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UNITS

Select the appropriate units for each parameter.

This worksheet must be filled before the PumpCalcs sheet and LineLoss sheet.

Changing the units after data has been entered will lead to conversion failures.

Parameter Units for project

Temperature #NAME?

Pressure #NAME?

Density

Viscosity #NAME?

Roughness #NAME?

Length/Level/Head #NAME?

Mass Flow #NAME?

Flow #NAME?Velocity #NAME?

Dynamic Pressure Loss #NAME?

Power #NAME?

Modifications to the master spreadsheet

Date By Description

2003-01-10 MRL

2003-01-14 MRL

2003-01-20 MRL2003-02-13 MRL

2003-03-10 MRL

2004-10-21 MRL

2005-11-10 MRL

2007-03-19 AT

6/9/2009 CB Add a check list worksheet, add Control Valve calculations and min flow control valve

Unit Conversion Table

Units Index Temperature 2 Pressure 2 Density 6 Viscosity 3

Allowed values Conversion factor C 1 Pa 1 kg/m3 1 kg/m s 1

Base unit is first line Multiply secondary unit by F 0.555555556 psi 6894.8 g/cm3 1000 cP 0.001

Secondary units are next factor to obtain base unit K 1 kPa 1000 ton/m3 1000 lb/ft s 1.488164

R 0.555555556 kg/cm2 98064.74 lb/USG 119.8264 Poise 0.1

#N/A bar 100000 lb/IG 99.77633 g/cm s 0.1

#N/A #N/A lb/ft3 16.018 Pa-s 1

#N/A #N/A #N/A #N/A

#N/A #N/A #N/A #N/A

#N/A #N/A #N/A #N/A

#N/A #N/A #N/A #N/A

#N/A #N/A #N/A #N/A

#N/A #N/A #N/A #N/A

The Index refers to the proper line in the range and is named UnitIndex

The Names refer to the allowed names and are named UnitNames. The selected name is found on the UnitIndex line of the range.

The Conversion factors are named UnitConv. The proper factor is found on the UnitIndex line of the range.

Major rewrite; change of sg to density; correction in conversions of head to pressure and vice-versa; also correction in calculation of K

values

Corrected display of base unit for viscosity in LineLoss; added complete reference for K value calculations

Added two additional segments at the pump discharge for line loss calculationsCalculation of shut-off pressure corrected so no calculation take place unless a value is entered for the shut-off head

Corrected the formula in E33, correction to use minimum flow to pro-rate DP

Corrected the inside diameter for HDPE pipes ("DR" schedule) for nominal diameter 4 to 12" inclusively

Corrected the "Safety factor for slurry" in LineLoss sheet, should be calculated only on pipe friction loss. Added a "Safety factor for

fittings". Added notes to explain the difference in usage between the two factors. Changed the logic in the Slurry worksheet to minimize

the risk of inconsistencies between PumpCalcs, LineLoss and Slurry. Also added dimensionnal data for HDPE pipe as per ANSI/AWWA

C906 ("DR" schedules)

Added contraction, ennlargement and reducing tees to line loss calculation

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Client Contr. No Rev. Date By Chkd App.

Project #######

PROCESS DATA SHEET

CENTRIFUGAL PUMP DESIGN CALCULATIONS

Calculation No.

ITEM NUMBER

TITLE

FIRE WATER PUMP

OBJECTIVE

METHOD

REFERENCES

DESIGN CONDITIONS CONFIRMATION

REQUIRED

Flow as per data sheet Flow as per mass balance table ITEM YES NO

ft3/h ft3/h

Max

Nor

Data sheet Calculated

Discharge Pressure - rated 257.2 psi (g)

Suction Pressure 0.8 psi (g)

NPSH Available 1.3 ft

MAX Suction Pressure 16.2 psi (g)

CONCLUSIONS CONFIRMATION

Data sheet Calculated REQUIRED

ITEM YES NO

Pump Differential Pressure 256.39 psi

Hydraulic Power 920.09 kW

Brake Power 0.0 kW

\\vboxsrv\conversion_tmp\scratch_2\[255601832.xls.ms_office.xls]Design Notes

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Client 0 Contr. No 0

Project 0

PROCESS DATA SHEET

Calculation No.

ITEM NAMEITEM NUMBER

PUMP TYPE

PFD NO.

