Solvent Property & Sizing Calculator

Access dynamic thermophysical properties, safety data, and perform preliminary engineering calculations for line sizing and heat transfer.

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1. Project Data

2. Solvent & Operating Conditions

3. Engineering Calculation Module

Boiling Point Calculator
Calculates the exact boiling temperature at the specified target pressure using the Antoine equation.
Line Sizing Parameters
NPSHa — Suction Side
Sensible Heating/Cooling
Utility Specifications
Vaporization / Boil-off
Utility Specifications
Condensation
Utility Specifications
Fluid Properties (at Op. Conditions)
Molecular Wt. -
Density (lb/ft³) -
Viscosity (cP) -
Heat Cap ($C_p$, Btu/lb°F) -
Vapor Press. (psia) -
Latent Heat (Btu/lb) -
Calculation Results
Safety Data: Select a solvent to view Flash Point and Explosive Limits.
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Property vs Temperature Plot

No chart data.

Solvent Comparison

Engineering Reference & Technical Basis

1. Thermophysical Property Models

Fluid properties are dynamically evaluated using standard chemical engineering empirical correlations. Base parameters are derived from industry literature including Yaws' Chemical Properties Handbook and the DIPPR Database.

  • Vapor Pressure (Antoine Equation): $\log_{10}(P) = A - \frac{B}{T + C}$. Determines the vapor pressure ($P$ in mmHg) at a given temperature ($T$ in °C) utilizing substance-specific constants.
  • Boiling & Dew Point (Inverse Antoine): $T = \frac{B}{A - \log_{10}(P)} - C$. Calculates the exact saturation temperature at the given system operating pressure.
  • Liquid Viscosity (Andrade Equation): $\mu = \exp\left(A + \frac{B}{T}\right)$. Evaluates dynamic viscosity (cP) as a non-linear function of absolute temperature ($T$ in Kelvin).
  • Latent Heat of Vaporization (Watson Relation): $\Delta H_{vap} = \Delta H_{v1} \cdot \left(\frac{T_c - T}{T_c - T_1}\right)^{0.38}$. Estimates heat of vaporization adjusting for the fluid's critical temperature ($T_c$). Evaluated at exact saturation conditions for phase-change modules.
  • Density & Heat Capacity: Approximated using linear temperature-dependent correlations optimized for typical industrial liquid operating ranges (0°C to 150°C).
2. Process Calculation Models

The engineering modules utilize fundamental mass and energy conservation equations alongside steady-state thermodynamic principles.

  • Fluid Hydraulics & Line Sizing: Pressure drop is calculated via the Darcy-Weisbach equation ($h_f = f \frac{L}{D} \frac{v^2}{2g}$). The Darcy friction factor ($f$) is determined using the Colebrook-White approximation for fully turbulent rough pipe flow based on dynamically selected pipe material roughness.
  • Sensible Heat Transfer: Computes required heat duty via $Q = m \cdot C_p \cdot \Delta T$. The heat exchanger surface area is estimated using the fundamental design equation $A = \frac{Q}{U \cdot LMTD}$, assuming strict counter-current flow log mean temperature differences.
  • Latent Heat Transfer (Vaporization & Condensation): Calculates required phase-change duty via $Q = m \cdot \Delta H_{vap}$, assuming isothermal phase change at the calculated saturation pressure. Mass flowrates are balanced directly against the utility's dynamic properties.
References
  • Yaws' Chemical Properties Handbook: Thermophysical properties and empirical correlations.
  • DIPPR Database: Pure component property data.
  • Antoine Equation: Vapor pressure and saturation temperature determination.
  • Andrade Equation: Dynamic liquid viscosity evaluation.
  • Watson Relation: Latent heat of vaporization estimation.
  • Darcy-Weisbach & Colebrook-White Equations: Fluid hydraulics and pipe sizing calculations.
Disclaimer: This application relies on generalized literature values and empirical correlations. Supercritical fluid dynamics are safeguarded to prevent errant sizing. Always consult substance-specific Safety Data Sheets (SDS) and utilize rigorous thermodynamic process simulators for detailed equipment design.