Solubility of carbon dioxide in aqueous solutions of 2-amino-2-ethyl-1,3-propanediol

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1 Fluid Phase Equilibria 202 (2002) Solubility of carbon dioxide in aqueous solutions of 2-amino-2-ethyl-1,3-propanediol Jung-Yeon Park a, Sang Jun Yoon a, Huen Lee a,, Ji-Ho Yoon b, Jae-Goo Shim b, Jae Keun Lee b, Byung-Yeon Min b, Hee-Moon Eum b, Min Cheol Kang c a Department of Chemical and Biomolecular Engineering, Korea Advanced Institute of Science and Technology, Guseong-dong, Yuseong-gu, Daejeon , South Korea b Radiation and Environment Group, Korea Electric Power Research Institute, Munji-dong, Yusong-ku, Daejeon , South Korea c Korea Energy Management Corporation, 300-1, Pungdeokcheon-ri, Suji-eup, Yongin, Gyeonggi , South Korea Received 13 March 2002; accepted 13 May 2002 Abstract The solubilities of carbon dioxide in aqueous solutions of 2-amino-2-ethyl-1,3-propanediol (AEPD) were measured at , , and K over the partial pressure range of carbon dioxide from 1 to 3000 kpa. The concentrations of aqueous AEPD solutions were 10 and 30 mass%. The solubilities of carbon dioxide in aqueous 10 mass% AEPD solutions at K and 30 mass% at K were compared with those in aqueous solutions of various amines such as monoethanolamine (MEA), 2-amino-2-methyl-1,3-propanediol (AMPD), 2-amino- 2-methyl-1-propanol (AMP), and N-methyldiethanolamine (MDEA) Elsevier Science B.V. All rights reserved. Keywords: Vapor liquid equilibria (VLE); Carbon dioxide; AEPD; Absorption; Data 1. Introduction The issue of global climate change due to emissions of so-called man-made greenhouse gases including carbon dioxide is of great importance to the future development of energy and power technology. The study for removing carbon dioxide from natural or refinery gases has been made in many ways. The CO 2 absorption into a liquid agent is the most commonly used process for the bulk removal of carbon dioxide. Alkanolamines such as monoethanolamine (MEA) have been used as absorption agents and successfully applied in industrial processes. In the present work, 2-amino-2-ethyl-1,3-propanediol (AEPD), which is a sterically hindered amine, was studied for CO 2 absorbent. A sterically hindered amine is a primary amine in which the amino group Corresponding author. Tel.: ; fax: address: hlee@mail.kaist.ac.kr (H. Lee) /02/$ see front matter 2002 Elsevier Science B.V. All rights reserved. PII: S (02)

2 360 J.-Y. Park et al. / Fluid Phase Equilibria 202 (2002) is attached to a tertiary carbon atom, or a secondary amine in which the amino group is attached to a secondary or a tertiary carbon atom. Due to its structural bulkiness, the sterically hindered amine provides several advantages over other amines such as MEA in terms of its high CO 2 loading capacity and easy regeneration. A hindered amine reacts with carbon dioxide and produces very unstable carbamates and these unstable carbamates can be readily hydrolyzed to re-form free amines. The solubilities of carbon dioxide in aqueous 10 and 30 mass% AEPD solutions were measured at , , and K and over the partial pressure of carbon dioxide ranging from 1 to 3000 kpa. These solubility data are essential to the design of gas treating processes and the modeling of absorption phenomena. 2. Experimental section 2.1. Materials Aqueous alkanolamine solutions were prepared with distilled water, >99.5% MEA from the Aldrich Chemical Co., and 97% AEPD from Acros Organics. All the chemicals were used without further purification. The carbon dioxide and nitrogen gases were of commercial grade with a purity of 99.9% Apparatus The apparatus used for this work consisted of an equilibrium cell, gas chromatograph, pressure gauge and thermometer, circulation pump, valves, and cylinders of carbon dioxide, nitrogen, and helium. The equilibrium cell was made of 316 stainless steel with an internal volume of about 450 ml. This cell was connected to a gas chromatograph (Hewlett-Packard, 5890 Series II Plus) by a vapor sampling valve (Rheodyne. 7410) with a loop of about 500 l to determine the composition of vapor phase. For the gas chromatograph, the column was 1.8m 3 mm diameter and packed with Porapak Q and helium, carrier gas, with a flow rate of 30 ml/min and a thermal conductivity detector (TCD) were used for analysis. The temperatures of the oven, injector, and detector in the gas chromatograph were 40, 120, and 120 C, respectively. The equilibrium cell was immersed in a water bath maintained at ±0.1 C of the set point temperature by a refrigerator/heater (Jeio Tech, RBC-20) and the temperature in the equilibrium cell Table 1 Solubilities of carbon dioxide in aqueous MEA solutions at K 10 mass% MEA 15.3 mass% MEA P (kpa) α (mol of CO 2 /mol of MEA) P (kpa) α (mol of CO 2 /mol of MEA)

