Reynolds number

The plume from this candle flame transitions from laminar to turbulent.

The transition from laminar (left) to turbulent (right) flow of water from a tap occurs as the Reynolds number increases.

A vortex street around a cylinder. This can occur around cylinders and spheres, for any fluid, cylinder size, and fluid speed provided that it has a Reynolds number between roughly 40 and 1000.

George Stokes introduced Reynolds numbers.

Osborne Reynolds popularised the concept.

In fluid dynamics, the Reynolds number (Re) is a dimensionless quantity that helps predict fluid flow patterns in different situations by measuring the ratio between inertial and viscous forces. At low Reynolds numbers, flows tend to be dominated by laminar (sheet-like) flow, while at high Reynolds numbers, flows tend to be turbulent. The turbulence results from differences in the fluid's speed and direction, which may sometimes intersect or even move counter to the overall direction of the flow (eddy currents). These eddy currents begin to churn the flow, using up energy in the process, which for liquids increases the chances of cavitation.

The Reynolds number has wide applications, ranging from liquid flow in a pipe to the passage of air over an aircraft wing. It is used to predict the transition from laminar to turbulent flow and is used in the scaling of similar but different-sized flow situations, such as between an aircraft model in a wind tunnel and the full-size version. The predictions of the onset of turbulence and the ability to calculate scaling effects can be used to help predict fluid behavior on a larger scale, such as in local or global air or water movement, and thereby the associated meteorological and climatological effects.

The concept was introduced by George Stokes in 1851, but the Reynolds number was named by Arnold Sommerfeld in 1908 after Osborne Reynolds (1842–1912), who popularized its use in 1883. (cf. this list)

Definition

The Reynolds number is the ratio of inertial forces to viscous forces within a fluid that is subjected to relative internal movement due to different fluid velocities. A region where these forces change behavior is known as a boundary layer, such as the bounding surface in the interior of a pipe. A similar effect is created by the introduction of a stream of high-velocity fluid into a low-velocity fluid, such as the hot gases emitted from a flame in air. This relative movement generates fluid friction, which is a factor in developing turbulent flow. Counteracting this effect is the viscosity of the fluid, which tends to inhibit turbulence. The Reynolds number quantifies the relative importance of these two types of forces for given flow conditions and is a guide to when turbulent flow will occur in a particular situation.

This ability to predict the onset of turbulent flow is an important design tool for equipment such as piping systems or aircraft wings, but the Reynolds number is also used in scaling of fluid dynamics problems and is used to determine dynamic similitude between two different cases of fluid flow, such as between a model aircraft, and its full-size version. Such scaling is not linear and the application of Reynolds numbers to both situations allows scaling factors to be developed.

With respect to laminar and turbulent flow regimes:

• laminar flow occurs at low Reynolds numbers, where viscous forces are dominant, and is characterized by smooth, constant fluid motion;
• turbulent flow occurs at high Reynolds numbers and is dominated by inertial forces, which tend to produce chaotic eddies, vortices and other flow instabilities.

The Reynolds number is defined as:

$\mathrm {Re} ={\frac {uL}{\nu }}={\frac {\rho uL}{\mu }}$

where:

• ρ is the density of the fluid (SI units: kg/m³)
• u is the flow speed (m/s)
• L is a characteristic length (m)
• μ is the dynamic viscosity of the fluid (Pa·s or N·s/m² or kg/(m·s))
• ν is the kinematic viscosity of the fluid (m²/s).

The Brezina equation

The Reynolds number can be defined for several different situations where a fluid is in relative motion to a surface. These definitions generally include the fluid properties of density and viscosity, plus a velocity and a characteristic length or characteristic dimension (L in the above equation). This dimension is a matter of convention—for example radius and diameter are equally valid to describe spheres or circles, but one is chosen by convention. For aircraft or ships, the length or width can be used. For flow in a pipe, or for a sphere moving in a fluid, the internal diameter is generally used today. Other shapes such as rectangular pipes or non-spherical objects have an equivalent diameter defined. For fluids of variable density such as compressible gases or fluids of variable viscosity such as non-Newtonian fluids, special rules apply. The velocity may also be a matter of convention in some circumstances, notably stirred vessels.

In practice, matching the Reynolds number is not on its own sufficient to guarantee similitude. Fluid flow is generally chaotic, and very small changes to shape and surface roughness of bounding surfaces can result in very different flows. Nevertheless, Reynolds numbers are a very important guide and are widely used.

Derivation

If we know that the relevant physical quantities in a physical system are only $\rho ,u,L,\mu$, then the Reynolds number is essentially fixed by the Buckingham π theorem.

