Pipe Heat Loss - Imp (Rev 9)

WORLEYPARSONS CANADA EDMONTON DIVISION

Page 1

PIPEHLOSPIPING HEAT LOSS CALCULATION - IMPERIAL UNITS

WARNINGSpreadsheet Owner: Bob Chomyc Click "Set Recalculation" button

on Pipe Heat Loss worksheet

CAUTION before using.

PRIOR TO USING THIS PROGRAM, PLEASE MAKE SURE THAT YOU UNDERSTAND HOW IT WORKS, THAT YOU HAVE READ THE "BASIS", "INSTRUCTIONS" & "NOTES" WORKSHEETS AND THAT YOU HAVE A WORKING KNOWLEDGE OF EXCEL

THIS IS A READ ONLY FILE. COPY IT TO YOUR OWN DIRECTORY AND RENAME IT PRIOR TO USING IT.

ALWAYS CHECK YOUR RESULTS FOR "REASONABLENESS".

IF YOU HAVE ANY QUESTIONS, COMMENTS OR SUGGESTIONS PLEASE CONTACT BOB CHOMYC @ 5357.

Revision Number Revision Date Description9 18 Nov, 2009 Add Instr. 1. Revise Instr's 7, 9, 10, 12 & 13. Insert

cell comments.

8 21 Aug, 2009 Update headers, footers, and company name.

7 11 Jan, 2008 Revised Fluid Outlet Temp Est. to allow for

heat gain from pressure loss.

6 19 Apr, 2000 Added revision number to "Pipe Heat Loss"

sheet header.

5 8 Mar., 2000 Corrected handling of pipe support spacing.

4 6 Mar., 2000 Limited friction heat gain to liquid lines only.

3 31 Jan., 2000 Corrected calculation of outlet temp. below zero

and near ambient

2 17 Jan., 2000 Revised Basis and Instructions. Added error

checking for piping data.

1B 6 Jan., 2000 Added heat from friction, condensation & pump

temperature gain. Corrected coding errors

1 19 June, 1998 Converted spreadsheet from Quattro Pro. Updated

Notes, added Instructions and Basis.


Page 2

Click "Set Recalculation" button

on Pipe Heat Loss worksheet

Converted spreadsheet from Quattro Pro. Updated

Revision 9 PIPING HEAT LOSS CALCULATIONWORLEYPARSONS CANADA

EDMONTON DIVISION

File: document.xlsPrinted on: 04/19/2023

Page 3 Design By: xxxWorleyParsons Job: xx-E-xxxx

CLIENT/PROJECT: ABC CANADA PRODUCTSDESCRIPTION: Desuperheater SupplyCASE: Existing Piping Check

LINE SEGMENT DATA:Status New NewInlet Location In InOutlet Location Out Out

FLUID STATE - gas or liquid?: liquid gasFLUID PROPERTIES @ Avg Temp:

Density lb/ft³ 60.1 0.319 Specific Heat Btu/(lb·°F) 0.96 0.60 Thermal Conductivity Btu/(h·ft·°F) 0.3930 0.0193 Viscosity cP 0.3000 0.0165 Joule-Thomson Coefficient °F/psi 0.00 0.05 Condensation Latent Heat Btu/h 0 0

PROCESS DATA:Flow Rate lb/h 81,500 3,260 Pipeline (Pump) Inlet Pressure psig 300 140 Pump Outlet Pressure psig 600 Pipeline (Pump) Inlet Temp °F 200 400 Pump Efficiency % 60%

AMBIENT CONDITIONS: #VALUE! #VALUE!Temperature °F 40.0 -25.0 Pressure psia 13.70 13.70 Wind mph 15 Ground - Cover in 36 - Conductivity Btu/(h·ft·°F) 0.80

PIPE DATA:Length ft 1000 1000 Pipe Support Spacing ft 20 Absolute Roughness in 0.0018 0.0018 Conductivity of Pipe Wall Btu/(h·ft·°F) 25.0 25.0

Nominal Size/O.D. in 3 3

Schedule/Wall Thickness Sch/in 40 40 Inside Diameter in 3.068 3.068 Outside Diameter in 3.500 3.500

