🌊 Two-Phase Flow Patterns & Lockhart-Martinelli

Calculate two-phase liquid-gas pressure drop using Lockhart-Martinelli parameter (X) and Chisholm multiplier (phi2), void fraction, liquid holdup, and Baker flow regimes.

⚡ Fortran 90 Engine Double Precision (IEEE 754) ✓ ISO / ASME Validated
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⚡ Calculs faits 31
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📅 Mise en service Jun 2026
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🌊 Two-Phase Liquid-Gas Flow Patterns & Frictional Multiplier

Real-time visual simulation: Pipeline flow regime dynamics (Slug, Annular film, Bubbly, Stratified)

📝 Configuration & Presets

♨️ Steam-Water Boiler (x = 0.20) 🛢️ Subsea Oil-Gas Slug (500m) ❄️ R134a DX Evaporator Tube 💨 Gas-Condensate Annular Film
⚡ Flow Conditions & Vapor Quality
📏 Pipe Geometry
🧪 Phase Densities & Viscosities
Lockhart-Martinelli & Chisholm Formulation:
• Martinelli Parameter: X = √[ (dP/dL)L / (dP/dL)G ]
• Two-Phase Multiplier: ϕL² = 1 + C / X + 1 / X² (C = 20 for turbulent-turbulent)
• Two-Phase Frictional Drop: (dP/dL)tp = ϕL² · (dP/dL)L
• Void Fraction: α = 1 − εL (Butterworth holdup model).

📊 Two-Phase Results

Configure inputs and click Compute to view results.

📘 Calculation Methodology & Two-Phase Flow Standards

Lockhart-Martinelli & Chisholm Correlation

Relates the two-phase frictional pressure drop to single-phase liquid flow via multiplier $\phi_L^2 = 1 + C/X + 1/X^2$. The Chisholm parameter $C$ accounts for turbulent/viscous phase interactions.

Flow Pattern Regimes (Baker / Taitel-Dukler)

Identifies slugging risks in subsea oil-gas tiebacks, dryout in steam boilers, and liquid droplet entrainment in evaporators as a function of vapor quality and superficial velocities.

Key Engineering Assumptions

  • Separated two-phase flow formulation with empirical liquid holdup.
  • Smooth or commercial pipe friction factors for liquid and gas streams.
  • Applicable to oil-gas pipelines, refrigeration evaporators, and nuclear steam generators.