TwoFluidPipe Model Documentation

Overview

The NeqSim TwoFluidPipe model implements a transient two-fluid multiphase flow solver for pipeline and riser simulations. It solves separate conservation equations for gas and liquid phases, enabling accurate prediction of:

This document provides comprehensive documentation of the model’s capabilities, governing equations, and usage.

Conservation Equations

Mass Conservation

Separate mass conservation equations for gas and liquid phases:

Equation Mathematical Form Description
Gas mass ∂(αG ρG)/∂t + ∂(αG ρG vG)/∂x = ΓG Gas phase continuity with mass transfer
Liquid mass ∂(αL ρL)/∂t + ∂(αL ρL vL)/∂x = -ΓG Liquid phase continuity with mass transfer
Mass transfer ΓG Flash-based calculation Evaporation/condensation with optional kinetic limits

Where:

Momentum Conservation

Separate momentum equations for each phase:

Component Implementation
Gas momentum Full 1D momentum with wall shear, interfacial shear, pressure gradient
Liquid momentum Full 1D momentum with wall shear, interfacial shear, pressure gradient
Wall friction Pipe roughness-based (Colebrook/Blasius correlations)
Interfacial friction Flow-regime dependent correlations

Energy Conservation

Feature Description
Mixture energy equation Full energy balance including kinetic and potential terms
Joule-Thomson effect Enabled by default for accurate temperature prediction
Multi-layer heat transfer RadialThermalLayer and MultilayerThermalCalculator classes

Flow Regime Detection

The flow regime detector uses Taitel-Dukler transitions:

Regime Detection Criteria Status
STRATIFIED_SMOOTH Low gas velocity, stable interface ✅
STRATIFIED_WAVY Kelvin-Helmholtz instability criterion ✅
SLUG Liquid bridging criterion ✅
ANNULAR Weber number > 30 ✅
CHURN Transition between slug and annular ✅
BUBBLE High liquid fraction, low gas velocity ✅

Holdup Correlations

Minimum Holdup Configuration

The model enforces a minimum liquid holdup to prevent unrealistically low values in gas-dominant systems. By default, an adaptive minimum is used that scales with the no-slip holdup, making it suitable for both lean gas and rich condensate systems.

Configuration Methods

Method Default Description
setUseAdaptiveMinimumOnly(boolean) true Use correlation-based minimum only
setMinimumLiquidHoldup(double) 0.001 Absolute floor (when adaptive-only = false)
setMinimumSlipFactor(double) 2.0 Multiplier for no-slip holdup
setEnforceMinimumSlip(boolean) true Enable/disable minimum constraint

Lean Gas Systems

For lean wet gas (< 1% liquid loading), use adaptive-only mode:

pipe.setUseAdaptiveMinimumOnly(true);  // Default
pipe.setMinimumSlipFactor(2.0);
// Minimum holdup = lambdaL × 2.0 = 0.6% for 0.3% liquid loading

Rich Condensate Systems

For rich gas condensate (> 5% liquid loading), either mode works:

// Option 1: Adaptive (recommended)
pipe.setUseAdaptiveMinimumOnly(true);

// Option 2: Fixed floor (OLGA-style)
pipe.setUseAdaptiveMinimumOnly(false);
pipe.setMinimumLiquidHoldup(0.01);  // 1% floor

Minimum Holdup Correlations

The adaptive minimum uses Beggs-Brill type correlations:

Flow Regime Correlation Exponents
Stratified αL = 0.98 × λL^0.4846 / Fr^0.0868 Segregated flow
Slug/Churn αL = 0.845 × λL^0.5351 / Fr^0.0173 Intermittent flow
Annular Film model + 1.065 × λL^0.5824 / Fr^0.0609 Distributed flow

Where λL = no-slip liquid holdup, Fr = Froude number = v²/(g×D)

Stratified Flow Holdup

The calculateStratifiedHoldupMomentumBalance() method calculates liquid holdup from momentum balance:

Holdup = f(τwG, τwL, τi, ∂P/∂x, geometry)

Implementation features:

Velocity-Dependent Slip Model

The model captures liquid accumulation at low velocities using Froude number correlation:

// Slip ratio as function of mixture Froude number
double baseSlip = 3.0;
double maxSlip = 25.0;
double exponent = 0.85;
double slip = baseSlip + (maxSlip - baseSlip) * Math.exp(-exponent * Frm);
Parameter Value Physical Meaning
baseSlip 3.0 Minimum slip at high velocity
maxSlip 25.0 Maximum slip at near-zero velocity
exponent 0.85 Velocity sensitivity factor

Terrain Tracking

Terrain Effects Model

The applyTerrainAccumulation() method implements terrain-induced multiphase flow effects:

1. Low Point Liquid Accumulation

Uses Froude number criterion (Fr < 0.5 indicates accumulation):

double Fr_liquid = vL / Math.sqrt(g * diameter * (rhoL - rhoG) / rhoL);
if (Fr_liquid < 0.5) {
    // Calculate accumulated volume based on velocity deficit
}

