For oil/gas/petrochemical companies, the purpose of "Front End Engineering" is to do enough work to establish a cost estimate (to say a ± 10% certainty) and a detailed schedule. In parallel, their economists will try and determine the potential revenue. This is so they can determine whether to...
Like most things, the answer is "it depends". You need to consider what your perceived risks are and how far you are prepared to go to mitigate them. Examples to consider are:
individual tests you are undertaking on the compressors (performance test in addition to mechanical running test?)...
Contrary to one of the comments above, there is nothing wrong in engpes giving the molecular mass of methane as 16.043 g/mol, the mole is by definition the g mol. If using English (Imperial) units you state the molecular mass as 16.043 lb/lbmol - but the mole (g mol) and lbmol aren't the same...
I don't agree with the comment by BigInch above.
If the individual availability of a pump is 98% then the availability of the system will always improve with standby pumps in parallel. In the instance described in this thread of 3 x 50%, the system availability will be 99.74% if an individual...
For T2 and volumetric flow you need to get your thermodynamics books out.
However, in short to calculate the discharge temperature
T2=T1*r^((n-1)/n) where r is the pressure ratio
As you have the mass flow calculate the density at suction conditions from P1/(Z1*R*T1) where R is the Gas...
My stock answer to questions like this is "it depends".
Often the practice in Europe is to make the compressor vendor prime (but not always) whereas in the US the GT vendor is often prime (but again, not always). One party does need to take responsibility for the train and this can be done by...
As zdas04 said, you need to estimate the power on a stage by stage basis (I normally use polytropic equations, but as it is air, then adiabatic is OK). This gives you the "gas power". You need to add on an allowance for mechanical losses (bearings, seals). This will give you an estimate for...
I'd encourage you to develop your own rather than trying to take somebody elses spreadsheets if only to develop your understanding of the theory (like doing a hand calculation). They can be quite useful for studies when you can quickly see the effect of say changing the suction temperature. I...
The various gas turbine suppliers have differing fuel gas quality specifications, but the temperature requirement is generally around 28°C (50°F) above the hydrocarbon and water dewpoints at the supply point to the package (skid edge).
You want to minimise the inventory held between 3 points
1. Compressor discharge check valve
2. Anti-surge recycle valve (take-off for this, as pmover said, to be upstream of the discharge check valve)
3. Compressor discharge flange
If this inventory isn't minimised the anti-surge control system...
Solar's compressors are for natural gas (you didn't stipulate the product).
Solar aren't that renowned for their high pressure experience - they aren't in the "custom engineered" business and most of their experience is at lower pressures. I would get references for any conditions you are...
Assuming this is a centrifugal machine, the theoretical torque demand is proportional to the square of the speed (rpm). However, theory doesn't apply from say 0 to 25% speed - there is a "stiction" effect to overcome - you need to get the rotor moving. The vendor torque-speed curve should look...
