**Open Journal of Fluid Dynamics**

Vol.07 No.02(2017), Article ID:76919,12 pages

10.4236/ojfd.2017.72015

Process-Based Friction Factor for Pipe Flow

James M. Gregory^{1}, John A. McEnery^{2 }

^{1}Professor Emeritus, Civil Engineering Department, Texas Tech University, Lubbock, Texas, USA

^{2}McEnery Water Resources, LLC, Arlington, Texas, USA

Copyright © 2017 by authors and Scientific Research Publishing Inc.

This work is licensed under the Creative Commons Attribution International License (CC BY 4.0).

http://creativecommons.org/licenses/by/4.0/

Received: April 27, 2017; Accepted: June 13, 2017; Published: June 16, 2017

ABSTRACT

The Moody Diagram is widely used to determine the friction factor for fluid flow in pipes. The diagram combines the effects of Reynolds number and relative roughness to determine the friction factor. The relationship is highly non-linear and appears to have a complex interaction between viscous and boundary roughness effects. The Moody Diagram is based on predictions from an equation developed by Colebrook in 1939. The relationship requires an iteration process to make predictions. While empirical relationships have been developed that provide good predictions without an iteration process, no one has fully explained the cause for the observed results. The objective of this paper is to present a logical development for prediction of the friction factor. An equation has been developed that models the summed effect of both the laminar sublayer and the boundary roughness on the fluid profile and the resulting friction factor for pipes. The new equation does not require an iteration procedure to obtain values for the friction factor. Predicted results match well with values generated from Colebrook’s work that is expressed in the Moody Diagram. Predictions are within one percent of Colebrook values and generally less than 0.3 percent error from his values. The development provides insight to how processes operating at the boundary cause the friction factor to change.

**Keywords:**

Friction, Boundary Roughness, Turbulence, Pipe Flow, Moody Diagram

1. Introduction

Many people have contributed to understanding and describing fluid flow. The association of velocity, V, diameter, d, density, ρ, and viscosity, μ, to form the dimensionless term, Vdρ/μ, known as the Reynolds number was a major contribution in relating friction to fluid properties, especially for laminar flow [1] .

A subsequent major development was the concept of a mixing length for turbulent flow by Prandtl (1926) [2] . Building on this concept, an equation to describe the velocity distribution in turbulent flow can be developed

(1)

where U = fluid velocity at height Z above a reference

U_{*} = friction velocity

k = von Karman constant (0.4 for neutral conditions)

Z_{0} = fluid roughness height at the boundary.

Two other major contributions were by Nikuradse in 1933 [3] and Colebrook [4] in 1939. Nikuradse [3] created pipes lined with sand grains of various sizes and measured the friction associated with boundary roughness. Colebrook [4] , using information from the literature and other researchers, reported the following equation based on the log profile applied to pipe flow:

(2)

where f = friction factor

y_{1} = lower limit of integration

0.113 = the height in terms of diameter where the velocity in the profile is equal to the average velocity of flow.

Colebrook then used Equation (2) to develop two independent equations of similar form:

(3)

(4)

where R = Reynolds number

d_{p} = diameter of sand grain from Nikuradse’s experiments

3.7 = 33 x 0.113 ? The d_{p}/33 was the measured value for Z_{0} or y_{1} in the equations above.

We have chosen the form in Equations (3) and (4) so that d_{p}/d will follow the same form as e/d used in the Moody Diagram. The variable d_{p} communicates the specific geometry of spherical particles used by Nikuradse. Other shapes will produce a different calibration for Z_{0} [5] . Moody [6] (1944) used e for roughness height that would produce an equivalent to that of sand grain roughness. Colebrook reasoned that the two denominator terms were additive, leading to a general equation. Unfortunately, the presence of f on both sides of his equation requires an iteration process to solve for f. Also, his work did not express a deterministic explanation of the processes causing these interactions.

Moody (1944) used Colebrook’s work and rearranged the output into the more useable chart form with f as a function of Reynolds number and relative roughness with the results displayed in log-log graphical form. He, however, did not provide additional understanding about the underlying relationships. His diagram is now given in most modern fluid textbooks and is considered the standard for estimating the friction factor for pipe flow.

Swamee and Jain [7] (1976) and Haaland [8] (1983) expanded on the work of Colebrook [4] and developed closed-form equations that give good predictions but do not provide an explanation of the processes causing the results. It will be shown later that these equations provide results very close to those produced by a process-based outcome. Haaland’s [8] best equation is more accurate than the final equation of Swamee and Jain [7] .

The objective of this current work is to provide a non-iterative equation that is process based to predict the friction factor in the Moody Diagram for turbulent conditions. This equation improves predictions slightly over the best equation of Haaland [8] . The development provides a reasonable description of the process by which smooth and rough boundaries interact to determine the final value for the friction factor.

