DarcyWeisbach pressure loss and flow calculation is mobiledevicefriendly as of June 9, 2015
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Units:
cfs=cubic foot per second, cm=centimeter, cP=centipoise, cSt=centistoke, ft=foot, g=gram, gal=U.S. gallon, gpd=U.S. gallon per day, gpm=U.S. gallon per mimute, hp=horsepower, kg=kilogram, lb=pound, m=meter, min=minute, N=Newton, Pa=Pascal, psi=lb/inch^{2}, s=second
Topics: Piping Scenarios Equations Minor Loss
Coefficients Common Questions References
Introduction
Our calculation is based on the steady state incompressible energy equation utilizing
DarcyWeisbach friction losses as well as minor losses. The calculation can compute
flow rate, velocity, pipe diameter, elevation difference, pressure difference, pipe length,
minor loss coefficient, and pump head (total dynamic head). The density and viscosity of a
variety of liquids and gases are coded into the program, but you can alternatively select
"User defined fluid" and enter the density and viscosity for fluids not listed.
Though some industries use the term "fluid" when referring to liquids, we use it
to mean either liquids or gases. The calculation allows you to select from a variety of
piping scenaris which are discussed below.
Comments on gas flow
As mentioned above, the equations that our calculation is based upon are for
incompressible flow. The incompressible flow assumption is valid for liquids. It is also
valid for gases if the pressure drop is less than 40% of the upstream pressure. Crane
(1988, p. 33) states that if the pressure drop is less than 10% of the upstream gage
pressure (gage pressure is pressure relative to atmospheric pressure) and an
incompressible model is used, then the gas density should be based on either the upstream
or the downstream conditions. If the pressure drop is between 10% and 40% of the upstream
gage pressure, then the density should be based on the average of the upstream and
downstream conditions. If the pressure drop exceeds 40% of the upstream gage pressure,
then a compressible flow model, like the Weymouth, Panhandle
A, or Panhandle B should be used.
Piping Scenarios
Since boundary conditions affect the flow characteristics, our calculation allows you to
select whether your locations 1 and 2 are within pipes, at the surface of open reservoirs,
or in pressurized mains (same as pressurized tank). If there is no pump between locations
1 and 2, then enter the pump head (H_{p}) as 0.
Steady State Energy Equation
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The first equation shown is the steady state energy equation for incompressible flow. The
left side of the equation contains what we call the driving heads. These heads include
heads due to a pump (if present), elevation, pressure, and velocity. The terms on the
right side are friction loss and minor losses. Friction losses are computed using the
Darcy Weisbach friction loss equation. The friction factor for turbulent flow is
found using the Colebrook equation which represents the Moody diagram. f is the Moody
friction factor. The equations are wellaccepted in the field of fluid mechanics and can
be found in many references such as Cimbala and Cengel (2008), Munson et al. (1998), and
Streeter et al. (1998).
The equations above are dimensionally correct which means that the units for the
variables are consistent. A consistent set of English units would be mass in slugs, weight
and force in pounds, length in feet, and time in seconds. SI units are also a consistent
set of units with mass in kilograms, weight and force in Newtons, length in meters, and
time in seconds. Our calculation allows you to enter a variety of units and automatically
performs the unit conversions.
A = Pipe crosssectional area, ft^{2} or m^{2}.
D = Pipe diameter, ft or m.
Driving Head (DH) = left side of the first equation (or right side of the equation), ft or
m. This is not total dynamic head.
e = Pipe surface roughness, ft or m. Select from the dropdown menu in our calculation. Additional values.
f = Moody friction factor, unitless. Do not confuse the Moody f with the Fanning friction
factor. f = 4 f_{Fanning} .
g = acceleration due to gravity = 32.174 ft/s^{2} = 9.8066 m/s^{2}.
h_{f} = Major (friction) losses, ft or m.
h_{m} = Minor losses, ft or m.
H_{p} = Pump head (also known as Total Dynamic Head), ft or m.
K_{m} = Sum of minor losses coefficients. See table
below.
log = Common (base 10) logarithm.
Pump Power (computed by program) = SQH_{p}, lbft/s or Nm/s. Theoretical
pump power. Does not include an inefficiency term. Note that 1 horsepower = 550 ftlb/s.
P_{1} = Upstream pressure, lb/ft^{2} or N/m^{2}.
P_{2} = Downstream pressure, lb/ft^{2} or N/m^{2}.
Re = Reynolds number, unitless.
Q = Flow rate in pipe, ft^{3}/s or m^{3}/s.
S = weight density, lb/ft^{3} or N/m^{3}.
V = Velocity in pipe, ft/s or m/s.
V_{1} = Upstream velocity, ft/s or m/s.
V_{2} = Downstream velocity, ft/s or m/s.
Z_{1} = Upstream elevation, ft or m.
Z_{2} = Downstream elevation, ft or m.
v = kinematic viscosity, ft^{2}/s or m^{2}/s. Note that kinematic
viscosity = dynamic viscosity divided by density.
All of our calculations utilize double precision. Newton's method (a numerical
method) is used to solve the Colebrook equation accurate to 8 significant digits. A
cubic solver (numerical method) is used for "Solve for V, Q," "Q known.
Solve for Pipe Diameter," and "V known. Solve for Pipe Diameter."
More than one solution is possible for these three calculations since there could be a
result in the laminar range and the turbulent range. There may even be two possible
results in the laminar range for "Solve for V, Q" if scenario D or G is
selected. All of the possible solutions are computed and output. If multiple solutions are computed, please click in the numeric field and click the right arrow key to see all of the digits. If you have
selected "Q known. Solve for Pipe Diameter," and scenario D or G, you must enter
K_{m} >1. All calculations are analytic (closed form) except as
mentioned here.
Table of Minor Loss Coefficients (K_{m}
is unitless) References
Back to Calculation
Fitting 
K_{m} 
Fitting 
K_{m} 
Valves: 

