Calculations

Calculations

• Run results as component properties

  The liquid density and diffusion coefficient of a run in SI units for a process component.

  ρ (kg/m³) = ρ (g/cm³) × 1000; D (m²/s) = D (Ų/ps) × 1e-8

  Molecular dynamics molecular/props.js

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• Linear solve

  x from A x = b for a small dense system.

  Gaussian elimination with row exchange on the largest pivot, then back substitution

  Solvers shared by the process engine process/numeric.js

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• Newton iteration

  The solution of a set of nonlinear equations F(x) = 0.

  J Δx = −F, Jᵢⱼ ≈ (Fᵢ(x + h eⱼ) − Fᵢ(x)) ÷ h, h = 1e-7 × max(|xⱼ|, 1e-6); x ← x + λ Δx, λ halved until |F| falls

  Solvers shared by the process engine process/numeric.js

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• Adaptive Runge–Kutta integration

  y(x₁) for a system of ordinary differential equations, with the accepted points along the way.

  Dormand–Prince 5(4): error = max |h Σ(b₅ − b₄)k| ÷ (atol + rtol × max(|y|, |y_new|)) ≤ 1; h ← h × clamp(0.9 × error^(−0.2), 0.2, 5)

  Solvers shared by the process engine process/numeric.js

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• Bracketed root

  A root of one equation between two points where the function changes sign.

  c = (f_a b − f_b a) ÷ (f_a − f_b); the retained end's value is halved when the same side is kept twice

  Solvers shared by the process engine process/numeric.js

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• Temperature form of the parameters

  The interaction parameter of each pair at a temperature.

  pᵢⱼ = aᵢⱼ + bᵢⱼ ÷ T; 0 on the diagonal

  Activity coefficients and Henry's law process/activity.js

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• NRTL

  ln γ of every component by the NRTL model.

  ln γᵢ = Cᵢ ÷ Sᵢ + Σⱼ xⱼ Gᵢⱼ ÷ Sⱼ × (τᵢⱼ − Cⱼ ÷ Sⱼ), Gᵢⱼ = exp(−αᵢⱼ τᵢⱼ), Sⱼ = Σ xₖ Gₖⱼ, Cⱼ = Σ xₘ τₘⱼ Gₘⱼ

  Activity coefficients and Henry's law process/activity.js

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• Wilson

  ln γ of every component by the Wilson model.

  ln γᵢ = 1 − ln(Σⱼ xⱼ Λᵢⱼ) − Σₖ xₖ Λₖᵢ ÷ Σⱼ xⱼ Λₖⱼ

  Activity coefficients and Henry's law process/activity.js

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• UNIQUAC

  ln γ of every component by the UNIQUAC model.

  ln γᵢ = ln(φᵢ÷xᵢ) + z⁄2 qᵢ ln(θᵢ÷φᵢ) + lᵢ − φᵢ÷xᵢ Σ xⱼlⱼ + qᵢ (1 − ln Σ θⱼτⱼᵢ − Σ θⱼτᵢⱼ ÷ Σ θₖτₖⱼ)

  Activity coefficients and Henry's law process/activity.js

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• Infinite-dilution limits

  The closed-form ln γ of each component of a binary when it is infinitely dilute.

  NRTL: ln γ₁^∞ = τ₂₁ + τ₁₂ exp(−α τ₁₂); Wilson: ln γ₁^∞ = 1 − ln Λ₁₂ − Λ₂₁

  Activity coefficients and Henry's law process/activity.js

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• Henry's constant at temperature

  Henry's constant of a dissolved gas in pascals at a temperature.

  H(T) = H₂₉₈ (bar) × 1e5 × exp(slope × (1 ÷ T − 1 ÷ 298.15))

  Activity coefficients and Henry's law process/activity.js

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• Model constants

  The constants of the two equations of state and the correlation for κ(ω).

