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Gary T Rochelle - One of the best experts on this subject based on the ideXlab platform.
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absorption and desorption rates of carbon dioxide with Monoethanolamine and piperazine
Energy Procedia, 2009Co-Authors: Ross Dugas, Gary T RochelleAbstract:CO2 absorption/desorption was MEAsured in a wetted wall column at 40 and 60 ∘C with 7, 9, 11, and 13 m Monoethanolamine (MEA) and 2, 5, 8, and 12 m piperazine (PZ) at various CO2 loadings. 8 m PZ has about a 75% greater CO2 capacity than 7 m MEA. CO2 absorption and desorption is 2–3 times faster with PZ than with MEA at equivalent CO2 partial pressure. The CO2 flux normalized by the liquid side partial pressure driving force, kg, for both MEA and PZ is practically independent of temperature and amine concentration over the range of these experiments when represented as a function of the equilibrium partial pressure at 40 ∘C. Normalized flux decreases a factor of 10 as the equilibrium partial pressure at 40 ∘C increases from 100 to 10 000 Pa.
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carbon dioxide absorption and desorption in aqueous Monoethanolamine solutions in a rotating packed bed
Industrial & Engineering Chemistry Research, 2007Co-Authors: Majeed S Jassim, Gary T Rochelle, Dag Eimer, Colin RamshawAbstract:The absorption and desorption of carbon dioxide in aqueous Monoethanolamine (MEA) was MEAsured in a rotating packed bed of size 398 mm outside diameter, 156 mm inside diameter, and axial depth 25 mm. The effect of lean amine temperature (20 and 40 °C), peripheral rotor gravity (31 and 87 g), and various MEA concentrations were investigated. Using MEA concentrations above 30 wt % achieved lower CO2 penetration levels. This is particularly pronounced for the 100% MEA solution. Comparison with conventional columns showed the advantages of using rotating packed beds in terms of saving size and space and efficient operation.
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oxidation inhibitors for copper and iron catalyzed degradation of Monoethanolamine in co2 capture processes
Industrial & Engineering Chemistry Research, 2006Co-Authors: George S Goff, Gary T RochelleAbstract:This study examines the effect of a number of additives on the oxidative degradation of Monoethanolamine (MEA) in the presence of dissolved Cu. Additives were selected from three categories: O2 scavengers and reaction inhibitors, chelating agents, and stable salts. Three proprietary inhibitors have been identified that significantly inhibit the rate of degradation at concentrations below 100 mM. Inhibitor A is a stable compound, while Scavengers B and C are stoichiometrically degraded to products that must be removed in an industrial application. Hydroquinone, ascorbic acid, manganese sulfate, and potassium permanganate all increased the rate of oxidative degradation. EDTA (ethylene-diamine-tetraacetic acid) was an effective chelating agent but lost inhibiting capacity over time. Phosphate was a weak chelating agent. Heat stable salts, including potassium chloride, potassium bromide, and potassium formate, were also ineffective oxidation inhibitors. Potassium formate was the strongest of the stable salts...
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absorption of carbon dioxide in aqueous piperazine methyldiethanolamine
Aiche Journal, 2002Co-Authors: Sanjay Bishnoi, Gary T RochelleAbstract:Carbon dioxide absorption in 0.6 M piperazine (PZ)/4 M methyldiethanolamine (MDEA) was MEAsured in a wetted wall contactor. The data were simulated using a model that accounts for chemical reactions and transport effects with the eddy diffusivity theory. PZ/MDEA blends absorb CO 2 faster than Monoethanolamine (MEA) or diethanolamine (DEA) blends with MDEA at similar concentrations. The reaction of PZ to form a monocarbamate is dominant at low loading ( 50%) only at the top of the absorber.
Amornvadee Veawab - One of the best experts on this subject based on the ideXlab platform.
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corrosivity of single and blended amines in co2 capture process
Energy Procedia, 2013Co-Authors: Prakashpathi Gunasekaran, Amornvadee Veawab, Adisorn AroonwilasAbstract:Abstract This work investigated corrosion of carbon steel in the CO 2 capture process using various types of CO 2 absorption solvents. The tested solvents included Monoethanolamine (MEA), diethanolamine (DEA), methyl diethanolamine (MDEA), 2-amino-2-methyl-1-propanol (AMP), piperazine (PZ), and their blends. A series of laboratory corrosion tests was carried out using electrochemical techniques (cyclic potentiodynamic polarization and impedance MEAsurements) under CO 2 saturation and 80 °C for most experiments. Results show that the corrosivity order for the single amine systems was MEA > AMP > DEA > PZ > MDEA while the corrosivity order for blended amine systems was MEA- - -MDEA > MDEA-PZ > AMP-PZ.
