Pakistan Institute of Engineering and Applied Sciences

TEP LAB REPORT

FLUID FRICTION EXPERIMENT

Submitted To:

Dr. Inam-ul-Haq

Submitted By:

Fayaz Ali (MS-13-PH-21849)

Group:

3

Semister:

1

Department:

Nuclear Engineering

Objective:

1) Investigation of Friction Factor for water flow in various sectional pipes. 2) Investigation of Coefficient of head loss across small radius 90⁰ bend, sudden

enlargement and contraction tube, gradual enlargement and reduction tube, glove valve, gate valve and cock to Reynolds Number.

3) Investigation of Flow coefficient for orifice, nozzle and venturi tube

Head Loss:Head loss is the reduction in the total head of a fluid caused by the friction present in the fluid's motion.There are two types of head losses

1) Major Head LossMajor head loss occurs due to fluid friction as the fluid flows through the straight

pipes. From Bernoulli equation

Where hlossrepresents the total head lost

[ P1

γ+V 1

2

2g+Z1=

P2

γ+V 2

2

2g+Z2+hloss ]

From the above equation for horizontal pipe we can get the head loss hL as

HL=(P1-P2)/g*density

These losses is mainly due to friction plus other minor losses in the bends ,change in cross-section area etc.

Major loss due to friction is given by the Darcy-Weisbach equation

hf = fLV2/(2gD)

Where

ΔP = head Loss

f = friction factorV = Fluid velocityD = diameter of pipeL = Length of pipe

2) Minor Head LossMinor losses are head losses that occur due to bends, elbows, joints, valves, and other fittings in the systems. Whenever there is a change in the direction of flow or a change in the cross-sectional area a head loss will occur.

Minor loss is calculated from the following formula

hm = K(V2/2g)

‘K’ represents the ‘loss Co-efficient’. The value of ‘k’ strongly depends upon the geometry of component considered. It will be different for bends, elbows, joints, valves, and other fittings in the systems.

Reynolds Number:

In fluid mechanics, the Reynolds number (Re) is a dimensionless number that gives a measure of the ratio of inertial forces to viscous forces and consequently quantifies the relative importance of these two types of forces for given flow conditions.

For flow in a pipe or tube, the Reynolds number is generally defined as:[7]

where:

is the mean velocity of the fluid (SI units: m/s). is the dynamic viscosity of the fluid (Pa·s or N·s/m² or kg/(m·s)).

is the kinematic viscosity ( (m²/s). is the density of the fluid (kg/m³). D is inner diameter of pipe

The Reynolds Number can be used to determine if flow is laminar, transient or turbulent. The flow is

laminar when Re < 2300 transient when 2300 < Re < 4000 turbulent when Re > 4000

Moody Chart:The Moody chart or Moody diagram is a graph in non-dimensional form that relates the Darcy-Weisbach friction factor, Reynolds number and relative roughness for fully developed flow in a circular pipe.

Investigation of Flow coefficient for orifice, nozzle and venturi tube

The objective of this section of the experiment was to find out the behavior of fluid as it flows across the orifice, nozzle or a venture meter. In the end the relation between Reynolds’s number and Flow coefficient is seen graphically to easily visualize the observations.

The mathematical relations used are given below:

Qtheoritical=area*velocity = πd2/4(2gh)1/2

While the actual discharge is found from the rotameter.

Then the Flow coefficient is given by

C d=QactualQtheoretical

Measurements and graph of Reynolds Number VS Friction Flow Factor:

(for ½”,3/4”and 1” diameter pipe respectively

Q= l/h Q=m/sec

D= in Area=m2 v=Q/A

u level mm

lower level mm

del h mm

del p m

del p (Pascals) = (density of mercury)gh

hf=(del p )/(pg)

Re= DVp/u L f

for 1

/2 in

ch d

ia p

ipe

2700 0.00075 0.50 0.0001266 5.92357873 304 125 179 0.179 22554 2.2554 7507.9 20.0082