  PR: Ω_a = 0.45724, Ω_b = 0.07780, σ = 1 + √2, ε = 1 − √2; SRK: Ω_a = 0.42748, Ω_b = 0.08664

  Cubic equations of state process/eos.js

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• Real roots of a cubic

  The real roots of z³ + c₂z² + c₁z + c₀ = 0 in ascending order.

  p = c₁ − c₂² ÷ 3; q = 2c₂³ ÷ 27 − c₂c₁ ÷ 3 + c₀; disc = q² ÷ 4 + p³ ÷ 27; one root: ∛(−q⁄2 + √disc) + ∛(−q⁄2 − √disc) − c₂⁄3; three: 2√(−p⁄3) cos((acos(arg) − 2πk) ÷ 3) − c₂⁄3

  Cubic equations of state process/eos.js

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• Attraction parameter of each component

  a(T) and its temperature derivative for every pure component.

  aᵢ = a_c,ᵢ (1 + κᵢ (1 − √(T ÷ T_c,ᵢ)))²; daᵢ/dT = −a_c,ᵢ κᵢ (1 + κᵢ(1 − √(T÷T_c))) ÷ √(T T_c,ᵢ)

  Cubic equations of state process/eos.js

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• Mixture parameters

  a, da/dT and b of a mixture of given composition.

  a = Σᵢ Σⱼ yᵢ yⱼ √(aᵢ aⱼ) (1 − kᵢⱼ); b = Σ yᵢ bᵢ

  Cubic equations of state process/eos.js

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• Compressibility roots

  The physical compressibility factors of a mixture at a temperature and pressure.

  β = bP ÷ RT; A = aP ÷ (RT)²; Z³ + c₂Z² + c₁Z + c₀ = 0 with c from β, A, ε, σ; keep Z > β (1 + 1e-12)

  Cubic equations of state process/eos.js

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• Fugacity coefficients

  ln φ of every component for one compressibility root.

  ln φᵢ = bᵢ⁄b (Z − 1) − ln(Z − β) − a ÷ (bRT) × (2 Σⱼ yⱼ aᵢⱼ ÷ a − bᵢ⁄b) × I, I = ln((Z + σβ) ÷ (Z + εβ)) ÷ (σ − ε)

  Cubic equations of state process/eos.js

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• Enthalpy and entropy departures

  How far a real phase's enthalpy and entropy are from the ideal gas at the same temperature and pressure.

  H − H_ig = RT (Z − 1) + (T da/dT − a) ÷ b × I; S − S_ig = R ln(Z − β) + (da/dT) ÷ b × I

  Cubic equations of state process/eos.js

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• Vapor pressure of a pure component

  The pressure at which the liquid and vapor roots of one component have equal fugacity.

  P ← P × exp(ln φ_L − ln φ_V) until |ln φ_L − ln φ_V| < 1e-12

  Cubic equations of state process/eos.js

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• Ideal-gas enthalpy

  The ideal-gas enthalpy of a component, with its formation enthalpy, at a temperature.

  H = h_f + R (A (T − T₀) + B⁄2 (T² − T₀²) + C⁄3 (T³ − T₀³) − D (1⁄T − 1⁄T₀))

  Property package and flashes process/thermo.js

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• Ideal-gas entropy

  The ideal-gas entropy of a component at a temperature, relative to 298.15 K.

  S = R (A ln(T ÷ T₀) + B (T − T₀) + C⁄2 (T² − T₀²) − D⁄2 (1⁄T² − 1⁄T₀²))

  Property package and flashes process/thermo.js

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• Vapor pressure for the ideal and activity models

  The vapor pressure of a component from its Antoine constants, or an estimate when it has none.

  P = exp(A − B ÷ (T + C)); without Antoine: P = P_c exp(5.373 (1 + ω)(1 − T_c ÷ T))

  Property package and flashes process/thermo.js

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• Heat of vaporization

  The heat of vaporization of a component at a temperature.

  ΔH(T) = ΔH(T_b) × ((1 − T⁄T_c) ÷ (1 − T_b⁄T_c))^0.38

  Property package and flashes process/thermo.js

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• Liquid molar volume

  The saturated liquid volume of a component for the ideal and activity models.