In detail, since there are 4 quantities $\rho ,u,L,\mu$, but they have only 3 dimensions (length, time, mass), we can consider $\rho ^{x_{1}}u^{x_{2}}L^{x_{3}}\mu ^{x_{4}}$, where $x_{1},...,x_{4}$ are real numbers. Setting the three dimensions of $\rho ^{x_{1}}u^{x_{2}}L^{x_{3}}\mu ^{x_{4}}$ to zero, we obtain 3 independent linear constraints, so the solution space has 1 dimension, and it is spanned by the vector $(1,1,1,-1)$.

Thus, any dimensionless quantity constructed out of $\rho ,u,L,\mu$ is a function of $\rho uL\mu ^{-1}$, the Reynolds number.

Alternatively, we can take the incompressible Navier–Stokes equations (convective form):$${\frac {\partial \mathbf {u} }{\partial t}}+(\mathbf {u} \cdot \nabla )\mathbf {u} -\nu \,\nabla ^{2}\mathbf {u} =-{\frac {1}{\rho }}\nabla p+\mathbf {g}$$Remove the gravity term ${\mathbf {g}}$, then the left side consists of inertial force ${\frac {\partial \mathbf {u} }{\partial t}}+(\mathbf {u} \cdot \nabla )\mathbf {u}$, and viscous force $\nu \,\nabla ^{2}\mathbf {u}$. Their ratio has the order of ${\frac {(\mathbf {u} \cdot \nabla )\mathbf {u} }{\nu \,\nabla ^{2}\mathbf {u} }}\sim {\frac {u^{2}/L}{\nu u/L^{2}}}={\frac {uL}{\nu }}$, the Reynolds number. This argument is written out in detail on the Scallop theorem page.

Alternative derivation

The Reynolds number can be obtained when one uses the nondimensional form of the incompressible Navier–Stokes equations for a newtonian fluid expressed in terms of the Lagrangian derivative:

$\rho {\frac {D\mathbf {v} }{Dt}}=-\nabla p+\mu \nabla ^{2}\mathbf {v} +\rho \mathbf {f} .$

Each term in the above equation has the units of a "body force" (force per unit volume) with the same dimensions of a density times an acceleration. Each term is thus dependent on the exact measurements of a flow. When one renders the equation nondimensional, that is when we multiply it by a factor with inverse units of the base equation, we obtain a form that does not depend directly on the physical sizes. One possible way to obtain a nondimensional equation is to multiply the whole equation by the factor

${\frac {L}{\rho V^{2}}},$

where

• V is the mean velocity, v or v, relative to the fluid (m/s),
• L is the characteristic length (m),
• ρ is the fluid density (kg/m³).

If we now set

${\begin{aligned}\mathbf {v} '&={\frac {\mathbf {v} }{V}},&p'&=p{\frac {1}{\rho V^{2}}},&\mathbf {f} '&=\mathbf {f} {\frac {L}{V^{2}}},&{\frac {\partial }{\partial t'}}&={\frac {L}{V}}{\frac {\partial }{\partial t}},&\nabla '&=L\nabla ,\end{aligned}}$

we can rewrite the Navier–Stokes equation without dimensions:

${\frac {D\mathbf {v} '}{Dt'}}=-\nabla 'p'+{\frac {\mu }{\rho LV}}\nabla '^{2}\mathbf {v} '+\mathbf {f} ',$

where the term ⁠μ/ρLV⁠ = ⁠1/Re⁠.

Finally, dropping the primes for ease of reading:

${\frac {D\mathbf {v} }{Dt}}=-\nabla p+{\frac {1}{\mathrm {Re} }}\nabla ^{2}\mathbf {v} +\mathbf {f} .$

Universal sedimentation equation — drag coefficient, a function of Reynolds number and shape factor, 2D diagram

Universal sedimentation equation — drag coefficient, a function of Reynolds number and shape factor, 3D diagram

This is why mathematically all Newtonian, incompressible flows with the same Reynolds number are comparable. Notice also that in the above equation, the viscous terms vanish for Re → ∞. Thus flows with high Reynolds numbers are approximately inviscid in the free stream.

History

Osborne Reynolds's apparatus of 1883 demonstrating the onset of turbulent flow. The apparatus is still at the University of Manchester.

Diagram from Reynolds's 1883 paper showing onset of turbulent flow.

Osborne Reynolds famously studied the conditions in which the flow of fluid in pipes transitioned from laminar flow to turbulent flow. In his 1883 paper Reynolds described the transition from laminar to turbulent flow in a classic experiment in which he examined the behaviour of water flow under different flow velocities using a small stream of dyed water introduced into the centre of clear water flow in a larger pipe.

The larger pipe was glass so the behaviour of the layer of the dyed stream could be observed. At the end of this pipe, there was a flow control valve used to vary the water velocity inside the tube. When the velocity was low, the dyed layer remained distinct throughout the entire length of the large tube. When the velocity was increased, the layer broke up at a given point and diffused throughout the fluid's cross-section. The point at which this happened was the transition point from laminar to turbulent flow.