INSULATION & COVERING DATA:Type Fiberglass FiberglassThickness in 1.500 1.500 I.D. in 3.500 3.500 Conductivity (override) Btu·in/(h·ft²·°F)Covering - Material Aluminum Aluminum - Emissivity 0.30 0.30

HYDRAULIC CALCULATIONS:Mass Velocity lb/(h·ft²) 1,587,521 63,501 Reynolds Number 559,289 406,756 Friction Factor 0.0181 0.0184 K Pipe 70.90 71.96 Velocity ft/s 7.34 55.30 Pressure Loss psi 24.75 7.57

THERMAL CALCULATIONS:Insul - OD in 6.50 6.50 - Average Temp °F #VALUE! #VALUE! - Conductivity Btu·in/(h·ft²·°F) #VALUE! #VALUE!Air Properties @ Film Temp °F #VALUE! (22.2) - Specific Heat Btu/(lb·°F) #VALUE! 0.24 - Conductivity Btu/(h·ft·°F) #VALUE! 0.01262 - Absolute Viscosity lb/(ft·h) #VALUE! 0.0398 - Density lb/ft³ #VALUE! 0.0845 - Natural Convection: Prandlt Number #VALUE! 0.758 Grashoff Number #VALUE! 7.02E+06 - Forced Convection: Reynolds Number #VALUE! 90958 Nusselt Number #VALUE! 238.24 Fluid Properties @ Avg Temp °F #VALUE! #VALUE! - Prandlt Number 1.781 1.241

Btu/(h·ft²·°F) 801.70 27.06 Btu/(h·ft²·°F) 0.00 5.57 Btu/(h·ft²·°F) 0.00 0.17

Surface Temp °F #VALUE! #VALUE!Overall Heat Transfer Coef Btu/(h·ft²·°F) #VALUE! #VALUE!Heat Loss Btu/(h·ft) #VALUE! #VALUE!Asymptotic Temperature °F #VALUE! #VALUE!LMTD °F 160.5 #VALUE!Pump fluid power fluid hp 49.3 Heat Gains: friction, condensation Btu/hr 6212 14327 Pipeline inlet temp (pump outlet) °F 200.6 #VALUE!

- Film Coeff, hio

Convect Loss, hc

Radiation Loss, hr

F5

Review the "Instructions" & "Notes" prior to using this program.

G5

Review the "Instructions" & "Notes" prior to using this program.

F19

Enter eff. in row 21 before entering outlet P.

G19

Enter eff. in row 21 before entering outlet P.

F21

Delete outlet P. in row 19 before deleting eff.

G21

Delete outlet P. in row 19 before deleting eff.

F25

Enter values in rows 26 & 27 before deleting values in rows 25 & 30.

G25


F26


G26


F27


G27


F30


G30


F32

Available in TEMA, GPSA or other sources.

G32

Available in TEMA, GPSA or other sources.

F38

Spelling of insul. type must be correct or program defaults to "no insulation".

G38

Spelling of insul. type must be correct or program defaults to "no insulation".

F39

Enter zero if the insul. type is "none".

G39

Enter zero if the insul. type is "none".

Revision 9 PIPING HEAT LOSS CALCULATIONWORLEYPARSONS CANADA

EDMONTON DIVISION

File: document.xlsPrinted on: 04/19/2023

Page 4 Design By: xxxWorleyParsons Job: xx-E-xxxx

Fluid Outlet Temp °F #VALUE! #VALUE!

Revision 9 PIPE HEAT LOSS CALCULATIONWORLEY PARSONS CANADA

EDMONTON DIVISION

Page 5

Mat/Sch SS-5 CS-10 CS-20 CS-30 CS-40 CS-60 CS-80 CS-100 CS-120 CS-140 CS-160 CS-Strong CS-X Stg CS-XX Stg SS-10 # 5 10 20 30 40 60 80 100 120 140 160 161 162 163 10SOffset 1 2 3 4 5 6 7 8 9 10 11 12 13 14 15

NPS O.D.0.125 0.265 0.215 0.269 0.215 0.307 0.405

0.25 0.364 0.302 0.364 0.302 0.410 0.540 0.375 0.493 0.423 0.493 0.423 0.545 0.675

0.5 0.710 0.622 0.546 0.466 0.622 0.546 0.252 0.674 0.840 0.75 0.920 0.824 0.742 0.614 0.824 0.742 0.434 0.884 1.050