2500 0.00069 0.50 0.0001266 5.48479512 290 135 155 0.155 19530 1.953 6951.8 20.0082

2300 0.00064 0.50 0.0001266 5.04601151 276 150 126 0.126 15876 1.5876 6395.6 20.0079

2000 0.00056 0.50 0.0001266 4.38783609 263 165 98 0.098 12348 1.2348 5561.4 20.0081

1800 0.0005 0.50 0.0001266 3.94905248 255 174 81 0.081 10206 1.0206 5005.3 20.0083

1500 0.00042 0.50 0.0001266 3.29087707 245 180 65 0.065 8190 0.819 4171.1 20.0096

1200 0.00033 0.50 0.0001266 2.63270166 235 193 42 0.042 5292 0.5292 3336.9 20.0097

1000 0.00028 0.50 0.0001266 2.19391805 217 200 17 0.017 2142 0.2142 2780.7 20.0057

for 3

/4 in

ch d

ia p

ipe

2700 0.00075 0.75 0.0002849 2.63270166 240 188 52 0.052 6552 0.6552 5005.3 2 0.018

2500 0.00069 0.75 0.0002849 2.43768672 235 140 95 0.095 11970 1.197 4634.5 20.0384

2300 0.00064 0.75 0.0002849 2.24267178 233 190 43 0.043 5418 0.5418 4263.8 20.0205

2000 0.00056 0.75 0.0002849 1.95014937 230 198 32 0.032 4032 0.4032 3707.6 20.0202

1800 0.0005 0.75 0.0002849 1.75513444 230 200 30 0.03 3780 0.378 3336.9 20.0234

1500 0.00042 0.75 0.0002849 1.46261203 225 203 22 0.022 2772 0.2772 2780.7 20.0247

1200 0.00033 0.75 0.0002849 1.17008962 222 205 17 0.017 2142 0.2142 2224.6 20.0298

1000 0.00028 0.75 0.0002849 0.97507469 219 206 13 0.013 1638 0.1638 1853.8 20.0328

for 1

inch

dia

pip

e

2700 0.00075 1.00 0.0005065 1.48089468 230 200 30 0.03 3780 0.378 3754 20.0438

2500 0.00069 1.00 0.0005065 1.37119878 225 204 21 0.021 2646 0.2646 3475.9 20.0357

2300 0.00064 1.00 0.0005065 1.26150288 222 205 17 0.017 2142 0.2142 3197.8 20.0342

2000 0.00056 1.00 0.0005065 1.09695902 225 205 20 0.02 2520 0.252 2780.7 20.0532

1800 0.0005 1.00 0.0005065 0.98726312 222 207 15 0.015 1890 0.189 2502.6 20.0493

1500 0.00042 1.00 0.0005065 0.82271927 220 208 12 0.012 1512 0.1512 2085.5 20.0567

1200 0.00033 1.00 0.0005065 0.65817541 219 209 10 0.01 1260 0.126 1668.4 20.0739

1000 0.00028 1.00 0.0005065 0.54847951 217 209 8 0.008 1008 0.1008 1390.4 20.0851

1000 2000 3000 4000 5000 6000 7000 80000

0.01

0.02

0.03

0.04

0.05

0.06

0.07

0.08

0.09

3/4 inch dia1 inch dia1/2 inch dia

Reynold Number

fric

tion

fact

or f

Measurements and graph of Coefficient of Head Loss VS Reynolds Number (k vs Re:

