The velocity field and the induced magnetic field are calculated by an iteration procedure and have been found up to second order terms inM (Hartmann number) which is taken to be small. We have also neglected the term involving (= 4/) the self inductance of the fluid, which is valid for small values ofM.Since the pressure gradient is not necessarily a constant in unsteady flow, we have assumed it to be an arbitrary function of time. A particular case when the pressure gradient is an exponential function of time has also been investigated in detail. For a constant pressure gradient the curves for the velocity field and the induced magnetic field have been drawn (at different values of Hartmann number and time). It has been found that for small values of time the fluid is accelerated near the centre in contrast to the case of a non-conducting fluid.     

Velocity field in isothermal turbulent bubbly gas-liquid flow through a pipe

Velocity field was measured by laser Doppler velocimetry in isothermal, turbulent bubbly gas-liquid flow through a 26.6 mm inner diameter vertical pipe. The measurements were made about 33 diameters downstream from the pipe entrance, gas injection being just upstream of the entrance. The gas phase radial distribution at the measurement plane exhibited influence of the injection device in that higher gas fraction existed in the central region of the pipe. For comparison, velocity field was also measured in isothermal, turbulent single-phase liquid flow through the same pipe at the same axial plane. Measured were the radial distributions of liquid mean axial and radial velocities, axial and radial turbulent intensities, and axial Reynolds shear stress. The radial distributions of gas bubble mean axial velocity and axial velocity fluctuation intensity were also measured by LDV. A dualsensor fiberoptic probe was used at the same time to measure the radial distributions of gas fraction, bubble mean axial velocity and size slightly downstream of the LDV measurement plane.List of Symbols an average gas bubble diameter - f, f _TP friction factor, friction factor for gas-liquid flow - k _L liquid turbulent kinetic energy - , gas, liquid mass flow rate - R inner radius of pipe - r, {sitR}^* radial coordinate; nondimensional radial coordinate (=r/R) - Re _L liquid Reynolds number - U _G mean axial velocity of gas bubble - U _L mean axial velocity of liquid - U _LO mean axial velocity for flow at the total mass velocity with properties of the liquid phase - u _L ⁺ nondimensional mean axial velocity of liquid in wall coordinate - friction velocity - axial velocity fluctuation intensity of liquid - axial velocity fluctuation intensity of gas bubbles - V_L mean radial velocity of liquid - v _L radial velocity fluctuation intensity of liquid - (uv)_L single-point cross-correlation between axial and radial velocity fluctuations of liquid ( axial Reynolds shear stress) - T _in mean liquid temperature at test section inlet - x flow quality - y normal distance from wall - y ⁺ nondimensional normal distance from wall in wall coordinate (=yu/v_L) - _G gas phase residence time fraction - _L rate of dissipation in the liquid - _L Kolmogorov length scale in the liquid - _L liquid kinematic viscosity - _L characteristic turbulence length scale in the liquid - _G, _L density of gas, liquid - _m gas-liquid mixture density This work was partly supported by National Science Foundation, Thermal Transport and Thermal Processing Program, Chemical and Thermal Systems Division, under Grant No. CTS-9411898.     

Heavy particle dispersion from a point source in turbulent pipe flow

Dispersion of heavy particles from a point source in high-Reynolds pipe flow was studied using large-eddy simulation, LES. A stochastic Langevin type Lagrangian model developed by Berrouk et al. was used to account for heavy particle transport by the sub-grid scale motion. In both the LES and in an experiment by Arnason, the larger particles dispersed more than the small ones. The change in diffusivity with particle size is interpreted in terms of the effect of inertia and cross-trajectory effects and qualitatively compared with the analysis of heavy particle dispersion in isotropic turbulence by Wang and Stock. Particle inertia has a much larger influence on the dispersion than the crossing-trajectories effects.