2. Development of Equations

2.1. Laminar Flow

The friction factor for laminar flow is

(5)

where f_{L} = friction factor for laminar flow.

This equation applies to Reynolds numbers less than 2000.

2.2. Turbulent Flow with Smooth Boundary

Using a similar form to Equation (5) (inverse of Reynolds number), an equation was developed to describe the friction factor associated with turbulent flow for smooth boundary conditions:

(6)

where f_{S} = friction factor for smooth turbulent flow.

This equation was developed by observing that the slope of the curve on the Moody Diagram for smooth conditions near the beginning of the turbulent flow range at Reynolds number of approximately 4000 was one half of that of laminar conditions. In other words, the exponent on Reynolds number changes from 1.0 to 0.5 when the change from laminar to turbulent flow occurs. It was also observed that the slope of this curve gradually decreases as Reynolds number increases. Numerical coefficients of 2.3 and 0.104 were obtained by minimizing the least square difference between predictions and values read from the Moody Diagram for smooth conditions. An R^{2} of 0.9997 was obtained and the worst-case individual point prediction was 1.6 percent error for Reynolds number of 4000. Generally the prediction error was random and less than plus or minus one percent of the values from the Colebrook equation. The new equation is valid for Reynolds numbers greater than 4000 through the full range of Reynolds numbers on the Moody Diagram. It has a similar form as laminar flow (Equation (5)) and is valid over a greater range of Reynolds numbers than the Blasius equation (presented later) for turbulent flow.

3. Turbulent Flow General Relationships

Colebrook (1939) in effect separated his variable y_{1} in Equation (2) into two roughness components, one for boundary roughness and one for viscous effects, which we will associate with the laminar sublayer. Equation (1) can be rewritten to express these components,

(7)

where Z_{0L} = roughness height associated with laminar sublayer.

Roughness height can be related to geometry of the roughness elements for solid boundaries with the following equation from [5] :

(8)

where H = maximum height of roughness element

D = displacement height of surface (average height of elements).

This equation is valid for a surface of 30 percent or more coverage of roughness elements such as sand grains, pine trees, broadleaf trees, etc. It is valid for flow across ridges. It is not valid to describe the effects of a telephone pole in the middle of a large field. For equations to deal with both sparse tall elements like telephone poles and other surface elements see Gregory et al. (2004) [9] .

Abtew et al. (1989) [5] calculated the roughness height for an average of open and closed packed spheres to obtain

(9)

(10)

(11)

If 15 percent of the diameter of the particles were covered by the glue in Nikuradse’s [3] experiment, then both H and D are reduced to only 0.85 of their original value above the surface boundary and

(measured result from Nikuradse) (12)

Colebrook [4] used this measured result to obtain the 3.7 in Equation (4). A 15 percent reduction in heights associated with the glued surface seems reasonable.

Darwish [10] and Abtew (personal communication) have both applied Equation (8) to predict Z_{0} associated with wind and wave interaction. Abtew applied Equation (8) directly to get a roughness estimate and Darwish [10, page 128] used a constant of 0.148 to reduce Z_{0} because both the wind and the wave are moving together. If both the wind and the wave moved at the same velocity, the wave would have no effect on the wind and the wind would have no effect on the wave. For this case, the wave height would have zero effect on Z_{0}. Darwish [10] found that her model for predicting evaporation from lakes gave optimum results when she used Equation (8) with an adjustment factor of 0.148 to predict Z_{0}.

From observations of the sea being ruffled by the wind, Lord Kelvin [11] described the effects of viscosity and relative velocity upon a fluid surface. The movement of one layer of fluid over another causes a boundary disturbance commonly known as the Kelvin-Helmholtz (KH) instability [11] [12] . This phenomenon is discussed extensively in references by Miles [13] , Lamb [14] and others. Figure 1 illustrates an assumed bulk roll-up of the fluid interface between the laminar and turbulent regions similar in form to the KH instability. This figure illustrates flow conditions over a smooth boundary. The presence of boundary roughness elements compound this bulk roll-up as the laminar region moves upward over the roughness elements. This process can be visualized as a wave increases in height when it comes ashore on a beach.

The interface between turbulent flow and the surface of the laminar sublayer has to be disturbed and irregular in shape similar to wind moving over waves. Immediately above the laminar sublayer eddies are developing and diffusing throughout the turbulent layer above. As these eddies protrude into the laminar sublayer, the sublayer must speed up or slow down and adjust in depth to accommodate this intrusion. Both the turbulent flow and the laminar sublayer are moving in the direction of flow, but the turbulent flow is moving faster than the irregular wave forms on the surface of the laminar sublayer. The wave-like irregular shape of the surface of the disturbed laminar sublayer causes a roughness that interferes with the turbulent flow above. We will assume that we can model this roughness effect with the following equation:

Figure 1. Instability and roughness at interface of laminar and turbulent flow.