From these experiments came the dimensionless Reynolds number for dynamic similarity—the ratio of inertial forces to viscous forces. Reynolds also proposed what is now known as the Reynolds averaging of turbulent flows, where quantities such as velocity are expressed as the sum of mean and fluctuating components. Such averaging allows for 'bulk' description of turbulent flow, for example using the Reynolds-averaged Navier–Stokes equations.

Flow in a pipe

For flow in a pipe or tube, the Reynolds number is generally defined as

$\mathrm {Re} ={\frac {uD_{\text{H}}}{\nu }}={\frac {\rho uD_{\text{H}}}{\mu }}={\frac {\rho QD_{\text{H}}}{\mu A}}={\frac {WD_{\text{H}}}{\mu A}},$

where

• D_H is the hydraulic diameter of the pipe (the inside diameter if the pipe is circular) (m),
• Q is the volumetric flow rate (m³/s),
• A is the pipe's cross-sectional area (A = ⁠πD²/4⁠) (m²),
• u is the mean velocity of the fluid (m/s),
• μ (mu) is the dynamic viscosity of the fluid (Pa·s = N·s/m² = kg/(m·s)),
• ν (nu) is the kinematic viscosity (ν = ⁠μ/ρ⁠) (m²/s),
• ρ (rho) is the density of the fluid (kg/m³),
• W is the mass flowrate of the fluid (kg/s).

For shapes such as squares, rectangular or annular ducts where the height and width are comparable, the characteristic dimension for internal-flow situations is taken to be the hydraulic diameter, D_H, defined as

$D_{\text{H}}={\frac {4A}{P}},$

where A is the cross-sectional area, and P is the wetted perimeter. The wetted perimeter for a channel is the total perimeter of all channel walls that are in contact with the flow. This means that the length of the channel exposed to air is not included in the wetted perimeter.

For a circular pipe, the hydraulic diameter is exactly equal to the inside pipe diameter:

$D_{\text{H}}=D.$

For an annular duct, such as the outer channel in a tube-in-tube heat exchanger, the hydraulic diameter can be shown algebraically to reduce to

$D_{\text{H,annulus}}=D_{\text{o}}-D_{\text{i}},$

where

• D_o is the inside diameter of the outer pipe,
• D_i is the outside diameter of the inner pipe.

For calculation involving flow in non-circular ducts, the hydraulic diameter can be substituted for the diameter of a circular duct, with reasonable accuracy, if the aspect ratio AR of the duct cross-section remains in the range ⁠1/4⁠ < AR < 4.

Laminar–turbulent transition

Main article: Laminar–turbulent transition

In boundary layer flow over a flat plate, experiments confirm that, after a certain length of flow, a laminar boundary layer will become unstable and turbulent. This instability occurs across different scales and with different fluids, usually when Re_x ≈ 5×10⁵, where x is the distance from the leading edge of the flat plate, and the flow velocity is the freestream velocity of the fluid outside the boundary layer.

For flow in a pipe of diameter D, experimental observations show that for "fully developed" flow, laminar flow occurs when Re_D < 2300 and turbulent flow occurs when Re_D > 2900. At the lower end of this range, a continuous turbulent-flow will form, but only at a very long distance from the inlet of the pipe. The flow in between will begin to transition from laminar to turbulent and then back to laminar at irregular intervals, called intermittent flow. This is due to the different speeds and conditions of the fluid in different areas of the pipe's cross-section, depending on other factors such as pipe roughness and flow uniformity. Laminar flow tends to dominate in the fast-moving center of the pipe while slower-moving turbulent flow dominates near the wall. As the Reynolds number increases, the continuous turbulent-flow moves closer to the inlet and the intermittency in between increases, until the flow becomes fully turbulent at Re_D > 2900. This result is generalized to non-circular channels using the hydraulic diameter, allowing a transition Reynolds number to be calculated for other shapes of channel.

These transition Reynolds numbers are also called critical Reynolds numbers, and were studied by Osborne Reynolds around 1895. The critical Reynolds number is different for every geometry.

Flow in a wide duct

For a fluid moving between two plane parallel surfaces—where the width is much greater than the space between the plates—then the characteristic dimension is equal to the distance between the plates. This is consistent with the annular duct and rectangular duct cases above, taken to a limiting aspect ratio.

Flow in an open channel

For calculating the flow of liquid with a free surface, the hydraulic radius must be determined. This is the cross-sectional area of the channel divided by the wetted perimeter. For a semi-circular channel, it is a quarter of the diameter (in case of full pipe flow). For a rectangular channel, the hydraulic radius is the cross-sectional area divided by the wetted perimeter. Some texts then use a characteristic dimension that is four times the hydraulic radius, chosen because it gives the same value of Re for the onset of turbulence as in pipe flow, while others use the hydraulic radius as the characteristic length-scale with consequently different values of Re for transition and turbulent flow.

