Quality in Project

A: A: That's exactly the blocked outlet case the PSV sizing basis covers. Flow in, no flow out, pressure climbs, PSV opens. Fine. B: PSV only limits pressure. It doesn't stop liquid level rising or mist being dragged out. Different failure path entirely. C: Fire case is usually included in PSV design unless explicitly excluded. The valve lifts, pressure stays under MAWP. D: Full bore valve failure is a classic contingency in the relief scenario list. PSV sees it.

A: A: You're moving hardware before proving the measurement chain. Backwards risk order. B: Signal in, logic response, final element last. That isolates errors without process energy. C: Live pressure without confirmed scaling or trip action is how spurious trips get baked in. D: Continuity says nothing about polarity, scaling, or logic direction.

A: A: sqrt((700−5)/5) ≈ sqrt(139) ≈ 11.8. Times 0.107 lands around 0.29 m/s. B: Treats K as a velocity limit by itself. That's not how API 12J defines it. C: Inverts the relationship. That would penalize high liquid density the wrong way. D: Liquid density alone ignores gas inertia. Field failures come from that shortcut.

A: A: CO2 may be present, but H2S changes the chemistry and scale behavior. B: SSC needs tensile stress and hardness thresholds. Not automatic. C: Wet H2S plus water gives FeS films and general metal loss. Seen it many times. D: HTHA needs high temperature. 40°C doesn't get you there.