1 1.185 1.049 0.957 0.815 1.049 0.957 0.599 1.097 1.315 1.25 1.380 1.278 1.160 1.380 1.278 0.896 1.442 1.660

1.5 1.770 1.610 1.500 1.338 1.610 1.500 1.100 1.682 1.900 2 2.245 2.067 1.939 1.689 2.067 1.939 1.503 2.157 2.375

2.5 2.709 2.469 2.323 2.125 2.469 2.323 1.771 2.635 2.875 3 3.334 3.068 2.900 2.624 3.068 2.900 2.300 3.260 3.500 4 4.334 4.026 3.826 3.624 3.438 4.026 3.826 3.152 4.260 4.500 6 6.407 6.065 5.761 5.501 5.189 6.065 5.761 4.897 6.357 6.625 8 8.407 8.125 8.071 7.981 7.813 7.625 7.439 7.189 7.001 6.813 7.981 7.625 6.875 8.329 8.625

10 10.482 10.250 10.136 10.020 9.750 9.564 9.314 9.064 8.750 8.500 10.020 9.750 8.750 10.420 10.750 12 12.438 12.250 12.090 11.938 11.626 11.376 11.064 10.750 10.500 10.126 12.000 11.750 10.750 12.390 12.750 14 13.500 13.376 13.250 13.124 12.814 12.500 12.126 11.814 11.500 11.188 13.250 13.000 13.624 14.000 16 15.500 15.376 15.250 15.000 14.688 14.314 13.938 13.564 13.124 12.814 15.250 15.000 15.624 16.000 18 17.500 17.376 17.124 16.876 16.500 16.126 15.688 15.250 14.876 14.438 17.250 17.000 17.624 18.000 20 19.500 19.250 19.000 18.814 18.376 17.938 17.438 17.000 16.500 16.064 19.250 19.000 19.564 20.000 24 23.500 23.250 22.876 22.626 22.064 21.564 20.938 20.375 19.876 19.314 23.250 23.000 23.500 24.000 30 29.376 29.000 28.750 29.250 29.000 29.376 30.000 36 35.376 35.000 34.750 34.500 35.250 35.000 36.000 42 41.250 41.000 42.000 48 47.250 47.000 48.000

NPS O.D.0.125 0.405

0.25 0.540 0 0.675

0.5 0.840 0.75 1.050

1 1.315 1.25 1.660

1.5 1.900 2 2.375

2.5 2.875 3 3.50 4 4.50 6 6.625 8 8.625

10 10.75 12 12.75 14 14 16 16 18 18 20 20 24 24 30 30 36 36 42 42 48 48

Revision 9PIPE HEAT LOSS CALCULATION


Page 6

BASIS

Equation References

Darcy-Weisbach Friction Factor: Chen Equationf = (1/( -2*LOG((Rough/d)/3.7065 "Alternate to Standard Friction

- 5.0452/Re*LOG((Rough/d)^1.1098/2.8257 Factor Equation"

+ (7.149/Re)^0.8981))))^2 Gregory & Fogarasi,

O&G J Apr, 1985

f = friction factor

Rough = absolute roughness (in)

d = pipe inner diameter (in)

Re = Reynolds Number

K pipeK pipe = f·L·12/d "Fundamentals of Fluid

Mechanics, 2nd Edition"

f = friction factor Gerhart, Gross & Hochstein,

L = length of pipe (ft) Addison Wesley, 1992

d = pipe inner diameter (in)

Pressure Loss - Darcy Formula"Fundamentals of Fluid


Gerhart, Gross & Hochstein,

Addison Wesley, 1992

v = velocity (ft/s)

Air Properties"Maximize your energy savings

/(4186.69 J/(kg·°C)/1 Btu/(lb·°F)) with proper insulation size"

Cp = heat capacity (Btu/(lb·°F)) Barry A Sloane, Hydrocarbon

Procession, October 1992

"Spreadsheets For Heat Loss

Rates and Temperatures"

k = thermal conductivity (Btu/h·ft·°F) Butch Bront, Chemical

Engineering, December 1995

"Maximize Your Energy Savings

with Proper Insulation Size"

