1.
Group
Leader
Report
Julianne
Rutenbeck
CHEN
3130-­‐004
Dr.
Wendy
Young
02/10/2015

2. 2
Table
of
Contents
Objectives
….………………………………………………………………………………………………………………
3
Apparatus
and
Equipment
………………………………………………………………………………………….
4
Process
Flow
Diagram
………………………..………………………………………………………………….
4
Operating
Instructions
……………………………………………………………………………………………….
5
Start
up
………….…………………………………………………………………………………………………….
5
Calibrations
………………………………………………………………………………………………......................
5
Data
Collection
………………………..………………………………………………………………….....................
6
Shut
Down
…………………………………………………………………………………………………………...
6
Safety
…………………………………………………………………………………………………………………..
6
Calculations
…………………………………………………………………………………………………....................
7
Calculation
Flowcharts
…..………………………………………………………………………………………
7
Error
Analysis
……………………………………………………………………………………………………………
9
Bibliography
…………………………………………………………………………………………………………...
10
Appendices
……………………………………………………………………………………………………………...
11
Appendix
I:
Table
of
Nomenclature
and
Physical
Properties
……………………………………...
11
Appendix
II:
Instrument
Specifications
……………………………………………………………............
12
Appendix
III:
Specified
flow
rates
to
be
studied…………………………………………………………..
12
Appendix
IV:
Pipe
Specifications
………………………………………………………………………………..
13
Appendix
V:
Example
Moody
Diagram
……………………………………………………………………...
14

3. 3
Objectives
This
experiment
will
investigate
how
physical
parameters
affect
the
pressure
drop
in
pipes.
The
pressure
drop
in
straight
pipes
over
a
given
length
will
be
measured
for
various
pipe
diameters
and
volumetric
flow
rates.
With
these
data,
an
experimental
moody
chart
will
be
created
and
compared
to
typical
versions.
A
typical
moody
chart
plots
the
Reynolds
number
–
a
dimensionless
parameter
used
to
characterize
fluid
flow
–
versus
the
friction
factor,
at
various
values
of
the
relative
roughness
(ϵ/D),
which
is
characteristic
of
the
piping
material
(Refer
to
Appendix
V
for
an
example
Moody
chart).
The
plot
created
from
this
experiment
will
have
only
one
value
of
the
roughness
factor
and
therefore
the
relative
roughness
will
depend
only
on
the
pipe
diameter.
The
Reynolds
number
and
friction
factor
can
both
be
calculated
from
properties
of
the
fluid
and
knowledge
of
the
flow
rate,
pipe
diameter,
and
the
pressure
change
over
a
given
length
of
tube
(equations
5,
8;
see
Calculations,
Flow
Chart
II,
pg.
8).
Flow
rate
and
diameter
will
be
varied
and
the
pressure
drop
for
each
combination
will
be
recorded.
Pressure
changes
through
a
number
of
flow
components
will
also
be
observed.
Similar
to
the
method
used
for
straight
pipes,
the
pressure
drop
around
the
components
will
be
measured
as
a
function
of
flow
rate.
These
components
consist
of
a
ball
valve
(H),
a
bonnet
valve
(G),
a
90o
bend
(K),
a
venturi
meter
(I),
and
an
orifice
meter
(J,
see
Figure
1,
pg.
4).
Once
the
data
have
been
obtained,
a
plot
will
be
created
for
each
of
the
two
valves
and
the
bend,
showing
equivalent
length
versus
the
Reynolds
number.
The
equivalent
length
is
an
effective
distance,
equivalent
to
the
length
of
straight
pipe
that
would
cause
the
same
change
in
pressure
at
the
given
flow
rate
and
diameter;
it
can
be
calculated
from
these
three
parameters
(equation
10,
Calculation
Flow
Chart
III,
pg.
9).
The
venturi
and
orifice
meters
will
each
be
analyzed
with
a
plot
of
the
discharge
coefficient
versus
the
Reynolds
number
at
various
flow
rate
and
diameter
values.
The
discharge
coefficient
is
a
dimensionless
parameter
used
to
describe
the
relative
efficiency
of
a
valve
discharging
to
a
reservoir
(equation
11,
Calculation
Flow
Chart
IV,
pg.
9).
By
the
end
of
the
experiment,
the
dependence
of
the
pressure
drop
on
diameter
and
flow
rate
will
be
approximately
known.
The
resulting
correlations
and
relationships
may
be
used
in
the
future
to
help
design
a
new
piping
network
with
this
piping
material.

