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Apeldoorn, Netherlands

Hamborg E.S.,Procede Gas Treating BV | Hamborg E.S.,Statoil | Versteeg G.F.,University of Groningen
Chemical Engineering Journal | Year: 2012

The chemical enhancement factors have been measured in a controlled environment for absorption and desorption mass transfer processes in aqueous 2.0M MDEA solutions at temperatures of 298.15, 313.15, and 333.15K and the loading of CO 2 ranging from 0 to 0.8 in a batch-operated stirred tank reactor. At identical operating conditions, the chemical enhancement factor for absorption and desorption appears to be the same within the reported experimental uncertainty. In a continuous effort to describe the fundamentals of gas-liquid desorption processes [E.S. Hamborg, S.R.A. Kersten, G.F. Versteeg, Absorption and desorption mass transfer rates in non-reactive systems, Chem. Eng. J. 161 (2010) 191-195], it has been shown in the current work that a reactive absorbent influences the absorption and desorption rates to the same extent at identical operational conditions. © 2012 Elsevier B.V. Source


Hamborg E.S.,Procede Gas Treating BV | Hamborg E.S.,Statoil | Versteeg G.F.,University of Groningen
Chemical Engineering Journal | Year: 2012

The forward and reverse kinetic rate parameters have been determined for CO 2 absorption and desorption mass transfer processes in aqueous 2.0M MDEA solutions at temperatures of 298.15, 313.15, and 333.15K and the loading of CO 2 ranging from 0 to 0.8. The derived kinetic rate parameters have been based on the results of experimental work in a controlled environment in a batch operated stirred tank reactor. In a continuous effort to describe the fundamentals of gas-liquid desorption processes [1,2], it has within applied experimental conditions been shown that; (1) the forward and reverse kinetic rate parameters derived by an analytical relation based on the Higbie penetration theory are within 25% of those numerically derived by a system of partial differential equations based on the Higbie penetration theory. The analytical relations were based on reversible reactions of finite rate in solutions of different CO 2 loadings and diffusivities, (2) the reaction order of the forward reaction in solutions of different CO 2 loadings is close to unity, and in agreement with the proposed reaction mechanism, (3) Arrhenius type of equations already developed for correlation of forward kinetic rate parameters were further modified in order to sufficiently correlate reverse kinetic rate parameters. These types of equations thus form a tool for the correlation and prediction of reverse kinetic rate parameters for engineering purposes and (4) the experimentally determined forward and reverse kinetic rate parameters were accordingly found to be related by an overall temperature dependent chemical equilibrium constant. © 2012 Elsevier B.V. Source


Penders-van Elk N.J.M.C.,Procede Gas Treating BV | Fradette S.,CO Solutions Inc. | Versteeg G.F.,University of Groningen
Chemical Engineering Journal | Year: 2015

The absorption of carbon dioxide in various aqueous alkanolamine solutions have been studied with and without carbonic anhydrase respectively in a stirred cell reactor at 298K. The examined alkanolamines were: N,N-diethylethanolamine (DEMEA), N,N-dimethylethanolamine (DMMEA), monoethanolamine (MEA), triethanolamine (TEA) and tri-isopropanolamine (TIPA). This work confirms that the CO2 hydration is catalysed by the enzyme in presence of alkanolamines. The differences in reaction rate between the tested alkanolamines are attributed to the enzyme regeneration step in the mechanism - that is, an acid base reaction. A Langmuir-Hinshelwood-like equation has been postulated to describe the observed overall rate constant of the enzymatic reaction as a function of the enzyme concentration. The two kinetic constants in the postulated equation both depend exponentially on the pKa value of the alkanolamine present in the solution. © 2014 Elsevier B.V.All rights reserved. Source


Meerman J.C.,University Utrecht | Hamborg E.S.,Procede Gas Treating BV | Hamborg E.S.,Statoil | van Keulen T.,University Utrecht | And 3 more authors.
International Journal of Greenhouse Gas Control | Year: 2012

This study aimed to identify the optimal techno-economic configuration of CO 2 capture at steam methane reforming facilities using currently available technologies by means of process simulations. Results indicate that the optimal system is CO 2 capture with ADIP-X located between the water-gas shift and pressure swing adsorption units. Process simulations of this system configuration showed a CO 2 emission reduction of 60% at 41€/t CO 2 avoidance. This is at the lower end of the range reported in open literature for CO 2 capture at refineries (26-82€/t CO 2) and below the avoidance costs for CO 2 capture at natural gas-fired power plants (44-93€/t CO 2). CO 2 avoidance costs are dominated by the natural gas consumption, responsible for up to 66% of total costs. Using imported steam and electricity can reduce CO 2 avoidance costs by 45%. Addition of small amounts of piperazine to aqueous MDEA solutions results in up to 70% smaller absorbers or 10% lower reboiler heat duty. Optimising the whole capture process instead of individual units resulted in lower piperazine concentrations than the common industrial practice (3mass% vs. 5mass%). Finally, keeping the solvent rate constant when operating the capture unit below its design load resulted in a lower specific energy for CO 2 capture than when the solvent rate was downscaled with the syngas flow. © 2012 Elsevier Ltd. Source


Hamborg E.S.,Procede Gas Treating BV | van Aken C.,Procede Gas Treating BV | Versteeg G.F.,University of Groningen
Fluid Phase Equilibria | Year: 2010

The dissociation constants of protonated monoethanolamine and N-methyldiethanolamine have been determined in methanol-water, ethanol-water, and t-butanol-water solvents. The alcohol mole fractions were ranging from 0.2 to 0.95 and the temperatures from 283 to 323 K, 283 to 333 K, and at 298.15 K, respective to the different solvents. The experimental results are reported with the standard state thermodynamic properties. The basic strength of the protonated alkanolamine decreases with decreasing dielectric constant and increasing temperature of the solvent. By using the dissociation constants of the alkanolamines in pure water, it is shown that a Born treatment alone is not able to estimate the dissociation constants when the composition of the solvent is changed to an aqueous organic mixture. © 2009 Elsevier B.V. All rights reserved. Source

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