Hydrocarbon Processing

October, 1992

= di·mass vel/viscosity/2.419

Ploss = (K pipe·r·v²)/2*(1 lbf/32.174 (lb·ft/s²))*(1 ft/12")²

Ploss = Friction pressure loss (psi)

r = density (lb/ft³)

Cp = (0.0004132·Tfilm² - 0.2049·Tfilm + 1030.14)

Tfilm = temperature (K)

k = 0.0099 +1.71E-5·Tfilm - 2189/Tfilm² + 5.58E6/Tfilm³

Tfilm = air film temperature (°R)

m = (-1.312 x 10-8·Tfilm2+4.935 x 10-5·Tfilm + 0.005256)·2.419

m = Absolute viscosity (cP)

Tfilm = Air film temperature (K) 200K < Tfilm < 1,000 K



Page 7

Ideal Gas Law

M = molecular mass of air

R = ideal gas law constant (10.73 ft³ psia/(lb-mole °R)

T = air temperature (°R)

Grashoff Number (Air)"Introduction to Heat

Transfer"

Gr = Grashof Number (unitless) F. Incropera, D. De Witt,

Wiley, 1990

Nussult Number (Air Forced Convection)"Perry's Chemical

Engineering Handbook"

7th Edition.

Re m Eqn 5-44

40 - 4000 0.683 0.466

4000 - 40000 0.193 0.618

>40000 0.0266 0.805

Nussult Number (Air Natural Convection)"Heat Transfer - A Basic

Approach"

Gr = Grashoff number for the air around the pipe M. Necati Ozisik, McGraw Hill,

Pr = Prandlt number for the air around the pipe 1985

Gr·Pr c n

0.480 0.250

0.125 0.333

Convective Heat Transfer Coefficient (Air)"Maximize your energy savings

with proper insulation size"

Barry A Sloane, Hydrocarbon

k = air conductivity (Btu/h·ft·°F) Processing, October 1992

d = pipe diameter (in)

r = P·M/(R·T)


Gr = (do/12)³·r³·g·(Tsurf - Tamb)/(Tamb·m²)

do = outer diameter of pipe (in)

r = density of air (lb/ft³)

Tsurf = surface temperature (°R)

Tfilm = air film temperature (°R)

m = absolute viscosity (lb/(h·ft))

Nuforced = Cr·Rem·Pr1/3

Re = mph·5280·do/12/viscosity·density

Cr

Nufree = c·(Gr·Pr)n

104 - 107

107 - 1012

hc = (Nufree² + Nuforced²)1/2·k/(d/12)

hc = convective coefficient Btu/(h·ft²·°F)



Page 8

Radiative Heat Transfer Coefficient"Introduction to Heat

Transfer"

F. Incropera, D. De Witt,

Wiley, 1990

"Heat Transfer - A Basic

Approach"

M. Necati Ozisik, McGraw Hill,

Re = Reynolds number for the fluid in the pipe 1985

Pr = Prandlt number for the fluid in the pipe

k = thermal conductivity for the fluid inside of the pipe (Btu/(h·ft·°F)

d = inner diameter of the pipe (in)

Overall Heat Transfer Coefficient

Asymptotic Temperature (Gas Pipelines)"Equation Predicts Buried

Pipeline Temperatures"

Graeme G. King

O&GJ, March 16, 1981

J = Joule-Thompson Coefficient (°F/psi)

aL = aL factor (see below)

D = pipe outer diameter (ft)

L = length of pipe (ft)

m = mass flow rate (lb/h)

hrad = e·s·(Ts+Tamb)·(Ts²+Tamb²)

hrad = radiation loss

e = emissivity of the surface (Btu/(h·ft²·°F))

s = Stefan-Boltzmann constant (0.1714 x 10-8 Btu/(h·ft2·°R4)

Tsurf = Surface Temperature (°R)

Tamb = Ambient Temperature (°R)

Inside Film Coefficient (hio): Colburn Equationhio = 0.023·Re0.8·Pr1/3·k/(d/12)

hio = inside film coefficient (Btu/(h·ft²·°F))

Uoverall = 1/(1/hio +Rpipe + Rinsulation + Rsoil + Rsurface)

Uoverall = overall heat transfer coefficient (Btu/(h·ft²·°F))

hio see above

Ppipe, Rinsulation, Rsoil, Rsurface see below

Ta = Tamb - (J·Dp + Dy/(j·Cp))/aL

Ta = asymptotic temperature (see below) (°F)

