I have found x2 comments made on the use of Equal% & Linear control valves on LinkedIn
I cannot understand the relationship between length of pipe & valve characteristics? Secondly per my operational experience the 2nd point is not true as even at very long Cl2 lines I can see Equal%...
I am attaching images perhaps someone can provide insight as to what may be the reason & how we can avoid it.
The pump in picture are brine pumps as well as vacuum pumps [both are provide by HB company]
I am attaching pdf & SMath sheet that provides a x3 page calculation & perhaps someone can review it.
The background is I have a liquid ring compressor that vendor provides performance curve tested with air media while actually it will be used for H2. From this data I have calculated polytropic...
@ MJCronin
I must reply to your allegations
First this thread has x3 great posts ...& I starred them! Thats a quantitative thanks you.
Second go through this whole reply [the bold part]
@ LittleInch
I get the impression I'm annoying you and your answers are coming across as a bit "spiky". You might not like having your design being questioned, but we're all just trying to help here.
Haha. Sir English is not my native language so I can write what I think is correct but its...
So the CL tank should be fed by a separate tank or a separate water line. Only if there are very good reasons not to ( and cost isn't one of them)
It is not possible
What length is that? Exactly 5m as well?
As you can see in the illustration it is (dip leg) exactly 5m
Loose less than a metre...
Cl2 & H2 should never mix ...but I have a situation where I have H2 compressor, H2 seal & Cl2 seal being fed by same water line.
What if x2 events happen simultaneously:
1] Supply water tank become empty so water line is empty
2] H2 seal is CS (carbon steel) & the immersed line can develop...
@ LittleInch
Over time even a small discrepancy between flow in and flow out will lead to either high pressure or low pressure in your system. This is the downside of using a PD compressor with a flow control valve..
True, I think this discrepancy can be assumed not to be present. Even if it is...
@ LittleInch
I get your 936nm3/hr to be about 90kg/hr, so if your inlet flow is 101 you are going to pretty fast have an overpressure in the system up stream the PRV?
I think one thing is missing here. When you burn Cl2 with H2 ...H2 is always 7-10% excess to avoid Chlorinated HCl. That should...
@ LittleInch
@ georgeverghese
I have updated the drawing & added further details which represent field actuality. I had also included paper / per calculation which is based on previous discussion
@ georgeverghese
Thanks for your recommendations.
Fully automate the PIC - PCV control loop to...
Thanks for all your inputs
ALL PD pumps I have ever see have a spring relief valve system installed to provide a high integrity pressure relief. Your system doesn't seem to have this.
Correct, it has 800mbarg setting
@ LittleInch
So this pressure rise on furnace trip will almost certainly lead to the vent opening and pressure will rise until the PD pump stops.
So at some u/s pressure an interlock with compressor motor can be thought of. However this 5m water seal should avoid pressures beyond 500mbarg
Note...
@ LittleInch
The compressor is a pd compressor (as indicated) which translates 160mbarg to 250mbarg. At the downstream of compressor till the furnace pressure will increase & can go beyond 250 easily if FCV closes at furnace tripping. The compressor (like all pd compressor) have a check calve at...
@ LittleInch
So in this case you could simply forget about your water seal and vent and the PCV at 250 mbar because it will never get there.
So all you need is your FCV before the burner, or maybe your cooler, but nothing else in terms of vents or pressure control.
No, Like I said upstream...
