Maximum viscosity ranges are a major consideration in pump selection because of possible deterioration in performance wiht increasing viscosity.
In general terms, which are the limits in viscosity range for using a pd or a centrifugal pump?
I would like to find a CHART or TABLE which shows...
I would like if someone could clarify my doubts...
when a multistage pump has a balance axial thrust device (drum, sleeve or combination of both), is the axial thrust eliminated to the extend that it is not required axial thrust bearings?
If it should be required thrust bearings, what type of...
I would like if someone could clarify my doubts...
when a multistage pump has a balance axial thrust device (drum, sleeve or combination of both), is the axial thrust eliminated to the extend that it is not required axial thrust bearings?
If it should be required thrust bearings, what type of...
I understand that it should be a minimum sumergible level for vertical pumps to avoid vortix. However how to calculate the NPSH available of the system? Obviusly the static head has to be at least the minimum sumergible level? Any comments?
Thanks a lot
Any names of books for ranges of equivalent lenghts of pipes? Does anyone recognize "PIA Pipe Friction Handbook" from Australian Pump Industry Assosiation? I would rather prefer values in International System...
Thanks again
Trying to understand how to use equivalent length or factor "k", I would like if someone could clarify the following.
Looking at the book: "Practical Centrifugal Pumps" (Paresh Girdhar & Octo Moniz), there is an example for calculating friction losses. However I understand that is mixing up...
By knowing pipe pressure (6 bar gauge) and pipe diameter (60 mm). How can I know the flow? I guess I dont have enough data, however could anyone tell me the typical flow speeds for a pipe of water supply?
Thanks a lot
I would estimate savings by installing a variable speed in a centrifugal pump of 355 kW, 1480 rpm. Could anyone give me an idea about how much a variable speed regulator would cost?
Thanks in advance
An horizontal Between Bearing, Axially Split, Single Stage Pump @ 1000m3/h, 38m, 1480 rpm, 119 kw (impeller 368 mm). The system curve is H=26+12.10^-6.q^2
When changing duty conditions to (500 m3/h, 29m) checking online pumps charts, changing speed impeller to 1200 rpm, new power is 52,4 kw...
When pump working between two tanks, and we apply the bernoulli equation, we normaly consider v1 (suction) and v2 (discharge) = 0 (the area of the tanks very big, so velocities will come very small)
However if the discharge pie is above the liquid level in the discharge tank, i should consider...
Could you please, let me know how to calculate the NPSHA if I wish to take in account the velocity head in the suction tank?
- For suction lift:
NPSHA= ha - hvpa - hst - hfs -v2/2g
- For positive (flooded) suction:
NPSHA= ha - hvpa + hst - hfs +v2/2g
Are those calculations right? (+ or -...
Could you explain exactly the meaning from API the standard 2.1.12? What is the diference the preferred operating region and rated capacity region? why there is more margin on the left (i.e. 70%) of bep than on the right (i.e. 120%)?
Thanks a lot