Tamb = ambient temperature (°F)

Dp = pressure loss (psi)

Dy = change in elevation (because change of altitude

has not been worked into this spreadsheet, Dy=0)

j = Joule's Constant = 778 ft·lbf/Btu

Cp = specific heat capacity (Btu/(lb·°F))

aL = p·D·Uoverall·L·(1+Ps·6/100)/(m·Cp)


Ps = pipe supports per 100 ft



Page 9

Pipeline Booster Pump Power


E = pump efficiency (%)

Pipeline Inlet Temperature (Liquids)

Pump Power (see above) (hp)

E = efficiency (%)


Cp = Specific Heat (Btu/(lb·°F))

Surface Temperature

Log Mean Temperature Difference"Perry's Chemical

Engineering Handbook"

7th Edition.

Eqn 11-5a

Outlet Temperature from Energy Balance


condensation latent heat (Btu/h)

Pump Power = (Pout-Pin)·m·24/5.61/(r·E) (hp)

Pout = Pump outlet pressure (psig)

Pin = Pump inlet pressure (psig)

r = density (lb/ft3)

Tin = Tpump·inlet+2544.4·Pump Power·(1-E)/m/Cp (°F)

Tpump = Pump Inlet Temperature (°F)

Given that Q = Uoverall·A·DToverall and that Q = hsurface·A·DTsurface

then Tsurface = Uoverall·(Tmean - Tamb)/h + Tamb


Tmean = log mean temperature of fluid in pipe (°F)

Tamb = Ambient Temperature (°F)

hsurface = heat transfer coefficient at the surface, hrad + hc (Btu/(h·ft²·°F))

LMTD = ((Tin - Ta) - (Tout - Ta))/LN((Tin - Ta)/(Tout - Ta))

Tin = inlet temperature (°F)

Tout = outlet temperature (°F)

Ta = asymptotic temperature (see above) (°F)

m·Cp·(Tin-Tout) + friction heat + condensation latent heat = Uoverall·pi·d/12·LMTD·L·(1+Ps·6/100)

friction heat = m· Ploss·144/(r·778)

Ploss = Friction pressure loss (psi)

mechanical equivalent of heat = 778 ft·lbf/Btu




Page 10

Soil Resistance"Equation predicts buried

pipeline temperatures"

Graeme G. King

k = conductivity of the soil (Btu/(h·ft·°F)) O&G J, 16 Mar., 1981

h = depth of burial to pipe centerline (in)

Insulation Resistance"Incorporating rigorous heat

balance prevents overdesign

of gas pipelines"

Oil & Gas Journal,

k = insulation thermal conductivity (Btu·in/(h·ft²·°F)) 17 Sept., 1984

Pipe Resistance

k = pipe thermal conductivity (Btu/(h·ft²·°F))

Rsoil = do/(24·k·cosh-1(2h/D))

do = outer diameter of the pipe & insulation (in)

Rinsulation = do/2/k·ln(do/di)

do = insulation outside diameter (in)

di = insulation inside diameter (in)

Rpipe = do/24/k·ln(dpo/dpi)

do = insulation outside diameter (in)

dpo = pipe outside diameter (in)

dpi = pipe inside diameter (in)



Page 11

"Alternate to Standard Friction





"Maximize your energy savings



Procession, October 1992

"Spreadsheets For Heat Loss

Rates and Temperatures"

Engineering, December 1995

"Maximize Your Energy Savings

with Proper Insulation Size"



Page 12


"Maximize your energy savings



Processing, October 1992



Page 13


"Equation Predicts Buried

Pipeline Temperatures"



Page 14

"Incorporating rigorous heat

balance prevents overdesign

Revision 9 PIPE HEAT LOSS CALCULATIONWORLEYPARSONS CANADA

EDMONTON DIVISION

Page 15

INSTRUCTIONS1 This spreadsheet calculation is the property of WorleyParsons Edmonton. Do not send working

(Excel) copies to any third parties. In addition, do not send copies of the Basis, Instructions or

Notes sheets to any third parties. Hard copies or PDF copies of the results page(s) can be included

in calculation packages or sent to third parties.

