Hello all,
In API 510 section 3.1.1. the definition for Abandoned-in-place is as follows:
A pressure vessel meeting all of the following: has been decommissioned with no intention of future use; has been completely de-inventoried/purged of hydrocarbon/chemicals; and is physically disconnected...
Yes it is a total recovery system with a shell and tube exchanger to cool the recirculating water. There is currently no level control system in place so I am thinking of a quicker/cheaper way to have a control system without the need for a control valve/floats.
Has anyone had any experience with makeup water for a total recovery liquid ring vacuum pump system? Through our condensed vapors as well as mechanical seal flush, we still can't seem to maintain the level in the separator. This causes us to keep the initial priming valve opened. The issue is...
1. I believe 4' submergence is more than adequate for a vertical sump pump. What are you calculating it at?
2. And that may be true but it its low flow that doesn't match up with the discharge pressure I am getting either...
My issue with some of the testing is I am not exactly sure what values I need to be trusting. My amps, dP, and flowrate are not aligned which is why I am having issues with evaluating the performance. And of course I'll keep to forum updated, this was a project that got put on hault, and then...
There are a ton of lines that tie into this main lie before dumping into that atmospheric tank (that's what all those arrows are representing). I have a lot to start digging into now with all of your responses. Air entrapment could be our main culprit in all of this..
The liquid is gravity fed from the areas walkways into the sloped sump. It's most water but debri from all over can make its way in there. The liquid travel through screens and into the settling chamber where the level rises and dumps over a weir into the pumping chamber. I imagine there is some...
About 3.5 ft level sorry about that. And you can't really see inside the bottom of the sump, and unfortunately this sump can't ever be stopped. I'm working on a PM to get vacuum truck periodically to pump out the pumping chamber. We already have one that comes out to pump out the settling chamber.
Not totally sure, we operate at 35% level which I believe should be adequate submergence. I hear you on the impeller however we did have a brand new pump swapped in there and it exhibited same exact characteristics...
There is a semi-open impeller.
All of these data points were taken with re-circulation line closed. The whole reason for the initial re-circulation line was a quick and cheap way to protect the pumps before we can get another project for VFDs implemented (already have done analysis on this...
I've analyzed the entire piping system the system is way more complex than what I have illustrated, but that is the general idea. I am not asking anyone to do the job for me, I have calculated my head loss/requirements in the system. I was just asking about possible reasons that I could be...
In terms of data, the three readings I gathered were 20 psig (at discharge gauge), 25.5 amps, ~275 GPM. Motor is 40 hp, 86% PF, 94.5% efficiency which equates to about 23 hp using 480 volts.
Suction screens were relatively clean, however there is a chance the pumping chamber has a layer of mud...
Well I did install the re-circulation line as referring to those old posts. I wasn't entirely sure the project needed to be brought up, it was more of a fundamental question in my eyes. The amp is reading was taken by my tech, and I used the efficiency on the motor name plate for calculation...
Hello,
I have 3 vertical sump pumps at our plant. I've been having trouble finding where it runs on its curve and need some advice. I took amp readings (converted to bhp), NEW gauge dP readings, and downstream flow meter readings, and none of the points really line up on my curve. Any hunches...
Yeah there are already quiete a few meetings set in place in my unit. There are the daily morning 30 min meetings of whats going on, status's, safety...etc. Then daily 1:30pm maintenance/work items to be conducted next day. Shutdown meetings...etc But not a "reliability" meeting per say. I'm new...
I'd like to hear any of your experiences in holding bi-weekly or monthly reliability engineering meetings. Whether it be for a specific unit in a chemical plant like myself, or other applications. Do you start off with the big hitters of the month? Equipment of focus? Safety...etc? Include...
I'm quite unfamiliar with these hydraulic profile lines. Doing some homework on it now. When sketching the profile, are they different points just calculated at different elevations throughout the system?
