For the
anatomical structure, see
Boundary layer of uterus.
In physics and fluid mechanics, a boundary layer is the layer of fluid in the immediate vicinity of a bounding surface where the effects of viscosity are significant. In the Earth's atmosphere, the planetary boundary layer is the air layer near the ground affected by diurnal heat, moisture or momentum transfer to or from the surface. On an aircraft wing the boundary layer is the part of the flow close to the wing, where viscous forces distort the surrounding nonviscous flow. See Reynolds number.
Laminar boundary layers can be loosely classified according to their structure and the circumstances under which they are created. The thin shear layer which develops on an oscillating body is an example of a Stokes boundary layer, while the Blasius boundary layer refers to the wellknown similarity solution near an attached flat plate held in an oncoming unidirectional flow. When a fluid rotates and viscous forces are balanced by the Coriolis effect (rather than convective inertia), an Ekman layer forms. In the theory of heat transfer, a thermal boundary layer occurs. A surface can have multiple types of boundary layer simultaneously.
Aerodynamics
The aerodynamic boundary layer was first defined by Ludwig Prandtl in a paper presented on August 12, 1904 at the third International Congress of Mathematicians in Heidelberg, Germany. It simplifies the equations of fluid flow by dividing the flow field into two areas: one inside the boundary layer, dominated by viscosity and creating the majority of drag experienced by the boundary body; and one outside the boundary layer, where viscosity can be neglected without significant effects on the solution. This allows a closedform solution for the flow in both areas, a significant simplification of the full Navier–Stokes equations. The majority of the heat transfer to and from a body also takes place within the boundary layer, again allowing the equations to be simplified in the flow field outside the boundary layer. The pressure distribution throughout the boundary layer in the direction normal to the surface (such as an airfoil) remains constant throughout the boundary layer, and is the same as on the surface itself.
The thickness of the velocity boundary layer is normally defined as the distance from the solid body at which the viscous flow velocity is 99% of the freestream velocity (the surface velocity of an inviscid flow). Displacement Thickness is an alternative definition stating that the boundary layer represents a deficit in mass flow compared to inviscid flow with slip at the wall. It is the distance by which the wall would have to be displaced in the inviscid case to give the same total mass flow as the viscous case. The noslip condition requires the flow velocity at the surface of a solid object be zero and the fluid temperature be equal to the temperature of the surface. The flow velocity will then increase rapidly within the boundary layer, governed by the boundary layer equations, below.
The thermal boundary layer thickness is similarly the distance from the body at which the temperature is 99% of the temperature found from an inviscid solution. The ratio of the two thicknesses is governed by the Prandtl number. If the Prandtl number is 1, the two boundary layers are the same thickness. If the Prandtl number is greater than 1, the thermal boundary layer is thinner than the velocity boundary layer. If the Prandtl number is less than 1, which is the case for air at standard conditions, the thermal boundary layer is thicker than the velocity boundary layer.
In highperformance designs, such as gliders and commercial aircraft, much attention is paid to controlling the behavior of the boundary layer to minimize drag. Two effects have to be considered. First, the boundary layer adds to the effective thickness of the body, through the displacement thickness, hence increasing the pressure drag. Secondly, the shear forces at the surface of the wing create skin friction drag.
At high Reynolds numbers, typical of fullsized aircraft, it is desirable to have a laminar boundary layer. This results in a lower skin friction due to the characteristic velocity profile of laminar flow. However, the boundary layer inevitably thickens and becomes less stable as the flow develops along the body, and eventually becomes turbulent, the process known as boundary layer transition. One way of dealing with this problem is to suck the boundary layer away through a porous surface (see Boundary layer suction). This can reduce drag, but is usually impractical due to its mechanical complexity and the power required to move the air and dispose of it. Natural laminar flow techniques push the boundary layer transition aft by reshaping the aerofoil or fuselage so that its thickest point is more aft and less thick. This reduces the velocities in the leading part and the same Reynolds number is achieved with a greater length.
