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BIG Inch----------- I got an answer I just wanted to cross check it. secondly i am more confused with schedule of the pipe....due to which my calculations will get wrong because it is highly viscous fluid.... Thirdly during calculation of NPSHA do we add the atm pressure to the tank pressure or...

Hi, Help to calculate the frictional loss for the below said pipeline system Flow----680 m3/hr Pipe----SEAMLESS BE STD SCH B-36.10 ASTM A 106 GR.B 14" pipe---40.6 mtrs 12"-----1.8 mtrs 1.1/2"---- 0.2mtrs Fittings-----gate valve 14" 150# RF- 01 no.,,,, valve-PERM str bw 150# t-type eil std type...

HI Guys... Can any body tell me the schedule for this pipe..: SEAMLESS BE SCH STD B36.10 ASTM A 106 GR.B....Also tell where to look for its frictional loss data..... help me ASAP

Hi Guys... I am having pump using mechanical seal with API Plan32. The problem here is we need a operating pressure of 2 barg and flow of 10LPM. But in this case if flow is set to 10LPM then pressure reduces to almost zero & if we set the pressure as 2 barg then the flow increases much beyond...

BIGInch---- That is the maximum design temperature.The pumping range has varied from 145C to 160C at some of the times. The vapour pressure range is 3.28-3.84 kg/cm2a.

micalbrch This is a two stage pump with first impeller having double suction and pump having top-top configuration. The normal fluid being pumped is preflashed crude oil at temp.of 165C. and specific gravity of 0.7888.

1gibson--- there is no increase in vibration until pump cavitates & then vibration increases due to it Also the impeller is keyed to shaft.

Hi guys, I am facing a certain condition in which I am unable to acertain the cause of loss of suction & reduction of flow and discharge pressure of a pump abruptly which leads to cavitation. The pump is not showing any symptoms which conclude for any wear & tear in pump. Other wise the pump...

Hi, can anybody tell me the possibility of overheating of seal FLO line????

tnx BigInch... let me give you some more details..... the flow is 225m3/hr.... the vapour pressure is 4 hPa. specific gravity is 0.87... the NPSHr is 4.4m........ can you explain me more?

Hi.. IF NPSHA IS ABOVE NPSHR BY MARGIN OF 3FT,WILL THIS BE OK FOR ALL OPERATING PUMPS AT THEIR RATED CONDITION????CONDITIONS MAY VARY viz.PUMP MAY BE HAVING NEGATIVE OR POSITIVE SUCTION LIFT.AND ALSO THE VISCOSITY MAY REDUCE.....