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Thanks danw2 My answers: 3) I'm sure. The purge is for lowering the conductivity. This is a lot more than 10 us/cm 4) At 20 m3/hr I have 1 m/s. Is it enough?

Hi, I attached a diagram of the situation. http://files.engineering.com/getfile.aspx?folder=f81381a2-ffd0-4dc4-8347-7344f9452c79&file=Purge.pdf We want to measure the flowrate of the purge of an evaporator. This works as a distiller (it evaporates water), so the purge is just water with high...

Thank again for your answers, I review the pressure at the BFW, dearator an it is in a range of 2,0-2,5 barg (29-36 psig). The heat exchanger is barely used currently. I don't know how it worked on operation Another information is that the pipeline is 6 inches. There is not much pressure loss...

zdas04, georgeverghese & LittleInch thanks all of you for your answers. For better understanding I attached in this link http://files.engineering.com/getfile.aspx?folder=ed677fa5-d317-4c76-9744-cf3e62d3beda&file=Vortex_Flowmeter.pdf The condensate come from an evaporator. The normal flow is 80...

Hi, I attached a diagram where i sketched the current situation of the installation of a vortex floweter. This flowmeter reads relatively well at max. flow but we have incorrect measuring at lower flows and startups. (The fluid is pumped condensate) I also drawed a new proposed situation. Will...

Hi I'm looking for I way to measure the flow of a condensate line which is flashing, so I found this technology http://cadillacmeter.com/products/cadillac-cmag-pumped-condensate-meter/ Do you know or have any experience with these type of flowmeters? Do you know some other brands that sells...

Thanks for your answer metengr, I have antother question. Is it specified in ASME IX, or other document, the procedures for welding to materials with diffrent P-No. if it is possible.

Hi, At the drum level measurement we have a DN25 connection available, the material of that piping is 16Mo3 EN10216-2 1.5415. We want to install another level measuremnet systems. For this purpose we have to weld some pipes to this connection. The only material available we have is P11/T11...

Hi Everyone I want to estimate the operating point of a series o pumps.} I have a drawing attached in a excel format in the next link http://files.engineering.com/getfile.aspx?folder=bb491a82-3f4b-4b5d-a79d-4307c5c33347&file=ESQUEMAS_BOMBAS.xlsx There are two pumps of my interest right now...

Sorry I made a mistake in the first post "When the control valve is at its 100% of lift the steam pressure upstream of this valve is 0,8 bara.". It's really downstream the control valve where the pressure is measured. a draft of a P&ID of the steam line is in the next link...

yet, it doesn't make sense to me. -The pressure at the valve inlet should not be a bit less than 2.6 bara, considering the friction losses are negligible. -Based on the valve Data Sheet the maximum pressure drop across the valve is 0.5 bar. So the minimum pressure at the valve outlet should be...

it's absolute pressure. I'm pretty sure of that. For example when the plant is stopped the measurement is around 1000 mbar (seen at the control room)

the length of the 6" pipe is around 25 m, and the inlet of the control valve is 4" I have done the pressure loss calculation and is negligible at 4000 kg/h of steam http://www.tlv.com/global/TI/calculator/steam-pressure-loss-through-piping.html

Hi Everyone, This is a situation about the steam pressure drop at the steam feeding of a 3 effect evaporator. The steam for various process of the plant is produced on another 1 effect evaporator, and the pressure of this steam is 2.6 bara (measured). Part of this steam is used to evaporate...

Hi everyone, I have this doubt. I have seen on the plant where I work these typical configurations of control on heat exchangers. if STEAM is used to heat water or product, the control valve is placed in the steam inlet for all the heat exchangers I have seen (the majority are of plate and...