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Hi all, My question is straight forward. Can you size a thermal relief valve FOR GAS ONLY SYSTEM? If yes, how do you calculate the load requirement? I have gone through API 520 and 521, and nowhere do they discuss or explain thermal relief for a gas only system. I know 521 section 5.14 talks...

Hi experts, I have a few questions about PSV sizing. I got some drawings and datasheets from a vendor for a fuel gas skid and I don't think the vendor calculations are correct. I will appreciate if you can help me with answers to the following questions: (1) Fuel gas skid is designed for a...

Sorry, was out of the country on vacation. Here is a PFD of what I've been trying to describe. The safety valve in question is the one in red. As you can see, it is not discharging directly into the pump suction - there is a valve between the discharge and the pump suction. Also, note the...

The suction is around 100 psig and the discharge is 700 psig. The pipe ANSI ratings are higher on the discharge piping as can be expected (150 vs 600). However, the pump flanges are ANSI 900. Also, don't overlook that there is a bypass around the pump. I assumed that even if we need to relieve...

Yes, there is a TRV around the discharge valve too.

Latexman, thanks for the reply. I did not show the valves on the discharge line because I did not think it was important to the question. However, we DO have valves on the discharge line.

I have a facility set up as shown in the attachment. It is a crude oil pump station. Oil comes in, it is metered and it is pumped to another facility. We have valves on the suction and discharge side of the pump. To account for thermal relief we have installed a TRV on both the suction and...

You can use dynamic simulation in Hysys to model the problem. See the Hysys manual or contact Hysys helpdesk.

Yes, @ georgeverghese, the max developed pressure will exceed the pipeline MAOP. Not by much, but by 60 psig. Littleinch, the pumps are positive displacement pumps. I think the full flow is required to size the safety valve on the pumps. I use API 521. Thanks, to both of you. I think I have a...

Thanks, LittleInch, Yes, the flowrate has doubled to 144000 barrels per day because the client wants a 100% design factor in the facility (first time I’ve heard of that). Anyway, it seems like there will be more crude passing through the facility BUT they can’t tell, definitively, how much...

Hi, I am sizing relief valves for liquid system for the first time. I usually work with natural gas. I know the code/standard and the equations and I can calculate orifice sizes. However, I do have a question regarding blocked outlet on a pump. The facility is a pump station with 18 inch...

Hi all, I am working on a crude pipeline transporting around 3000 barrels/hour of crude. I have done the system relief analysis, but have a few of questions: Is blocked outlet a credible scenario? Especially at pump discharges? If not, why? Finally, if sizing blocked discharge on a pump, do...

Hi, Can anyone help me with how to size a sump? I have searched extensively for this and the only things that come up have to do with aquariums and aquatics. So, how do I size a sump? What volumes do I use? Low level of all the vessels? Also, how do you decide between an open or closed...

Hi everyone, We are installing a new low pressure 2-phase separator in the field. The operating P is around 120 psig. The pipeline and the vessel are to 1375 psig @ 185 F. I had a discussion with another engineer on how best to protect this vessel. His point is that since the operating P is...

Hi all, I am designing a fractionation train to recover ethane, propane and butanes. Can anyone help me with typical condenser pressures and temperatures? Also, I have substantial methane in the deethanizer distillate stream that I would like to remove to get pure ethane. Can anyone help me...

I recently came across a P&ID that shows a shell and tube heat exchanger. In addition to increasing the temperature of the natural gas with the steam, the P&ID shows TEG going into the exchanger as a heat transfer fluid. Does anyone have a practical knowledge of how this process work? Not how...

Thanks, LittleItch, for your help. No, you did not insult me...I was just trying to explain the extent of my understanding of the issue. That's what the forum is about - helping others, and you did just that. It's quite clear to me now. I really appreciate your assistance.

Sorry, forgot the file.http://files.engineering.com/getfile.aspx?folder=2651a0a9-b355-41e2-b7e2-653a4d7ae65f&file=12321.JPG

LittleInch, I think I have quite a good grasp on regulator operations and design equations. I am still a little confused on what the pressure drop will be in some situations (such as when the regulator is a last layer of protection and is not expected to be activated). I have included a scenario...

Thanks, LittleInch, for the help. By the way, i'd rather send this to a valve engineer. But, for some reason, the senior engineer wants it done in-house. We've always sent control valves and regulators out to be sized.