Thank you Mr. Pellin for your advice!
I thought that between bearing pumps are generally large and are used when the capacity and head are high.
You mean that BB1, BB2, BB3 or even BB5 could be used for low flow? (like 40~60 gpm)
In the following condition:
Diff. Head = 270m
Rated Flow= 14.3 m3/hr
Viscosity= 0.2027 Cp
I've selected OH6 pump but a friend of mind said a reciprocating pump may also meet these conditions.
Is there any preference (technical of economical) to choose between these two types of pumps?
Thank...
A Reciprocating pump has been previously chosen for working in the following condition:
FLUID HANDLED Heavy Residue
PUMPING TEMPERATURE (oC)= 50
VISCOSITY @ P.T CP= 415.44
VAPOR PRESSURE @P.T BARA= 6.029×10^(-8)
DENSITY@P.T (KG/M3)= 975.85
OPERATING CONDITIONS
CAPACITY (M3/Hr)= 0.5...
Hi
What is you idea for a seal plan for a demineralized water pump?
As the main fluid is corrosive do you recommend it for flushing?
The main flow at most could do heat removal for us, what about lubricant? We have to use an external fluid for lubrication purpose?
Thanks;
Hi;
For a centrifugal pump we usually use a pressure gauge or flow meter to know whether the pump is working properly or not. Choosing between these two gauges I just know one preference;
We usually use a pressure gauge unless when the performance curve is too flat to detect the operating flow...
Hi;
As I had a hot talk with my friend over the use of bypass in Cent. Pumps I want to examine whether I am right or not?
Based on my knowledge I know three cases in which we can use bypass for Cent. pumps:
1- When the minimum flow is prone to be less than the minimum flow which was determined...
I am grateful to those who shared their experiences with me. You have almost answered my question but two more points are still remained:
1- Because of NPSH problem, it isn't possible to work at end of the curve (let NPSHa increment be off the table), therefore vendor promised to reduce the...
Little Inch where is BIG inch? I missed him!
I'm following your motto and try to learn something new every day but not today yet because I still don't know how a pump manufacturer calculate NPSHr and Max. flowrate?
Hi;
I have recently received a vendor datasheet for a Cent. pump and the pump has a problem on NPSH margin at Max. flow. Then vendor replied us we will reduce the Max. flow in order to see you project Spec.
I got confused!
Is it possible to reduce a pump Max. flowrate?
As this pump is API, is...
Hi,
In API-610 it has been mentioned that "Pumps shall have a preferred operating region of 70 % to 120 % of best efficiency flowrate of the pump as furnished. Rated flow shall be within the region of 80 % to 110 % of best efficiency flowrate of the pump as furnished."
For instance if a pump...
Thank you very much Mr. Reifleman!
When I read your comment I feel I am reading a technical handbook which its author writes the book in the way that I want.
So I want to ask another question if it's possible
Have you ever seen 53B plan alone? I want you to describe the conditions where there is...
As I know two way are used for starting a Cen. pump:
Closed Delivery Valve
Open Delivery Valve
In an oil and gas plant, the starting condition is chosen by instrument&control discipline or process discipline?
The problem is we have high NPSHr (exceeding NPSHa) at the end of curve and if the...
I have read the post and the responses and a question raised for me. I have seen in API-610 the some different method for coupling balancing like:
- ISO 1940-1 G6.3
- WITH PROPRIETARY CLAMPING DEVICE
- PER ISO 14691
- PER ISO 10441
- API 671
I don't know any criteria for choosing one of them...
Thank you LittleInch for your comment.
As mechanical engineer, I don't have an extended knowledge about electricity so if I figured it out correctly, this means that the electrical motor which used for a centrifugal pump should have capability to work with a voltage lower than the design and...
Thank you again Mr. Reifleman!
I understand that here isn't a good place for asking people to comment about a project in detail but in our project the vendor has offered 53B with tandem arrangement. No other plan has been proposed as the process fluid is corrosive and not suitable for flushing...
