Development of Two Novel Processes for Hydrogenation of CO2 to Methanol over Cu/ZnO/Al2O3 Catalyst to Improve the Performance of Conventional Dual Type Methanol Synthesis Reactor
Abstract
:1. Introduction
2. Results and Discussion
2.1. Reaction Scheme and Kinetics
2.2. Process Description
2.2.1. Conventional Methanol Synthesis Process with Two Reactors (CR Configuration)
2.2.2. AW Configuration
2.2.3. ACW Configuration
2.3. Mathematical Model
2.3.1. Reactor Model
2.3.2. Thermodynamic Model
Dew Point Calculation
Flash Calculation
2.4. Model Validation
2.5. Comparison between Temperature Profiles of CR, AW, and ACW Configurations
2.6. Comparison between Pressure Profiles of CR, AW, and ACW Configurations
2.7. Comparison between Molar Flow Rate of Methanol in CR, AW, and ACW Configurations
2.8. Comparison of H2, CO, and CO2 Conversions between CR, AW, and ACW Configurations
2.9. Comparison of H2O Mole Fraction between CR, AW, and ACW Configurations
2.10. Energy Requirement and Methanol Molar Flow Rate Comparison between CR, AW, and ACW Configurations
3. Conclusions
Author Contributions
Conflicts of Interest
Nomenclatures
Ac | reaction side cross-section (m2) |
Ei | activation energy of reaction (kJ kmol−1) |
Cp | specific heat of gas (J mol−1 K−1) |
dp | diameter of particle (m) |
fi | fugacity (Pa) |
Ft | total molar flow rate (mol s−1) |
Fi | the component’s molar flow rate (mol s−1) |
∆Hf,i | component (i) formation enthalpy (J mol−1) |
ki | reaction rate coefficient (mol kg-1 s−1 bar−1/2) |
Ki | adsorption equilibrium constant (bar−1) |
Ki | k value |
Kpi | constant of equilibrium |
L | length of reactor (m) |
P | total pressure (Pa) |
R | universal gas constant (J mol−1 K−1) |
ri | rate of reaction (mol kg−1 s−1) |
U | overall heat transfer coefficient between two sides (W m−2 K−1) |
Vfrac | vapor fraction |
T | temperature (K) |
ug | gas velocity (m s−1) |
xi | component mole fraction in the liquid phase |
yi | component mole fraction in the gas phase |
z | axial reactor coordinate (m) |
Z | compressibility factor |
Greek letter | |
∆H | heat of reaction (J mol−1) |
𝜈i,j | component stoichiometric coefficient in each reaction |
𝜀 | void fraction of bed |
φi | fugacity coefficient |
𝜇 | viscosity (Pa s) |
𝜌 | gas phase density (kg m−3) |
𝜌b | catalyst bed density (kg m−3) |
𝜂 | effectiveness factor of catalyst |
Subscript and Superscripts | |
i | indicator of component |
j | indicator of reaction |
0 | inlet condition |
v | vapor phase |
l | liquid phase |
g | in bulk of gas phase |
Abbreviations | |
CFD | computational fluid dynamics |
CR | conventional methanol synthesis reactor |
AW | name of the proposed configuration |
ACW | name of the proposed configuration |
RWGS | reverse water gas shift reaction |
DAE | differential-algebraic equations |
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Adsorption Equilibrium Constants | ||
---|---|---|
A | B | |
KCO | ||
KCO2 | ||
Rate Constants | ||
A | B | |
Equilibrium Constants | ||
A | B | |
5139 | 12.621 | |
3066 | 10.592 | |
−2073 | −2.029 |
Parameters | Water-Cooled Reactor | Gas-Cooled Reactor |
---|---|---|
Values | Values | |
Shell diameter (m) | 4.5 | 5.5 |
Tube diameter (m) | 0.038 | 0.0254 |
Reactor length (m) | 8.4 | 10.5 |
Particle diameter (m) | 0.0057 | 0.0057 |
Catalyst bed density (kg/m3) | 1140 | 1140 |
Bed void fraction | 0.39 | 0.39 |
Number of tubes | 5955 | 3026 |
Molar flow of feed in each tube (mol/s) | 1.5 | - |
Input shell side pressure (bar) | - | 71.8 |
Input tube side pressure (bar) | 75 | 76.98 |
Temperature of the shell side (K) | 513 | - |
Mass flow rate of the shell side (kg/h) | 151,437 | - |
Feed Composition (Mole Basis) | Values | |
H2 | 0.6334 | |
CH4 | 0.1006 | |
CO2 | 0.0832 | |
H2O | 0.00039 | |
N2 | 0.093 | |
CH3OH | 0.0049 | |
CO | 0.085 |
Feed Conditions | Values |
---|---|
Feed mole fraction | |
CO | 0.0868 |
CO2 | 0.0849 |
H2 | 0.6461 |
CH4 | 0.0947 |
N2 | 0.0847 |
H2O | 0.001 |
