Gas / Vapour Properties
g/mol
MW ref: CH₄=16.04 · C₂H₆=30.07 · C₃H₈=44.10 · C₄H₁₀=58.12 · Air=28.97 · N₂=28.01 · CO₂=44.01 · H₂S=34.08 · H₂=2.02 · Steam=18.02 · Nat.Gas≈17–19
barg
°C
—
Ideal gas Z=1.0 · HC gas: 0.80–0.95
mPa·s
Calculated ρ_G = P·M / (Z·R·T)
—
kg/m³
Liquid Properties
kg/m³
mPa·s
Pipe Selection — ASME B36.10M
mm
Carbon steel=0.046 · Stainless=0.015 · HDPE=0.007
Flow Conditions
m³/h
Mass Flow ṁ = ρ × Q
—
kg/h
Design Criteria & Pipe Length
m/s
Liquid: 1–3 m/s typical
bar/100m
m
m
Fittings & valves equiv.
m
Positive (+) = upward flow · Negative (−) = downward · 0 = horizontal
📐 Formula Reference
ρ_G = P·M / (Z·R·T) R=8.314 J/mol·K
V = Q / (π/4·ID²) [m/s]
Re = ρ·V·D / μ → Colebrook-White → f
ΔP/L = f·ρ·V² / (2D) [Pa/m]
X_LM = √(ΔP_L/ΔP_G) · φ²_G = 1 + C·X + X² (gas mult.)
φ²_L = 1 + C/X + 1/X² (liq. mult.) · C: tt=20 vt=12 tv=10 vv=5
── API RP 14E (Two-Phase) ──
ρ_m = (12409·S_l·P + 2.7·R·S_g·P) / (198.7·P + R·T·Z) [lb/ft³ × 16.02 → kg/m³]
P=psia · T=Rankine · R=GOR (scf/stb) · S_l=liq SG · S_g=gas SG
V_e = c × 1.22 / √ρ_m [m/s] · c per API RP 14E Table
c=100 (corrosive·cont.) · c=125 (corrosive·int.)
c=150–200 (non-corr./CRA·cont.) · c=250 (non-corr.·int.)
V = Q / (π/4·ID²) [m/s]
Re = ρ·V·D / μ → Colebrook-White → f
ΔP/L = f·ρ·V² / (2D) [Pa/m]
X_LM = √(ΔP_L/ΔP_G) · φ²_G = 1 + C·X + X² (gas mult.)
φ²_L = 1 + C/X + 1/X² (liq. mult.) · C: tt=20 vt=12 tv=10 vv=5
── API RP 14E (Two-Phase) ──
ρ_m = (12409·S_l·P + 2.7·R·S_g·P) / (198.7·P + R·T·Z) [lb/ft³ × 16.02 → kg/m³]
P=psia · T=Rankine · R=GOR (scf/stb) · S_l=liq SG · S_g=gas SG
V_e = c × 1.22 / √ρ_m [m/s] · c per API RP 14E Table
c=100 (corrosive·cont.) · c=125 (corrosive·int.)
c=150–200 (non-corr./CRA·cont.) · c=250 (non-corr.·int.)
Enter input data on the left and click ▶ CALCULATE to see results.
Supports: Single Phase Liquid · Single Phase Gas/Vapour · Two-Phase Gas+Liquid
Supports: Single Phase Liquid · Single Phase Gas/Vapour · Two-Phase Gas+Liquid
Single Phase
Total Pressure Drop
—
bar (total pipeline incl. fittings)
Velocity
—
m/s
ΔP / 100m
—
bar/100m
Reynolds No.
—
Friction f
—
Mass Flow
—
kg/h
Flow Regime
—
Calculation Breakdown
| Parameter | Value | Unit |
|---|
Two Phase — Gas + Liquid
Flow Regime
—
—
Flow Pattern
Two-Phase ΔP / 100m
—
bar/100m
Gas ṁ_G
—
kg/hLiquid ṁ_L
—
kg/hj_G / j_L
—
m/sBaker λ / ψ
—
Martinelli X_LM
—
Chisholm φ²_G
—
ΔP_G / 100m (gas only)
—
bar/100mΔP_L / 100m (liq only)
—
bar/100mGas Density ρ_G
—
kg/m³Mix. Density ρ_m (API Eq.2)
—
kg/m³Erosional V_e (c=—)
—
m/sΔP_static (elevation)
—
barTOTAL ΔP (friction + static)
—
barTwo-Phase Calculation Breakdown — Step by Step
Churchill (1977) friction · Szilas (1975) Baker parameters · Chisholm (1967) multiplier · API RP 14E erosion
| Parameter | Value | Unit |
|---|
Baker Flow Regime Map & Illustrations — Baker (1954) · Horizontal Pipeline
Baker Chart — Operating Point (●) · B_x = G_L/(λ·ψ) vs B_y = G_G·λ [kg/m²s]
All Flow Regime Illustrations — Highlighted = Current Operating Regime
Light blue = gas phase · Blue = liquid phase · Dark dots = liquid droplets · Flow: left → right