Absorption of carbon dioxide into diisopropanolamine solutions of polar organic solvents

Hwang, Kyu-Suk; Park, Sang-Wook; Park, Dae‐Won; Oh, Kwang–Joong; Kim, Seong-Soo

doi:10.1016/j.jtice.2009.05.009

Cited by 25 publications

(27 citation statements)

References 15 publications

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“…The difference between the calculated value and the measured value is presented in Figure 10. The regression result showed that KGa was proportional to u to the power of 1.68 and the obtained value was closer than that reported earlier, which was between 0.58 and 1.67 [7,[9][10][11][12], and the empirical formula also shows that KGa increased with the increase in y1 and pH value. The overall mass transfer coefficients at different pH values, y1, and u could be estimated from Equation 14, and after the values were determined, the volume of the absorption tower could be estimated.…”

Section: Effects Of Variables On Kgasupporting

confidence: 79%

“…More than 1000 factories have developed the alkanolamine processes over the past few decades, among which the monoethylamine (MEA) process has the advantages in terms of price, characteristics, and recovery, although, it still consumes energy during recovery and brings cost burdens due to the treatment of concentrated CO 2 [5]. To develop an energy-saving process, new solvents [6][7][8][9][10], and new processes [11,12] have been proposed and explored to find a process with a lower regeneration energy requirement. Some of them studied the absorption kinetics of the mixed solvents [9,13,14].…”

Section: Introductionmentioning

confidence: 99%

“…To develop an energy-saving process, new solvents [6][7][8][9][10], and new processes [11,12] have been proposed and explored to find a process with a lower regeneration energy requirement. Some of them studied the absorption kinetics of the mixed solvents [9,13,14]. Alternatively, the hot potassium carbonate process is also applied in many cases, however, solvent regeneration and reuse during recovery not only increases the cost but also causes secondary pollution [1,15].…”

Section: Introductionmentioning

confidence: 99%

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CO2 Capture in A Bubble-Column Scrubber Using MEA/CaCl2/H2O Solution—Absorption and Precipitation

Chen

Zhuo

2020

Crystals

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This study used the solvent monoethylamine (MEA)/CaCl2/H2O to investigate CO2 absorption and CaCO3 crystallization in a bubble column scrubber. The variables explored were pH, gas flow rate, gas concentration, the liquid flow rate of the solution to absorb CO2, and CaCO3 crystallization. Under a continuous mode, the solution of CaCl2 was fed continuously, and the pH dropped after CO2 absorption. To maintain the set pH value, there was an automatic input of the MEA solvent into the bubble column. In addition to maintaining the pH, the solution could also absorb CO2 and produce CaCO3 crystals, which served two purposes. The results showed that there were mainly vaterite crystals. At different pH values, the lower the pH, the higher the precipitation rate of vaterite (Fp), and vice versa. However, under different gas flow rates, the Fp decreased as the pH value increased. Additionally, the process variables also affected the absorption rate (RA) and the overall mass-transfer coefficient (KGa) generally increased with increasing pH, gas concentration, and gas flow rate. However, it slowed down under operating conditions at high pH and high gas flow rate. Finally, correlation equations for RA, KGa, and Fp were also obtained and discussed in the study.

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Section: Effects Of Variables On Kgasupporting

confidence: 79%

Section: Introductionmentioning

confidence: 99%

Section: Introductionmentioning

confidence: 99%

See 1 more Smart Citation

CO2 Capture in A Bubble-Column Scrubber Using MEA/CaCl2/H2O Solution—Absorption and Precipitation

Chen

Zhuo

2020

Crystals

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“…However, energy consumption has been demonstrated to be the key factor reducing the efficiency of power plants by many researchers (Chakma, 1995;Oexmann and Kather, 2010;Tan et al, 2011). Recently, non-aqueous solutions have been extensively investigated using organic solvents, such as methanol, ethanol, ethylene glycol (EG), diethylene glycol (DEG), triethylene glycol (TEG), diethylene glycol monomethyl ether (DGME), Nmethyl-2-pyrrolidone (NMP) and tributyl phosphate (TBP) (Leites, 1998;Jou et al, 2000;Park et al, 2005Park et al, , 2006aUsubharatana and Tontiwachwuthikul, 2009;Hwang et al, 2010;Tan et al, 2011), which provide significant advantages as for reducing solvent decomposition at high temperature and saving water evaporation energy in the CO 2 stripping process (Barzagli et al, 2013Yu et al, 2013.…”

Section: Introductionmentioning

confidence: 99%

An investigation of the role of N-methyl-diethanolamine in non-aqueous solution for CO2 capture process using 13C NMR spectroscopy

