Hi,
I have a pump which is going close to over load current for a prolonged period during start up when the pump is running at low flow. Other than flow, what can be causing the high current?
Thanks.
I have a 6" line with a 3" control valve installed on it. Pump min flow recycle with continuous recycle flow. Crude oil service.
When i do line sizing, 6" line velocity is below the erosional velocity limit, but the 3" line is well above it. The 3" line is only the redcers for the control...
Are there any cases where it is unacceptable to leak test the downstream flange of a PSV i.e. can a relief valve be damaged by an artificially high back pressure due to leak testing?
I'm not proposing to leak test in excess of the flange rating but leak testing will mean that the downstream...
We are running a centrifugal gas compressor train (x 3 compressors in series).
The compressors were designed for gas MW of 23. Due to a change in gas composition, we may need to periodically operate the compression train on gas with MW 17.5.
We have confirmed that the compressors can...
My gas sweetening plant was designed to run with 50% wt amine solution. I'd like to increase concentration to 70% wt amine (the reason for this change is not important for this query).
Other than higher frictional losses due to higher viscosity, are there are other issues with operating my...
In a gas blow by relief case where level is lost in a two phase vessel allowing gas to flow via the LCV, I normally size the PSV for the gas rate via the 100% open LCV.
If the liquid displaced pre gas blow has significant amount of flashing in the LP vessel, is it possible to say with certainty...
I have a vessel with lots of large bore liquid pipework within a fire area.
I want to confirm the correct option for gire heat input as per the API 521 equation. Is it
Option 1: calculate total wetted surface area then do A^0.82
Or
Option 2: calculate A^0.82 for all pipes and vessels...
What discharge coefficients are recommended for low pressure tank PSVs when designed to API 2000?
This is for preliminary sizing. Service is gas. For API 520 I'd use 0.975 but not sure this applies to an API 2000 psv.
Thanks.
I have a demethanizer column and im sizing the psv for the blocked vapor outlet case.
Ive simulated the scenario in hysys with max reboiler duty allowed for in the model.
Is steady state simulation the correct approach for this scenario?
Thanks.
I have a heat exchanger with a PSV on the cold side. My scenario is control valve failure on the hot side sending more hot fluid via the exchanger than is quoted on the data sheet.
Is there a simple way for me to estimate worst case heat transfer rate to the cold side for this scenario?
Thanks.
I'm sizing a PSV for a dense phase fluid. It will enter the PSV as dense phase but will become two phase leaving the PSV.
What discharge coefficient should I use for preliminary PSV sizing. Based on API 520 Part 1 guidance I'm unsure whether to use 0.975 (gas) or 0.85 (two phase).
Thanks.
I have a centrifugal pump. It cannot overpressurise the discharge in a dead head (no flow) scenario. Do I need to provide a PSV for fire relief?
Thanks.
I have a diesel genset / diesel engine that will be located in a fire rated enclosure.
Generally, you do not get diesel fires. However, in the diesel engine temperature will be high. Is it possible to get an explosion in the enclosure due to the diesel fuel being ignited by a failure in the...
I have an offshore platform.
Gas lifted well with lift gas in the 'A' annulus. If the production tubing suddenly & catastrophically fails, the wellhead will be rapidly pressurised to gas lift pressure. The rate of flow across the production choke will be massive with gas lift pressure...
I'm sizing a vertical two phase separator (hydrocarbon gas / water). The vessel will not have a gas outlet mist eliminator.
What height should i allow above my vessel's max liquid level to ensure adequate liquid disengagement from the gas leaving the vessel's gas outlet?
Thanks.
I have an existing overboard dump caisson which sends produced water from an offshore platform overboard.
I'm increasing the water rate to this caisson. The new rate will exceed the Froude No. 0.3 limit as per Norsok P-001 but the line size meets all other sizing criteria typical for...
I have a new vessel with a range of relief cases. I'm proposing to install a single conventional PSV.
The governing case is gas blow by. For the fire case, the relief load is less than 25% PSV capacity so i believe chatter may be a risk for the fire case (as per guidance in API 521)...
I have a water vessel and a gas blow by relief case.
I have a cold gas blow by relief stream at -20oC. To reach the PSV the relief stream must pass through stagnant water in the vessel (1 m id x 2 m height). The water is initially at 20oC. The relief load of cold gas is around 15,000 kg/h...
How can i calculate the vapour pressure of produced water leaving an offshore production separator. My process simulator predicts it to be as per pure water but I'm not convinced that the somulator is accounting for dissolved gases.
Thanks.