P&ID NO.

Yes NoNot

A licable

0

FIRE WATER PUMP0

0

0

0

CHECK LIST

All the reference document should be attached to the excel calculation in PDF.

Once the calculation is done, print the calculation in order to sign it and make it verify and sign by another engineer.

Scan the signed copy and put in the binder and the directory (T:\proj\... ...\4900_Process\49EB Calculation&desig

There should only be one excel calculation in the directory, the last one.

For detailed engineering calculation should be in rev 00

Items

Cover page

Source of stream data

Destination pressure

Criteria and conception margin

Pipe sizing criteria

PFD and Mass Balance

Pump curve

Pump datasheet

P&ID

Isometrics(suction and discharge line)

Suction vessel Datasheet / drawing

Discharge vessel datasheet / Drawing

Heat exchanger, mixer datasheet (for pressure losses)

Comments :

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Signature

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Rev. Date

0 10/18/2013

n brief\).

Comments/Actions

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Client 0 Contr. No 0 Rev. Date

Project 0 0 10/18/2013

PROCESS DATA SHEETCENTRIFUGAL PUMP DESIGN CALCULATIONS

Calculation No.

ITEM NAME

ITEM NUMBER

PUMP TYPE

PFD NO.

P&ID NO.

REV. NO. DESIGN NOTES

PA

0

FIRE WATER PUMP

0

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PROCESS DATA SHEET

PUMP DESIGN CALCULATIONS

Calculation No.

ITEM NAME ATMOSPHERIC PRESSURE psi (a) 14.7

ITEM NO.

PFD NO. MINIMUM NORMAL RATED

P&ID NO. Flowrate ft3/h 0.0 44114.0 66171.0

Fluid Name D) FIXED PRESSURE (DISCHARGE)

NORMAL Discharge Vessel Pressure (Note 4) psi (g) 35.0 50.0 65.0

Pumping Temperature (PT) F 60 Liquid Level (Ref. to grade) (Note 4) ft 40.0 40.0 40.0

Vapour Pressure at PT psi (a) 14.09 Static Head (Ref. to Pump C/L) ft 37.5 37.5 37.5

Density at PT lb/ft3 62.2 Static Pressure psi 16.2 16.2 16.2

Viscosity at PT lb/ft s 0.000672 Total Disch. Fixed Pressure psi (g) 51.2 66.2 81.2

Solids Contents wt% 0%

E) VARIABLE LOSSES (DISCHARGE)

Line Losses Before Control Valve psi 0.0 68.9 155.0

MINIMUM NORMAL RATED Equipment Losses Before Control Valve (Note 1)

Pump Capacity at PT ft3/h 44114 66171.00 (A) Exchangers psi 0.0 0.0 0.0

% Overdesign 50% (B) Orifice psi 0.0 0.0 0.0

(C) Mixer psi 0.0 0.0 0.0

A) FIXED PRESSURE (SUCTION) (D) Miscellaneous psi 0.0 0.0 0.0

Suction Vessel Pressure (Note 3) psi (g) 0.0 0.0 0.0 Control Valve Pressure Drop psi 0.0 0.0 0.0

Liquid Level (Ref. To Grade) (Note 3) ft 40.0 10.0 10.0 Equipment Losses After Control Valve (Note 1)

Pump Centerline Elevation (Ref. To Grade ft 2.50 Line Losses After Control Valve psi 0.0 9.3 21.0

Static Head (Ref. To Pump C/L) ft 37.5 7.5 7.5 (A) Exchangers psi 0.0 0.0 0.0

Static Pressure psi 16.2 3.2 3.2 (B) Orifice psi 0.0 0.0 0.0

Total Suction Fixed Pressure psi (g) 16.2 3.2 3.2 (C) Mixer psi 0.0 0.0 0.0

(D) Miscellaneous psi 0.0 0.0 0.0

B) VARIABLE LOSSES (SUCTION) Total Disch. Var. Losses psi 0.0 78.2 176.0

Line Losses psi 0.0 0.6 1.3

Equipment Losses (Notes 1) psi 0.0 0.5 1.1 F) DIFFERENTIAL PRESSURE AND TDH

Miscellaneous Losses (Note 1) psi 0.0 0.0 0.0 Discharge Pressure from typical pump curve psi (g) 51.2 144.4 257.2