CH3OH | 0.0037 |
Input temperature (K) | 401 |
Molar flow of feed in each tube (mol/s) | 1.8 |
Feed input pressure (bar) | 76 |
Parameters | Adiabatic Reactor | Water-Cooled Reactor |
---|---|---|
Values | Values | |
Shell diameter (m) | - | 4.5 |
Tube diameter (m) | - | 0.038 |
Reactor diameter (m) | 5.5 | - |
Reactor length (m) | 2.6 | 8.4 |
Particle diameter (m) | 0.0057 | 0.0057 |
Catalyst bed density (kg/m3) | 1140 | 1140 |
Bed void fraction | 0.39 | 0.39 |
Number of tubes | - | 5955 |
Rate of feed stream (mol/s) | 17,865 | - |
Input pressure (bar) | 75 | - |
Input temperature (K) | 513 | - |
Input tube side pressure (bar) | - | 74.64 |
Input shell side temperature (K) | - | 513 |
Mass flow rate of the shell side (kg/h) | - | 151,437 |
Feed Composition (Mole Basis) | Values | |
H2 | 0.6334 | |
CH4 | 0.1006 | |
CO2 | 0.0832 | |
H2O | 0.00039 | |
N2 | 0.093 | |
CH3OH | 0.0049 | |
CO | 0.085 |
Parameters | Values |
---|---|
Shell diameter (m) | 4.5 |
Tube diameter (m) | 0.038 |
Reactor length (m) | 8.4 |
Number of tubes | 5955 |
Molar flow of feed in each tube (mol/s) | 1.34 |
Input tube side pressure (bar) | 74.24 |
Input tube side temperature (K) | 534.4 |
Temperature of the shell side (K) | 513 |
Mass flow rate of the shell side (kg/h) | 151,437 |
Feed Mole Fraction | Values |
H2 | 0.5871 |
CH4 | 0.1119 |
CO2 | 0.0632 |
H2O | 0.0020 |
N2 | 0.1036 |
CH3OH | 0.0568 |
CO | 0.0754 |
Parameters | Values |
---|---|
Reactor diamaeter (m) | 5.5 |
Reactor length (m) | 2.6 |
Rate of feed stream (mol/s) | 17,865 |
Input pressure (bar) | 75 |
Input temperature (K) | 513 |
Feed Mole Fraction | Values |
H2 | 0.6334 |
CH4 | 0.1006 |
CO2 | 0.0832 |
H2O | 0.00039 |
N2 | 0.093 |
CH3OH | 0.0049 |
CO | 0.085 |
Parameters | Inlet Flow | Outlet Flow (Vapor Phase) | Outlet Flow (Liquid Phase) |
---|---|---|---|
Molar flow (mol/s) | 17,217 | 15,955 | 1260 |
Component | Mole Fraction | Mole Fraction | Mole Fraction |
CH3OH | 0.1185 | 0.0568 | 0.8988 |
CO2 | 0.0598 | 0.0632 | 0.0173 |
CO | 0.0700 | 0.0754 | 0.0016 |
H2O | 0.0067 | 0.0020 | 0.0652 |
H2 | 0.5445 | 0.5871 | 0.0054 |
N2 | 0.0962 | 0.1036 | 0.0037 |
CH4 | 0.1043 | 0.1119 | 0.0080 |
Condenser Duty (KJ/s) | 138,861 |
Parameters | Model | Industrial Data | Error % | |
---|---|---|---|---|
Reactor Outlet | Reactor Inlet | Reactor Outlet | ||
Temperature (K) | 493.43 | 401 | 495 | 0.31 |
Mole Fraction | ||||
CH3OH | 0.1062 | 0.0037 | 0.104 | 2.14 |
CO2 | 0.0815 | 0.0849 | 0.0709 | 14.89 |
CO | 0.0227 | 0.0868 | 0.0251 | −9.42 |
H2O | 0.0204 | 0.001 | 0.0234 | −12.70 |
H2 | 0.5572 | 0.6461 | 0.5519 | 0.96 |
N2 | 0.1009 | 0.0828 | 0.1107 | −8.81 |
CH4 | 0.1133 | 0.0947 | 0.114 | −0.64 |
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Rahmatmand, B.; Rahimpour, M.R.; Keshavarz, P. Development of Two Novel Processes for Hydrogenation of CO2 to Methanol over Cu/ZnO/Al2O3 Catalyst to Improve the Performance of Conventional Dual Type Methanol Synthesis Reactor. Catalysts 2018, 8, 255. https://doi.org/10.3390/catal8070255
Rahmatmand B, Rahimpour MR, Keshavarz P. Development of Two Novel Processes for Hydrogenation of CO2 to Methanol over Cu/ZnO/Al2O3 Catalyst to Improve the Performance of Conventional Dual Type Methanol Synthesis Reactor. Catalysts. 2018; 8(7):255. https://doi.org/10.3390/catal8070255
Chicago/Turabian StyleRahmatmand, Behnaz, Mohammad Reza Rahimpour, and Peyman Keshavarz. 2018. "Development of Two Novel Processes for Hydrogenation of CO2 to Methanol over Cu/ZnO/Al2O3 Catalyst to Improve the Performance of Conventional Dual Type Methanol Synthesis Reactor" Catalysts 8, no. 7: 255. https://doi.org/10.3390/catal8070255
APA StyleRahmatmand, B., Rahimpour, M. R., & Keshavarz, P. (2018). Development of Two Novel Processes for Hydrogenation of CO2 to Methanol over Cu/ZnO/Al2O3 Catalyst to Improve the Performance of Conventional Dual Type Methanol Synthesis Reactor. Catalysts, 8(7), 255. https://doi.org/10.3390/catal8070255