3 J.-Y. Park et al. / Fluid Phase Equilibria 202 (2002) Fig. 1. Solubilities of carbon dioxide in 15.3 mass% MEA aqueous solution at K: ( ) this work; ( ) Shen and Li [4]; ( ) Song et al. [5]. Table 2 Solubilities of carbon dioxide in aqueous AEPD solutions 10 mass% AEPD 30 mass% AEPD K K K K P (kpa) α (mol of CO 2 / mol of AEPD) P (kpa) α (mol of CO 2 / mol of AEPD) P (kpa) α (mol of CO 2 / mol of AEPD) P (kpa) α (mol of CO 2 / mol of AEPD)

4 362 J.-Y. Park et al. / Fluid Phase Equilibria 202 (2002) was measured by a K-type thermocouple with an accuracy of ±0.1 K. To measure the system pressure, a Heise gauge (CM , kpa range) was used with an accuracy of ±0.1% of the gauge range Procedure The cell was filled with 300 ml of aqueous amine solution and completely purged with nitrogen gas to remove remaining air at first and after that all nitrogen from the cell was vented to atmosphere. Then the amount of carbon dioxide determined by the pressure was fed into the cell. In particular, for the experiments at CO 2 partial pressures lower than atmospheric pressure, the mixed gas of carbon dioxide and nitrogen was used, as nitrogen did not react with aqueous amine solutions. The nitrogen gas was fed because it is not possible to measure the exact pressure of carbon dioxide at lower partial pressures. The composition of carbon dioxide could be then accurately determined from the gas chromatography. All vapor samples were analyzed four times at each equilibrium point. The average of the individual compositions was taken as the equilibrium composition at the specified condition. The reproducibility of vapor mole fraction was found to be within ± When the system pressure and vapor composition did not change any more during 10 h, the liquid and vapor phases in the cell were considered to reach an equilibrium state. The liquid samples withdrawn from the equilibrium cell were analyzed at least Fig. 2. Solubilities of carbon dioxide in 10 mass% aqueous AEPD solution: ( ) K; ( ) K; ( ) K.

5 J.-Y. Park et al. / Fluid Phase Equilibria 202 (2002) twice by the titration method [4]. The experimental error in the loading of CO 2 was estimated to be about ±3%. 3. Results and discussion To check the reliability of the equilibrium apparatus, the solubility of carbon dioxide in aqueous 15.3 mass% MEA solutions was measured at K and compared with the available data in the literature [4,5]. In addition, the solubility of carbon dioxide in aqueous 10 mass% MEA solutions at K was measured and also compared with those in aqueous AEPD solutions obtained at the same temperature. The experimental results of aqueous MEA solutions are listed in Table 1 and compared with the literature data in Fig. 1. A good agreement with the reference indicates the validity of the apparatus used in this study. The solubilities of carbon dioxide in aqueous 10 and 30 mass% AEPD solutions were measured at , , and K and over the partial pressure of carbon dioxide ranging from 1 to 3000 kpa. The experimental solubility data points are presented in Table 2 and plotted in Figs. 2 and 3. Solubilities were in the same manner in tendency as general amines, i.e. decreased with increasing temperature and increased with increasing CO 2 partial pressure. The temperature effect on the solubility of carbon Fig. 3. Solubilities of carbon dioxide in 10 and 30 mass% aqueous AEPD solutions at K: ( ) 10 mass%; ( ) 30 mass%.