Flow around airfoils

Reynolds numbers are used in airfoil design to (among other things) manage "scale effect" when computing/comparing characteristics (a tiny wing, scaled to be huge, will perform differently). Fluid dynamicists define the chord Reynolds number R = Vc/ν, where V is the flight speed, c is the chord length, and ν is the kinematic viscosity of the fluid in which the airfoil operates, which is 1.460×10⁻⁵ m²/s for the atmosphere at sea level. In some special studies a characteristic length other than chord may be used; rare is the "span Reynolds number", which is not to be confused with span-wise stations on a wing, where chord is still used.

Object in a fluid

The high viscosity of honey results in perfectly laminar flow when poured from a bucket, while the low surface tension allows it to remain sheet-like even after reaching the fluid below. Analogous to turbulence, when the flow meets resistance it slows and begins oscillating back and forth, piling upon itself.

The Reynolds number for an object moving in a fluid, called the particle Reynolds number and often denoted Re_p, characterizes the nature of the surrounding flow and its fall velocity.

In viscous fluids

Creeping flow past a falling sphere: streamlines, drag force F_d and force by gravity F_g.

Where the viscosity is naturally high, such as polymer solutions and polymer melts, flow is normally laminar. The Reynolds number is very small and Stokes' law can be used to measure the viscosity of the fluid. Spheres are allowed to fall through the fluid and they reach the terminal velocity quickly, from which the viscosity can be determined.

The laminar flow of polymer solutions is exploited by animals such as fish and dolphins, who exude viscous solutions from their skin to aid flow over their bodies while swimming. It has been used in yacht racing by owners who want to gain a speed advantage by pumping a polymer solution such as low molecular weight polyoxyethylene in water, over the wetted surface of the hull.

It is, however, a problem for mixing polymers, because turbulence is needed to distribute fine filler (for example) through the material. Inventions such as the "cavity transfer mixer" have been developed to produce multiple folds into a moving melt so as to improve mixing efficiency. The device can be fitted onto extruders to aid mixing.

Sphere in a fluid

Drag coefficient C_d for a sphere as a function of Reynolds number Re, as obtained from laboratory experiments. The dark line is for a sphere with a smooth surface, while the lighter line is for the case of a rough surface (e.g. with small dimples). There is a range of fluid velocities where a rough-surfaced golf ball experiences less drag than a smooth ball. The numbers along the line indicate several flow regimes and associated changes in the drag coefficient:

2. attached flow (Stokes flow) and steady separated flow,
3. separated unsteady flow, having a laminar flow boundary layer upstream of the separation, and producing a vortex street,
4. separated unsteady flow with a laminar boundary layer at the upstream side, before flow separation, with downstream of the sphere a chaotic turbulent wake,
5. post-critical separated flow, with a turbulent boundary layer.

For a sphere in a fluid, the characteristic length-scale is the diameter of the sphere and the characteristic velocity is that of the sphere relative to the fluid some distance away from the sphere, such that the motion of the sphere does not disturb that reference parcel of fluid. The density and viscosity are those belonging to the fluid. Note that purely laminar flow only exists up to Re = 10 under this definition.

Under the condition of low Re, the relationship between force and speed of motion is given by Stokes' law.

At higher Reynolds numbers the drag on a sphere depends on surface roughness. Thus, for example, adding dimples on the surface of a golf ball causes the boundary layer on the upstream side of the ball to transition from laminar to turbulent. The turbulent boundary layer is able to remain attached to the surface of the ball much longer than a laminar boundary and so creates a narrower low-pressure wake and hence less pressure drag. The reduction in pressure drag causes the ball to travel farther.

Rectangular object in a fluid

The equation for a rectangular object is identical to that of a sphere, with the object being approximated as an ellipsoid and the axis of length being chosen as the characteristic length scale. Such considerations are important in natural streams, for example, where there are few perfectly spherical grains. For grains in which measurement of each axis is impractical, sieve diameters are used instead as the characteristic particle length-scale. Both approximations alter the values of the critical Reynolds number.

Fall velocity

The particle Reynolds number is important in determining the fall velocity of a particle. When the particle Reynolds number indicates laminar flow, Stokes' law can be used to calculate its fall velocity or settling velocity. When the particle Reynolds number indicates turbulent flow, a turbulent drag law must be constructed to model the appropriate settling velocity.