Elbows: 

Globe, fully open 
10 
Regular 90°, flanged 
0.3 
Angle, fully open 
2 
Regular 90°, threaded 
1.5 
Gate, fully open 
0.15 
Long radius 90°, flanged 
0.2 
Gate 1/4 closed 
0.26 
Long radius 90°, threaded 
0.7 
Gate, 1/2 closed 
2.1 
Long radius 45°, threaded 
0.2 
Gate, 3/4 closed 
17 
Regular 45°, threaded 
0.4 
Swing check, forward flow 
2 


Swing check, backward flow 
infinity 
Tees: 



Line flow, flanged 
0.2 
180° return bends: 

Line flow, threaded 
0.9 
Flanged 
0.2 
Branch flow, flanged 
1.0 
Threaded 
1.5 
Branch flow, threaded 
2.0 




Pipe Entrance (Reservoir to Pipe): 

Pipe Exit (Pipe to Reservoir) 

Square Connection 
0.5 
Square Connection 
1.0 
Rounded Connection 
0.2 
Rounded Connection 
1.0 
Reentrant (pipe juts into tank) 
1.0 
Reentrant (pipe juts into tank) 
1.0 
Common Questions
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I took fluid mechanics a long long time ago. What is head? Why does it have
units of length? Head is energy per unit weight of fluid (i.e. Force x
Length/Weight = Length). The program on this page solves the energy equation (shown
above); we call energy "head."
Why is Pressure=0 for a reservoir? A reservoir is open to the atmosphere, so its
gage pressure is zero.
Why is Velocity=0 for a reservoir? This is a common assumption in fluid
mechanics and is based on the fact that a reservoir has a large surface area. Therefore,
the liquid level drops very little even if a lot of liquid flows out of the
reservoir. A reservoir may physically be a lake or a large diameter tank.
What is a "main" and a "lateral"? A "main" is
a large diameter supply pipe that has many smaller diameter "laterals" branching
off of it. In fluid mechanics, we set V=0 for the main since it has a large diameter
(relative to the lateral) and thus a very small velocity. To further justify the V=0
assumption, the main's pressure is typically high, so the velocity head in the main is
negligible. The main is drawn such that it is coming out of your computer monitor.
Can I model flow between two reservoirs using either Scenario B or E? Yes,
you can. If using Scenario E, just set P_{1}P_{2}=0. Scenario B
automatically sets P_{1}P_{2}=0.
Can I model flow between two mains using either Scenario B or E? Only if the
pressure is the same in both mains.
How do I model a pipe discharging freely to the atmosphere? Use Scenario A,
C, or F. Since P_{2}=0 (relative to atmospheric pressure), P_{1}P_{2}
that is input or output will be P_{1}.
What are minor losses? Minor losses are head (energy) losses due to valves,
pipe bends, pipe entrances (for fluid flowing from a tank to a pipe), and pipe exits
(fluid flowing from a pipe to a tank), as opposed to a major loss which is due to the
friction of fluid flowing through a length of pipe. Minor loss coefficients (K_{m})
are tabulated below. For our program, all of the pipes have the same diameter, so
you can add up all your minor loss coefficients and enter the sum in the Minor Loss
Coefficient input box.
Why do I sometimes get the message, "Infeasible Input"? The
governing equations for fluid flow must be satisfied. Fluids must flow from higher energy
to lower energy; driving head must always be > 0. Pipe roughness, fluid
viscosity, pipe diameter, and velocity must be such that the Reynolds number is <=10^{8}
and other conditions shown with the equations below are satisfied. It is possible to
enter values that are not physically or mathematically feasible.
I'm confused about pumps. Only input Pump Head if the pump is between points
1 and 2. Otherwise, enter 0 for Pump Head. Pump Head, H_{p}, is also
known as total dynamic head.
Your program is great! What are its limitations? Pipes must all have
the same diameter. Pump curves cannot be implemented.
What is Driving Head? See above in the variable definitions.
References
Back to Calculation
Cimbala, John M. and Yunus A. Cengel. 2008. Essentials of Fluid Mechanics: Fundamentals
and Applications. McGrawHill.
Crane Co. 1988. Flow of Fluids through Valves, Fittings, and Pipe.
Technical Paper 40 (TP40). http://www.craneco.com.
Munson, Bruce R. Donald F. Young, and Theodore H. Okiishi. 1998.
Fundamentals of Fluid Mechanics. John Wiley and Sons. Inc. 3ed.
Streeter, Victor L., E. Benjamin Wylie, and Keith W. Bedford. 1998. Fluid
Mechanics. McGrawHill. 9ed.
© 19992015 LMNO Engineering, Research, and
Software, Ltd. All rights reserved.
Please contact us for consulting or other questions.
LMNO Engineering, Research, and Software, Ltd.
7860 Angel Ridge Rd. Athens, Ohio 45701 USA Phone and
fax: (740) 5921890
LMNO@LMNOeng.com http://www.LMNOeng.com
August 25, 2015: Made text fields narrower to show 8 significant figures rather than 16. Calculation still uses double precision internally.

To:
LMNO Engineering home page (more calculations)
Other single pipe calculators:
DarcyWeisbach with pump curve
HazenWilliams without pump curve
HazenWilliams with pump curve
Multiple pipes:
Pipe Network
Bypass Loop Calculator
Videos of experiment and analysis of friction loss
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