- Defines the suction and discharge conditions (P,T, Flowrate) and gas composition.
- Main input to the compressor vendor.
- Define all possible options of suction and discharge conditions and gas compositions, present and future.
- The vendor selects the model which fits these conditions the best.
Compressor performance curves:
- Input from the compressor vendor
- Relationship of Flow vs. Head (polytropic, isentropic)
- Surge point and choking (stone wall)
- Variation with RPM
- Input to HYSYS for generation of performance at different conditions
- Input from compressor vendor.
- Defines the interstage pressures and temperatures.
- Gives input for the HYSYS simulation.
- HYSYS simulation model
- Based on the Compressor performance data
- Forms the basis for material and energy balance.
- Defines the cooler heat duty.
- Generates property data for the calculations.
- Compressor and Motor
- Coupling (e.g. Voith)
- Lube oil System
- Seal oil / Seal gas system
- Piping and Instrumentation
- Air Coolers
Advantages Seal gas system:
- No seal oil system required
- No need to dispose/clean up contaminated oil
- Eliminates fouling problems due to oil ingress in process streams
- Less gas loss
- The dry gas seal advantages significantly outweigh the seal oil benifits
- Settle out Calculations
- Blowdown calculation
- Pipe sizing calculations
- Hydrate calculations
Settle out calculation:
- Equalised pressure during a compressor shutdown.
- High pressure trip conditions taken as pressures before settle out.
- Enthalpy balance of the system.
- Can be done using spread sheet or HYSYS.
- Can define the design pressure for some of the sections.
- Intent: Reduce the pressure of the equipment to 50% of design pressure within 15 minutes during a fire emergency.
- Typically done using Dynamic depressurising Utility in HYSYS
- Relief valves are not a depressurisation device.
- Ball valve + Orifice combination OR control valve
The blow down calculation takes the following into account:
- Vaporization of liquid due to pressure reduction,
- Vaporization due to heat input from the external fire,
- Pressure after 15 minutes is reduced from design pressure to 50% of design pressure,
- Start at settle out conditions.
- Gas compressor system is blocked in and no additional mass is fed into the system during blow down.
- Maximum allowable depressurization rate for the compressor O-rings of 20 bar/min,
- There is no other heat input into the system other than fire.
- The relief rate calculated is not limited by the flare.
- Use to find the lowest temperature attained and hydrate formation possibilities.
- Uncontrolled vs. Staged Blowdown
Pipe sizing calculations:
- Importance of pressure drop and machine performance.
- Tools used.
- Cooler header sizing.
- Avoiding loops in suction.
- Provision of drain boots.
- Hydrates are ice-like non-stoichiometric crystal structures composed of water molecules encaging natural gas molecules.
- Solid formation, chokes piping.
- Flow problems.
- Formation depends on P,T conditions and composition.
- Predicted by HYSYS.
Gas Blowby calculations:
- Caused by loosing liquid level in the scrubbers.
- High pressure gas flows into the low pressure system potentially over pressurising it.
- Calculations are done to ensure that the downstream system is adequately protected.
- The control valve is considered to be fully open during this case.
- The highest operating pressure of the upstream system is considered for sizing.
- Vertical Knock out vessels.
- Limit liquid carry over to the compressors.
- Internals – SMS / SV / SVS
- Heat duty based on Process Simulation.
- Process parameters based on the simulation.
- Vendor does the sizing with HTRI or other proprietary software.
- Pressure drop is critical.
Flare and Blowdown system:
- The flare system needs to be designed for
- Blowdown depressurising load.
- Flaring due to compressor trip
- Fire case relief
- Blocked discharge of the compressor
- The flare system may require a KOD based on the quality of gas flared. (Liquid presence)
- Capacity control
- Antisurge control
- Scrubber level control
- Process shutdown.
- Emergency shutdown.
- Other shutdowns.
- Close the discharge ESD valve. The suction ESD valve shall remain in open position. The blowdown ESD valve shall remain in closed position. The antisurge valves and capacity control valve goes to open position. The motor stops and the compressor settle out to suction pressure. The auxiliaries keep running.
- Generally initiated on trips on process parameters.
- Enables faster start-up compared to ESD
- PSD1 shall Trip the compressor motor & auxiliaries, and Close the ESD valve on the suction and discharge header.
- The antisurge valves and capacity control valve goes to open position.
- The external seal gas supply shall be isolated by the ESD valve on the seal gas line.
- The compressor blowdown valves shall open and depressurise the gas to flare.
- Initiated on Fire, Station ESD.
- The suction, inter-stage(s) and discharge scrubbers low low level closes liquid outlet ESD valves.
- The inter-stage(s) and After-cooler fan high vibration shall trip the respective fan.
- Low Low temperature at the after cooler outlet shall trip the first working fan at 30 deg C and the next at 20 deg C.
- External seal gas high high pressure downstream of external seal gas pressure letdown valve for LP casing shall close the external seal gas supply ESD valve.