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electrochemical investigation on the effect of heat stable salts on corrosion in co2 capture plants using aqueous solution of MEA
Industrial & Engineering Chemistry Research, 2006Co-Authors: W Tanthapanichakoon, Amornvadee Veawab, Bryce McgarveyAbstract:Amine treating plants have long encountered the problem of solvent degradation associated with nonregenerable heat-stable salts. This work investigated the effect of six heat-stable salts on corrosion of process equipment made of carbon steel 1018 and stainless steel 304. The investigation was done by conducting electrochemical corrosion experiments in a 5 kmol/m3 aqueous solution of Monoethanolamine (MEA) at 80 °C under 0.20 mol/mol CO2 loading. The results show that heat-stable salts caused the solution corrosiveness to increase to various degrees, depending upon type and concentration of salt. Oxalate was the most corrosive, followed by malonate and formate. No salts induced pitting corrosion on either test material.
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polarization behavior and performance of inorganic corrosion inhibitors in Monoethanolamine solution containing carbon dioxide and heat stable salts
Corrosion, 2005Co-Authors: W Tanthapanichakoon, Amornvadee VeawabAbstract:Abstract This work has extended the knowledge of corrosion inhibition by sodium metavanadate (NaVO3) and copper carbonate (CuCO3) in the carbon dioxide (CO2) separation process using aqueous solutions of Monoethanolamine (MEA). The inhibition behavior and performance of these two inhibitors were examined using the electrochemical polarization technique in a 5-kmol/m3 MEA saturated with CO2 at 80°C. The results showed that NaVO3 generally offered superior inhibition performance over CuCO3. The performance of both inhibitors deteriorated when the heat-stable amine salt represented by oxalate was present in the solution. The CuCO3 was found to induce some pitting tendency but NaVO3 did not.
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characterization and comparison of the co2 absorption performance into single and blended alkanolamines in a packed column
Industrial & Engineering Chemistry Research, 2004Co-Authors: Amornvadee VeawabAbstract:The performance of carbon dioxide (CO2) absorption into aqueous solutions of single and blended alkanolamines was evaluated experimentally in a bench-scale absorber packed with high-efficiency packings. The absorption experiments were conducted under atmospheric pressure, using a feed gas mixture containing 10% CO2 and 90% nitrogen. Monoethanolamine (MEA), diethanolamine (DEA), diisopropanolamine (DIPA), methyldiethanolamine (MDEA), 2-amino-2-methyl-1-propanol (AMP), and their mixtures including MEA−MDEA, DEA−MDEA, MEA−AMP, and DEA−AMP were tested in this work. The absorption performance was presented in terms of the CO2 removal efficiency, absorber height requirement, effective interfacial area for mass transfer, and overall mass-transfer coefficient (KGae). Comparison of the absorption performance between the tested alkanolamines was made over ranges of operating conditions to establish the correlation between single- and blended-alkanolamine systems.
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identification of oxidizing agents in aqueous amine co2 systems using a mechanistic corrosion model
Corrosion Science, 2002Co-Authors: Amornvadee Veawab, Adisorn AroonwilasAbstract:Abstract The purpose of this paper was to perform studies in order to obtain a better understanding of corrosion in an aqueous amine–CO 2 environment. A mechanistic corrosion model, built as a fortran-90 program, is established to identify the oxidizing agents responsible for corrosion reactions. The model incorporates the rigorous electrolyte nonrandom two-liquid (NRTL) equilibrium model and mixed potential theory in order to simulate the concentrations of chemical species and polarization behavior taking place at a metal–solution interface. The simulation results, based on Monoethanolamine (MEA) system, indicates that bicarbonate ion (HCO 3 − ) and water (H 2 O) are the primary oxidizing agents and hydrogen ion (H + ) or hydronium ion (H 3 O + ) plays an insignificant role in the reduction reaction.
Syamalendu S Bandyopadhyay - One of the best experts on this subject based on the ideXlab platform.