4. 4
Apparatus
and
Equipment
Figure
1.
Process
Flow
Diagram.
Orifice Meter
Venturi Meter
Air release valves
Bonnet Valve
Ball Valve
Pressure Gauge/Transducer Connection
Gate valve
Rotameter switch valve
Rotameter
Flow in
Flow out
Line 6
Line 5
Line 4
Line 3
Line 2
Line 1
Reservoir
Pump
A
B
C
D
E
F
G H
I J
2 psid pressure transducer
5 psid pressure transducer
10 psid pressure transducer
L
K
Entrance length
L=length of P drop
Exit Length
M

5. 5
Apparatus
&
Equipment
The
Process
Flow
The
pump
pushes
water
up
from
the
reservoir,
through
one
of
the
rotameters
(M),
and
up
the
left
side
of
the
apparatus.
The
air
release
valves
(F),
allow
the
water
to
air
push
up
and
out
of
the
system.
Each
line
has
a
ball
valve
that
controls
the
flow
into
that
tube.
Lines
one,
four,
five,
and
six
are
just
straight
pipes
with
pressure
sensor
ports
on
opposite
ends.
Line
two
has
the
Venturi
meter
(I),
the
orifice
meter
(J),
and
the
bend
(K).
Line
three
has
two
different
kinds
of
valves
–
Ball
(H)
and
Bonnet
(G).
Each
of
these
components
has
pressure
sensor
ports
on
either
side
of
them.
The
water
flows
out
on
the
opposite
side
of
the
apparatus,
passes
through
the
gate
valve
(L),
and
drains
back
into
the
reservoir
to
be
recycled.
Table
1.
Process
Flow
Diagram
Components
Component
G
Bonnet
valve
A
Pump
H
Ball
valve
B
Valve
to
switch
rotameters;
Orifice
0.01905
m
I
Venturi
Meter
C
Ball
valve
to
open
each
line
J
Orifice
Meter
D
Pressure
sensor
connection
port
K
Bend
E
Brass
Alloy
260
Tubing
L
Gate
valve
F
Air
release
valves
M
Rotameter
Operating
Instructions
and
Safety
Start
Up
Before
engaging
the
pump
and
beginning
data
collection,
the
apparatus
must
be
in
the
proper
state.
One
of
the
rotameter
valves
should
be
open
and
the
other
closed
(B;
see
figure
1,
pg.
4);
if
both
are
in
the
same
position,
damage
to
the
pump
may
occur.
The
entry
valves
to
each
pipe
should
be
such
that
the
lines’
under
study
are
open
and
the
rest
are
closed
(C).
On
the
exiting
side,
the
gate
valve
leading
into
the
drain
tub
(L)
should
be
all
the
way
open
and
secured
to
the
reservoir.
Once
the
water
has
established
full
flow
and
the
experiment
begun,
the
exit
valve
may
be
adjusted
accordingly
to
avoid
vacuum
pressures.
When
all
of
this
has
been
accomplished,
the
pump
is
ready
to
be
engaged.
When
the
pump
is
started,
the
lines
must
be
cleared
of
air
to
avoid
hammering
and
equipment
damage.
To
clear
the
line,
open
the
air
release
valves
on
each
side
of
the
apparatus
(F).
When
water
can
be
seen
in
the
tube,
all
the
air
has
been
cleared
from
the
lines
and
the
valve
can
be
shut.
Calibration
The
rotameters
(M)
will
be
calibrated
with
a
catch
and
weigh.
Once
full
flow
has
been
established
–
the
¾”
lines
may
take
several
minutes
–
the
process
can
begin.
The
information
being
recorded
will
be
the
time
for
which
water
is
allowed
to
flow
into
the
bucket,
along
with
the
mass
of
the
bucket,
before
and
after
the
water
is
allowed
to
drain
into
it.
With
this
information,
equation
(1)
can
be
used
to
calculate
the
actual
flow
rate
and
compare
it
to
the
rotameter
reading.
For
each
rotameter,
five
different
flow
rates
will
be
measured,
and
three
replicates
will
be
performed
at
each
level.
This
data
should
then
be