At lower Reynolds numbers, such as those seen with model aircraft, it is relatively easy to maintain laminar flow. This gives low skin friction, which is desirable. However, the same velocity profile which gives the laminar boundary layer its low skin friction also causes it to be badly affected by adverse pressure gradients. As the pressure begins to recover over the rear part of the wing chord, a laminar boundary layer will tend to separate from the surface. Such flow separation causes a large increase in the pressure drag, since it greatly increases the effective size of the wing section. In these cases, it can be advantageous to deliberately trip the boundary layer into turbulence at a point prior to the location of laminar separation, using a turbulator. The fuller velocity profile of the turbulent boundary layer allows it to sustain the adverse pressure gradient without separating. Thus, although the skin friction is increased, overall drag is decreased. This is the principle behind the dimpling on golf balls, as well as vortex generators on aircraft. Special wing sections have also been designed which tailor the pressure recovery so laminar separation is reduced or even eliminated. This represents an optimum compromise between the pressure drag from flow separation and skin friction from induced turbulence.
When using halfmodels in wind tunnels, a peniche is sometimes used to reduce or eliminate the effect of the boundary layer.
Naval architecture
Many of the principles that apply to aircraft also apply to ships, submarines, and offshore platforms.
For ships, unlike aircraft, one deals with incompressible flows, where change in water density is negligible (a pressure rise close to 1000kPa leads to a change of only 2–3 kg/m^{3}). This field of fluid dynamics is called hydrodynamics. A ship engineer designs for hydrodynamics first, and for strength only later. The boundary layer development, breakdown, and separation become critical because the high viscosity of water produces high shear stresses. Another consequence of high viscosity is the slip stream effect, in which the ship moves like a spear tearing through a sponge at high velocity.
Boundary layer equations
The deduction of the boundary layer equations was one of the most important advances in fluid dynamics (Anderson, 2005). Using an order of magnitude analysis, the wellknown governing Navier–Stokes equations of viscous fluid flow can be greatly simplified within the boundary layer. Notably, the characteristic of the partial differential equations (PDE) becomes parabolic, rather than the elliptical form of the full Navier–Stokes equations. This greatly simplifies the solution of the equations. By making the boundary layer approximation, the flow is divided into an inviscid portion (which is easy to solve by a number of methods) and the boundary layer, which is governed by an easier to solve PDE. The continuity and Navier–Stokes equations for a twodimensional steady incompressible flow in Cartesian coordinates are given by
 $\{\backslash partial\; u\backslash over\backslash partial\; x\}+\{\backslash partial\; \backslash upsilon\backslash over\backslash partial\; y\}=0$
 $u\{\backslash partial\; u\; \backslash over\; \backslash partial\; x\}+\backslash upsilon\{\backslash partial\; u\; \backslash over\; \backslash partial\; y\}=\{1\backslash over\; \backslash rho\}\; \{\backslash partial\; p\; \backslash over\; \backslash partial\; x\}+\{\backslash nu\}\backslash left(\{\backslash partial^2\; u\backslash over\; \backslash partial\; x^2\}+\{\backslash partial^2\; u\backslash over\; \backslash partial\; y^2\}\backslash right)$
 $u\{\backslash partial\; \backslash upsilon\; \backslash over\; \backslash partial\; x\}+\backslash upsilon\{\backslash partial\; \backslash upsilon\; \backslash over\; \backslash partial\; y\}=\{1\backslash over\; \backslash rho\}\; \{\backslash partial\; p\; \backslash over\; \backslash partial\; y\}+\{\backslash nu\}\backslash left(\{\backslash partial^2\; \backslash upsilon\backslash over\; \backslash partial\; x^2\}+\{\backslash partial^2\; \backslash upsilon\backslash over\; \backslash partial\; y^2\}\backslash right)$
where $u$ and $\backslash upsilon$ are the velocity components, $\backslash rho$ is the density, $p$ is the pressure, and $\backslash nu$ is the kinematic viscosity of the fluid at a point.
