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Introduction to Computational Mass Transfer pp 111–149Cite as

Application of Computational Mass Transfer (II) Chemical Absorption Process

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Part of the book series: Heat and Mass Transfer ((HMT))

Abstract

In this chapter, the two CMT models, i.e., \(\overline{{c^{{{\prime }2}} }} \text{ - }\varepsilon_{{c^{{\prime }} }}\) model and Reynolds mass flux model (in standard, hybrid, and algebraic forms) are used for simulating the chemical absorption of CO2 in packed column by using MEA, AMP, and NaOH separately and their simulated results are closely checked with the experimental data. It is noted that the radial distribution of \(D_{t}\) is similar to \(\alpha_{t}\) but quite different from \(\mu_{t}\). It means that the conventional assumption on the analogy between the momentum transfer and the mass transfer in turbulent fluids is unjustified and thus the use of CMT method for simulation is necessary. In the analysis of the simulation results, some transport phenomena are interpreted in terms of the co-action or counter-action of the turbulent mass flux diffusion.

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Abbreviations

a :

Surface area per unit volume of packed bed, m−1

a eff :

Effective area for mass transfer between the gas phase and liquid phase, 1/m

a w :

Wetted surface area, m−1

\(\overline{{c^{2} }}\) :

Concentration variance, kg2 m−6

\(\overline{C}\) :

Average concentration of mass fraction, kg m−3

C μ ,c 1, c 2 :

Model parameters in k-ε model equations, dimensionless

C c0,C c1, C c2, C c3 :

Model parameters in \(\overline{{c^{2} }}\)-\(\varepsilon_{c}\) model equations, dimensionless

\(C_{p}\) :

Liquid phase specific heat, J/kg/K

C t0,C t1, C t2, C t3 :

Model parameters in \(\overline{{t^{2} }}\)-\(\varepsilon_{t}\) model equations, dimensionless

D :

Molecular diffusivity, m2 s−1

D eff :

Effective diffusivity, m2 s−1

D G :

Molecular diffusivity of CO2 in gas phase, m2 s−1

D t :

Turbulent diffusivity for mass transfer, m2 s−1

d e :

Equivalent diameter of random packing, m

d H :

Hydraulic diameter of random packing, m

d p :

Nominal diameter of the packed particle, m

E :

Enhancement factor, dimensionless

G :

Gas phase flow rate per unit cross-section area, kg m2 s−1

H A :

Physical absorption heat of mol CO2 absorbed, J kmol−1

H R :

Chemical reaction heat of mol CO2 absorbed, J kmol−1

H s :

Static holdup, dimensionless

H t :

Total liquid holdup, dimensionless

k :

Turbulent kinetic energy, m2/s2

k 2 :

Second-order reaction rate constant, m3 kmol.s−1

k G :

Gas phase mass transfer coefficient, kmol.m.s.kPa−1

k L :

Liquid phase mass transfer coefficient without chemical reaction, m s−1

k R, L :

liquid phase mass transfer coefficient with chemical reaction, m s−1

L :

Liquid flow rate per unit cross-section area, kg.m2 s−1

R :

Position in radial direction, m

R c :

The rate of reaction, kmol m3 s−1

r :

Radius of the column, m

\(\overline{{t^{2} }}\) :

Temperature variance, dimensionless

T :

Liquid temperature, K

U :

Liquid superficial velocity, m s−1

\(X\) :

Molar concentration in the liquid bulk, kmol m−3

\(X_{i}\) :

Molar concentration at interface, kmol m−3

x :

Distance measured from column top (x = 0 at the column top), m

α,α eff, α t :

Molecular, turbulent and effective thermal diffusivities, respectively, m2 s−1

\(\beta\) :

Volume fraction of liquid phase based on pore space, dimensionless

ε :

Turbulent dissipation rate, m2 s−3

ε c :

Turbulent dissipation rate of concentration fluctuation, kg2 m−6 s−1

ε t :

Turbulent dissipation rate of temperature fluctuation, s−1

\(\varPhi\) :

Variable, dimensionless

\(\nu_{t}\) :

Turbulent diffusivity, m2 s−1

ρ :

Liquid density, kg/m3

ρ G :

Gas phase density, kg/m3

σ :

Surface tension of aqueous solutions, dynes/cm, or N/m

σ c , \(\sigma_{{\varepsilon_{c} }}\) :

Model parameters in \(\overline{{c^{2} }}\)-\(\varepsilon_{c}\) model equations, dimensionless

σ t , \(\sigma_{{\varepsilon_{t} }}\) :

Model parameters in \(\overline{{t^{2} }}\)-\(\varepsilon_{t}\) model equations, dimensionless

σ k ,σ ε :

Model parameters in k–ε model equations, dimensionless

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  1. School of Chemical Engineering and Technology, Tianjin University, Tianjin, People’s Republic of China

    Kuo-Tsung Yu & Xigang Yuan

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Correspondence to Kuo-Tsung Yu .

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Yu, KT., Yuan, X. (2017). Application of Computational Mass Transfer (II) Chemical Absorption Process. In: Introduction to Computational Mass Transfer. Heat and Mass Transfer. Springer, Singapore. https://doi.org/10.1007/978-981-10-2498-6_3

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  • DOI: https://doi.org/10.1007/978-981-10-2498-6_3

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