Dear all,
I am using TANKS EPA software to estimate the emissions of a storage tank farm but I am facing two problems I don't know how to handle.
- I am using internal floating roof tanks with nitrogen blanketing in the space between the floating cover and the fixed roof. How does it affect the...
Dear all,
I am looking for any book or document providing corrosion rates (mm/year) for different services depending on the pipe material used (it is for a general study, so I am not looking for only one specific fluid).
Do you know of any good source?
Best regards and thank you for your help.
The event we usually simulate is the quick closure of the turbine stop valve.
I think that we need a software that can handle both compressible and incompressible flows but not necessary two-phase flow.
Regards
Thank you.
In fact I was focusing on BOS Fluids and Pipenet Transient (by Sunrise). The price difference between them is high.
Any expereince using these softwares? Advantages or disadvantages?
Anyone know which is the leader in this type of products?
Regards
Hi all,
I am looking for a software to simulate fluid transients (mainly water and steam hammer in CCPP) with the following main features:
- Valid for compressible and incompressible simulations.
- With capabilities to define unbalanced forces in piping system (for a subsequent time-history...
Dear all! I am trying to estimate the losses (standing, working) of a floating roof tank using EPA Tanks software. In my case the storage tank receives gasoline from process units at a normal temperature of 35ºC, so the gasoline will cool down until its unloading to tankers. I have estimated...
Thank you for your help. For flashing losses I refer to the losses which occur when a hydrocarbon goes from a higher to a lower pressure. I attach a link to a web explaining that:
www.deq.state.ok.us/factsheets/air/CalculationLosses.pdf
Do they happen at refineries?
Regards
Dear all,
I am preparing an initial report describing the emissions due to storage tanks (crude, intermediate products, final products) in refineries. I am considering working and standing losses and I am looking for information about flashing losses but everything I find regards to Exploration...
Dear all,
I am looking for any method to estimate the pressure variation inside a closed pressure vessel which is initillay filled with, for example, propane, at atmospheric temperature, when the liquid is taken out from it by means of a pump.
As far as I know, at a first stage, the propane...
Dear all,
I have a doubt regarding the most suitable type of tank (technically, economically) to storage products with a vapor pressure at the storage temperature close to the atmospheric (80 kPa<TVP<150 kPa). In this case, as far as I know floating roof tanks are not suitable so I suppose...
Sorry, perharps I misunderstood the discussion.
Sshep said in a previous post that "When the partial pressure of LPG vapor is zero, you can't calculate the minimum liquid temperature from the total pressure". I understood that he wanted to mean that in case of liquid propane discharging to a...
I would like to calculate the resulting temperature when discharging a liquid LPG from a pressure storage to the atmosphere since it is not the saturation temperature at the discharge pressure, according to above posts. Any idea, documentation, web, book... which could help?
Moreover, I...
According to your simulations the HC content at vapor phase at 1000 psig would be 2% whereas at 500 psig would be 2,5%. So, when there was an increase in the liquid level of the tank of, for example, 1 m3, it would be expelled 1 m3 of the vapor. Since the vapor of the tank at 1000 psig has a...
Hello and thank your for your answer.
There are a couple of things I am afraid I don't understand very well:
- You mention that the liqid phase will be 5% N2. Does it mean that some nitrogen can become liquid or what you mean is that it is dissolved in the HC liquid?
- In your example at 1000...
