Recent content by mucour

Thanks BigInch. But on doing further research, I came across the concept of applying a kind of “stand-pipe” that is located upstream a PD pump. In a pump article, the introduction of a stand-pipe was used to reduce the acceleration head loss in a situation when the suction length of the piping...

Hello, Thank you for the explanations given in the thread: thread124-196619. However, Doug and BigInch should clarify a conflicting statement concerning that the heat exhanger cannot be regarded as doing the work of a suction stabilizer. According to BigInch, the heat exchanger breaks the...

dcasto, thanks. I guess it is always a challenge dealing with operations department who want production at all cost. Engineering always battle with their short-cut measures. I will make effort to escalate this issue to management so that operations can heed to our advice. Thanks again.

Hello, Please can you share with me the potential danger (or otherwise) of operating a centrifugal compressor plant with the anti-surge valve control system deactivated but running with the anti-surge valve opened permanently at 30% open position. We have a situation in our plant (3...

Imans, what is the type of seal you are using. I mean is it double tandem or single seal? What do you use as your seal gas and separation gas? Because when you say buffer gas, it means you have different supplies for seal gas supply and separation gas supply in addition to the buffer gas supply.

I have read somewhere that the affinity law can be used for rough estimation if you want to determine new conditions of Head, Flow and Power, speed, Imp. diameter. But using the affinity law for a centr. compr. can only be applicable to a certain pressure limit that I cannot say offhand unless...

I have never seen MMSCFDM. I only know of MMSCFD has defined by you.

David, you could not have described it better. It was a wonderful piece. I could have given more stars but I am entitled to only 1 vote. Thank you.

Thank you all. The eductor was not accepted because the amount of pressure and volume required of the motive fluid (liquid or gas) is very high to boost 1250 m3/h gas from near atmospheric to 60psig. The wet screw compressor was considered advantageous because of the high compression ratio...

Hello, We are considering a wet gas screw compressor for vapour recovery application. The gas is wet, water saturated and a heavy gas. Could anybody advise from the experience in their plant where they have this wet screw compressor for similar service the manufacturer that they will recommend...

I am not clear with your description. If the compressor anti-surge control valve opens and it causes the suction inlet volume flow to increase because of a poor antisurge control design, then I do not see how this leads to a pressure spike. What I see is infact a reverse, ie. the suction...

CompressorExpert, It is interesting that basic fundamentals get one confused. This is just like a thread posted on centrifugal compressor under "Chemical Process Engineering group" It was put into proper pespective by JJPellin. If you follow my response on the recip, I did mentioned that a...

In my last posting on line 9, I meant to say compressor not pump. Surge condition does not happen in pumps.

Thanks JJPellin, for your better explanantion. In centrifugal pump, a scenario of higher system resistance due to e.g. blocked outlet or pumps installed in parallel imposes higher resistance or back pressure on another parallel pump causes the operating point to shift to the left on the...

Montemayor, now it is very, very clear. Thank you. I do not mind the abuse as long as I get the support. Thanks again