(13)

where C = adjustment for a moving roughness (0 < C ≤ 1)

H_{L} = height of wave of laminar sublayer above the boundary

D_{L} = average height of laminar sublayer.

For a symmetrical wave pattern, the maximum value for H_{L} is two times D_{L}, in which case the lowest part of the wave contacts the boundary (Figure 2). The turbulent flow, thus, contacts the boundary part of the time. It could be argued that there is always a small thickness of laminar flow at the boundary because at the boundary the velocity of fluid movement must be zero. This boundary effect may distort the lower shape of the assumed wave pattern. This distortion should not affect the Z_{0} value, however, because according to Equation (8) by Abtew et al. [5] , the Z_{0} is a function of the top half (H-D) of a wave pattern. Interference by roughness elements slows the turbulent movement and further bunches the laminar flow causing it to amplify the laminar sublayer surface roughness.

Because H_{L} is twice D_{L}, Equation (13) reduces to

. (14)

The fluid roughness changes in proportion to the change in average sublayer depth. Street et al. [15] (1996, page 334) give the following equation for the average depth of the laminar sublayer:

. (15)

If we substitute the expression for D_{L} from this equation into D_{L} in Equation (14), we obtain

. (16)

The friction factor, f, is not independent of R for smooth pipe flow. We can,

Figure 2. Illustration of apparent roughness at the surface of the laminar sublayer.

thus, eliminate f in terms of R. We have a couple of ways to estimate f in terms of Reynolds number. The simplest method is to use the Blasius equation [15, page 336]:

. (17)

If we use this relationship to estimate f, Equation (16) reduces to

. (18)

If we now expand Equation (2) to include both the stationary roughness and the roughness associated with the laminar sublayer, the following is obtained:

. (19)

This equation reduces to

. (20)

This equation is very similar in form to those developed by Swamee and Jain [7] and Haaland [8]

. (21)

Based on the success reported by Haaland (1983) of less than three percent error for his results (Equation (21)) and the similarity between Equations (20) and (21), it appears that Equation (20) is a valid model to describe the effects of surface and fluid roughness on the friction factor in pipe flow.

It appears that Haaland [8] adopted the ratio of 6.9/R from the relationship given by Colebrook [4] for smooth pipes over a half century ago,

. (22)

It is interesting that Haaland adjusted the 6.9/R with a power of 0.9, which is very similar to 0.875 obtained in the development of Equation (20).

Equation (20) was tested with data generated using Colebrook’s [4] equation and running enough iterations to obtain no change in the friction factor at the fifth decimal place. A value of C = 0.062 gave the best results. An R^{2} of 0.9997 was obtained. The worst individual percent error relative to the Colebrook values was 3.4 percent. Only one point out of 357 points had an error in excess of three percent. The error for most points was less than one percent. Of the 357 points, 33 or 9.2 percent had relative error greater than two percent.

To improve those results, we return to Equation (16) and substitute Equation (6) for f, rather than the Blausius equation. As mentioned earlier, there are alternate ways to estimate the friction factor in Equation (16). Although Equation (6) is more complex, it should provide better results. Using Equation 6 to estimate the f in Equation (16) produces

. (23)

This equation reduces to

. (24)

After substitution of this new relationship, Equation (19) becomes

. (25)

which reduces to

. (26)

This equation was also tested with the generated points from Colebrook’s equation. A value of 0.0618 for C gave the best results. The R^{2} remained the same at 0.9997. The number of points with greater than three percent error dropped to zero. The number of points with two or more percent error dropped to three out of the 357 points or 0.84 percent.

Equations (20) and (26) are acceptable and well within the range of scatter reported by Haaland [8] for the experimental data used by Colebrook in his analysis. However, there remains an inherent problem in the development of both equations pertaining to the conceptual basis for f in the square root of the friction factor of the laminar sublayer depth term (Equation (15)). Both the Blausius equation (Equation (17)) and Equation (6), used to compute f in Equations (20) and (26) respectively, are based upon flow passing a smooth boundary. To rectify this problem, Equation (26) can be expanded with an adjustment to f. This is done by returning to Equation (16) with the following modification in the development:

(27)

where f_{s} = the friction factor for a smooth boundary

f_{adjusted} = an adjusted friction factor for the actual flow condition.