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density and viscosity of aqueous solutions of n methyldiethanolamine Monoethanolamine n methyldiethanolamine diethanolamine 2 amino 2 methyl 1 propanol Monoethanolamine and 2 amino 2 methyl 1 propanol diethanolamine
Journal of Chemical & Engineering Data, 2003Co-Authors: Bishnu P Mandal, Madhusree Kundu, Syamalendu S BandyopadhyayAbstract:The densities and viscosities of aqueous blends of N-methyldiethanolamine (MDEA) and 2-amino-2-methyl-1-propanol with Monoethanolamine (MEA) and diethanolamine (DEA) have been MEAsured at (25, 30, 35, 40, 45, and 50) °C. The total amine strength in the solution was kept at 30 mass % in view of recent interest in using concentrated amine solutions in gas treating. Correlations for the density and viscosity of the ternary mixtures are presented.
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removal of carbon dioxide by absorption in mixed amines modelling of absorption in aqueous mdea MEA and amp MEA solutions
Chemical Engineering Science, 2001Co-Authors: Bishnupada Mandal, M Guha, Asok K Biswas, Syamalendu S BandyopadhyayAbstract:This work presents an investigation of CO 2 absorption into aqueous blends of methyldiethanolamine (MDEA) and Monoethanolamine (MEA), as well as 2-amino-2-methyl-1-propanol (AMP) and Monoethanolamine (MEA). The combined mass transfer-reaction kinetics-equilibrium model to describe CO 2 absorption into the amine blends has been developed according to Higbie's penetration theory following the work of Hagewiesche et al. (Chem. Eng. Sci. 50 (1995) 1071). The model predictions have been found to be in good agreement with the experimental rates of absorption of CO 2 into (MDEA + MEA + H 2 O) of this work and into (AMP + MEA + H 2 O) reported by Xiao et al. (Chem. Eng. Sci. 55 (2000) 161), MEAsured at higher contact times using wetted wall contactor. The good agreement between the model predicted rates and enhancement factors and the experimental results indicate that the combined mass transfer-reaction kinetics-equilibrium model with the appropriate use of model parameters can effectively represent CO 2 mass transfer for the aqueous amine blends MDEA/MEA and AMP/MEA.
Paul Feron - One of the best experts on this subject based on the ideXlab platform.
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systematic study of aqueous Monoethanolamine MEA based co2 capture process techno economic assessment of the MEA process and its improvements
Applied Energy, 2016Co-Authors: Wardhaugh Leigh, Paul Feron, Moses O TadeAbstract:Abstract The present study investigated the technical and economic performance of the Monoethanolamine (MEA)-based post-combustion capture process and its improvements integrated with a 650-MW coal-fired power station. A rigorous, rate-based model developed in Aspen Plus® was employed to evaluate technical performance, while a comprehensive economic model was used to determine the required capital investment and evaluate economic performance. The techno-economic model was validated with published cost results. Our estimation of the capital investment for the baseline MEA capture plant was US$1357/kW, with a CO 2 avoided cost of US$86.4/tonne. We then proposed process improvements such as parameter optimisation, lean/rich heat exchanger optimisation and flow sheet modifications to improve energy and cost performance. The combined process improvements reduced the capital investment by US$72/kW (a 5.3% saving) while cutting overall energy consumption by 24.5 MW/h (a 13.5% reduction). As a result, the CO 2 avoided cost fell to $75.1/tonne CO 2 , a saving of US$11.3/tonne CO 2 compared with the baseline. Lastly, we performed a sensitivity study and cost breakdown analysis to understand how the CO 2 avoided cost would be apportioned to the economic and technical parameters. The results indicate the directions of technical development to further improve the economic viability of the CO 2 capture process.