Packed bed

For fluid flow through a bed, of approximately spherical particles of diameter D in contact, if the voidage is ε and the superficial velocity is v_s, the Reynolds number can be defined as

$\mathrm {Re} ={\frac {\rho v_{\text{s}}D}{\mu }},$

or

$\mathrm {Re} ={\frac {\rho v_{\text{s}}D}{\mu \varepsilon }},$

or

$\mathrm {Re} ={\frac {\rho v_{\text{s}}D}{\mu (1-\varepsilon )}}.$

The choice of equation depends on the system involved: the first is successful in correlating the data for various types of packed and fluidized beds, the second Reynolds number suits for the liquid-phase data, while the third was found successful in correlating the fluidized bed data, being first introduced for liquid fluidized bed system.

Laminar conditions apply up to Re = 10, fully turbulent from Re = 2000.

Stirred vessel

In a cylindrical vessel stirred by a central rotating paddle, turbine or propeller, the characteristic dimension is the diameter of the agitator D. The velocity V is ND where N is the rotational speed in rad per second. Then the Reynolds number is:

$\mathrm {Re} ={\frac {\rho ND^{2}}{\mu }}={\frac {\rho VD}{\mu }}.$

The system is fully turbulent for values of Re above 10000.

Pipe friction

The Moody diagram, which describes the Darcy–Weisbach friction factor f as a function of the Reynolds number and relative pipe roughness.

Pressure drops seen for fully developed flow of fluids through pipes can be predicted using the Moody diagram which plots the Darcy–Weisbach friction factor f against Reynolds number Re and relative roughness ⁠ε/D⁠. The diagram clearly shows the laminar, transition, and turbulent flow regimes as Reynolds number increases. The nature of pipe flow is strongly dependent on whether the flow is laminar or turbulent.

Similarity of flows

Qualitative behaviors of fluid flow over a cylinder depends to a large extent on Reynolds number; similar flow patterns often appear when the shape and Reynolds number is matched, although other parameters like surface roughness have a big effect.

In order for two flows to be similar, they must have the same geometry and equal Reynolds and Euler numbers. When comparing fluid behavior at corresponding points in a model and a full-scale flow, the following holds:

${\begin{aligned}\mathrm {Re} _{\text{m}}&=\mathrm {Re} ,\\\mathrm {Eu} _{\text{m}}&=\mathrm {Eu} ,\end{aligned}}$

where $\mathrm {Re} _{\text{m}}$ is the Reynolds number for the model, and $\mathrm {Re}$ is full-scale Reynolds number, and similarly for the Euler numbers.

The model numbers and design numbers should be in the same proportion, hence

${\frac {p_{\text{m}}}{\rho _{\text{m}}v_{\text{m}}^{2}}}={\frac {p}{\rho v^{2}}}.$

This allows engineers to perform experiments with reduced scale models in water channels or wind tunnels and correlate the data to the actual flows, saving on costs during experimentation and on lab time. Note that true dynamic similitude may require matching other dimensionless numbers as well, such as the Mach number used in compressible flows, or the Froude number that governs open-channel flows. Some flows involve more dimensionless parameters than can be practically satisfied with the available apparatus and fluids, so one is forced to decide which parameters are most important. For experimental flow modeling to be useful, it requires a fair amount of experience and judgment of the engineer.

An example where the mere Reynolds number is not sufficient for the similarity of flows (or even the flow regime – laminar or turbulent) are bounded flows, i.e. flows that are restricted by walls or other boundaries. A classical example of this is the Taylor–Couette flow, where the dimensionless ratio of radii of bounding cylinders is also important, and many technical applications where these distinctions play an important role. Principles of these restrictions were developed by Maurice Marie Alfred Couette and Geoffrey Ingram Taylor and developed further by Floris Takens and David Ruelle.

Typical values of Reynolds number

• Dictyostelium amoebae: ~ 1 × 10⁻⁶
• Bacterium ~ 1 × 10⁻⁴
• Ciliate ~ 1 × 10⁻¹
• Smallest fish ~ 1
• Blood flow in brain ~ 1 × 10²
• Blood flow in aorta ~ 1 × 10³
• Onset of turbulent flow ~ 2.3 × 10³ to 5.0 × 10⁴ for pipe flow to 10⁶ for boundary layers
• Typical pitch in Major League Baseball ~ 2 × 10⁵
• Person swimming ~ 4 × 10⁶
• Fastest fish ~ 1 × 10⁸
• Blue whale ~ 4 × 10⁸
• A large ship (Queen Elizabeth 2) ~ 5 × 10⁹
• Atmospheric tropical cyclone ~ 1 x 10¹²

Smallest scales of turbulent motion

In a turbulent flow, there is a range of scales of the time-varying fluid motion. The size of the largest scales of fluid motion (sometimes called eddies) are set by the overall geometry of the flow. For instance, in an industrial smoke stack, the largest scales of fluid motion are as big as the diameter of the stack itself. The size of the smallest scales is set by the Reynolds number. As the Reynolds number increases, smaller and smaller scales of the flow are visible. In a smokestack, the smoke may appear to have many very small velocity perturbations or eddies, in addition to large bulky eddies. In this sense, the Reynolds number is an indicator of the range of scales in the flow. The higher the Reynolds number, the greater the range of scales. The largest eddies will always be the same size; the smallest eddies are determined by the Reynolds number.