6. 6
consolidated
into
a
calibration
curve,
which
then
can
be
used
for
the
duration
of
the
experiment.
Table
5
in
appendix
III
shows
the
specified
levels
to
be
calibrated.
At
each
of
the
flow
rates,
the
pressure
transducers
will
also
be
calibrated.
Using
the
same
gauge,
measurements
will
be
taken
across
the
pipe
at
the
same
sites
that
the
transducers
connect
to.
Since
there
are
two
rotameters
and
two
pressure
transducers
that
require
calibration,
the
ten-­‐psid
transducer
will
be
calibrated
with
the
0.2-­‐2
gpm
rotameter,
and
the
five-­‐psid
transducer
with
the
2-­‐15
gpm
rotameter.
The
gauge
and
transducer
data
will
be
compared
in
a
calibration
curve.
Between
each
replicate
of
the
calibrations,
the
flow
rate
should
be
varied
slightly
and
brought
back
to
the
original
level.
Data
Collection
Since
the
aim
of
this
experiment
is
to
explore
a
wide
range
of
Reynolds
numbers
and
pressure
changes,
a
wide
variety
flow
rates
will
be
investigated.
For
each
straight
tube,
four
flow
rates
have
been
specified
and
three
replicates
will
be
performed
at
each.
If
time
does
not
permit
for
this
many
trials,
one
flow
rate
for
each
line
has
been
specified
as
being
less
necessary;
table
6
(appendix
III)
shows
the
specified
flow
rates
to
be
studied.
At
each
specified
flow
rate,
the
actual
flow
reading
and
pressure
drop
across
the
appropriate
transducer
will
be
recorded.
Pressure
drop
will
be
measured
via
LabView
Software.
The
experiment
will
generate
between
thirty-­‐six
and
forty-­‐eight
data
points.
These
will
be
used
to
create
an
experimental
moody
chart
(see
calculations
flow
chart
II
for
more
information).
The
generated
plot
will
be
compared
to
typical
ones
found
in
literature.
An
example
Moody
chart
has
been
attached
in
Appendix
V
for
comparison
with
the
results
obtained.
Since
all
the
lines
will
be
used,
when
switching
between
them,
one
must
open
the
next
valve
before
closing
the
current
one.
If
all
entry
valves
are
closed,
damage
to
the
equipment
may
result.
After
the
straight
pipe
data
have
been
taken,
lines
two
and
three
will
be
studied.
Again,
flow
rate
and
pressure
drop
around
each
component
will
be
varied
and
recorded.
These
data
will
be
used
to
make
two
more
plots
–
discharge
coefficient
(calculation
flow
chart
IV)
versus
Reynolds
number
for
the
venturi
and
orifice
meters
and
equivalent
length
(calculation
flow
chart
III)
versus
Reynolds
number
for
the
valves
and
bend.
Shut
Down
To
shut
down
the
apparatus,
simply
turn
off
the
pump.
After
this,
shut
all
the
gate
valves
to
the
lines
and
all
other
valves
should
be
in
safe
positions
for
future
use.
Because
water
may
leak
from
the
lines
or
reservoir,
dry
the
surrounding
area
for
the
safety
of
others
in
the
lab.
Safety
• As
stated
above,
water
leakage
increases
the
risk
of
slipping
in
the
lab.
• The
pump
is
an
electrical
component
in
a
water
reservoir.
Be
careful
not
to
allow
loose
wires,
or
other
conductors
that
have
electricity
running
through
them,
to
come
into
contact
with
the
water.