The approximation states that, for a sufficiently high Reynolds number the flow over a surface can be divided into an outer region of inviscid flow unaffected by viscosity (the majority of the flow), and a region close to the surface where viscosity is important (the boundary layer). Let $u$ and $\backslash upsilon$ be streamwise and transverse (wall normal) velocities respectively inside the boundary layer. Using scale analysis, it can be shown that the above equations of motion reduce within the boundary layer to become
 $\{\backslash partial\; u\backslash over\backslash partial\; x\}+\{\backslash partial\; \backslash upsilon\backslash over\backslash partial\; y\}=0$
 $u\{\backslash partial\; u\; \backslash over\; \backslash partial\; x\}+\backslash upsilon\{\backslash partial\; u\; \backslash over\; \backslash partial\; y\}=\{1\backslash over\; \backslash rho\}\; \{\backslash partial\; p\; \backslash over\; \backslash partial\; x\}+\{\backslash nu\}\{\backslash partial^2\; u\backslash over\; \backslash partial\; y^2\}$
and if the fluid is incompressible (as liquids are under standard conditions):
 $\{1\backslash over\; \backslash rho\}\; \{\backslash partial\; p\; \backslash over\; \backslash partial\; y\}=0$
The asymptotic analysis also shows that $\backslash upsilon$, the wall normal velocity, is small compared with $u$ the streamwise velocity, and that variations in properties in the streamwise direction are generally much lower than those in the wall normal direction.
Since the static pressure $p$ is independent of $y$, then pressure at the edge of the boundary layer is the pressure throughout the boundary layer at a given streamwise position. The external pressure may be obtained through an application of Bernoulli's equation. Let $u\_0$ be the fluid velocity outside the boundary layer, where $u$ and $u\_0$ are both parallel. This gives upon substituting for $p$ the following result
 $u\{\backslash partial\; u\; \backslash over\; \backslash partial\; x\}+\backslash upsilon\{\backslash partial\; u\; \backslash over\; \backslash partial\; y\}=u\_0\{\backslash partial\; u\_0\; \backslash over\; \backslash partial\; x\}+\{\backslash nu\}\{\backslash partial^2\; u\backslash over\; \backslash partial\; y^2\}$
with the boundary condition
 $\{\backslash partial\; u\backslash over\backslash partial\; x\}+\{\backslash partial\; v\backslash over\backslash partial\; y\}=0$
For a flow in which the static pressure $p$ also does not change in the direction of the flow then
 $\{\backslash partial\; p\backslash over\backslash partial\; x\}=0$
so $u\_0$ remains constant.
Therefore, the equation of motion simplifies to become
 $u\{\backslash partial\; u\; \backslash over\; \backslash partial\; x\}+\backslash upsilon\{\backslash partial\; u\; \backslash over\; \backslash partial\; y\}=\{\backslash nu\}\{\backslash partial^2\; u\backslash over\; \backslash partial\; y^2\}$
These approximations are used in a variety of practical flow problems of scientific and engineering interest. The above analysis is for any instantaneous laminar or turbulent boundary layer, but is used mainly in laminar flow studies since the mean flow is also the instantaneous flow because there are no velocity fluctuations present.
