Procede Gas Treating BV

Enschede, Netherlands

Procede Gas Treating BV

Enschede, Netherlands
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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.


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.


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.


Hamborg E.S.,Procede Gas Treating BV | Kersten S.R.,University of Twente | Versteeg G.F.,University of Groningen
Chemical Engineering Journal | Year: 2010

Liquid phase mass transfer coefficients have been measured in a controlled environment during gas absorption into a liquid and gas desorption from a liquid in a batch operated stirred tank reactor over a wide range of operating conditions. At identical operating conditions, the mass transfer coefficients for absorption and desorption appear to be the same within the reported experimental uncertainty. The desorption mass transfer coefficients depend, in the same manner as the absorption mass transfer coefficients, on the physico-chemical and the dynamic properties of the system, and can thus be related by the Sherwood, Reynolds, and Schmidt numbers. Desorption mass transfer processes can be further described by the well-known film theory, the penetration theory, the surface renewal theory, etc. in the same manner as absorption mass transfer processes. © 2010 Elsevier B.V.


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.


Penders-van Elk N.J.M.C.,Procede Gas Treating BV | Hamborg E.S.,Procede Gas Treating BV | Hamborg E.S.,Statoil | Huttenhuis P.J.G.,Procede Gas Treating BV | And 3 more authors.
International Journal of Greenhouse Gas Control | Year: 2013

In the present work the absorption of carbon dioxide in aqueous N-methyldiethanolamine (MDEA) and aqueous sodium carbonate with and without carbonic anhydrase (CA) was studied in a stirred cell contactor in the temperature range 298-333. K. The CA was present as free enzyme and is compared to the opportunity to immobilise CA on particles and on fixed packing. Based on the results with MDEA and sodium carbonate, the observed kinetics as a function of the free enzyme concentration are described. These results were incorporated into the Procede Process Simulator (Arendsen et al., 2012) to determine the impacts of the kinetic benefit of CA on commercial absorber sizing for carbon dioxide capture from flue gases. Based on simulations performed, CA in the absorption solution can provide substantial benefits for reducing absorber sizing with these normally kinetically limited, but energy efficient solvents. It was also shown that CA immobilised to fixed packing material is not a viable option for using CA in a carbon dioxide capture process. © 2012 Elsevier Ltd.


Penders-van Elk N.J.M.C.,Procede Gas Treating BV | Derks P.W.J.,Procede Gas Treating BV | Fradette S.,CO Solutions Inc. | Versteeg G.F.,University of Groningen
International Journal of Greenhouse Gas Control | Year: 2012

In present work the absorption of carbon dioxide in aqueous N-methyldiethanolamine (MDEA) solutions with and without the enzyme carbonic anhydrase has been studied in a stirred cell at 298K, with MDEA concentrations ranging from 0.5 to 4kmolm -3 and carbonic anhydrase concentrations ranging from 0 to 2275gm -3, respectively. The obtained experimental results show that carbonic anhydrase significantly enhances the absorption of carbon dioxide in aqueous MDEA solution. When the enzyme is present in the absorption solution, MDEA concentration does not materially influence on the absorption rate. Therefore, the enzyme does not enhance the reaction of CO 2 with MDEA, since the rate of this reaction is a function of the MDEA concentration. Rather, the enzyme enhances the reaction of carbon dioxide with water. In the presence of enzyme this reaction is not only first order in CO 2, but also first order in water. Thus, carbonic anhydrase may provide a solution for the efficient capture of carbon dioxide from flue gases by significantly increasing the kinetics of its absorption in MDEA, a tertiary amine which requires less energy for regeneration than monoethanolamine (MEA), the current industry benchmark. © 2012 Elsevier Ltd.


Klepacova K.,Procede Gas Treating B.V. | Huttenhuis P.J.G.,Procede Gas Treating B.V. | Derks P.W.J.,Procede Gas Treating B.V. | Versteeg G.F.,Procede Gas Treating B.V. | Versteeg G.F.,University of Groningen
Journal of Chemical and Engineering Data | Year: 2011

For the design of acid gas treating processes, vapor-liquid equilibrium (VLE) data must be available of the solvents to be applied. In this study the vapor pressures of seven frequently industrially used alkanolamines (diethanolamine, N-methylethanolamine, N,N-dimethylethanolamine, N,N-diethylethanolamine, diisopropanol-amine, 2-(2-aminoethoxy)ethanol, 2-amino-2-methyl-1-propanol) were measured in an ebulliometer. The VLE experiments were carried out at presssures between (1 and 400) kPa and at a maximum temperature of 453 K. The experimental data can be used to improve the thermodynamic models in gas treating processes and to determine the amine losses in the absorber and desorber. © 2011 American Chemical Society.


Hamborg E.S.,Procede Gas Treating BV | Derks P.W.J.,Procede Gas Treating BV | Van Elk E.P.,Procede Gas Treating BV | Versteeg G.F.,Procede Gas Treating BV | Versteeg G.F.,University of Groningen
Energy Procedia | Year: 2011

Process concepts of using alkanolamines in aqueous organic solvents have been evaluated by experimental work and process simulations using the Procede Process Simulator. N-methyldiethanolamine (MDEA), methanol, and ethanol were chosen as the respective alkanolamine and organic compounds in the current work. In previous work, the dissociation constants of protonated MDEA at infinite dilution in methanol-water and ethanol-water solvents and the initial mass transfer rates of CO 2 in 3 kmol m -3 MDEA in methanol-water and ethanol-water solvents were determined. In the current work, experimental values of the CO 2 vapor liquid equilibria in 3 kmol m -3 MDEA have been determined in methanol-water and ethanol-water solvents. The experimentally determined results have been implemented into the Procede Process Simulator, which has been used to simulate a CO 2 removal plant with 90% CO 2 removal based on the specification of the flue gas of an 827 MWe pulverized coal fired power plant. A solvent of 3 kmol m -3 MDEA in aqueous methanol solution was considered for conceptual purposes. The results indicatively show a maximum decrease in the reboiler duty of the desorber of about 7.5% at methanol fractions of about 0.06 compared to purely aqueous solutions and a reboiler temperature decrease with increasing methanol fractions. Further experimental results are, however, necessary in order to more precisely simulate CO 2 removal processes by alkanolamines in aqueous organic solvents. © 2011 Published by Elsevier Ltd.


Meerman J.C.,University Utrecht | Hamborg E.S.,Procede Gas Treating B.V. | 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.

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