7. 7
Calculations
-­‐Refer
to
Appendix
I
for
variable
definitions
and
physical
property
values.
I.
Calibration
of
Rotameter
II.
Experimental
Moody
Chart
Catch
&
Weigh
• Measure
mass
of
empty
bucket.
• Time
how
long
water
llows
into
the
bucket.
• Measure
the
mass
of
the
bucket
and
water(m).
Obtain
Flow
Rates
• Q=(m/t)(1/ρ)
(1)
• Record
observed
llow
rate
from
rotameter.
Callibration
Curve
• Plot
Q
vs.
the
readings
from
the
rotameter.
Velocity
• ν=Q/A
(2)
Pipe
properties
• A=π(D/2)2
(3)
• Relative
Roughness
=
ϵ/D
(4)
Reynolds
Number
• Re=ρνD/μ
(5)
• τw=
-­‐(dP/dz)(D/4)
(6)
Friction
Factor
• ff=2τw/ρν2
(7)
• Assuming
the
shear
stress
is
constant.
• ff
=
(ΔP)D/2ρν2L
=
(P1-­‐P2)D/2ρν2L
(8)
Moody
Chart
• Plot
ff
vs.
Re
for
different
experimental
values
of
ν,
ΔP/L,
and
D.
Compare
this
with
charts
found
in
literature.

8. 8
Assume
• Horizontal
llow
• Uniform
velocity
prolile
upstream
and
downstream
Discharge
Coeflicient
Reynolds
Number
• Re=ρνD/μ
(4)
Graph
• Plot
Cd
vs.
Re
for
each
meter
at
various
llow
rates.
Analyze
the
graphs.
III.
Bend
and
Valves
IV.
Venturi
meter
and
Orifice
meter
𝐶! =
!!
!!!
!
!(!!(
!!
!!
)!)
! !"
11
Reynolds
Number
• Re=ρνD/μ
(4)
• Use
this
along
with
the
experimental
moody
chart
to
get
ff
Loss
Coeflicient
• Assuming
fully-­‐developed,
steady,
incompressible
llow.
• KL
=
2Ploss/ρν2
=
2(P1-­‐P2)/ρν2
(9)
Equivalent
Length
• leq=KLD/ff
(10)
• Graph
leq
vs.
Re
for
the
bend
and
both
valves
at
various
values
of
ΔP,
ff,
and
ν.