Turbulent boundary layers
The treatment of turbulent boundary layers is far more difficult due to the timedependent variation of the flow properties. One of the most widely used techniques in which turbulent flows are tackled is to apply Reynolds decomposition. Here the instantaneous flow properties are decomposed into a mean and fluctuating component. Applying this technique to the boundary layer equations gives the full turbulent boundary layer equations not often given in literature:
 $\{\backslash partial\; \backslash overline\{u\}\backslash over\backslash partial\; x\}+\{\backslash partial\; \backslash overline\{v\}\backslash over\backslash partial\; y\}=0$
 $\backslash overline\{u\}\{\backslash partial\; \backslash overline\{u\}\; \backslash over\; \backslash partial\; x\}+\backslash overline\{v\}\{\backslash partial\; \backslash overline\{u\}\; \backslash over\; \backslash partial\; y\}=\{1\backslash over\; \backslash rho\}\; \{\backslash partial\; \backslash overline\{p\}\; \backslash over\; \backslash partial\; x\}+\; \backslash nu\; \backslash left(\{\backslash partial^2\; \backslash overline\{u\}\backslash over\; \backslash partial\; x^2\}+\{\backslash partial^2\; \backslash overline\{u\}\backslash over\; \backslash partial\; y^2\}\backslash right)\backslash frac\{\backslash partial\}\{\backslash partial\; y\}(\backslash overline\{u\text{'}v\text{'}\})\backslash frac\{\backslash partial\}\{\backslash partial\; x\}(\backslash overline\{u\text{'}^2\})$
 $\backslash overline\{u\}\{\backslash partial\; \backslash overline\{v\}\; \backslash over\; \backslash partial\; x\}+\backslash overline\{v\}\{\backslash partial\; \backslash overline\{v\}\; \backslash over\; \backslash partial\; y\}=\{1\backslash over\; \backslash rho\}\; \{\backslash partial\; \backslash overline\{p\}\; \backslash over\; \backslash partial\; y\}+\backslash nu\; \backslash left(\{\backslash partial^2\; \backslash overline\{v\}\backslash over\; \backslash partial\; x^2\}+\{\backslash partial^2\; \backslash overline\{v\}\backslash over\; \backslash partial\; y^2\}\backslash right)\backslash frac\{\backslash partial\}\{\backslash partial\; x\}(\backslash overline\{u\text{'}v\text{'}\})\backslash frac\{\backslash partial\}\{\backslash partial\; y\}(\backslash overline\{v\text{'}^2\})$
Using the same orderofmagnitude analysis as for the instantaneous equations, these turbulent boundary layer equations generally reduce to become in their classical form:
 $\{\backslash partial\; \backslash overline\{u\}\backslash over\backslash partial\; x\}+\{\backslash partial\; \backslash overline\{v\}\backslash over\backslash partial\; y\}=0$
 $\backslash overline\{u\}\{\backslash partial\; \backslash overline\{u\}\; \backslash over\; \backslash partial\; x\}+\backslash overline\{v\}\{\backslash partial\; \backslash overline\{u\}\; \backslash over\; \backslash partial\; y\}=\{1\backslash over\; \backslash rho\}\; \{\backslash partial\; \backslash overline\{p\}\; \backslash over\; \backslash partial\; x\}+\{\backslash nu\}\{\backslash partial^2\; \backslash overline\{u\}\backslash over\; \backslash partial\; y^2\}\backslash frac\{\backslash partial\}\{\backslash partial\; y\}(\backslash overline\{u\text{'}v\text{'}\})$
 $\{\backslash partial\; \backslash overline\{p\}\; \backslash over\; \backslash partial\; y\}=0$
The additional term $\backslash overline\{u\text{'}v\text{'}\}$ in the turbulent boundary layer equations is known as the Reynolds shear stress and is unknown a priori. The solution of the turbulent boundary layer equations therefore necessitates the use of a turbulence model, which aims to express the Reynolds shear stress in terms of known flow variables or derivatives. The lack of accuracy and generality of such models is a major obstacle in the successful prediction of turbulent flow properties in modern fluid dynamics.
A laminar sublayer exists in the turbulent zone; it occurs due to those fluid molecules which are still in the very proximity of the surface, where the shear stress is maximum and the velocity of fluid molecules is zero.
Heat and mass transfer
In 1928, the French engineer André Lévêque observed that convective heat transfer in a flowing fluid is affected only by the velocity values very close to the surface.^{[1]}^{[2]} For flows of large Prandtl number, the temperature/mass transition from surface to freestream temperature takes place across a very thin region close to the surface. Therefore, the most important fluid velocities are those inside this very thin region in which the change in velocity can be considered linear with normal distance from the surface. In this way, for
 $u(y)\; =\; u\_0\; \backslash left[\; 1\; \; \backslash frac\{(y\; \; h)^2\}\{h^2\}\; \backslash right]\; =\; u\_0\; \backslash frac\{y\}\{h\}\; \backslash left[\; 2\; \; \backslash frac\{y\}\{h\}\; \backslash right]\; \backslash ;,$
when $y\; \backslash rightarrow\; 0$, then
 $u(y)\; \backslash approx\; 2\; u\_0\; \backslash frac\{y\}\{h\}\; =\; \backslash theta\; y$,
where θ is the tangent of the Poiseuille parabola intersecting the wall.