Q= l/h Q=m/sec D= in Area1''=m^2 v1''=Q/A(m/sec)

u level mm

l level mm

del h mmdel p mdel p (Pascals) = (density of mercury)gh hm=(del p )/(pg)Re= DVp/u

k A(1/2)''=m^2v2

1-2

for 9

0 be

nd

2500 0.00069 1.00 0.0005065 1.371198779 9 0.009 1134 0.1134 3475.9 0.1 0.000127 5.482200 0.00061 1.00 0.0005065 1.206654926 10 0.01 1260 0.126 3058.8 1.7 0.000127 4.832000 0.00056 1.00 0.0005065 1.096959023 8 0.008 1008 0.1008 2780.7 1.7 0.000127 4.391800 0.0005 1.00 0.0005065 0.987263121 9 0.009 1134 0.1134 2502.6 2.3 0.000127 3.951500 0.00042 1.00 0.0005065 0.822719268 7 0.007 882 0.0882 2085.5 2.6 0.000127 3.291300 0.00036 1.00 0.0005065 0.713023365 3 0.003 378 0.0378 1807.5 1.5 0.000127 2.851000 0.00028 1.00 0.0005065 0.548479512 1 0.001 126 0.0126 1390.4 0.8 0.000127 2.19

700 0.00019 1.00 0.0005065 0.383935658 3 0.003 378 0.0378 973.25 5.1 0.000127 1.54

3-4

for s

udde

n ex

ppan

sion

2500 0.00069 1.00 0.0005065 1.371198779 2 0.002 252 0.0252 3475.9 0.3 0.000127 5.482200 0.00061 1.00 0.0005065 1.206654926 2 0.002 252 0.0252 3058.8 0.3 0.000127 4.832000 0.00056 1.00 0.0005065 1.096959023 2 0.002 252 0.0252 2780.7 0.4 0.000127 4.391800 0.0005 1.00 0.0005065 0.987263121 2 0.002 252 0.0252 2502.6 0.5 0.000127 3.951500 0.00042 1.00 0.0005065 0.822719268 2 0.002 252 0.0252 2085.5 0.7 0.000127 3.291300 0.00036 1.00 0.0005065 0.713023365 2 0.002 252 0.0252 1807.5 1 0.000127 2.851000 0.00028 1.00 0.0005065 0.548479512 2 0.002 252 0.0252 1390.4 1.7 0.000127 2.19

700 0.00019 1.00 0.0005065 0.383935658 2 0.002 252 0.0252 973.25 3.4 0.000127 1.54

5-6

for s

udde

n co

ntra

ction

2500 0.00069 1.00 0.0005065 1.371198779 10 0.01 1260 0.126 3475.9 1.3 0.000127 5.482200 0.00061 1.00 0.0005065 1.206654926 10 0.01 1260 0.126 3058.8 1.7 0.000127 4.832000 0.00056 1.00 0.0005065 1.096959023 8 0.008 1008 0.1008 2780.7 1.7 0.000127 4.391800 0.0005 1.00 0.0005065 0.987263121 9 0.009 1134 0.1134 2502.6 2.3 0.000127 3.951500 0.00042 1.00 0.0005065 0.822719268 7 0.007 882 0.0882 2085.5 2.6 0.000127 3.291300 0.00036 1.00 0.0005065 0.713023365 6 0.006 756 0.0756 1807.5 3 0.000127 2.851000 0.00028 1.00 0.0005065 0.548479512 4 0.004 504 0.0504 1390.4 3.4 0.000127 2.19

700 0.00019 1.00 0.0005065 0.383935658 4 0.004 504 0.0504 973.25 6.8 0.000127 1.54

Q= l/h Q=m/sec D= in Area=m^2 v1=Q/A(m/sec)

u level mm

l level mm

del h mmdel p mdel p (Pascals) = (density of mercury)gh hm=(del p )/(pg)Re= DVp/u

k A(1/2)''=m^2v2

7-8

for g

ate

valv

e

2500 0.00069 1.00 0.0005065 1.371198779 10 0.01 1260 0.126 3475.9 1.3 0.000127 5.482200 0.00061 1.00 0.0005065 1.206654926 10 0.01 1260 0.126 3058.8 1.7 0.000127 4.832000 0.00056 1.00 0.0005065 1.096959023 7 0.007 882 0.0882 2780.7 1.5 0.000127 4.391800 0.0005 1.00 0.0005065 0.987263121 6 0.006 756 0.0756 2502.6 1.6 0.000127 3.951500 0.00042 1.00 0.0005065 0.822719268 7 0.007 882 0.0882 2085.5 2.6 0.000127 3.291300 0.00036 1.00 0.0005065 0.713023365 6 0.006 756 0.0756 1807.5 3 0.000127 2.851000 0.00028 1.00 0.0005065 0.548479512 4 0.004 504 0.0504 1390.4 3.4 0.000127 2.19

