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Thanks BigInch By any chance... do you know a good web for viscosity conversion (ssu, cts, cp, mm2/sec ...)on line? And in general, for engineering units conversion? In the past you gave a good one,but i cannot find it!

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...

GregLamberson, My concern was about confusing minimum liquid level and NPSH available when working with vertical pumps...

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

katmar, thanks!! I have lost a few hours trying to find an explanation!! I feel like complaying to the publisher!!

In the example, calculate friction loss using h=kv^2/2g and the valued is added to the equivalent length. I.e: From chart 140 l/s, 250 mm, sch 40, st -> 2.30 m per 100m, v^2/2g=0.386 For foot valve with strainer: k=5.88,k.v^2/2g=5.88x0.386 m -> 2.27 m equivalent lenght of pipe So according...

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...

Where can I find information about range for grease lubrication? What is the speed and power limit? Thanks a lot!

I am not very sure how to do it...It is a new project for a fire protection system and I require to know the flow of the general supply water pipe to be able to calculate the time I need to fill a tank. The available pressure of the water supply from the street is 6 bar. The pipe diameter 60...

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

The flow rate changes from 2200 m3/h @ 105 BEP, to 1680 m3/h @ 90% BEP The total head at 2200 m3/h is 50 m (Hst= 40m) The total head at 168 m3/h is 46 m (Hst=40 m) Is not worth it to use the vsd? In which cases it would be a good way of flow regulation? thanks again

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

BigInch, Thanks! Your information is always very helpful!

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...

BigInch thanks a lot for your reply. I am still a little confuse...Could I summarize as follow? 1) For a new installation, the NPSHA in the pump is: - For suction lift: NPSHA= (ha - hst - hfs)-v2/2g - hvp - For positive (flooded) suction: NPSHA= (ha + hst - hfs) -hvp (more conservative since I...

However, I have just read in "Cameron Hydraulic Data", to calculate he NSPHA on an existing installation would be the reading of a gage at the suction flange converte to feet of liquid absolute and correcte to the pump centerline elevation less the vappor pressure plus the velocity head in feet...