Although Lévêque's solution was specific to heat transfer into a Poiseuille flow, his insight helped lead other scientists to an exact solution of the thermal boundarylayer problem.^{[3]} Schuh observed that in a boundarylayer, u is again a linear function of y, but that in this case, the wall tangent is a function of x.^{[4]} He expressed this with a modified version of Lévêque's profile,
 $u(y)\; =\; \backslash theta(x)\; y$.
This results in a very good approximation, even for low $Pr$ numbers, so that only liquid metals with $Pr$ much less than 1 cannot be treated this way.^{[3]}
In 1962, Kestin and Persen published a paper describing solutions for heat transfer when the thermal boundary layer is contained entirely within the momentum layer and for various wall temperature distributions.^{[5]} For the problem of a flat plate with a temperature jump at $x\; =\; x\_0$, they propose a substitution that reduces the parabolic thermal boundarylayer equation to an ordinary differential equation. The solution to this equation, the temperature at any point in the fluid, can be expressed as an incomplete gamma function.^{[2]} Schlichting proposed an equivalent substitution that reduces the thermal boundarylayer equation to an ordinary differential equation whose solution is the same incomplete gamma function.^{[6]}
Convective Transfer Constants from Boundary Layer Analysis
Paul Richard Heinrich Blasius derived an exact solution to the above laminar boundary layer equations.^{[7]} The thickness of the boundary layer $\backslash delta$ is a function of the Reynolds number for laminar flow.
$\backslash delta\; \backslash approx\; \{5.0\; *\; x\; \backslash over\; \backslash sqrt\; \{Re\}\}$
$\backslash delta$ = the thickness of the boundary layer: the region of flow where the velocity is less than 99% of the far field velocity $v\_\backslash infty$; $x$ is position along the semiinfinite plate, and $Re$ is the Reynolds Number given by $\backslash rho\; v\_\backslash infty\; x\; /\; \backslash mu$ ($\backslash rho\; =$ density and $\backslash mu\; =$ dynamic viscosity).
The Blasius solution uses boundary conditions in a dimensionless form:
$\{v\_x\; \; v\_S\; \backslash over\; v\_\backslash infty\; \; v\_S\}\; =\; \{v\_x\; \backslash over\; v\_\backslash infty\}\; =\; \{v\_y\backslash over\; v\_\backslash infty\}=\; 0$ at $y=0$
$\{v\_x\; \; v\_S\; \backslash over\; v\_\backslash infty\; \; v\_S\}\; =\; \{v\_x\; \backslash over\; v\_\backslash infty\}\; =\; 1$ at $y=\backslash infty$ and $x=0$
Note that in many cases, the noslip boundary condition holds that $v\_S$, the fluid velocity at the surface of the plate equals the velocity of the plate at all locations. If the plate is not moving, then $v\_S\; =\; 0$. A much more complicated derivation is required if fluid slip is allowed.^{[8]}
In fact, the Blasius solution for laminar velocity profile in the boundary layer above a semiinfinite plate can be easily extended to describe Thermal and Concentration boundary layers for heat and mass transfer respectively. Rather than the differential xmomentum balance (equation of motion), this uses a similarly derived Energy and Mass balance:
Energy: $v\_x\; \{\backslash partial\; T\; \backslash over\; \backslash partial\; x\}\; +\; v\_y\; \{\backslash partial\; T\; \backslash over\; \backslash partial\; y\}\; =\; \{k\; \backslash over\; \backslash rho\; Cp\}\{\backslash partial^2\; T\; \backslash over\; \backslash partial\; y^2\}$
Mass: $v\_x\; \{\backslash partial\; c\_A\; \backslash over\; \backslash partial\; x\}\; +\; v\_y\; \{\backslash partial\; c\_A\; \backslash over\; \backslash partial\; y\}\; =\; D\_\{AB\}\{\backslash partial^2\; c\_A\; \backslash over\; \backslash partial\; y^2\}$
For the momentum balance, kinematic viscosity $\backslash nu$ can be considered to be the momentum diffusivity. In the energy balance this is replaced by thermal diffusivity $\backslash alpha\; =\; \{k\; /\; \backslash rho\; C\_P\}$, and by mass diffusivity $D\_\{AB\}$ in the mass balance. In thermal diffusivity of a substance, $k$ is its thermal conductivity, $\backslash rho$ is its density and $C\_P$ is its heat capacity. Subscript AB denotes diffusivity of species A diffusing into species B.