2. Riser Base Severe Slugging

Detects severe slugging potential using Pots criterion:

double pi_ss = (inletPressure - outletPressure) / (rhoL * g * riserHeight);
if (pi_ss > 1.0) {
    // Severe slugging potential flagged
}

3. Uphill Liquid Fallback

Uses Turner droplet model for critical gas velocity:

double vG_critical = 3.0 * Math.pow(sigma * g * (rhoL - rhoG) / (rhoG * rhoG), 0.25);
if (vG < vG_critical) {
    // Liquid fallback occurs
}

4. Downhill Drainage

double drainageRate = Math.sqrt(2 * g * dz * holdup);

Multi-Layer Thermal Model

New Classes

  1. RadialThermalLayer - Represents a single thermal layer with material properties
  2. MultilayerThermalCalculator - Calculates U-value and transient heat transfer

Supported Layer Materials

Material k [W/(m·K)] ρ [kg/m³] Cp [J/(kg·K)]
Carbon Steel 50.0 7850 480
FBE Coating 0.3 1400 1000
PU Foam 0.035 80 1500
Syntactic Foam 0.15 650 1100
Aerogel 0.015 150 1000
Concrete 1.4 2400 880

Usage Example

TwoFluidPipe pipe = new TwoFluidPipe("subsea-export", inletStream);
pipe.setLength(20000.0); // 20 km
pipe.setDiameter(0.254); // 10 inch
pipe.setWallThickness(0.015);
pipe.setSurfaceTemperature(4.0, "C"); // Cold seabed

// Configure with 50mm PU foam + 40mm concrete
pipe.configureSubseaThermalModel(0.050, 0.040, 
    RadialThermalLayer.MaterialType.PU_FOAM);

// Set hydrate formation temperature
pipe.setHydrateFormationTemperature(20.0, "C");

// Calculate cooldown time
double cooldownHours = pipe.calculateHydrateCooldownTime();
System.out.printf("Cooldown to hydrate: %.1f hours%n", cooldownHours);

// Run simulation
pipe.run();

// Get thermal summary
System.out.println(pipe.getThermalSummary());

Thermal Calculations

Model Capabilities Summary

Category Feature Method/Correlation
Conservation Equations    
Gas mass Full continuity equation Flash-based mass transfer
Liquid mass Full continuity equation Flash-based mass transfer
Gas momentum 1D momentum balance Wall and interfacial shear
Liquid momentum 1D momentum balance Wall and interfacial shear
Mixture energy Full energy balance Optional J-T effect
Closure Models    
Stratified holdup Momentum balance Taitel-Dukler geometry
Annular holdup Film model Ishii-Mishima entrainment
Slug holdup Empirical correlation Dukler correlation
Interfacial friction Flow-regime specific Multiple correlations
Terrain Effects    
Low point accumulation Froude criterion Fr < 0.5 triggers accumulation
Riser base slugging Pots criterion πSS > 1.0 indicates severe slugging
Uphill fallback Turner model Critical gas velocity check
Thermal Model    
Multi-layer heat transfer Series resistance RadialThermalLayer class
Cooldown calculation Lumped capacitance MultilayerThermalCalculator
Hydrate/wax risk Temperature tracking Section-by-section monitoring
Numerical Methods    
Time stepping CFL-based Fixed step with sub-cycling
Spatial discretization Finite volume Upwind scheme

Validation Status

Implemented Tests

Integration Tests (TwoFluidPipeIntegrationTest)

Validation Tests (TwoFluidPipeValidationTest)

Beggs-Brill Correlation Comparison:

Pipeline Scenario Validation:

Terrain-Induced Slugging Patterns:

Test Coverage Summary

Test Category Tests Status
Integration Tests 24 ✅ All passing
Validation Tests 13 ✅ All passing
Total 37 ✅ All passing

References

  1. Bendiksen, K.H., Maines, D., Moe, R., & Nuland, S. (1991). “The Dynamic Two-Fluid Model OLGA: Theory and Application.” SPE Production Engineering, 6(02), 171-180.

  2. Taitel, Y., & Dukler, A.E. (1976). “A model for predicting flow regime transitions in horizontal and near horizontal gas-liquid flow.” AIChE Journal, 22(1), 47-55.

  3. Pots, B.F.M., Bromilow, I.G., & Konijn, M.J.W.F. (1987). “Severe Slug Flow in Offshore Flowline/Riser Systems.” SPE Production Engineering, 2(04), 319-324.

  4. Turner, R.G., Hubbard, M.G., & Dukler, A.E. (1969). “Analysis and Prediction of Minimum Flow Rate for the Continuous Removal of Liquids from Gas Wells.” Journal of Petroleum Technology, 21(11), 1475-1482.

  5. Bai, Y., & Bai, Q. (2010). “Subsea Pipelines and Risers.” Elsevier. Chapter on Thermal Design.

  6. Beggs, H.D. & Brill, J.P. (1973). “A Study of Two-Phase Flow in Inclined Pipes.” Journal of Petroleum Technology, SPE-4007-PA.