700 0.00019 1.00 0.0005065 0.383935658 3 0.003 378 0.0378 973.25 5.1 0.000127 1.54

9-10

for g

lobe

val

ve

2500 0.00069 1.00 0.0005065 1.371198779 260 162 98 0.098 12348 1.2348 3475.9 13 0.000127 5.482200 0.00061 1.00 0.0005065 1.206654926 258 172 86 0.086 10836 1.0836 3058.8 15 0.000127 4.832000 0.00056 1.00 0.0005065 1.096959023 249 179 70 0.07 8820 0.882 2780.7 15 0.000127 4.391800 0.0005 1.00 0.0005065 0.987263121 244 185 59 0.059 7434 0.7434 2502.6 15 0.000127 3.951500 0.00042 1.00 0.0005065 0.822719268 237 196 41 0.041 5166 0.5166 2085.5 15 0.000127 3.291300 0.00036 1.00 0.0005065 0.713023365 235 194 41 0.041 5166 0.5166 1807.5 20 0.000127 2.851000 0.00028 1.00 0.0005065 0.548479512 226 200 26 0.026 3276 0.3276 1390.4 22 0.000127 2.19

700 0.00019 1.00 0.0005065 0.383935658 222 205 17 0.017 2142 0.2142 973.25 29 0.000127 1.54

Q= l/h Q=m/sec D= in Area=m^2 v1=Q/A(m/sec) k v2

11-1

2 fo

r bal

l val

ve2500 0.00069 1.00 0.0005065 1.371198779 220 207 13 0.013 1638 0.1638 3475.9 1.7 0.000127 5.482200 0.00061 1.00 0.0005065 1.206654926 10 0.01 1260 0.126 3058.8 1.7 0.000127 4.832000 0.00056 1.00 0.0005065 1.096959023 10 0.01 1260 0.126 2780.7 2.1 0.000127 4.391800 0.0005 1.00 0.0005065 0.987263121 8 0.008 1008 0.1008 2502.6 2.1 0.000127 3.951500 0.00042 1.00 0.0005065 0.822719268 8 0.008 1008 0.1008 2085.5 3 0.000127 3.291300 0.00036 1.00 0.0005065 0.713023365 8 0.008 1008 0.1008 1807.5 4 0.000127 2.851000 0.00028 1.00 0.0005065 0.548479512 5 0.005 630 0.063 1390.4 4.2 0.000127 2.19

700 0.00019 1.00 0.0005065 0.383935658 4 0.004 504 0.0504 973.25 6.8 0.000127 1.54

Q= l/h Q=m/sec D= in Area=m^2 v1=Q/A(m/sec)

u level mm

l level mm

del h mmdel p mdel p (Pascals) = (density of mercury)gh hm=(del p )/(pg)Re= DVp/u

k A(1/2)''=m^2v2

13-1

4 fo

r noz

zle

2500 0.00069 1.00 0.0005065 1.371198779 300 125 175 0.175 22050 2.205 3475.9 23 0.000127 5.482200 0.00061 1.00 0.0005065 1.206654926 285 147 138 0.138 17388 1.7388 3058.8 24 0.000127 4.832000 0.00056 1.00 0.0005065 1.096959023 274 154 120 0.12 15120 1.512 2780.7 25 0.000127 4.391800 0.0005 1.00 0.0005065 0.987263121 269 160 109 0.109 13734 1.3734 2502.6 28 0.000127 3.951500 0.00042 1.00 0.0005065 0.822719268 253 175 78 0.078 9828 0.9828 2085.5 29 0.000127 3.291300 0.00036 1.00 0.0005065 0.713023365 246 180 66 0.066 8316 0.8316 1807.5 33 0.000127 2.851000 0.00028 1.00 0.0005065 0.548479512 236 192 44 0.044 5544 0.5544 1390.4 37 0.000127 2.19