2 This spreadsheet requires the Iteration option to be selected to solve the circular references and

the Automatic Recalculation option to be selected so that the sheet will adjust automatically when

input values are changed. To do this choose click the "Set Recalculation" button on the Pipe Heat

3 Save this worksheet often! Entering physically impossible input values can cause #ERROR type

messages in the formula cells of the corresponding column. The only recovery is to close the

4 The heat loss basis is for pipe temperatures above ambient and has not been verified for pipe

temperatures below ambient.

5 the protection is on. These cells should not normally be changed and the protection should be

left on.

6 Enter the fluid type "gas" or "liquid" in row 8. Enter the fluid properties for the average temperature

and pressure of the fluid. Enter the Joule-Thomson Coefficient if desired. If not or if the Fluid

Type is a liquid, enter 0 or blank.

7 Enter the pipeline inlet pressure in row 18 and the inlet temperature in row 20. If the pipeline

contains liquid and there is a pump upstream of the pipeline, enter the Pump Efficiency in row 21

The spreadsheet will calculate the pump outlet temperature. If there is no pump, the Pump

Outlet Pressure and Pump Efficiency should be left blank (delete the Pump Outlet Pressure

8 The designer's initials and WorleyParsons job number are entered in the footer. These must be updated

File Name, Page Number and "Printed on" date are also printed in the Footer. This applies to the

"Piping Heat Loss" worksheet only.

9 Each column in the spreadsheet represents an entire pipe length or a segment of pipe and can be

only one diameter. Columns can be added or deleted as desired. Use Copy & Paste from

Rows 5 to 92 (there is a warning message formula in Row 92). DO NOT move columns or

relative cell references to other columns will not increment appropriately.

10 Rows 25, 26, 27and 30 pertain to the pipe being above ground or underground. To switch from

Row 27 (Conductivity), otherwise a "#DIV/0!" error will appear and worksheet will need to be closed

Loss worksheet, which will make the necessary selections in Tools, Options, Calculations.

worksheet without saving and reopening the file. See Iinstruction 10.

Bold blue text and values indicate user input. Black text and values/formulas are locked when

and the Pump Outlet Pressure in row 19 (enter the Pump Efficiency first to avoid a "#DIV/0!" error).

before deleting the Efficiency, to avoid a "#DIV/0!" error).

for each new job. Use File, Page Setup, Header/Footer, Custom Footer to edit the Footer. The

underground to above ground in a particular column, values must be entered in both Row 25 (Wind)

and Row 30 (Pipe Support Spacing) before deleting the values from Row 26 (Ground - Cover) and

without saving to recover. To switch from above ground to underground, values must be entered in

both Rows 26 and 27 before deleting the values from Rows 25 and 30. Delete the values that are not


EDMONTON DIVISION

Page 16

required (rather than entering zero's). The presence of a number in either Row 25 or 26 changes the

formulas used in the calculations and will cause erroneous results if the cell should be empty instead.


EDMONTON DIVISION

Page 17

11 steel entries are: 10, 20, 30, 40, 60, 80, 100, 120, 160, STD, XH and XXH. Two acceptable

schedules which pertain only to stainless steels are: 5 and 10S. See the PipeData worksheet to

find the pipe diameters these schedules apply to. Entering Pipe Size and Schedule entries not in "PipeData" will result in zero or #error in line 23.Special inside diameters, i.e. for tubing or pipeline pipe, can be achived by doing the following:

If the entry in Row 34 is less than 1", the Row 35 cell subtracts 2*(Row 34) from Row 33 to give

the inside diameter of the tubing.

12 For Insulation Type enter one of the following: "Fiberglass", "Foamglass", "CalSilicate", "Mineralwool",

"Polyurethane" or "none". The insulation types are not "case sensitive", however if they are misspelled

in any way, the program defaults to using no insulation (i.e., equivalent to entering "none"). If the

insulation type is "none", the thickness should be entered as 0 inches, otherwise the calculation of

the outer surface diameter of the line (Row 52) will be incorrect and the calculated heat loss will be

higher. If the insulation doesn't fall under one of the above catagories, or if you wish to enter your

own insulation conductivity (different from the values calculated by the formulas in the spreadsheet),

enter the insulation conductivity value into the "Conductivity (override)" cell (Row 41) in units of

13 Insulation "Covering-Material" in Row 42 is for information only, however the Emissivity of the covering

(or outer pipe surface) in Row 43 is used in the calculations and a value must be entered for above

ground piping. See Notes for a table of values.

