This application determines vapor liquid equilibrium properties for a hydrocarbon mixture of almost any composition Including upto a maximum of 112 components. A total of 38 paraffins, 14 cycloparafins, 24 olefins, 6 di-olefins, 10 aromatics, 5 acetylenes and 3 inorganic gases are included by default as possible components in the application. **LIST OF HYDROCARBONS – EQ-COMP**.The present application uses Peng-Robinson cubic equation of state which is the most preferred equation for calculating vapor-liquid equilibrium properties for non-polar hydrocarbons. It can include suitable binary interaction parameters in its calculations in case the same are provided by the person requesting the results. EQ-COMP can include temperature dependent binary interaction parameters as per Predictive Peng Robinson 78 (PPR 78) equation in its calculations.". Its various modules calculate.

PHASE ENVELOPE FOR A TYPICAL NATURAL GAS COMPOSITION

**Module 1: Bubble Point Temperature Calculation**

Bubble point temperatures, compositions, K values, liquid and vapour compressibility factor values, liquid and vapour densities and liquid and vapour molecular weight at desired pressure.

Equilibrium temperature, compositions, K values and compressibility factor values at pressure values throughout the bubble point curve at increments of 0.4 bars.

Phase envelope temperature at increments of 0.4 bars throughout the phase envelope and phase envelope curve.

**Sample Result** - Download

**Calculation cost (without Binary Interaction Parameters) : USD 25
Calculation cost (with constant or user defined BIPs for max 10 components) : USD 100**

**Module 2: Hydrocarbon dew point Temperature Calculation**

Hydrocarbon dew point temperature/ s, compositions, K values, liquid and vapour compressibility factor values, liquid and vapour densities and liquid and vapour molecular weight at desired pressure.

Equilibrium temperature, compositions, K values and compressibility factor values at pressure values throughout the hydrocarbon dew point curve at increments of 0.4 bars.

Phase envelope temperature at increments of 0.4 bars throughout the phase envelope and phase envelope curve.

**Sample Result** - Download

Calculation cost (with constant or user defined BIPs for max 10 components) : USD 100

**Module 3: Bubble Point Pressure Calculation**

Bubble point pressure/ s, compositions, K values, liquid and vapour compressibility factor values, liquid and vapour densities and liquid and vapour molecular weight at desired temperature.

Densities and liquid and vapour molecular weight at desired temperature. Equilibrium temperature, compositions, K values and compressibility factor values at pressure values throughout the bubble point curve at increments of 0.4 bars.

Phase envelope temperature at increments of 0.4 bars throughout the phase envelope and phase envelope curve.

**Sample Result** - Download

Calculation cost (with constant or user defined BIPs for max 10 components) : USD 100

**Module 4: Hydrocarbon dew point Pressure Calculation**

Hydrocarbon dew point pressure/ s, compositions, K values, liquid and vapour compressibility factor values, liquid and vapour densities and liquid and vapour molecular weight at desired temperature.

Equilibrium temperature, compositions, K values and compressibility factor values at pressure values throughout the hydrocarbon dew point curve at increments of 0.4 bars.

**Sample Result** - Download

Calculation cost (with constant or user defined BIPs for max 10 components) : USD 100

**Module 5: Two Phase Composition Calculation**

Two phase compositions, K values, liquid and vapour compressibility factor values, liquid and vapour densities and liquid and vapour molecular weight at desired temperature and pressure.

Hydrocarbon dew point temperature/ s, compositions, K values, liquid and vapour compressibility factor values, liquid and vapour densities and liquid and vapour molecular weight at two phase pressure.

Equilibrium temperature, compositions, K values and compressibility factor values at pressure values throughout the hydrocarbon dew point curve at increments of 0.4 bars.

Bubble point temperature/ s, compositions, K values, liquid and vapour compressibility factor values, liquid and vapour densities and liquid and vapour molecular weight at desired pressure.

Equilibrium temperature, compositions, K values and compressibility factor values at pressure values throughout the bubble point curve at increments of 0.4 bars.

Phase envelope temperature at increments of 0.4 bars throughout the phase envelope.

**Sample Result** - Download

Calculation cost (with constant or user defined BIPs for max 10 components) : USD 100

**Module 6: Phase Envelope Calculation**

Critical point temperature and pressure and compositions, K values, liquid and vapour compressibility factor values, liquid and vapour densities and liquid and vapour molecular weight at critical point as per bubble point curve.

Equilibrium temperature, compositions, K values and compressibility factor values at pressure values throughout the bubble point curve at increments of 0.4 bars.

Critical point temperature and pressure and compositions, K values, liquid and vapour compressibility factor values, liquid and vapour densities and liquid and vapour molecular weight at critical point as per hydrocarbon dew point curve.

**Sample Result** - Download

Calculation cost (with constant or user defined BIPs for max 10 components) : USD 100

**Module 7: Water Dew Point Temperature Calculation**

Water dew point temperature, compositions, K values, liquid and vapour compressibility factor values, liquid and vapour densities and liquid and vapour molecular weight at desired pressure.

Equilibrium temperature, compositions, K values and compressibility factor values at pressure values throughout the water dew point curve at increments of 0.4 bars.

Water dew point curve and water dew point temperature at increments of 0.4 bars throughout the water dew point curve.

**Sample Result** - Download

**Calculation cost (with temperature dependent or user defined BIPs for max 10 components) : USD 50**

**Module 8: Liquid compressibility factor calculation**

Liquid compressibility factor values for the provided range of temperatures and pressures with provided increments in temperatures and pressures. Total number of temperature increments or pressure increments can not exceed value of 250.