  V = R T_c ÷ P_c × Z_ra^(1 + (1 − T_r)^(2⁄7)), Z_ra = 0.29056 − 0.08775 ω

  Property package and flashes process/thermo.js

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• Enthalpy, entropy and volume of one phase

  The molar enthalpy, entropy and volume of a liquid or vapor of given composition.

  EOS: H = Σ xᵢ H_ig,ᵢ + departure; V = ZRT ÷ P. Activity liquid: H = Σ xᵢ (H_ig,ᵢ − ΔH_vap,ᵢ) + H^E, H^E = −RT² Σ xᵢ ∂ln γᵢ⁄∂T

  Property package and flashes process/thermo.js

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• K-values

  ln K of every component between a liquid and a vapor composition.

  EOS: ln Kᵢ = ln φᵢ(liquid) − ln φᵢ(vapor); activity: ln Kᵢ = ln γᵢ + ln(P_sat,ᵢ ÷ P), or ln(Hᵢ ÷ P) for a Henry solute

  Property package and flashes process/thermo.js

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• Vapor fraction (Rachford–Rice)

  The vapor fraction that balances a feed for given K-values.

  Σ zᵢ (Kᵢ − 1) ÷ (1 + V (Kᵢ − 1)) = 0, 0 ≤ V ≤ 1

  Property package and flashes process/thermo.js

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• Phase stability test

  Whether a mixture at a temperature and pressure stays one phase or splits.

  Yᵢ ← exp(ln zᵢ + ln φᵢ(z) − ln φᵢ(y)); unstable when ΣY > 1 + 1e-8

  Property package and flashes process/thermo.js

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• Two-phase flash iteration

  The vapor fraction and the two compositions at a temperature and pressure.

  V from Rachford–Rice; xᵢ = zᵢ ÷ (1 + V (Kᵢ − 1)); yᵢ = Kᵢ xᵢ; K ← exp(ln K(x, y)) until max |Δ ln K| < 1e-13

  Property package and flashes process/thermo.js

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• Liquid–liquid split

  Two liquid phases and their fractions for an activity model.

  trial phases from each component at 0.9; split when the tangent-plane distance < −1e-9; K ← exp(ln γ(x₂) − ln γ(x₁)) until max |Δ ln K| < 1e-12

  Property package and flashes process/thermo.js

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• Saturation residual

  How far a mixture is from its bubble or dew point at a trial temperature or pressure.

  bubble: Σ Kᵢ zᵢ − 1; dew: 1 − Σ zᵢ ÷ Kᵢ

  Property package and flashes process/thermo.js

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• Bubble and dew points

  The bubble or dew temperature at a pressure, or pressure at a temperature.

  scan a geometric grid for a sign change of the residual, then bisect on √(a b) until b ÷ a − 1 < 1e-13

  Property package and flashes process/thermo.js

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• Temperature for a given enthalpy or entropy

  The temperature at which a PT flash has the wanted enthalpy or entropy.

  false position inside a bracket; stop when b − a < 1e-10 K or |f| < 1e-9 (|target| + 1)

  Property package and flashes process/thermo.js

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• Flash at a vapor fraction

  The state at a pressure and a wanted vapor fraction.

  bisect T between the bubble and dew temperatures until the bracket is below 1e-9 K

  Property package and flashes process/thermo.js

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• Saturation temperature of a pure component

  The temperature at which a pure component's vapor pressure equals the pressure.

  bisect T on [20 K, T_c − 1e-6] until the bracket is below 1e-11 K

  Property package and flashes process/thermo.js

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• Gas constant

  R, used by the property package, the equations of state, the reactors and the dynamic simulation.

  R = 8.314462618 J/(mol K)

  Property package and flashes process/data.js

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• Component data to SI

  A component's critical pressure, molar mass and Antoine constants in the units the engine works in.