Total Suction Losses psi 0.0 1.1 2.4 Discharge Pressure from vendor psi (g) 257.2

Pump Suction Pressure psi (g) 16.2 2.2 0.8 Suction Pressure psi (g) 16.2 2.2 0.8

Overplus psi

Differential Pressure psi 35.0 142.3 256.4

C) NPSHA Total Dynamic Head ft 81.0 329.3 593.4

Pump Suction Pressure psi (a) 15.5

Vapour Pressure psi (a) 14.1 G) SHUT-OFF PRESSURE

Net Press. Over Vapour Press. psi (a) 1.4 Max Suction Pressure psi (g) 0.0

NPSH (Calculated) ft 3.3 Max Suction Liquid Level (Ref. to Grade) ft 40.0Safety Margin ft 2.0 Static Head (Ref. to Pump C/L) psi (g) 16.2

NPSHA ft 1.3 Max Suction Pressure psi (g) 16.2

NPSHR (Note 6) ft Shut-Off Head from typical pump Curve psi (g) 308.4

Shut-Off Head from Vendor psi (g)

Shut-Off Pressure psi (g) 324.6

NOTES H) POWER

Hydraulic Power kW 920.1

Estimate Efficiency % 88861199

Efficiency from vendor %

Brake Power kW 0.0

I) CONTROL VALVE SPECIFICATION

Ratio of Control Valve dP/Line Loss dP 0.00

Ratio of Control Valve dP/Total Disch. Var. Loss 0.00

Static Head (Ref. to pump CenterLine) ft NA NA 1.0

Static Pressure psi NA NA NA

Pressure Upstream Valve P1 psi (g) NA NA NA

Pressure Dowstream Valve P2 psi (g) NA NA NA

Control Valve CV NA NA NA

Rangeability (CV Max/CV Min) NA

SPECIAL NOTES :

2. Conditions for normal flow are based on normal operating pump head,

calculated from from rated flow and head and pump shutoff head

3. Use minimum for Rated case and maximum for Minimum case. Normal

case is as seems appropriate.

4. Use maximum for Rated case and minimum for Minimum case. Normal

case is as seems appropriate.

5. For no control valve or variable speed pump, write 0 for control valve

pressure drop at rated flow. Pump Head will be calculated automatically as

required.

0

0

FIRE WATER PUMP

0

0

1. Equipment allowable pressure drops are entered under the normal

columns and then the rated pressure drops are calculated based on the ratio

of the square of the flows.

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PROCESS DATA SHEET

PUMP DESIGN CALCULATIONS

Calculation No. 0

Item Name FIRE WATER PUMP Item No.

RATED FLOW HYDRAULIC CALCULATIONS - SUCTION AND DISCHARGE

Piping Section SUCTION

Segment 1 2 1 2 3 4 5 6

Line No.

P&ID Number

Nominal Pipe Size in 15 8 13 11 11 11 10 10

Pipe Schedule 5 7 5 5 5 5 5 5

Pipe ID in 18.812 5.761 15 11.938 11.938 11.938 10.02 10.02

Roughness in 0.0457 0.0457 0.0457 0.0457 0.0457 0.0457 0.0457 0.0457

Pipe ID mm 478 146 381 303 303 303 255 255

Pipe X-Sectional Area m 0.179 0.017 0.114 0.072 0.072 0.072 0.051 0.051

Roughness mm 1.1608 1.1608 1.1608 1.1608 1.1608 1.1608 1.1608 1.1608Pipe Length ft 30 3000 200 400 475 200 200

Flow Factor 1.0 0.0 1.0 0.5570 0.4120 0.0234 0.2 0.2

Flow Rate ft3/h 66171.0 0.0 66171.0 36857.2 27262.5 1548.4 13664.3 13664.3

FITTINGS Qty Qty Qty Qty Qty Qty Qty Qty

90 Elbow - Std. (R/D=1), Screwed

90 Elbow - Std. (R/D=1), Flanged/Welded 4.0 5.0

90 Elbow - LR. (R/D=1.5), All

Mitred Elbow, 1 Weld (90 Angle)

Mitred Elbow, 2 Welds (45 Angle)


Mitred Elbow, 4 Welds (22.5 Angle)