9. 9
Error
Propagation
Three
replicates
will
be
done
for
each
measurement.
The
data
taken
from
these
measurements
will
be
analyzed
with
the
equations
and
graphs
mentioned
previously.
The
error
associated
with
the
measurements
will
propagate
when
these
calculations
are
performed,
so
the
equations
below
should
be
used
to
estimate
the
error
associated
with
a
calculated
value.
𝛿𝑄 =
1
𝜌𝑡
!
(𝛿𝑚)! + (
−𝑚
𝜌𝑡!
)!(𝛿𝑡)! (1)
𝛿𝑉 =
𝛿𝑄
𝐴
(2)
𝛿𝑓! =
𝐷
2𝜌𝑣! 𝐿
!
𝛿Δ𝑃 ! + (
−Δ𝑃𝐷
𝜌𝑣! 𝐿
)! 𝛿𝑣 ! (8)
𝛿𝐾! =
2
𝜌𝑣!
!
(𝛿Δ𝑃)! +
−4Δ𝑃
𝜌𝑣!
!
(𝛿𝑣)! (9)
𝛿𝑙!" =
𝐷
𝑓!
!
𝛿𝐾!
! + (
−𝐷𝐾!
𝑓!
! )!(𝛿𝑓!)! (10)
𝛿𝐶! =
4
𝜋𝐷!
!
𝜌(1 − (
𝐷!
𝐷!
)!)
2 𝛥𝑃
!
(𝛿𝑄)! +
−2𝑄
𝜋𝐷!
!
𝜌(1 − (
𝐷!
𝐷!
)!)
2(Δ𝑃)!
!
(𝛿Δ𝑃)! (11)
The
equations
for
which
these
errors
should
be
used
are
noted
on
the
right
of
the
equation.
The
error
for
each
measurement
will
be
the
greater
of
two
errors:
the
error
associated
with
reading
the
measurement
and
random
error
between
measurements
due
to
random
fluctuations
(standard
deviation).
The
error
associated
with
equation
one
should
not
be
used
as
the
error
value
in
the
latter
equations;
it
is
only
for
the
catch
and
weigh.
Manufacturer
data
are
shown
in
appendix
II,
table
4.
The
precision
is
an
estimate
based
on
the
markings
on
the
instrument.
No
measurements
were
taken
with
them
in
order
to
verify
the
estimates.
The
systematic
error
for
measurements
of
volumetric
flow
rate
and
pressure
drop
should
be
eliminated
with
the
calibration
of
the
instruments.

10. 10
Bibliography
Kestin,
J.,
Sokolov,
M.,
Wakeham,
W.
A.
(1978).
Viscosity
of
Liquid
Water
in
the
Range
-­‐8oC
to
150oC.
J.
Phys.
Chemical
Reference
Data,
Vol.
7.
Retrieved
from:
http://www.nist.gov/data/PDFfiles/jpcrd121.pdf
The
Engineering
Page.
Retrieved
from:
http://www.the-­‐engineering-­‐
page.com/forms/dp/typ_eps.html
The
Engineering
Toolbox.
Retrieved
from:
http://www.engineeringtoolbox.com/moody-­‐
diagram-­‐d_618.html

11. 11
Appendices
Appendix
I
Table
2.
Table
of
Nomenclature.
Symbol
Definition
Units
Obtained
by:
Q
Volume
flow
rate
m3/s
Calculated/measured
m
Mass
of
water
kg
Measured
ρ
Density
of
water
@
Twater
≅
25oC
kg/m3
Constant
(varies
with
T)
t
time
s
Measured
T
Temperature
of
water
oC
Measured
(LabView)
τw
Shear
stress
at
the
wall
N/m2
Calculated
A
Cross
sectional
area
of
pipe
m2
Calculated
D
Diameter
of
pipe
in
Constant
ν
Velocity
m/s
Calculated
ff
Fanning
friction
factor
-­‐-­‐
Calculated
ΔP
Differential
pressure
psid
Measured
(LabView)
P1
Upstream
pressure
psig
Measured
P2
Downstream
pressure
psig
Measured
L
Length
of
pipe
between
P1
&
P2
in
Constant
Re
Reynolds
number
-­‐-­‐
Calculated
μ
Dynamic
viscocity
of
water
at
25oC
Ns/m2
Constant
(varies
with
T)
D1
Large
diameter
of
venturi/orifice
meter
in
Constant
D2
Small
diameter
of
venturi/orifice
meter
in
Constant
Cd
Discharge
Coefficient
-­‐-­‐
Calculated
KL
Loss
Coefficient
-­‐-­‐
Calculated
leq
Equivalent
length
of
straight
pipe
m
Calculated
ϵ
Roughness
Factor
m
Constant
Table
3.
Table
of
Physical
Properties.
Property
Value
Units
1ρ
(at
25oC)
997.1
kg/m3
1μ
(at
25oC)
8.902E-­‐4
Ns/m2
2ϵ
(Brass)
1.0E-­‐7–1.5E-­‐7
m
1-­‐
Kestin
et
al.,
1978
2-­‐
“The
Engineering
Page”