What is the explanation for this phenomenon? A large Reynolds number indicates that viscous forces are not important at large scales of the flow. With a strong predominance of inertial forces over viscous forces, the largest scales of fluid motion are undamped—there is not enough viscosity to dissipate their motions. The kinetic energy must "cascade" from these large scales to progressively smaller scales until a level is reached for which the scale is small enough for viscosity to become important (that is, viscous forces become of the order of inertial ones). It is at these small scales where the dissipation of energy by viscous action finally takes place. The Reynolds number indicates at what scale this viscous dissipation occurs.

In physiology

Poiseuille's law on blood circulation in the body is dependent on laminar flow. In turbulent flow the flow rate is proportional to the square root of the pressure gradient, as opposed to its direct proportionality to pressure gradient in laminar flow.

Using the definition of the Reynolds number we can see that a large diameter with rapid flow, where the density of the blood is high, tends towards turbulence. Rapid changes in vessel diameter may lead to turbulent flow, for instance when a narrower vessel widens to a larger one. Furthermore, a bulge of atheroma may be the cause of turbulent flow, where audible turbulence may be detected with a stethoscope.

Complex systems

Reynolds number interpretation has been extended into the area of arbitrary complex systems. Such as financial flows, nonlinear networks, etc. In the latter case, an artificial viscosity is reduced to a nonlinear mechanism of energy distribution in complex network media. Reynolds number then represents a basic control parameter that expresses a balance between injected and dissipated energy flows for an open boundary system. It has been shown that Reynolds critical regime separates two types of phase space motion: accelerator (attractor) and decelerator. High Reynolds number leads to a chaotic regime transition only in frame of strange attractor model.

Relationship to other dimensionless parameters

There are many dimensionless numbers in fluid mechanics. The Reynolds number measures the ratio of advection and diffusion effects on structures in the velocity field, and is therefore closely related to Péclet numbers, which measure the ratio of these effects on other fields carried by the flow, for example, temperature and magnetic fields. Replacement of the kinematic viscosity ν = ⁠μ/ρ⁠ in Re by the thermal or magnetic diffusivity results in respectively the thermal Péclet number and the magnetic Reynolds number. These are therefore related to Re by-products with ratios of diffusivities, namely the Prandtl number and magnetic Prandtl number.

See also

• Reynolds transport theorem – 3D generalization of the Leibniz integral rule
• Drag coefficient – Dimensionless parameter to quantify fluid resistance
• Deposition (geology) – Geological process in which sediments, soil and rocks are added to a landform or landmass
• Kelvin–Helmholtz instability