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co2 absorption into aqueous amine blended solutions containing Monoethanolamine MEA n n dimethylethanolamine dMEA n n diethylethanolamine deea and 2 amino 2 methyl 1 propanol amp for post combustion capture processes
Chemical Engineering Science, 2015Co-Authors: William Conway, Stefan Bruggink, Yaser Beyad, Graeme Puxty, Ignacio Meliancabrera, Paul FeronAbstract:Presently Monoethanolamine (MEA) remains the industrial standard solvent for CO2 capture processes. Operating issues relating to corrosion and degradation of MEA at high temperatures and concentrations, and in the presence of oxygen, in a traditional PCC process, have introduced the requisite for higher quality and costly stainless steels in the construction of capture equipment and the use of oxygen scavengers and corrosion inhibitors. While capture processes employing MEA have improved significantly in recent times there is a continued attraction towards alternative solvents systems which offer even more improvements. This movement includes aqueous amine blends which are gaining momentum as new generation solvents for CO2 capture processes. Given the exhaustive array of amines available to date endless opportunities exist to tune and tailor a solvent to deliver specific performance and physical properties in line with a desired capture process. The current work is focussed on the rationalisation of CO2 absorption behaviour in a series of aqueous amine blends incorporating Monoethanolamine, N,N-dimethylethanolamine (DMEA), N,N-diethylethanolamine (DEEA) and 2-amino-2-methyl-1-propanol (AMP) as solvent components. Mass transfer/kinetic MEAsurements have been performed using a wetted wall column (WWC) contactor at 40°C for a series of blends in which the blend properties including amine concentration, blend ratio, and CO2 loadings from 0.0-0.4 (moles CO2/total moles amine) were systematically varied and assessed. Equilibrium CO2 solubility in each of the blends has been estimated using a software tool developed in Matlab for the prediction of vapour liquid equilibrium using a combination of the known chemical equilibrium reactions and constants for the individual amine components which have been combined into a blend.From the CO2 mass transfer data the largest absorption rates were observed in blends containing 3M MEA/3M Am2 while the selection of the Am2 component had only a marginal impact on mass transfer rates. Overall, CO2 mass transfer in the fastest blends containing 3M MEA/3M Am2 was found to be only slightly lower than a 5M MEA solution at similar temperatures and CO2 loadings. In terms of equilibrium behaviour a slight decrease in the absorption capacity (moles CO2/mole amine) with increasing Am2 concentration in the blends with MEA was observed while cyclic capacity followed the opposite trend. Significant increases in cyclic capacity (26-111%) were observed in all blends when compared to MEA solutions at similar temperatures and total amine concentrations. In view of the reasonable compromise between CO2 absorption rate and capacity a blend containing 3M MEA and 3M AMP as blend components would represent a reasonable alternative in replacement of 5M MEA as a standalone solvent.
Adisorn Aroonwilas - One of the best experts on this subject based on the ideXlab platform.
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corrosivity of single and blended amines in co2 capture process
Energy Procedia, 2013Co-Authors: Prakashpathi Gunasekaran, Amornvadee Veawab, Adisorn AroonwilasAbstract:Abstract This work investigated corrosion of carbon steel in the CO 2 capture process using various types of CO 2 absorption solvents. The tested solvents included Monoethanolamine (MEA), diethanolamine (DEA), methyl diethanolamine (MDEA), 2-amino-2-methyl-1-propanol (AMP), piperazine (PZ), and their blends. A series of laboratory corrosion tests was carried out using electrochemical techniques (cyclic potentiodynamic polarization and impedance MEAsurements) under CO 2 saturation and 80 °C for most experiments. Results show that the corrosivity order for the single amine systems was MEA > AMP > DEA > PZ > MDEA while the corrosivity order for blended amine systems was MEA- - -MDEA > MDEA-PZ > AMP-PZ.
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mass transfer efficiency of a spray column for co2 capture by MEA
Energy Procedia, 2009Co-Authors: Jeffery Kuntz, Adisorn AroonwilasAbstract:Abstract A parametric study of carbon dioxide (CO 2 ) absorption performance into an aqueous solution of Monoethanolamine (MEA) in the spray column was carried out experimentally over wide ranges of process conditions. The performance of the spray was interpreted in terms of the overall mass transfer coefficient (K G a e ) and was found to vary with process parameters, including gas flow rate, liquid flow rate, CO 2 partial pressure, MEA concentration, CO 2 loading, and size of spray nozzle. The performance of the spray column was compared to that of a packed column and showed a promise for CO 2 capture application.
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identification of oxidizing agents in aqueous amine co2 systems using a mechanistic corrosion model
Corrosion Science, 2002Co-Authors: Amornvadee Veawab, Adisorn AroonwilasAbstract:Abstract The purpose of this paper was to perform studies in order to obtain a better understanding of corrosion in an aqueous amine–CO 2 environment. A mechanistic corrosion model, built as a fortran-90 program, is established to identify the oxidizing agents responsible for corrosion reactions. The model incorporates the rigorous electrolyte nonrandom two-liquid (NRTL) equilibrium model and mixed potential theory in order to simulate the concentrations of chemical species and polarization behavior taking place at a metal–solution interface. The simulation results, based on Monoethanolamine (MEA) system, indicates that bicarbonate ion (HCO 3 − ) and water (H 2 O) are the primary oxidizing agents and hydrogen ion (H + ) or hydronium ion (H 3 O + ) plays an insignificant role in the reduction reaction.