Under the assumption that $\backslash alpha\; =\; D\_\{AB\}\; =\; \backslash nu$, these equations become equivalent to the momentum balance. Thus, for Prandtl number $Pr\; =\; \backslash nu/\backslash alpha\; =\; 1$ and Schmidt number $Sc\; =\; \backslash nu/D\_\{AB\}\; =\; 1$ the Blasius solution applies directly.
Accordingly, this derivation uses a related form of the boundary conditions, replacing $v$ with $T$ or $c\_A$ (absolute temperature or concentration of species A). The subscript S denotes a surface condition.
$\{v\_x\; \; v\_S\; \backslash over\; v\_\backslash infty\; \; v\_S\}\; =\; \{T\; \; T\_S\; \backslash over\; T\_\backslash infty\; \; T\_S\}\; =\; \{c\_A\; \; c\_\{AS\}\; \backslash over\; c\_\{A\backslash infty\}\; \; c\_\{AS\}\}=\; 0$ at $y=0$
$\{v\_x\; \; v\_S\; \backslash over\; v\_\backslash infty\; \; v\_S\}\; =\; \{T\; \; T\_S\; \backslash over\; T\_\backslash infty\; \; T\_S\}\; =\; \{c\_A\; \; c\_\{AS\}\; \backslash over\; c\_\{A\backslash infty\}\; \; c\_\{AS\}\}\; =\; 1$ at $y=\backslash infty$ and $x=0$
Using the streamline function Blasius obtained the following solution for the shear stress at the surface of the plate.
$\backslash tau\_0\; =\; \backslash left(\; \{\backslash partial\; v\_x\; \backslash over\; \backslash partial\; y\}\; \backslash right)\; \_\{y=0\}=0.332\; \{v\_\backslash infty\; \backslash over\; x\}\; Re^\{1/2\}$
And via the boundary conditions, it is known that
$\{v\_x\; \; v\_S\; \backslash over\; v\_\backslash infty\; \; v\_S\}\; =\; \{T\; \; T\_S\; \backslash over\; T\_\backslash infty\; \; T\_S\}\; =\; \{c\_A\; \; c\_\{AS\}\; \backslash over\; c\_\{A\backslash infty\}\; \; c\_\{AS\}\}$
We are given the following relations for heat/mass flux out of the surface of the plate
$\backslash left(\; \{\backslash partial\; T\; \backslash over\; \backslash partial\; y\}\; \backslash right)\; \_\{y=0\}=0.332\; \{T\_\backslash infty\; \; T\_S\; \backslash over\; x\}\; Re^\{1/2\}$
$\backslash left(\; \{\backslash partial\; c\_A\; \backslash over\; \backslash partial\; y\}\; \backslash right)\; \_\{y=0\}=0.332\; \{c\_\{A\backslash infty\}\; \; c\_\{AS\}\; \backslash over\; x\}\; Re^\{1/2\}$
So for $Pr=Sc=1$
$\backslash delta\; =\backslash delta\; \_T=\; \backslash delta\; \_c=\; \{5.0*x\backslash over\backslash sqrt\{Re\}\}$
Where $\backslash delta\_T,\backslash delta\_c$ are the regions of flow where $T$ and $c\_A$ are less than 99% of their far field values.^{[9]}
Because the Prandtl number of a particular fluid is not often unity, German engineer E. Polhausen who worked with Ludwig Prandtl attempted to empirically extend these equations to apply for $Pr\backslash ne\; 1$. His results can be applied to $Sc$ as well.^{[10]} He found that for Prandtl number greater than 0.6, the thermal boundary layer thickness was approximately given by:
$\{\backslash delta\; \backslash over\; \backslash delta\_T\}\; =\; Pr^\{1/3\}$ and therefore $\{\backslash delta\; \backslash over\; \backslash delta\_c\}\; =\; Sc^\{1/3\}$
From this solution, it is possible to characterize the convective heat/mass transfer constants based on the region of boundary layer flow. Fourier’s law of conduction and Newton’s Law of Cooling are combined with the flux term derived above and the boundary layer thickness.