References

Sources

• Bird, R. Byron; Stewart, Warren E.; Lightfoot, Edwin N. (2006). Transport Phenomena. John Wiley & Sons. ISBN 978-0-470-11539-8.
• Dusenbery, David B. (2009). Living at Micro Scale. Cambridge, Massachusetts: Harvard University Press. ISBN 9780674031166.
• Dwivedi, P. N. (1977). "Particle-fluid mass transfer in fixed and fluidized beds". Industrial & Engineering Chemistry Process Design and Development. 16 (2): 157–165. doi:10.1021/i260062a001.
• Ehrenstein, Uwe; Eloy, Christophe (2013). "Skin friction on a moving wall and its implications for swimming animals" (PDF). Journal of Fluid Mechanics. 718: 321–346. Bibcode:2013JFM...718..321E. doi:10.1017/jfm.2012.613. ISSN 0022-1120. S2CID 56331294. Archived from the original (PDF) on 2019-03-02.
• Falkovich, Gregory (2018). Fluid Mechanics. Cambridge University Press. ISBN 978-1-107-12956-6.
• Fox, R. W.; McDonald, A. T.; Pritchard, Phillip J. (2004). Introduction to Fluid Mechanics (6th ed.). Hoboken: John Wiley and Sons. p. 348. ISBN 978-0-471-20231-8.
• Holman, J. P. (2002). Heat Transfer (Si Units ed.). McGraw-Hill Education (India) Pvt Limited. ISBN 978-0-07-106967-0.
• Incropera, Frank P.; DeWitt, David P. (1981). Fundamentals of heat transfer. New York: Wiley. ISBN 978-0-471-42711-7.
• Lissaman, P. B. S. (1983). "Low-Reynolds-Number Airfoils". Annu. Rev. Fluid Mech. 15 (15): 223–39. Bibcode:1983AnRFM..15..223L. CiteSeerX 10.1.1.506.1131. doi:10.1146/annurev.fl.15.010183.001255. S2CID 123639541.
• Los, Cornelis (2006). Financial Market Risk: Measurement and Analysis. Routledge. ISBN 978-1-134-46932-1.
• Manneville, Paul; Pomeau, Yves (25 March 2009). "Transition to turbulence". Scholarpedia. 4 (3): 2072. Bibcode:2009SchpJ...4.2072M. doi:10.4249/scholarpedia.2072.
• Patel, V. C.; Rodi, W.; Scheuerer, G. (1985). "Turbulence Models for Near-Wall and Low Reynolds Number Flows—A Review". AIAA Journal. 23 (9): 1308–1319. Bibcode:1985AIAAJ..23.1308P. doi:10.2514/3.9086.
• Potter, Merle C.; Wiggert, David C.; Ramadan, Bassem H. (2012). Mechanics of Fluids (4th, SI units ed.). Cengage Learning. ISBN 978-0-495-66773-5.
• Reynolds, Osborne (1883). "An experimental investigation of the circumstances which determine whether the motion of water shall be direct or sinuous, and of the law of resistance in parallel channels". Philosophical Transactions of the Royal Society. 174: 935–982. Bibcode:1883RSPT..174..935R. doi:10.1098/rstl.1883.0029. JSTOR 109431.
• Rhodes, M. (1989). Introduction to Particle Technology. Wiley. ISBN 978-0-471-98482-5.
• Rott, N. (1990). "Note on the history of the Reynolds number" (PDF). Annual Review of Fluid Mechanics. 22 (1): 1–11. Bibcode:1990AnRFM..22....1R. doi:10.1146/annurev.fl.22.010190.000245. S2CID 54583669. Archived from the original (PDF) on 2019-02-25.
• Schlichting, Hermann; Gersten, Klaus (2017). Boundary-Layer Theory. Springer. ISBN 978-3-662-52919-5.
• Sinnott, R. K.; Coulson, John Metcalfe; Richardson, John Francis (2005). Chemical Engineering Design. Vol. 6 (4th ed.). Elsevier Butterworth-Heinemann. ISBN 978-0-7506-6538-4.
• Sommerfeld, Arnold (1908). "Ein Beitrag zur hydrodynamischen Erkläerung der turbulenten Flüssigkeitsbewegüngen (A Contribution to Hydrodynamic Explanation of Turbulent Fluid Motions)" (PDF). International Congress of Mathematicians . 3: 116–124. Archived from the original (PDF) on 2016-11-15.
• Stokes, George (1851). "On the Effect of the Internal Friction of Fluids on the Motion of Pendulums". Transactions of the Cambridge Philosophical Society. 9: 8–106. Bibcode:1851TCaPS...9....8S.
• Streeter, Victor Lyle (1965). Fluid mechanics (3rd ed.). New York: McGraw-Hill. OCLC 878734937.
• Tansley, Claire E.; Marshall, David P. (2001). "Flow past a Cylinder on a Plane, with Application to Gulf Stream Separation and the Antarctic Circumpolar Current" (PDF). Journal of Physical Oceanography. 31 (11): 3274–3283. Bibcode:2001JPO....31.3274T. doi:10.1175/1520-0485(2001)031<3274:FPACOA>2.0.CO;2. Archived from the original (PDF) on 2011-04-01.

