Career in EPC projects for Freshers

A: Option A feels right because thermal expansion is a classic fresher trap, but a PSV on the vapor space will usually see that pressure rise unless the liquid is fully trapped. Option B is exactly what the PSV was sized for, so it does protect against that. Option D also seems plausible since level failures are common, but the PSV still limits vapor pressure regardless of level control performance. Option C breaks down because compressor surge is a dynamic upstream phenomenon; the PSV on the separator doesn't protect exchanger tubes or upstream equipment from surge-induced overpressure.

A: Option A looks tempting because many people stop at hydraulic power, but that ignores efficiency, which matters at EPC review. Option B mixes in temperature effects that barely move density enough to halve the power. Option D sounds like something an EPC contractor might oversize, yet margins don't triple the requirement. Option C lands near the correct value once flow, head, gravity, and efficiency are handled on the same basis.

A: Option A feels logical because stroke time matters, but it's usually confirmed during SAT or functional testing. Option B sounds thorough, yet temporary flow testing is rare and unsafe at this stage. Option D jumps too far ahead; PLC logic isn't meaningful until basic field correctness is locked. Option C is boring but deadly if missed—wrong orientation or fail action survives FAT and only shows up when you energize the loop.

A: Option A is tricky because placement height matters, but detectors can still catch buildup if designed well. Option B seems dramatic, yet detectors often alarm even during fast releases if the cloud passes them. Option D is a real concern, but detectors don't care where the gas came from. Option C fails because tiny flange leaks may disperse without ever reaching detector threshold, so the safeguard never actuates.