700 0.00019 1.00 0.0005065 0.383935658 228 200 28 0.028 3528 0.3528 973.25 48 0.000127 1.54

15-1

6 fo

r ven

turi

met

er

2500 0.00069 1.00 0.0005065 1.371198779 319 110 209 0.209 26334 2.6334 3475.9 28 0.000127 5.482200 0.00061 1.00 0.0005065 1.206654926 296 132 164 0.164 20664 2.0664 3058.8 28 0.000127 4.832000 0.00056 1.00 0.0005065 1.096959023 285 142 143 0.143 18018 1.8018 2780.7 30 0.000127 4.391800 0.0005 1.00 0.0005065 0.987263121 275 153 122 0.122 15372 1.5372 2502.6 32 0.000127 3.951500 0.00042 1.00 0.0005065 0.822719268 256 170 86 0.086 10836 1.0836 2085.5 32 0.000127 3.291300 0.00036 1.00 0.0005065 0.713023365 250 179 71 0.071 8946 0.8946 1807.5 35 0.000127 2.851000 0.00028 1.00 0.0005065 0.548479512 242 188 54 0.054 6804 0.6804 1390.4 45 0.000127 2.19

700 0.00019 1.00 0.0005065 0.383935658 228 198 30 0.03 3780 0.378 973.25 51 0.000127 1.54

17-1

8 fo

r ori

ficem

eter

2500 0.00069 1.00 0.0005065 1.371198779 310 118 192 0.192 24192 2.4192 3475.9 26 0.000127 5.482200 0.00061 1.00 0.0005065 1.206654926 292 135 157 0.157 19782 1.9782 3058.8 27 0.000127 4.832000 0.00056 1.00 0.0005065 1.096959023 280 148 132 0.132 16632 1.6632 2780.7 28 0.000127 4.391800 0.0005 1.00 0.0005065 0.987263121 273 155 118 0.118 14868 1.4868 2502.6 31 0.000127 3.951500 0.00042 1.00 0.0005065 0.822719268 255 172 83 0.083 10458 1.0458 2085.5 31 0.000127 3.291300 0.00036 1.00 0.0005065 0.713023365 246 182 64 0.064 8064 0.8064 1807.5 32 0.000127 2.851000 0.00028 1.00 0.0005065 0.548479512 235 195 40 0.04 5040 0.504 1390.4 34 0.000127 2.19

700 0.00019 1.00 0.0005065 0.383935658 228 198 30 0.03 3780 0.378 973.25 51 0.000127 1.54

500 1000 1500 2000 2500 3000 3500 40000

10

20

30

40

50

60

for 90 bendfor sudden expansionfor sudden con-tractionfor gate valvefor globe valvefor ball valvefor nozzlefor venturimeterfor orificemeter

Reynold Number

Head

loss

coeff

ecie

nt K

Measurements and graph of Reynolds Number VS Flow Coefficient:

Q= l/h Qact=m/secD= in Area pipe=m^2

v1=Q

/A(m

/sec

)