**Sample Result** - Download

**Calculation cost (without Binary Interaction Parameters) : USD 25**

**Module 9: Vapor compressibility factor calculation**

Vapor compressibility factor values for the provided range of temperatures and pressures with provided increments in temperatures and pressures. Total number of temperature increments or pressure increments can not exceed value of 250.

**Sample Result** - Download

**Calculation cost (without Binary Interaction Parameters) : USD 25**

**Module 10: Binary VLE calculation**

Concentration diagram (x-y plot) and concentration diagram (x-y plot) data.

Temperature-concentration diagram (T-x-y plot) and Temperature-concentration diagram (T-x-y plot) data.

Enthalpy-Concentration diagram (H-x-y plot) and Enthalpy-Concentration diagram (H-x-y plot) data.

Other VLE properties data like liquid and vapor compressibility factors, liquid and vapor densities and liquid and vapor molecular weights on 15 points on concentration diagram (x-y plot).

Phase envelope data for binary mixtures of same compounds with 9 different compositions starting from 0 % of one compound to 100 % of that compound with increments of 12.5 %.

Critical point data for binary mixtures of same compounds with 9 different compositions starting from 0 % of one compound to 100 % of that compound with increments of 12.5 %.

Critical point profile based on critical point data of binary mixtures of same compounds with 9 different compositions starting from 0 % of one compound to 100 % of that compound with increments of 12.5 %.

**Sample Result** - Download

**Calculation cost (without Binary Interaction Parameters) : USD 50**

**Module 11: Thermodynamic Properties calculation**

Equilibrium temperature, enthalpy change from standard conditions, entropy change from standard conditions, gibbs free energy change from standard conditions, heat capacity at constant pressure (Cp), heat capacity at constant volume (Cv), heat capacity ratio (Cp/Cv) and Sonic speed at desired pressure values and correspomding bubble point temperature values

temperature, enthalpy change from standard conditions, entropy change from standard conditions, gibbs free energy change from standard conditions, heat capacity at constant pressure (Cp), heat capacity at constant volume (Cv), heat capacity ratio (Cp/Cv) and Sonic speed at pressure values throughout the bubble point curve at increments of 0.4 bars.

Equilibrium temperature, enthalpy change from standard conditions, entropy change from standard conditions, gibbs free energy change from standard conditions, heat capacity at constant pressure (Cp), heat capacity at constant volume (Cv), heat capacity ratio (Cp/Cv) and Sonic speed at desired pressure values and correspomding dew point temperature values

Equilibrium temperature, enthalpy change from standard conditions, entropy change from standard conditions, gibbs free energy change from standard conditions, heat capacity at constant pressure (Cp), heat capacity at constant volume (Cv), heat capacity ratio (Cp/Cv) and Sonic speed at pressure values throughout the dew point curve at increments of 0.4 bars.

Phase envelope curve for the given composition of hydrocarbon mixture

**Sample Result** - Download

**Calculation cost (without Binary Interaction Parameters) : USD 100
Calculation cost (with constant or user defined BIPs for max 10 components) : USD 100**

**Module 12: Composition Profile Calculation**

Bubble point temperature/s, compositions, K values, liquid and vapour compressibility factor values, liquid and vapour densities and liquid and vapour molecular weights at upto 10 pressure values on the pressure profile of a pipeline.

Dew point temperature/s, compositions, K values, liquid and vapour compressibility factor values, liquid and vapour densities and liquid and vapour molecular weights at upto 10 pressure values on a pipeline.

Two phase compositions, K values, liquid and vapour compressibility factor values, liquid and vapour densities and liquid and vapour molecular weights at upto 10 temperature values and corresponding pressure values on a pipeline.

**Sample Result** - Download

**Calculation cost (without Binary Interaction Parameters) : USD 150
Calculation cost (with constant or user defined BIPs for max 10 components) : USD 150**

* The module can give composition profile of a pipeline with available temperature and pressure profiles However any temperature values and corresponding pressure values upto a maximum of 10 can be entered in the module to get upto 10 two phase results irrespective of whether they lie on a pipeline or not.

**1- Hydrate prediction with gas phase being 100 % methane.**

Temperature profile data with tabulation of pipeline temperature profile with height/ length of pipeline and pipeline pressure with indication for section of pipeline prone to hydrate formation.

Temperature profile curve showing pipeline temperature vs. pipe length.

Hydrate prediction curve data with tabulation of pipeline temperature profile and hydrate equilibrium temperature with pipeline pressure with indication for section of pipeline prone to hydrate formation.

Hydrate prediction curve showing pipeline temperature vs. pipeline pressure and hydrate equilibrium temperature vs. pipeline pressure.

**Sample Result - Hydrate prediction curve** - Download

**Calculation cost : USD 100**

**1- Hydrocarbon liquid property calculation**

Values of saturation pressure at desired temperature, hydrocarbon liquid density at saturation pressure at desired temperature, hydrocarbon liquid density at elevated pressure and desired temperature, latent heat of vaporization at atmospheric pressure and latent heat of vaporization at saturation pressure at desired temperature.

In case of system temperature greater than 95 % of pseudo-critical temperature, the desired values will be calculated at the validity limit of temperature.

In case of system pressure value below saturation pressure value at desired temperature implying hydrocarbon mixture not in 100 % liquid state, the desired values will be calculated at saturation pressure value.

**Sample Result** - Download

**Calculation cost : USD 10**