During recent PHAs, it became clear that we were lacking protection on steam jackets for the scenario of external fire. Several clients have equiped their jackets with PSVs, however, the concern has been raised, that the relief valve may not provide adequate protection for a jacket as there is...
The formula from ASME Sec I, assumes a latent heat of 1000 BTU/LB. At low pressures, around atmospheric, this is a reasonable assumption, however, the heat vaporization drops as the pressure goes up. If you want to calculate a more accurate rate find the heat of vaporization at the relief...
Most likely, your relief pressure is based on the MAWP not the relief valve set pressure. That is not a standard, but I believe it is the approach most companies use.
By the way, the lower the relief pressure the lower the bobble point temperature will be. So, no, you can not lower your set...
First you need to determine your composition. You are going to have to ask for more information, maybe an MSDS or something. CH4+ is too vauge.
To determine if you are relieving vapor or liquid, you need to determine if the HC side is going to vaporize at your relieving pressure. If the...
I say you take the job, but keep looking.
Your number one priority is you and your family if you have one. It is NOT your problem to worry about him and his company. It is obvious his priority is himself or company and not his employees.
Do not let this guy guilt you in to staying at a job...
One thing to keep in mind is that internal PSV's are not inspected and maintained in most plants. Therefore, most of my clients chose to add external PSV's that can be inspected and maintained to ensure that if a blocked outlet were to occur, the equipment is protected.
From what I understand, usually only one tube is considered to break. It is not forbidden, but it may be too conservative.
The biggest problem with oversizing relief valves, is the cost. API recommends less than 3% inlet loss at capacity for all overpressure scenarios. If your valve is...
If you are a PE in a state that has lower standards, your license may not transfer. For example, where I work, we had several PE's from Texas who had been "grandfathered" in, meaning they didn't take the exam and used years experience instead. When they moved to Louisiana, they had to take the...
I add 15% additional wetted area to account for piping. This is based on a standard that one of our clients uses. If the piping is large, meaning 12" and above, I would try to do some more precise calculations.
I am a chemical engineer that graduated 3 years ago. My number 1 advice, it to get work in a plant or refinery. Unless, it is a matter of survival, I suggest that you not go into consulting.
I have been in consulting for 3 years now, and my experience is that every employer is looking for...
You are not right because the pressure on the outlet of your valve is not 5 ATM, that is your set pressure.
You can think of the relief valve as an orifice in a pipe. It will cause most of the pressure drop but not all. Therefore, the pressure at the outlet of your valve would equal the...
I don't think the pressure drop will be linear. It depends on your outlet piping. For example, there is a higher pressure drop at bends than straight pipe.
To find out where most of the pressure drop is, you need to calculate the pressure drop in the outlet pipe and then see which segments...
I have on occasion used this to take a scenario from 10% accumulation to a remote contingency and get 50% accumulation. Mostly overfilling scenarios on towers.