Chen

Zhang

et al. 2015

International Journal of Greenhouse Gas Control

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“…9 In brief, the disadvantages of the conventional CO 2 capture processes with aqueous amine solutions are commonly ascribed to water. If water is substituted by other high-boilingpoint solvents, a considerable amount of thermal energy can be saved during the solvent heating cycle, 9,13 and the corrosion will also be eliminated.…”

Section: Introductionmentioning

confidence: 99%

Solubility of CO₂ in Nonaqueous Absorption System of 2-(2-Aminoethylamine)ethanol + Benzyl Alcohol

et al. 2014

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A mixture of 2-(2-aminoethylamine)ethanol (AEEA) with benzyl alcohol (BP) as absorbent was developed to reduce energy consumption in an amine-based CO 2 capture process. The solubility of CO 2 in the AEEA + BP solution was compared with AEEA + diethylene glycol (DEG), AEEA + triethylene glycol (TEG), and AEEA + H 2 O. The CO 2 loading (mol CO 2 /kg amine) at the same CO 2 partial pressure was in the order AEEA + H 2 O > AEEA + BP > AEEA + TEG > AEEA + DEG, and CO 2 loading of all these solutions increased with increasing vapor pressure of CO 2 . Besides, the CO 2 loading in AEEA + BP solution significantly decreased with increasing reaction temperature. The desorption rate of AEEA + BP solution was about 1.3 times faster than that of aqueous AEEA solution at the same desorption temperature, and AEEA + BP solution needed 30% time less than AEEA + H 2 O solution to reach reaction end point. The AEEA + BP solution showed stable repeatability in four cycles of absorption−desorption tests. INTRODUCTIONCO 2 capture technology in postcombustion continues to be one of the attractive options for the reduction of CO 2 emissions from the fossil fuel combustion process, particularly coal-fired power plants. Among the applicable CO 2 removal processes, chemical absorption using aqueous alkanolamine solutions is the most effective method. 1 The major aqueous alkanolamine solutions applied in the industrial process are monoethanolamine (MEA), diethanolamine (DEA), diglycolamine (DGA), N-methyldiethanolamine (MDEA), and 2-amino-2-methyl-1-propanol (AMP). Recently, attention has been paid to diamines which present a higher absorption capacity than primary and secondary alkanolamines. 2−5 Among them, aqueous 2-(2-aminoethylamine)ethanol (AEEA) solutions (5 to 25) wt % have a CO 2 capacity of (1.35 to 1.12) mol CO 2 /mol amine at 296 K and atmospheric pressure. 2,3 In the modern industry, the heat of regeneration for the stripping out of CO 2 from rich amine solutions in a regeneration process, which consists of sensible heat, reaction heat, latent heat of partial water, and partial latent heat of solvent vaporization, contributes (50 to 80) % of the total energy consumption in a chemical solvent based on the CO 2 separation process. 6 Many researchers have used blended amines, a solution of two or more amines in a variety of compositions, to improve absorption or desorption ability. 7,8 However, regardless of what the compositions of solutions are, the high sensible heat, and the latent heat of water vaporization will inevitably consume excessive energy in the regeneration process. During the regeneration process, a large amount of sensible heat is first utilized to increase the solution temperature to the stripping temperature because of the specific heat capacity of the aqueous solution. Meanwhile,

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Absorption of carbon dioxide into diisopropanolamine solutions of polar organic solvents

Cited by 25 publications

References 15 publications

CO2 Capture in A Bubble-Column Scrubber Using MEA/CaCl2/H2O Solution—Absorption and Precipitation

CO2 Capture in A Bubble-Column Scrubber Using MEA/CaCl2/H2O Solution—Absorption and Precipitation

An investigation of the role of N-methyl-diethanolamine in non-aqueous solution for CO2 capture process using 13C NMR spectroscopy

Solubility of CO₂ in Nonaqueous Absorption System of 2-(2-Aminoethylamine)ethanol + Benzyl Alcohol

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Absorption of carbon dioxide into diisopropanolamine solutions of polar organic solvents

Cited by 25 publications

References 15 publications

CO2 Capture in A Bubble-Column Scrubber Using MEA/CaCl2/H2O Solution—Absorption and Precipitation

CO2 Capture in A Bubble-Column Scrubber Using MEA/CaCl2/H2O Solution—Absorption and Precipitation

An investigation of the role of N-methyl-diethanolamine in non-aqueous solution for CO2 capture process using 13C NMR spectroscopy

Solubility of CO2 in Nonaqueous Absorption System of 2-(2-Aminoethylamine)ethanol + Benzyl Alcohol

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Solubility of CO₂ in Nonaqueous Absorption System of 2-(2-Aminoethylamine)ethanol + Benzyl Alcohol