45 Elbow - Std. (R/D=1), All 2.0

45 Elbow, L-R (R/D=1.5), All




180 Elbow - Std. (R/D=1), Flanged/Welded


Tee - Used as Elbow, Std., Screwed

Tee - Used as Elbow, L-R, Screwed

Tee - Used as Elbow, Std., Flanged/Welded 2.0 4.0 3.0 3.0 3.0 6.0 6.0

Tee - Used as Elbow, Stub-in Type

Tee - Run-Though, Std., Screwed

Tee - Run-through, Std., Flanged/Welded

Tee - Run-through, Stub-in Type

Gate/Ball/Plug, Full Line Size, Beta=1.0Gate/Ball/Plug, Reduced Trim, Beta=0.9

Gate/Ball/Plug, Reduced Trim, Beta=0.8

Globe Valve, Std.

Globe Valve, Angle or Y-type

Diaphragm Valve, dam type

Butterfly Valve 1.0 6.0 3.0 3.0 3.0 6.0 6.0

Check Valve - Lift type

Check Valve - Swing type

Check Valve - Tilting Disk type

Pipe Entrance (i.e. Vessel Outlet) 1.0 6.0 1.0 1.0 1.0 1.0 1.0

Pipe Exit (i.e. Vessel Inlet) 1.0 6.0 1.0 1.0 2.0 6.0 6.0

Custom fitting, enter K value associated with pipe size

Reducing tee, flanged or buttweld, through run 30 1.0 25 22 20 22 19 19

Number of items above 1 1 2 2 6 6 6


Number of items above 1 1 1 1


Number of items above 3

Reducing tee, flanged or buttweld, as elbow 1 1.0 1 1 1 1 1 1

Number of items above

Reducer (K1=small dia, K2=large dia) 1 1.0 1 1 1 1 1 1


Enlargement (K1=small dia, K2=large dia) 1 1.0 1 1 1 1 1 1


Safety Factor for Slurry (see notes) %

Safety Factor for Fittings (see notes)%

Total K1 for all fittings except entrances and exits 0.00 #DIV/0! 0.01 0.00 0.00 0.07 0.01 0.01

Total Kinf for all fittings except entrances and exits 3.21 0.00 8.40 3.82 4.30 4.23 7.46 7.46

Total K value for fittings incl entrances and exits 4.71 #DIV/0! 17.40 5.32 5.81 6.80 13.97 13.97

Fittings Equivalent Length w/o S.F. ft 100.00 #DIV/0! 826.32 188.40 205.31 228.82 393.25 393.25

Fittings Equiv. Length with S.F. ft 100.00 #DIV/0! 826.32 188.40 205.31 228.82 393.25 393.25

Pipe Length with S.F. ft 30.00 #N/A 3000.00 200.00 400.00 475.00 200.00 200.00

Total Equivalent Length with S.F. ft 130.00 #DIV/0! 3826.32 388.40 605.31 703.82 593.25 593.25

Minimum Equivalent Piping Length ft 130.00 3825.00 380.00 600.00 710.00 580.00 580.00

Velocity at rated flow (user units) ft/s 9.52 0.00 14.98 13.17 9.74 0.55 6.93 6.93

Density (base units) kg/m3 996.32 996.32 996.32 996.32 996.32 996.32 996.32 996.32

Viscosity (base units) lb/ft s 0.0007 0.00 0.000672 0.00 0.00 0.00 0.00 0.00

Dynamic Pressure Loss psi/100 ft 0.96 #DIV/0! 3 3 2 0 1 1

Total Dynamic Loss (w/o S.F) psi 1.2 #DIV/0! 121 13 11 0 7 7

Specified Pressure Drop psi 1.3 125.0 16.0 14.0 1.0 10.0 10.0Total Line Loss (w/ S.F.) psi 1.3000 #DIV/0! 125.0 16.0 14.0 1.0 10.0 10.0

Total Delta P (w/ S.F.) psi

Velocity at normal flow ft/s 6.35 0.00 9.99 8.78 6.50 0.37 4.62 4.62

Velocity at minimim flow ft/s #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A

NOTES:

The "Safety factor for Slurry" is used to account for the fact that the friction loss in the pipe for a slurry is greater than for a newtonian fluid.

This safety factor is not applied on fittings. See Turian 1983 for details. The factor is calculated using the Slurry worksheet.

The "Safety factor for fittings" is used to add provision for the fitting losses when the exact number of fittings is unknown, typically early in engineering.