  P_c (Pa) = P_c (bar) × 1e5; M (kg/mol) = M ÷ 1000; A′ = A + ln 1000; C′ = C − 273.15

  Property package and flashes process/data.js

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• 2×2 solve

  The Newton step for the two phase fractions.

  det = a d − b c; x = (r₁ d − b r₂) ÷ det; y = (a r₂ − c r₁) ÷ det

  Three-phase flash process/vlle.js

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• Phase fractions

  The vapor and second-liquid fractions for the current K-values.

  gⱼ = Σ zᵢ (Kⱼᵢ − 1) ÷ Dᵢ = 0, Dᵢ = 1 + β_v (K_v,ᵢ − 1) + β_l (K_l,ᵢ − 1)

  Three-phase flash process/vlle.js

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• Composition update

  The liquid compositions and the new K-values after each pass.

  x₁,ᵢ = zᵢ ÷ Dᵢ; x₂,ᵢ = x₁,ᵢ K_l,ᵢ; error = max |ln(K_new ÷ K)|

  Three-phase flash process/vlle.js

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• Residuals of a result

  The largest iso-fugacity difference between the phases and the largest component-balance error, as the calculator reports them.

  iso = max |ln(xᵢγᵢ)₁ − ln(xᵢγᵢ)₂|, |ln(yᵢP) − ln(xᵢγᵢP_sat,ᵢ)|; balance = max |Σ_phases frac × xᵢ − zᵢ|

  Three-phase flash process/vlle.js

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• Reference-state offsets

  The shifts that put CoolProp's enthalpy and entropy on the engine's reference state.

  ΔH = h_f − H(298.15 K, 1e-4 mol/m³); ΔS = −(S(298.15 K, 1e-4 mol/m³) − R ln(1e5 ÷ (1e-4 R T₀)))

  Pure-fluid properties from CoolProp process/coolprop.js

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• Properties at a temperature and pressure

  Enthalpy, entropy, heat capacity, molar density, molar mass and phase of a pure fluid.

  H = H_CoolProp + ΔH; S = S_CoolProp + ΔS; M (g/mol) = M (kg/mol) × 1000

  Pure-fluid properties from CoolProp process/coolprop.js

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• Saturation values

  Vapor pressure, saturated liquid and vapor densities and heat of vaporization at a temperature.

  ΔH_vap = H(T, vapor) − H(T, liquid)

  Pure-fluid properties from CoolProp process/coolprop.js

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• Ideal-gas heat-capacity fit

  A quadratic C_p ÷ R = A + B T + C T² fitted to the dilute-gas enthalpy slope over a temperature range.

  C_p(T) ≈ H(T + 0.5) − H(T − 0.5) at 13 temperatures; normal equations M s = v solved by 3×3 determinants

  Pure-fluid properties from CoolProp process/coolprop.js

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• Component from a fluid

  A component for the property package from CoolProp's critical constants, acentric factor, boiling point and the heat-capacity fit.

  P_c (bar) = P_c (Pa) ÷ 1e5; M (g/mol) = M × 1000; ΔH_vap(T_b) = H(1 atm, vapor) − H(1 atm, liquid)

  Pure-fluid properties from CoolProp process/coolprop.js

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• Minimum stages (Fenske)

  The least number of stages at total reflux for a split of two key components.

  N_min = ln((d_LK ÷ d_HK)(b_HK ÷ b_LK)) ÷ ln α

  Distillation and absorption columns process/column.js

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• Gilliland correlation (Eduljee)

  The stage ratio Y for a reflux ratio X above the minimum.

  Y = 0.75 (1 − X^0.5668)

  Distillation and absorption columns process/column.js

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• Gilliland correlation (Molokanov)

  The same stage ratio by the fit of Molokanov and others.

  Y = 1 − exp((1 + 54.4X) ÷ (11 + 117.2X) × (X − 1) ÷ √X)

  Distillation and absorption columns process/column.js

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• Number of stages

  The stages needed at a reflux ratio, from the minimum stages and minimum reflux.

  X = (R − R_min) ÷ (R + 1); N = (N_min + Y) ÷ (1 − Y)

  Distillation and absorption columns process/column.js

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