Guide
Tank Strapping Tables: Level-to-Volume Without Mistakes
Strap vertical tanks with pi/4 D^2 h, horizontal tanks with the fill-factor table, add 2:1 SE heads, and time transfers with t = V/Q.
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Worked examples for process engineering.
Hand calculations you can reproduce: valve sizing, head loss, NPSH, metering, tank strapping, and loop checks.
Guide
Orifice and Venturi Flow: Reading dP the Right Way
Read flow from differential pressure with a calibrated factor Q = C sqrt(dP/rho), then verify beta, straight runs, and density compensation.
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Pump Affinity Laws: What Changes When Speed Changes
Scale duty with speed: Q with N, H with N squared, P with N cubed. Re-intersect the system curve and recheck motor, NPSH, and shutoff.
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NPSH Explained: Why Pumps Cavitate and How to Keep Margin
NPSHa = (P_suction - P_vap) x 10.2 + static head - suction loss. Hold margin above NPSHr of at least 1 m or redesign suction.
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Pipe Sizing Rules of Thumb: Velocity Limits by Service
Keep water-like liquids at 1-2.5 m/s, suction below discharge velocity, and confirm regime with Reynolds before any loss calculation.
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Darcy-Weisbach Worked Example: From Re to Friction Loss
Chain velocity to Reynolds to friction factor to drop: water at 1.27 m/s in DN100 gives Re 127000, f 0.0167, and 0.135 bar over 100 m.
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Control Valve Sizing in 10 Minutes: Cv, dP, SG Workflow
Size liquid control valves in four steps: fix design flow and valve dP, compute required Cv, convert Cv/Kv with margin, and recheck drop, noise, and cavitation.
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Why Valve Opening % Is Not Flow % (And What to Enter Instead)
Valve opening % sets stem travel, not flow %. Flow follows the trim characteristic Cv(h) and the pressure drop available at that opening. Estimate flow only with datasheet curve data.
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