This factor is given as a percentage of the pipe length. This additional loss is added to any calculated loss for fittings that might be entered in

the worksheet. As engineering progress and the number of fittings is better defined, this number should be decreased to 0.

The "Minimum equivalent piping length" will override the calculated value "Total equivalent length" if the latter is smaller than the former.

The "Specified pressure drop" is used to impose a pressure drop for a pipe segment. This pressure drop override all other calculated values.

1.300

0

DISCHARGE BEFORE CONTROL VALVE DISCHARGE BEFORE CONTROL VALVE

155.000 21.000

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PROCESS DATA SHEETPUMP DESIGN CALCULATIONS

Calculation No. 0

Item Name FIRE WATER PUMP Item No.

RATED FLOW HYDRAULIC CALCULATIONS - SUCTION AND DISCHARGE

Piping Section SUCTION

Segment 1 2 1 2 3 4 5 6

Line No.

P&ID Number

Nominal Pipe Size in 6 1 6 1 1 1 1 1

Pipe Schedule 12 1 5 1 1 1 1 1

Pipe ID in 3.068 #N/A 3.068 #N/A #N/A #N/A #N/A #N/A

Roughness in 0.0457 0.0457 0.0457 0.0457

Pipe ID mm 78 #N/A 78 #N/A #N/A #N/A #N/A #N/A

Pipe X-Sectional Area m2

0.005 #N/A 0.005 #N/A #N/A #N/A #N/A #N/A

Roughness mm 1.1608 1.1608 1.1608 1.1608 #N/A #N/A #N/A #N/A

Pipe Length ft 50 100

Flow Factor 1.0 1.0 1.0 1.0 1.0 1.0 1.0 1.0

Flow Rate ft3/h 13234.2 13234.2 13234.2 13234.2 13234.2 13234.2 13234.2 13234.2

FITTINGS Qty Qty Qty Qty Qty Qty Qty Qty



90 Elbow - LR. (R/D=1.5), All






45 Elbow - Std. (R/D=1), All45 Elbow, L-R (R/D=1.5), All






Tee - Used as Elbow, Std., Screwed

Tee - Used as Elbow, L-R, Screwed

Tee - Used as Elbow, Std., Flanged/Welded

Tee - Used as Elbow, Stub-in Type

Tee - Run-Though, Std., Screwed

Tee - Run-through, Std., Flanged/Welded

Tee - Run-through, Stub-in Type

Gate/Ball/Plug, Full Line Size, Beta=1.0



Globe Valve, Std.

Globe Valve, Angle or Y-type

Diaphragm Valve, dam type

Butterfly Valve

Check Valve - Lift type

Check Valve - Swing type

Check Valve - Tilting Disk type

Pipe Entrance (i.e. Vessel Outlet)

Pipe Exit (i.e. Vessel Inlet)

Custom fitting, enter K value associated with pipe size

Reducing tee, flanged or buttweld, through run 1 1.0 1 1 1 1 1 1Number of items above





Reducing tee, flanged or buttweld, as elbow 1 1.0 1 1 1 1 1 1


Reducer (K1=small dia, K2=large dia) 1 1.0 1 1 1 1 1 1


Enlargement (K1=small dia, K2=large dia) 1 1.0 1 1 1 1 1 1


Safety Factor for Slurry (see notes) %

Safety Factor for Fittings (see notes) %

Fittings Equiv. Length with S.F. m 0.00 #N/A 0.00 #N/A #N/A #N/A #N/A #N/A

Pipe Length with S.F. m 50.00 #N/A 100.00 #N/A #N/A #N/A #N/A #N/A

Total Equivalent Length with S.F. ft 50.00 #N/A 100.00 #N/A #N/A #N/A #N/A #N/A

Minimum Equivalent Piping Length ft

Velocity at rated flow (user units) ft/s 71.61 #N/A 71.61 #N/A #N/A #N/A #N/A #N/A

Density (base units) kg/m3 996.32 996.32 996.32 996.32 996.32 996.32 996.32 996.32