Further reading

1. Batchelor, G. K. (1967). An Introduction to Fluid Dynamics. Cambridge University Press. pp. 211–215.
2. Brezina, Jiri, 1979, Particle size and settling rate distributions of sand-sized materials: 2nd European Symposium on Particle Characterisation (PARTEC), Nürnberg, West Germany.
3. Brezina, Jiri, 1980, Sedimentological interpretation of errors in size analysis of sands; 1st European Meeting of the International Association of Sedimentologists, Ruhr University at Bochum, Federal Republic of Germany, March 1980.
4. Brezina, Jiri, 1980, Size distribution of sand - sedimentological interpretation; 26th International Geological Congress, Paris, July 1980, Abstracts, vol. 2.
5. Fouz, Infaz "Fluid Mechanics," Mechanical Engineering Dept., University of Oxford, 2001, p. 96
6. Hughes, Roger "Civil Engineering Hydraulics," Civil and Environmental Dept., University of Melbourne 1997, pp. 107–152
7. Jermy M., "Fluid Mechanics A Course Reader," Mechanical Engineering Dept., University of Canterbury, 2005, pp. d5.10.
8. Purcell, E. M. "Life at Low Reynolds Number", American Journal of Physics vol 45, pp. 3–11 (1977)[1]
9. Truskey, G. A., Yuan, F, Katz, D. F. (2004). Transport Phenomena in Biological Systems Prentice Hall, pp. 7. ISBN 0-13-042204-5. ISBN 978-0-13-042204-0.
10. Zagarola, M. V. and Smits, A. J., "Experiments in High Reynolds Number Turbulent Pipe Flow." AIAA paper #96-0654, 34th AIAA Aerospace Sciences Meeting, Reno, Nevada, January 15–18, 1996.
11. Isobel Clark, 1977, ROKE, a Computer Program for Non-Linear Least Squares Decomposition of Mixtures of Distributions; Computer & Geosciences (Pergamon Press), vol. 3, p. 245 - 256.
12. B. C. Colby and R. P. Christensen, 1957, Some Fundamentals of Particle Size Analysis; St. Anthony Falls Hydraulic Laboratory, Minneapolis, Minnesota, USA, Report Nr. 12/December, 55 pages.
13. Arthur T. Corey, 1949, Influence of Shape on the Fall Velocity of Sand Grains; M. S. Thesis, Colorado Agricultural and Mechanical College, Fort Collins, Colorado, USA, December 102 pages.
14. Joseph R. Curray, 1961, Tracing sediment masses by grain size modes; Proc. Internat. Association of Sedimentology, Report of the 21st Session Norden, Internat. Geol. Congress, p. 119 - 129.
15. Burghard Walter Flemming & Karen Ziegler, 1995, High-resolution grain size distribution patterns and textural trends in the back-barrier environment of Spiekeroog Island (Southern North Sea); Senckenbergiana Maritima, vol. 26, No. 1+2, p. 1 - 24.
16. Robert Louis Folk, 1962, Of skewnesses and sands; Jour. Sediment. Petrol., vol. 8, No. 3/September, p. 105 - 111
17. FOLK, Robert Louis & William C. WARD, 1957: Brazos River bar: a study in the significance of grain size parameters; Jour. Sediment. Petrol., vol. 27, No. 1/March, p. 3 - 26
18. George Herdan, M. L. Smith & W. H. Hardwick (1960): Small Particle Statistics. 2nd revised edition, Butterworths (London, Toronto, etc.), 418 pp.
19. Douglas Inman, 1952: Measures for describing the size distribution of sediments. Jour. Sediment. Petrology, vol. 22, No. 3/September, p. 125 - 145
20. Miroslaw Jonasz, 1991: Size, shape, composition, and structure of microparticles from light scattering; in SYVITSKI, James P. M., 1991, Principles, Methods, and Application of Particle Size Analysis; Cambridge Univ. Press, Cambridge, 368 pp., p. 147.
21. William C. Krumbein, 1934: Size frequency distribution of sediments; Jour. Sediment. Petrol., vol. 4, No. 2/August, p. 65 - 77.
22. Krumbein, William Christian & Francis J. Pettijohn, 1938: Manual of Sedimentary Petrography; Appleton-Century-Crofts, Inc., New York; 549 pp.
23. John S. McNown & Pin-Nam Lin, 1952, Sediment concentration and fall velocity; Proc. of the 2nd Midwestern Conf. on Fluid Mechanics, Ohio State University, Columbus, Ohio; State Univ. of Iowa Reprints in Engineering, Reprint No. 109/1952, p. 401 - 411.
24. McNownn, John S. & J. Malaika, 1950, Effects of Particle Shape of Settling Velocity at Low Reynolds' Numbers; American Geophysical Union Transactions, vol. 31, No. 1/February, p. 74 - 82.
25. Gerard V. Middleton 1967, Experiments on density and turbidity currents, III; Deposition; Canadian Jour. of Earth Science, vol. 4, p. 475 - 505 (PSI definition: p. 483 - 485).
26. Osborne Reynolds, 1883: An experimental investigation of the circumstances which determine whether the motion of water shall be direct or sinuous, and of the law of resistance in parallel channels. Phil. Trans. Roy. Soc., 174, Papers, vol. 2, p. 935 - 982
27. E. F. Schultz, R. H. Wilde & M. L. Albertson, 1954, Influence of Shape on the Fall Velocity of Sedimentary Particles; Colorado Agricultural & Mechanical College, Fort Collins, Colorado, MRD Sediment Series, No. 5/July (CER 54EFS6), 161 pages.
28. H. J. Skidmore, 1948, Development of a stratified-suspension technique for size-frequency analysis; Thesis, Department of Mechanics and Hydraulics, State Univ. of Iowa, p. 2 (? pages).
29. James P. M. Syvitski, 1991, Principles, Methods, and Application of Particle Size Analysis; Cambridge Univ. Press, Cambridge, 368 pp.

External links

• The Reynolds number - The Feynman Lectures on Physics
• The Reynolds Number at Sixty Symbols
• Reynolds mini-biography and picture of original apparatus at Manchester University.
• Reynolds Number Calculation