12. 12
Appendix
II
Table
4.
Instrument
Specifications
Instrument
Mfr.1
Range
Units
3Accuracy/Bias
Precision
Tolerance
Pressure
Gauge
WIKA
0-­‐15
psig
±
2.5%
±0.5
If
the
same
gauge
is
used
to
measure
pressure
in
both
positions,
the
bias
should
be
eliminated
Pressure
Gauge
WIKA
0-­‐30
psig
±
2.5%
±1.0
Pressure
Transducer
Dwyer
0-­‐2
psid
±
.25%
±0.02
The
transducers
can
be
calibrated
using
the
gauges
to
measure
P1
and
P2
Pressure
Transducer
Dwyer
0-­‐5
psid
±
.25%
±0.02
Pressure
Transducer
Dwyer
0-­‐10
psid
±
.25%
±0.02
Rotameter
King
0.2-­‐2
gpm
±
5%
±
0.5
The
rotameters
will
be
calibrated
Rotameter
King
1.5-­‐15
gpm
±
5%
±
0.5
____________________________________
1-­‐Manufacturer
2-­‐The
data
are
collected
using
Labview
software.
3-­‐Estimates
based
on
multiple
possible
models
Appendix
III
Table
5.
Calibration
flow
rate
specifications
Rotameter
Flow
rates
to
be
calibrated
(gpm)
0.2-­‐2
gpm
0.35
0.8
1.2
1.6
2.0
2-­‐15
gpm
2.1
4.3
6.5
8.7
11
Table
6.
Data
collection
flow
rates
Flow
Rates
to
be
studied
(gpm)
Possible
flow
rates
Line
1
4
5.2
8
11
gpm
Line
4
3
4.5
8.5
5.3
gpm
Line
5
0.8
1
4.5
1.85
gpm
Line
6
0.35
0.5
1.3
0.9
gpm

13. 13
Appendix
IV
Table
7.
Straight
Tube
Specifications
and
Recommendations.
Line
1
Line
4
Line
5
Line6
I.D.
(m)
0.015748
0.0110744
7.8994E-­‐3
4.7244E-­‐3
Recommended
Gauge
15
psig
15
psig
30
psig
30
psig
Recommended
Transducer
5
psid
5
psid
10
psid
10
psid
Recommended
Flow
Rate
(m3/s)*104
6.94–2.52
5.36–1.89
2.84–0.505
0.82–0.221
Length
between
psid
measurements
(m)
1.0922
1.09855
1.09855
1.09855
Entry
Ball
Valve
Orifice
(m)
0.019304
0.0103124
7.1374E-­‐3
4.7498E-­‐3
Relative
Roughness
(x105)
0.64–0.95
0.9–1.35
1.27–1.9
2.12–3.18
Table
8.
Component
Specifications
and
Recommendations.
Venturi
Meter
Orifice
Meter
Bonnet
Valve
Ball
Valve
Line
2
2
3
3
Length
0.0889
m
n/a
n/a
n/a
Throat
1L
0.022225
m
n/a
n/a
n/a
Throat/Bore
Diameter
9.525E-­‐3
m
0.014732
m
n/a
n/a
1L
across
0.4572
m
0.34925
m
0.34925
m
0.3556
m
1L
upstream
.22225
m
0.18415
m
n/a
n/a
1L
down-­‐stream
.23495
m
0.1651
m
n/a
n/a
Entry
valve
orifice
(m)
0.019304
-­‐-­‐
0.0103124
-­‐-­‐
2Flow
Rate*104
5.68–2.52
m3
/s
4.1–1.89
m3
/s
-­‐-­‐
-­‐-­‐
2P
Gauge
15
psig
15
psig
30
psig
30
psig
2Transducer
5
psid
5
psid
10
psid
10
psid

14. 14
Appendix
V
Figure
2.
Example
experimental
Moody
Chart
(The
Engineering
Toolbox).