Viscosity (base units) lb/ft s 0.0010 0.00 0.00 0.00 0.00 0.00 0.00 0.00

Dynamic Pressure Loss psi/100 ft 586.69 #N/A 587 #N/A #N/A #N/A #N/A #N/A

Total Dynamic Loss (w/o S.F) psi 293.3 #N/A 587 #N/A #N/A #N/A #N/A #N/A

Specified Pressure Drop psi

Total Line Loss (w/ S.F.) psi 293.3441 #N/A 586.7 #N/A #N/A #N/A #N/A #N/A

Total Delta P (w/ S.F.) psi

Velocity at normal flow ft/s 47.74 #N/A 47.74 #N/A #N/A #N/A #N/A #N/AVelocity at minimim flow ft/s #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A

NOTES:

The "Safety factor for Slurry" is used to account for the fact that the friction loss in the pipe for a slurry is greater than for a newtonian fluid.

This safety factor is not applied on fittings. See Turian 1983 for details. The factor is calculated using the Slurry worksheet.

The "Safety factor for fittings" is used to add provision for the fitting losses when the exact number of fittings is unknown, typically early in engineering.

This factor is given as a percentage of the pipe length. This additional loss is added to any calculated loss for fittings that might be entered in

the worksheet. As engineering progress and the number of fittings is better defined, this number should be decreased to 0.

The "Minimum equivalent piping length" will override the calculated value "Total equivalent length" if the latter is smaller than the former.

The "Specified pressure drop" is used to impose a pressure drop for a pipe segment. This pressure drop override all other calculated values.

293.344

0

DISCHARGE

586.688

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Calculation No. 0

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Calculation No.

A) SUCTION LINE

Liquid properties Solid properties

Density (kg/m) : 1000 Density (Kg/m) : 3000

Viscosity (Kg/m/s) : 0.001000046 Average particules size (m) : 1.00E-05

Flow and line size Slurry calculated properties

Liquid only (Kg/hr): 1866858 Solids weight fraction : 0.000 Total flow 1866.86 m3/h

Solid only (kg/hr): 0 Solids volume fraction : 0.000

Pipe ID(m): 0.0530 Slurry density. (kg/m): 1000.0 Check densities, inconsistent with data in PumpCalcs!Roughness (m) : 0.00005 Density solid/liquid : 3.0

Solid terminal velocity in liquid Flow characteristics Calc of dP/l for slurry

Lambda = N Re*Cd^0.5 : 1.62E-01 Flowrate (m/h) : 1.87E+03

Log Lambda : -7.91E-01 Velocity (m/s) : 2.35E+02

N Re : 1.11E-03 N Re water : 1.25E+07 N Re slurry : 1.25E+07V infini (m/s) : 1.11E-04 Relative roughness : 0.000943396 Relative roughness : 0.000943396

Cd : 2.14E+04 f Fanning water fW : 0.0048 uncorrected f slurry: 0.0048

uncorrected dP/l for slurry: 10101.372

Flow regime Flow regime friction factor

R01 - 1 : #DIV/0! f0 - fW : 0.00E+00 Test 0 #DIV/0!



R02 - 1 : #DIV/0! f3 - fW : 0.00E+00 Test3 #DIV/0!

R03 - 1 : #DIV/0! Total #DIV/0!

R13 - 1 : #DIV/0!

Results

Flow regime No #DIV/0! Corrected f Fanning for slurry: #DIV/0!

Flow regime is #DIV/0!

Delta P/L (bar/100m) : #DIV/0! Average error : #DIV/0!

Delta P/L (PSI/100 ft) : #DIV/0!

Ratio slurry / single phase #DIV/0! to be entered in cell "Safety factor for slurry"

Notes:

The density used in the PumpCalc sheet is the slurry density. The densities used in this sheet are the phase densities.

The viscosity used in the PumpCalc is the liquid density, same as on this sheet.

The liquid and solid mass flow rate are calculated from the PumpCalc data, using the % solids.

The pipe ID and roughness need to be entered manually, but care should be taken to match the data in LineLoss.

The units used in this sheet are not user defined, and do not necessarily match the units used in the rest of the spreadsheet.

Interpreting these results:

Avoid if at all possible designing in stationary bed regime: if this is the case, try reducing the pipe size.

Try to balance the slurry / single phase ratio and the regime: the higher the flow regime number (0, 1, 2, 3)

the less chances of plugging, but the higher the energy cost.

Consider whether the flow will be upward, horizontal or downward. If upward, chances of plugging are higher.

Slurry hydraulic calculation

0

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