$\{q\backslash over\; A\}\; =\; k\; \backslash left(\{\backslash partial\; T\; \backslash over\; \backslash partial\; y\}\; \backslash right)\_\{y=0\}\; =\; h\_x(T\_ST\_\backslash infty)$
$h\_x\; =\; 0.332\{k\; \backslash over\; x\}\; Re^\{1/2\}\_x\; Pr^\{1/3\}$
This gives the local convective constant $h\_x$ at one point on the semiinfinite plane. Integrating over the length of the plate gives an average
$h\_L\; =\; 0.664\{k\; \backslash over\; x\}\; Re^\{1/2\}\_L\; Pr^\{1/3\}$
Following the derivation with mass transfer terms ($k$ = convective mass transfer constant, $D\_\{AB\}$ = diffusivity of species A into species B, $Sc\; =\; \backslash nu\; /\; D\_\{AB\}$ ), the following solutions are obtained:
$k\text{'}\_x\; =\; 0.332\{D\_\{AB\}\; \backslash over\; x\}\; Re^\{1/2\}\_x\; Sc^\{1/3\}$
$k\text{'}\_L\; =\; 0.664\{D\_\{AB\}\; \backslash over\; x\}\; Re^\{1/2\}\_L\; Sc^\{1/3\}$
These solutions apply for laminar flow with a Prandtl/Schmidt number greater than 0.6.^{[9]}
Boundary layer turbine
This effect was exploited in the Tesla turbine, patented by Nikola Tesla in 1913. It is referred to as a bladeless turbine because it uses the boundary layer effect and not a fluid impinging upon the blades as in a conventional turbine. Boundary layer turbines are also known as cohesiontype turbine, bladeless turbine, and Prandtl layer turbine (after Ludwig Prandtl).
See also
References

 A.D. Polyanin and V.F. Zaitsev, Handbook of Nonlinear Partial Differential Equations, Chapman & Hall/CRC Press, Boca Raton – London, 2004. ISBN 1584883553
 A.D. Polyanin, A.M. Kutepov, A.V. Vyazmin, and D.A. Kazenin, Hydrodynamics, Mass and Heat Transfer in Chemical Engineering, Taylor & Francis, London, 2002. ISBN 0415272378
 Hermann Schlichting, Klaus Gersten, E. Krause, H. Jr. Oertel, C. Mayes "BoundaryLayer Theory" 8th edition Springer 2004 ISBN 3540662707
 John D. Anderson, Jr., "Ludwig Prandtl's Boundary Layer", Physics Today, December 2005

 H. Tennekes and J. L. Lumley, "A First Course in Turbulence", The MIT Press, (1972).
External links
 National Science Digital Library – Boundary Layer
 Moore, Franklin K., "Displacement effect of a threedimensional boundary layer". NACA Report 1124, 1953.
 Benson, Tom, "Boundary layer". NASA Glenn Learning Technologies.
 Boundary layer separation
 – from EqWorld
 Jones, T.V.
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