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Once the stopple is removed, I'd treat it as a run tee. I can't be much worse than that. --Mike--

In general Latexman is correct. The only case that I would use the pressure drop from the header to PSV instead of the entire pressure drop would be the case where the header PSV is set to protect downstream equipment and the header piping is rated to a higher pressure. However, I would still...

In Hyssys/Unisim I just run a case study using the turboexpander with a 100% efficiency. --Mike--

Due to the length of the relief pipe, the rupture disk cannot be sized using a discharge coefficient. The hydraulic capacity of the relief system needs to show that it is capable of relieving. In a two phase situation, a two phase flow correlation is needed. Lockhart Martinelli is one choice...

I have seen this described as: oil flow rate: 100,000 bopd MAX water flow rate: 50,000 bopd MAX Total fluid flow rate: 140,000 bopd As the water cut increases, oil production tends to decrease. However, at no time would the combined flow exceed 140,000 bpd. --Mike--

The bottom line is that the vessel may fail before the PSV lifts. The PSV size is irrelevant. Install a blowdown system to vent the vapors in the event of a fire. But if you really need to size the relief valve, you can run thermal expansion calculations at various temperatures to determine...

Without seeing a sketch, I'm assuming the feed to the pump is from the surge vessel. Dumping a pump PSV discharging back to its source tank is common and has no effect on the low pressure system. --Mike--

If there is no exposed flame, then there is no radiation. That's why enclosed flares are used in congested areas. However, if you are interested in plume temperatures, I would suggest using CFD models. This is especially true if you are looking for small temperature differences for helicopter...

Unless I'm mistaken, steam reforming natural gas produces carbon dioxide. For each 4 H2 molecule produced, there will be 1 carbon dioxide produced. In addition, this reaction is endothermic,which means that some of the hydrogen will have to used to produced the energy needed to sustain the...

One does not normally size an SDV. These valves are normally in line ball, plug, or gate valves. Their size is the pipeline size. The pressure drop is based on the flow and valve Cv. However, since these valves are shut down valves, when specifying the shut off differential pressure, use the...

If you can maintain the regulator inlet piping pressure spec on the 1/4" outlet segment and then transition to the final piping design pressure at the 1.5 inch line, then the pressure losses in the 1/4 inch section would not be included in the inlet pressure loss calculation. --Mike--

The two methods will create latent heat of vaporization (HoV) that differ by a factor of 5 to 10. The individual HoV will be in the range of 50 to 150 BTU/lb (see the chart in API 521). If you sum the weight fractions times the individual HoV, the number will still be in the range of 50 to 150...

Apetri: The method that you describe will end up treating the wide boiling mixture as a single component with a heat of vaporization in the range of 50-150 BTU/lb. However, in order to boil off any vapor, the temperature must rise. In wide boiling mixtures, the sensible heat can account for...

It is a first, not second law issue. The egg falling changes its potential energy to kinetic. The kinetic energy is then absorbed into the breaking of the egg. There is no energy left to reassemble the egg and launch it back to its original position. Even if the heat of breaking was...

See API Std 521 section 5.14 for details. --Mike--

I've always used this case as a basis for Flare Scrubber sizing unless a SIL analysis shows that the shutdown system is reliable enought to stop the flow once high level/pressure has been reached. Remember that the shutdown valves are probably the least reliable part of your shutdown. If the...

1. The Day Tank serves as a surge of fuel for start up and running during the loss of the diesel supply pumps. The time is project specific. Look at your basis for design. 2. The day tank is meant to gravity feed the fuel to the turbine diesel feed pump. In must be close, or at least above...

The valve must withstand the temperature of the flowing fluid. I have seen projects where flowing subsea wellhead temperatures reach temperatures close to 300°F. Given that subsea flowlines are routinely insulated, even the topsides arrival temperatures can be much higher than the ambient...

If I understand Bragamor correctly, both the PSV and the rupture disk are connected to the pressure source in parallel and both vent to the atmosphere. In this case the rupture disk would be sized for a massive, improbable relief flow while the PSV could be sized for the more expected cases...

Restarting is the big problem, especially since your valves cannot close fast enough to prevent the problem. Items 1, 2 and 4 are not barriers since they cannot stop the problem once the choke is opened. This leaves a simple operator error causing the problem. Double jeopardy is not an issue...