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Non-equilibrium modeling of CO2 reactive-absorption process using sodium hydroxide–ammonia–water solution in a packed bed column

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Abstract

In this study, CO2 reactive-absorption process is modeled into the NaOH-NH3-H2O solution in an absorption column. A non-equilibrium or rate-based model is used to simulate the process performance, and the predicted results are compared with the experimental data. In this model, the steady and nonlinear film models are utilized for high and low solubility components, respectively. The average relative deviation (ARD%) is decreased from 9.73 to 4.36 by increasing the number of column stages from 20 to 60 in the simulation. On the other hand, the predicted values by the film and enhancement factor models are compared, and it was concluded that the film model was more accurate than the other. The effects of axial position through the column and initial NaOH concentration on the liquid flow rate, mole fraction of components, and temperature of the gas and liquid phases are also investigated. As a main result, the temperature of the liquid phase and the CO2 concentration in the liquid phase decrease by increasing the axial position through the column.

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Abbreviations

a I :

Area of interface per unit volume (m2.m−3)

a n :

A function in analytical solution

A :

Surface area of column (m2)

A I :

Surface area of interface (m2)

A eff :

Effective area of packing (m2)

A t :

Packing area (m2)

ARD :

Average Relative Deviation (%)

C :

Concentration (mol.m−3)

D :

Diffusion coefficient (m2.s−1)

E :

Enhancement factor of mass transfer

\(\overline{E}\) :

Heat transfer rate (N.m.s−1)

F :

A function in analytical solution

F V :

Gas capacity factor (Pa0.5)

g :

Gravity acceleration (m.s−2)

G :

Gas flow rate (mol.s−1)

h f :

Heat transfer coefficient of each phases (W.m−2.K−1)

h L :

Holdup

h L,S :

Holdup at loading point

H :

Column height (m)

\(\overline{H}_{i}^{f}\) :

Partial molar enthalpy of component i in the solution (N.m.mol−1)

k :

Mass transfer coefficient (m.s−1)

k i :

Reaction rate constant (s−1)

K :

Chemical equilibrium constant

K W :

Wall factor

L :

Liquid flow rate (mol.s−1)

M :

Mole number (mole)

N :

Mole flux (mol.m−2.s−1)

\(\overline{N}\) :

Mole rate (mol.s−1)

q n :

A function in analytical solution

\(\dot{Q}\) :

Input (or output) heat transfer rate (N.m.s−1)

r :

Reaction rate

R :

Universal gas constant (m3⋅Pa⋅K−1⋅mol−1)

RD :

Relative Deviation (%)

Re :

Reynolds number

t :

Time (s)

T :

Temperature (K)

u :

Velocity (m.s−1)

x, y :

Mole fraction

X :

Parameter

z :

Axial direction of column height

ρ :

Density (g.m−3)

μ :

Viscosity (g.m−1.s−1)

Δz :

Height of each stage (m)

σ :

Surface tension (N.m−1)

ψ :

Resistance coefficient

ξ :

Variable

L :

Liquid

G :

Gas

s :

Column number

I :

Interface

i :

Component

Exp:

Experimental

Cal:

Calculation

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Authors and Affiliations

  1. School of Chemical, Petroleum and Gas Engineering, Iran University of Science and Technology, Tehran, 16846, Iran

    Ahad Ghaemi, Alireza Hemmati & Hossein Mashhadimoslem

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  1. Ahad Ghaemi
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  2. Alireza Hemmati
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  3. Hossein Mashhadimoslem
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Correspondence to Ahad Ghaemi or Alireza Hemmati.

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Ghaemi, A., Hemmati, A. & Mashhadimoslem, H. Non-equilibrium modeling of CO2 reactive-absorption process using sodium hydroxide–ammonia–water solution in a packed bed column. J IRAN CHEM SOC 18, 2303–2314 (2021). https://doi.org/10.1007/s13738-021-02190-3

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  • DOI: https://doi.org/10.1007/s13738-021-02190-3

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