This equation allows the appropriate friction factor to be used in the laminar sublayer equation by an adjustment factor contained in the parentheses in the above equation. This will be shown to be a function of the relative roughness. An analysis was made to determine C for only smooth boundary values. The resulting C value became 0.0657. The analysis was repeated for a range of relative roughness values to determine the adjusted best fit value for the product of variables contained in parenthesis. This process greatly reduced the error between the Colebrook generated points and the points predicted with Equation (26). Next, the adjusted values relative to the value for a smooth boundary were used to calibrate the adjustment as a function of relative roughness. The relationship is shown in Figure 3. This fraction is an estimate of the square root of the ratio shown in the parenthesis in Equation (27).

The square root ratio was replaced with the equation developed with this analysis:

. (28)

Substitution of this adjustment factor into Equation (26) gives the following:

. (29)

Figure 3. Effects of relative roughness on the square root ratio of friction factors.

Equation (29) predicted values matching results from Colebrook’s equation with relatively little error and without the need for iteration. All errors were less than one percent. Most errors were less than 0.3 percent. The R^{2} improved to 0.99998. This is slightly superior to the R^{2} of 0.99996 for the correlation of Haaland’s equation to values from Colebrook’s equation. Based on a reasonable description of the process by which smooth and rough boundaries interact, this equation improves upon the work of Haaland both in accuracy and logic.

4. Discussion

It is interesting to examine Colebrook’s [4] development of the relationship that we cite as Equation (3). On page 139 of his paper, he reports the following:

Other experiments by Nikuradse show that for smooth pipes

. (30)

If we replace friction velocity V_{*} with the form U(f/8)^{0.5} [15, page 325, Equation 9.4] and multiple the numerator and denominator on the right side by the diameter of the pipe, we obtain the same relationship as Equation (15) in terms of the friction factor and Reynolds number,

. (31)

If we now recall that Z_{0L} in Equation (14) and y_{1} are the same when there is no roughness, we get the following relationship:

. (32)

Equation (32) has exactly the same form as Equation (15) given by Street et al. [15, page 334, Equation 9.22]. If we compare the 32.8 from Equation (15) to the value inside the parentheses in Equation (32), and solve for C, a value of 0.0663 is obtained. This value is close to the 0.0657 obtained for the adjusted Equation (26). The relative error between these two estimates of average depth for the laminar sublayer is between 0.90 and 0.91 percent depending on which one is used as reference. The experimental results of Nikuradse [3] seem to confirm that the laminar sublayer creates a roughness that interacts with the turbulent flow at the intersection of the two flows.

It is obvious that the experiments of Nikuradse produced key information for modeling both the effects of boundary roughness and smooth boundary effects to predict the friction factor. This concept explains why Z_{0} and Z_{0L} are additive. Colebrook assumed they were additive to develop his model for the friction factor but did not offer an explanation as to why they are additive. From Equation (8), the additive effect can be explained. The Z_{0} value in Equation (8) is just the difference in height of roughness elements and the average height times the constant of 0.13. Thus when we add Z_{0} terms in Equation (7), we are adding the roughness difference between the average element height and the displacement height of the roughness elements and the difference between the wave height and the displacement height or average height of the laminar sublayer. The total effect is the sum of these two differences.

It has been said that trying to teach something you don’t understand is like trying to describe a place you have never visited. Based on the information presented in this paper, the concepts affecting the friction factor are simple. The friction factor is simply a function of the Z_{0} or aerodynamic roughness at the boundary. This roughness is the sum of the physical roughness of the boundary surface and the apparent roughness from turbulence interacting with the laminar boundary layer. While the mathematical model to describe this process is messy, the concept is simple and logical.

5. Summary and Conclusions

An attempt has been made to explain how roughness at pipe boundaries affects friction. We acknowledge that a laminar sublayer exists between the region of turbulent flow and the pipe boundary. Furthermore, we use the roughness on the surface of this laminar sublayer to generate a fluid roughness height Z_{0L}. This roughness in turn affects the velocity profile in the turbulent region similar to the manner in which waves affect the wind profile above a water surface.

This concept was used along with relationships presented in the literature to develop mathematical equations for prediction of the friction factor as a function of Reynolds number and relative roughness as used in the development of the Moody Diagram.

Two equations were developed and tested against data generated from the accepted standard for predicting the friction factor in the Moody Diagram. The first used the Blasius equation to estimate the f factor for smooth pipe flow. The second used a more elaborate model to predict f as a function of Reynolds number for the full range of Reynolds numbers in the Moody Diagram. A final equation was developed that accurately predicts the friction factor without iteration. This equation was achieved by identifying an adjustment factor and relating it to relative roughness. The final equation also eliminates the need to iterate to obtain an accurate prediction.

Cite this paper

Gregory, J.M. and McEnery, J.A. (2017) Process-Based Friction Factor for Pipe Flow. Open Journal of Fluid Dynamics, 7, 219-230. https://doi.org/10.4236/ojfd.2017.72015

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