6 364 J.-Y. Park et al. / Fluid Phase Equilibria 202 (2002) dioxide in aqueous AEPD solutions is shown in Fig. 2, while the influence of AEPD concentrations on the solubility is shown in Fig. 3. The solubilities of carbon dioxide in aqueous 10 mass% AEPD solutions appeared to be higher than those in aqueous 30 mass% AEPD solutions. As the AEPD concentrations increase, the corresponding solubilities decrease even though the absolute amount of carbon dioxide absorbed into the aqueous amine solutions increases when expressed as a mole ratio between carbon dioxide and amine. The solubilities of carbon dioxide in aqueous 10 mass% AEPD solutions at K and 30 mass% at K were compared with those in aqueous solutions of various amines such as MEA [2], AMPD [1], AMP [6], and MDEA [3] in Figs. 4 and 5. Both Figures show that the CO 2 loading capacity of aqueous AEPD solutions is found to be much higher than that of aqueous MEA solutions at higher pressure while becoming less at the lower pressure region. However, it must be noted that the intersecting points exist at certain pressures when plotted against the solubilities of carbon dioxide for two different types of amines, AEPD, a hindered one and MEA, an unhindered one. The CO 2 partial pressure at the point of intersection varies according to the equilibrium temperature and concentration of amines. For two different sterically hindered amines the solubilities of carbon dioxide in aqueous AEPD solutions appeared to be higher than those in aqueous AMPD solutions at the same condition. This feature indirectly confirms that the bulkiness of amine influences the solubility of carbon dioxide positively at higher CO 2 partial pressure. Fig. 4. Solubilities of carbon dioxide in 30 mass% aqueous alkanolamine solution at K: ( ) AEPD (this work); ( ) MEA (Jou et al. [2]); ( ) AMPD (Baek and Yoon [1]); ( ) MDEA (Jou et al. [3]); ( ) AMP (Seo and Hong [6]).

7 J.-Y. Park et al. / Fluid Phase Equilibria 202 (2002) Fig. 5. Solubilities of carbon dioxide in 10 mass% aqueous alkanolamine solution at K: ( ) AEPD (this work); ( ) MEA (this work); ( ) AMPD (Baek and Yoon [1]). In Fig. 4, the tendency of the solubility of CO 2 in aqueous AEPD solution was found to be similar to those in AMPD and MDEA solution. 4. Conclusion The solubility of carbon dioxide in aqueous AEPD solutions was measured at , , and K over the partial pressure of carbon dioxide ranging from 1 to 3000 kpa. The concentrations of aqueous AEPD solutions were 10 and 30 mass%. As a result of comparing the solubilities of carbon dioxide in aqueous 10 mass% AEPD solutions at K and 30 mass% at K with those in aqueous solutions of various amines such as MEA, AMPD, AMP, and MDEA, the CO 2 loading capacity of aqueous AEPD solutions was much better than that in aqueous MEA solutions and aqueous AMPD solutions at higher CO 2 partial pressures. Acknowledgements This work was supported by Grant 2000-C-CD02-P-01 from the Korea Energy Management Corporation R&D Headquarter and also partially by the Brain Korea 21 Project.

8 366 J.-Y. Park et al. / Fluid Phase Equilibria 202 (2002) References [1] J.I. Baek, J.H. Yoon, J. Chem. Eng. Data 43 (1998) [2] F.Y. Jou, A.E. Mather, F.D. Otto, Can. J. Chem. Eng. 73 (1995) [3] F.Y. Jou, F.D. Otto, A.E. Mather, Ind. Eng. Chem. Res. 33 (1994) [4] K.P. Shen, M.H. Li, J. Chem. Eng. Data 37 (1992) [5] J.H. Song, J.H. Yoon, H. Lee, J. Chem. Eng. Data 41 (1996) [6] D.J. Seo, W.H. Hong, J. Chem. Eng. Data 41 (1996)

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