Adequacy check of existing relief devices (2No. 8T10s set @17.7 barg; conventional)for LPG storage spheres confirms they are grossly oversized in the event of governing external fire scenario.
Using API model I calculated relief load of 79,833 kg/hr. Relief fluid z factor is around 0.6691...
Regarding flare stack sizing using the simple approach in API 521, has anyone accurately determined the linear equation for Figure F.1 - Flame Length vs Heat Release - Industrial Sizes & Releases (SI units) and the nonlinear equation for Figure F.3 - Approximate Flame Distortion Due to Lateral...
We are currently designing a pressure regulating/let-down package for a natural gas pressure regulating and metering station (RMS) that consists of an active regulator, a monitor regulator and a safety shut-off valve (SSV) connected in series - in the direction of flow the SSV comes first, then...
So I am developing a first-principles model involving the combustion of a natural gas fuel source containing both nitrogen and CO2.
And even though this is quite basic, I have struggled with writing a balanced equation for the combustion of this fuel source with excess air, especially with the...
We are currently engaged in a conceptual study for a Natural Gas Pipeline Gas Turbine Driven Centrifugal Compressor Facility.
The overall compression ratio is 2.614. Even though the discharge temperature is below the limits commonly imposed for per stage, I am considering 2 preliminary concepts...
In using Aspen Flare System Analyser can anyone share how to force a certified rated capacity to flow from a fire case relief valve instead of the required relieving load. I am evaluating the flow properties of an existing flare system pipework.
In trying to determine an accurate latent heat of vapoourisation for an LPG tank exposed to an open pool fire, I recently came across this procedure (see link below) to determine the latent heat of vapourisation for multi-component mixtures using Aspen HYSYS.
Title: Determine Latent Heat for...
Here goes...
Having sized a fire case (Max. Accumulation = 1.21 x MAWP) relief valve using API 520 equations.
I selected a preliminary API 526 orifice size; in this case a "T".
I obtained the manufacturer's actual orifice area (which was larger than the API 526 orifice area) and the...
I'm currently applying the Lee-Kesler EoS to calculate enthalpy departure but I have run into problems applying the mixing rules mostly because different approaches are used in literature.
All the other formulas (Zci, vci and w and Pc) are straightforward except the critical molar volume (Vc)...
What is the best approach for sizing Pressure Safety Valves for 4No. LPG tanks connected to each other by a Pressure-Equalization line. The balancing line from each sphere connects to a common header. Each line from a Sphere has a Fail Close on/off ball valve which is to remain open during...
I am reviewing the sizing of a PSV for a pentanes product storage tank.
Current PSV Size: 3K4
Set Pressure: 3.4 barg
Maximum allowable Backpressure: 0.29 barg [1.30 bara]
Vessel data
ID = 2.5 m, Ls/s = 10.9 m, Liquid depth = 2.63 m, elevation = 1.2 m and so I am calculating wetted area to...
I'm not clear on this issue...share your thoughts to enable me clear up this issue..
My thought is this...from the laws of conservation of mass and energy...when a restriction is created on the flow path of a fluid, pressure reduces, velocity increases and density reduces as well so that both...
I would like to verify the adequacy of an existing inlet Separator for a Gas plant receiving gas from an offshore pipeline. An offshore FPSO exports raw gas through this pipeline to the plant. The FPSO is fitted with a production separator and in addition it carries out dehydration using TEG...
I am currently verifying whether a 3-phase separator inlet nozzle is undersized or not based on momentum sizing criteria.
Now, the inlet device in question is an inlet diverter/deflector.
In the Shell DEP and Norsok standards for momentum sizing criteria, an inlet deflector is not mentioned...