14 Pressure loss is calculated by Darcy formula. Gas pressure losses larger than 10% of inlet

pressure will not be accurate. Divide line into segments to reduce segment pressure loss

to less than 10%.

15 been added past column J in the "Piping Heat Loss" worksheet, the print area will have to be

changed.

16 The convergence on the outlet temperature may need to be adjusted. If the sheet is taking a

large number of iterations to arrive at the answer, put a larger number in row 91. If the sheet is

not converging, put a smaller number in row 91.

Enter the Pipe Nominal Size (inches) in row 33 and the Schedule in row 34. Acceptable carbon

a. Enter the tubing or pipe Outside Diameter (inches) in Row 33.

b. Enter the tubing or pipe wall thickness (inches) in Row 34.

(Btu·in)/(h·ft²·°F). This overrides the conductivity calculation within the spreadsheet.

To Print a worksheet, highlight the worksheet tab and press the Printer Icon. If columns have


EDMONTON DIVISION

Page 18


EDMONTON DIVISION

Page 19

Entering Pipe Size and Schedule entries not in "PipeData" will result in zero or #error in line 23.

Revision 9 PIPE HEAT LOSS NOTESWORLEY PARSONS CANADA

EDMONTON DIVISION

Page 20

NOTES1 Ground Conductivities

The following are some ground type conductivities. (SOURCE: HYSYS Engineering, pg 329)

Ground type Thermal Conductivity Ground type Thermal Conductivity

k (Btu/(h·ft·°R) k (Btu/(h·ft·°R)

Dry Peat 0.098 Frozen Clay 1.445

Wet Peat 0.312 Gravel 0.636

Icy Peat 1.092 Sandy Gravel 1.445

Dry Sand 0.289 LimeStone 0.751

Moist Sand 0.549 SandStone 1.127

Wet Sand 1.271 Ice 1.271

Dry Clay 0.277 Cold Ice 1.537

Moist Clay 0.433 Loose Snow 0.087

Wet Clay 0.809 Hard Snow 0.462

2 Absolute Roughness

The absolute roughness of commercial carbon steel pipe is 0.0018 in. Roughness values for

other pipe materials can be found in Crane Technical Paper and Cameron Hydraulics Handbook.

3 Insulation Thermal Conductivities

The following are typical insulation type thermal conductivities. (SOURCE: ESSO Resources Basic Practice

EBP 14-1-1, p. 1, June 1988)

Material Type / Name

Mineral wool

Calcium Silicate

Fiberglass

Foamglass

Polyurethane

Note: The equation for the polyurethane was derived from data between -100°F and 100°F. It may

not yield accurate results outside of that temperature range. Temperature ranges for the other

materials in this table are not known as they were not given in the ESSO Basic Practice.

4 Emissivity

The following are some typical emissivity values. (SOURCE: Perry's Chemical Engineering Handbook,

7th edition, pg 5-28, 5-29 and Chemical Engineering article, 27 July, 1981)

Material Surface

Oil paints, sixteen different, all colors 0.92 - 0.96

Aluminum paints, varying age & Al content 0.27 - 0.67

Black shiny lacquer 0.875

Flat black Lacquer 0.96

Aluminum, shiny jacketing 0.09

Aluminum with oil layer 0.56

Steel sheet, oxidized 0.66 - 0.80

Stainless Steel 0.16-0.39

Dull brass, copper or aluminum; galvanized steel; polished iron 0.20 - 0.30

Polished Brass 0.096

Canvas, oil painted or covered with thick dust 0.9

kdes at Mean Temperature, Tm; (Btu·in/(h·ft2·°F))

kdes = 0.00050 Tm + 0.360

kdes = 0.00043 Tm + 0.315

kdes = 0.00050 Tm + 0.210

kdes = 0.00080 Tm + 0.370

kdes = 3.9 x 10-8 Tm³ - 1.8 x 10-6 Tm² - 2.5 x 10-4 Tm + 0.18

Surface Emissivity, e

Documents

Pipe Heat Loss - Imp (Rev 9)