u level mm

l level mm

del h mm

del p

mde

l p (P

asca

ls) =

(d

ensi

ty o

f mer

cury

-de

nsity

of w

ater

)gh

area of instrument=m^2

Re=

DVp

/u

Qth Cd

Velo

city

2(Ve

ntur

i.Rel

ation

)=m

/sec

2500 0.00069 1.00 0.0005065 1.371198779 310 118 192 0.192 24192 0.00017 3475.9 0 0.577436 7.092200 0.00061 1.00 0.0005065 1.206654926 292 135 157 0.157 19782 0.00017 3058.8 0 0.562494 6.42000 0.00056 1.00 0.0005065 1.096959023 280 148 132 0.132 16632 0.00017 2780.7 0 0.557853 5.871800 0.0005 1.00 0.0005065 0.987263121 273 155 118 0.118 14868 0.00017 2502.6 0 0.531889 5.541500 0.00042 1.00 0.0005065 0.822719268 255 172 83 0.083 10458 0.00017 2085.5 0 0.528603 4.651300 0.00036 1.00 0.0005065 0.713023365 246 182 64 0.064 8064 0.00017 1807.5 0 0.521923 4.081000 0.00028 1.00 0.0005065 0.548479512 235 195 40 0.04 5040 0.00017 1390.4 0 0.50825 3.22

700 0.00019 1.00 0.0005065 0.383935658 228 198 30 0.03 3780 0.00017 973.25 0 0.412893 2.78

2500 0.00069 1.00 0.0005065 1.371198779 319 110 209 0.209 26334 0.000111 3475.9 0 0.845831 7.392200 0.00061 1.00 0.0005065 1.206654926 296 132 164 0.164 20664 0.000111 3058.8 0 0.840458 6.542000 0.00056 1.00 0.0005065 1.096959023 285 142 143 0.143 18018 0.000111 2780.7 0 0.818961 6.11800 0.0005 1.00 0.0005065 0.987263121 275 153 122 0.122 15372 0.000111 2502.6 0 0.798636 5.631500 0.00042 1.00 0.0005065 0.822719268 256 170 86 0.086 10836 0.000111 2085.5 0 0.792862 4.731300 0.00036 1.00 0.0005065 0.713023365 250 179 71 0.071 8946 0.000111 1807.5 0 0.757292 4.291000 0.00028 1.00 0.0005065 0.548479512 242 188 54 0.054 6804 0.000111 1390.4 0 0.670021 3.73

700 0.00019 1.00 0.0005065 0.383935658 228 198 30 0.03 3780 0.000111 973.25 0 0.630054 2.78

2500 0.00069 1.00 0.0005065 1.371198779 300 125 175 0.175 22050 0.000135 3475.9 0 0.760221 6.782200 0.00061 1.00 0.0005065 1.206654926 285 147 138 0.138 17388 0.000135 3058.8 0 0.753636 6.022000 0.00056 1.00 0.0005065 1.096959023 274 154 120 0.12 15120 0.000135 2780.7 0 0.735446 5.611800 0.0005 1.00 0.0005065 0.987263121 269 160 109 0.109 13734 0.000135 2502.6 0 0.695941 5.331500 0.00042 1.00 0.0005065 0.822719268 253 175 78 0.078 9828 0.000135 2085.5 0 0.685926 4.511300 0.00036 1.00 0.0005065 0.713023365 246 180 66 0.066 8316 0.000135 1807.5 0 0.647468 4.141000 0.00028 1.00 0.0005065 0.548479512 236 192 44 0.044 5544 0.000135 1390.4 0 0.611006 3.37

700 0.00019 1.00 0.0005065 0.383935658 228 200 28 0.028 3528 0.000135 973.25 0 0.537792 2.68

15-1

6 fo

r ven

turi

met

er13

-14

for n

ozzl

eCd

for o

rific

emet

er

500 1000 1500 2000 2500 3000 3500 40000

0.1

0.2

0.3

0.4

0.5

0.6

0.7

0.8

0.9

cd for orifemeterCd for venturimeterCd for nozzle

Reynold number Re

Cd C

oeffe

cient

of d

ischa

rge

Results and Comments:

There are prominent changes in the results of the graphs from theoretical graph trends, these may be due to1) Ill calibration of the apparatus 2) Air and vent contents in pipe and manometer3) Roughness of the inner surface of pipes4) Calculations5) Due to random error6) Error in taking readings of head loss 7) Due to opening of undesired valves instead of desired ones.

Due to minor head losses, k values are closely related to each others.