Complete Course on Pressure Vessel Engineering & Design as per ASME BPVC using PV Elite & Compress Software

A: Gauge range and location decide whether any pressure reading means anything. Option C feels tempting because everyone remembers the 1.3× MAWP number, but without a valid gauge you don't know what pressure you actually hit. Option D matters for code compliance, yet it doesn't invalidate a pressure hold if paperwork lags. Option B mixes up sequence; reinforcing pad leak tests come after hydro, but they don't govern whether the hydro itself was acceptable.

A: Hydro pressure scales MAWP by the ratio of allowable stresses. 1.3 × 20 × (152/138) lands at about 26.6 barg. Option B assumes 1.5× MAWP, a refinery habit that doesn't belong here. Option C forgets the stress ratio and under-tests. Option D applies the ratio but bumps the multiplier incorrectly, a slip that shows up often when someone mixes Div 1 memory with Div 2 habits.

A: SA-516 Gr.70 with NACE controls fits the pressure vessel rules and sour service damage mechanisms. Option B sounds right if your background is piping, but it's not a vessel plate material. Option C targets high-temperature hydrogen attack, which isn't the threat at 65°C. Option D resists corrosion, yet chloride stress cracking and cost make it a poor default for this duty.

A: A trapped liquid expands fast with temperature and has nowhere to go. Option D explains pressure rise, but only if a blanket exists and is connected. Option C is real, yet the rate is usually slow and small. Option B would show telltale chatter and loss, not a steady climb with no discharge.