1. 2/22/2019
Pump Design
Dick Hawrelak
Presented to UWO CBE 497
10 Oct 00

2. Good Design References
Flow of Fluid Through Valves and Fittings by Crane. Technical Paper No C.
Centrifugal Pumps and System Hydraulics, Chem Eng’g, 4 Oct 82, p-84, by Karassik.
Chem Eng Handbook, Perry 6, Sections 5 and 6
Primer software by Durco
PumpSel 6.2™ (rev .07) by Durco

3. Pump Design Stages Phase 2 – Process alternatives & optimization.
Phase 3 – P&IDs, preliminary layout, approx design, specification, pre-selection, cost estimate.
Phase 4 – detailed design.
Final layout – check piping & elevations.
Final detailed hydraulic design & selection.
Suitability (NPSH, SSS, Re-circulation).
Final cost estimate.

4. Excel Pump Design Program
Plant Design Programs on CD-ROM
Quick Pump Design V1.3
Contains Following Features
Line Sizing
Control Valve Sizing
Check Valve Sizing
Orifice Plate Sizing
NPSH, NS, SSS, HP calculations
System Head Curve
Limited Pump Selection
Used along with Durco’s PUMPSEL and PRIMER

5. Draw Sketch of Pump System
Collect physical property data (density, viscosity, vapor pressure).
Show line details, size, schedule or wall thk, check valves, control valves, block valves, reducers/expanders (may have to take a WAG).
Show origin (min.) and destination pressures (max.).
Show origin and destination elevations for static head.
Combine services where practical & economical.

6. Typical Pump Sketch

7. Size Suction and Discharge Lines
Break lines into sizable sections. There may be different sizes in any one branch. Eg 4”, 6” and 8” sections.
Estimate the number of elbows, block valves, fittings, etc. (WAG in Ph 2).
Expand line sizing routine for record keeping. This will simplify phase 4 checking.

8. Line Size Equations Re No. = 6.31 ( W ) / ( d ) / ( cP )
Darcy friction factor f = 4 ( f Fanning ) f Darcy by “all-in-one” Chen Equation
DP100 = ( f )( W )^2 / ( DL ) / ( d )^5
Max Dp100 usually limited to 1.0 psi per 100 ft.
K = ( f ) ( L / D ) for pipe
K = ( f Turb ) ( L / D ) for valves and fittings
K total = K pipe + K valves & fittings
DP = 2.8E-07 ( K total )( W )^2 / ( DL ) / ( d )^4
Abs roughness e = for clean pipe, ft.
Abs roughness e = for dirty pipe, ft.

9. Size Check Valves in Each Discharge Line Branch
Line sizing program built-into Pump pgm.
Check pipe spec for type of check valve.
Check minimum line velocity to keep ChV in open position. Prolonged operation at reduced rates may cause ChV chatter and damage to ChV.
Operation with damaged ChV is extremely hazardous.

10. Typical Check Valve Equation
For a Swing Check Valve (see Crane, page A-27)
K = 100 ( f Turb ) for pressure drop
Minimum Velocity, fps = 35 / ( DL )

11. Size Orifice Plates in Each Branch
See Line sizing routine.
Orifice Plate pressure drop usually in three ranges.
Typically 0.5, 1.0 or 2.0 psi

12. Typical Orifice Equation
Beta = d1 / d2 should be in range 0.2 to 0.7
d1 = orifice dia., d2 = pipe dia., inches
Re No. based on d2, the pipe diameter
W = 1891 ( d1 )^2 ( C ) (( DP )( DL))^0.5
C = Flow Coefficient for square edged orifices (see Crane, page A-20)
C = Function of Re No. and Beta ratio
C should be in range 0.6 to 0.8

13. Control Valves
Select each branch with control valves and use line size routine to size control valves assuming Fisher Equal Percentage type valves.
Poor CV selection – no control, pump running on by-pass…may need two control valves.
If too large DP taken across control valve, it may be better to trim impeller, save CV wear & energy.
Pump program should use CV in controlling line.
DP CV / (DP CV + DP fric) = approx 0.1 to 0.3. Default DP control valve = 10 psi.

14. Typical Control Valve Equations
Cv = ( USGPM )( SG / DP )^0.5
Cv = Liquid Sizing Coefficient
Typical control valve is an equal percentage type valve.
Cv depends on valve size, % valve opening, and flow.

15. Blocked-in Operation.
Determine features required for blocked-in operation.
Low flow shut-down.
High temperature shut-down.
Recycle plus cooling.
Pumps can explode in a short period of time if left running while blocked-in and no high temperature shut-down is provided.
Pump explodes, pieces rocket 275m, hits truck, kills driver.
Pump leaks under high pressure, liquid catches fire and destroys plant.

16. Suction Conditions Determine NPSH available.
NPSH = SP – VP + HL – DP friction all in ft of liq.
Boiling liquids, SP = VP. Raise height or reduce DP.
Poor NPSH causes pump cavitation, high vibration & ultimately pump failure (hazard).
Pump fails to perform as designed without NPSH available greater than NPSH required.
Typically, NPSH avail 12 ft. vs 10 ft. req’d.
Pump Vendor will tell you NPSH required based on pumps selection.

17. System Head Curve
Determine Controlling Branch – I.e the one that requires the maximum differential head.
Determine the system curve for all items except the control valve.
For Dp at reduced USGPM, assume DP is proportional to the square of the flow.
Include static head.

18. Pump Selection Hundreds of pumps to select from.
Which selection is best?
Which RPM to use?
What HP size & type of motor to select, explosion proof, TEFC?
Download Durco PUMPSEL and PRIMER on internet (program is free).

19. Durco PUMSEL Program Input
From Quick Pump Design V1.3 enter:
Design USGPM
System head, in ft.
Specific Gravity
Pumping temp, Deg F
Viscosity in Centipoise
NPSH available in ft.
3 points from system curve.

20. PUMPSEL Output Selects all available pumps Gives Impeller sizes
Gives HP and NPSH Required
Gives a cost estimate (PRIMER)
Gives options for types of pumps
Gives all kinds of help on all features.
PUMPSEL is a must for any design group.
Program also available from Gould.

21. Typical Pump Head Curves

22. Selected Pump

23. Suction Specific Speed, SSS
SSS is an Index number descriptive of the suction charateristics of a pump impeller.
SSS = BEP)^0.5 / BEP)^0.75
Pumps operating at SSS greater than 11,000 had a high failure frequency (hazard).
Low capacity operation causes inlet recirculation, impeller erosion, shaft deflections, bearing failures and seal problems which lead to leakage.
Pump program predicts recirculation as % of SSS.

24. Dissolved Gases Absorbed gas follows Henry’s Law xa = (pp / Pt) / H.
Dissolved gases are like entrained bubbles. Residence time in suction vessel may be too short.
Dissolved gases causes problems similar to NPSH cavitation.
Prevent vapor entrainment with vortex breakers.

25. Material Transfer
Need multiple checks on quantity of material transferred to storage.
Weigh scales, level checks, mass = (flow rate)(time) on computer.
Time control EBVs to minimize Water Hammer problems.

26. Excess Flow Protection
2/22/2019
Excess Flow Protection
Pumps cannot be allowed to run out on the impeller curve, may burnout motor if motor not selected for runout.
May need excess flow protection.