[1]杨文超,李舒宏,冯义康,等.N2在液态CO2中的溶解度分析[J].东南大学学报(自然科学版),2016,46(4):776-781.[doi:10.3969/j.issn.1001-0505.2016.04.017]
 Yang Wenchao,Li Shuhong,Feng Yikang,et al.Analysis of solubility on N2 in liquid CO2[J].Journal of Southeast University (Natural Science Edition),2016,46(4):776-781.[doi:10.3969/j.issn.1001-0505.2016.04.017]
点击复制

N2在液态CO2中的溶解度分析()
分享到:

《东南大学学报(自然科学版)》[ISSN:1001-0505/CN:32-1178/N]

卷:
46
期数:
2016年第4期
页码:
776-781
栏目:
能源与动力工程
出版日期:
2016-07-20

文章信息/Info

Title:
Analysis of solubility on N2 in liquid CO2
作者:
杨文超1李舒宏1冯义康2单贵苏1张小松1
1东南大学能源与环境学院, 南京210096; 2青岛海信日立空调系统有限公司, 青岛266510
Author(s):
Yang Wenchao1 Li Shuhong1 Feng Yikang2 Shan Guisu1 Zhang Xiaosong1
1School of Energy and Environment, Southeast University, Nanjing 210096, China
2Qingdao Hisense Hitachi Air-conditioning System Co. Ltd., Qingdao 266510, China
关键词:
低温碳捕集 溶解度 二元交互作用系数 参数优化
Keywords:
cryogenic carbon capture solubility binary interaction parameters parameter optimization
分类号:
TK01
DOI:
10.3969/j.issn.1001-0505.2016.04.017
摘要:
采用Henry常数法及PR,SRK状态方程法计算了N2在液态CO2中的溶解度.将溶解度计算结果与实验数据进行比较后得出:PR状态方程的计算精度最高,计算结果与实验数据的平均相对误差绝对值均小于9%;Henry常数法计算结果误差最大,计算结果与实验数据的平均相对误差绝对值均大于26%; N2的溶解度随温度降低或压力增大而逐渐增大.为进一步提高PR方程的计算精度,利用实验数据优化了N2与CO2之间的二元交互作用系数,并提出二元交互作用系数与温度、压力有关的关联式;将关联式运用于温度为220,240及250 K的N2溶解度计算中,计算结果与实验数据的相对误差绝对值均小于2%,当温度为220 K时,溶解度计算结果与实验数据的相对误差绝对值均小于0.7%,证明了所得关联式的准确性.
Abstract:
The solubility of N2 in liquid CO2 is calculated by using the Henry constant, PR(Peng-Robinson)and SRK(Soave-Redlich-Kwong)equation methods. The comparison results between calculation results with experimental data show that PR equation has the highest precision,and the average absolute values of relative deviation of calculation results and experimental data are less than 9%. The deviation of calculation results by using the Henry constant method is the largest, the average absolute values of the relative deviation of calculation results and the experimental data are more than 26%. With the decrease of the temperature and the increase of pressure, the solubility of N2 in liquid CO2 increases. In order to further improve the accuracy of the PR equation, the binary interaction parameters between N2 and CO2 are optimized using experimental data. In addition, a correlation between the binary interaction parameters with the temperature and pressure is proposed. Applying the correlation to the solubility calculations of N2 at 220, 240 and 250 K, the absolute values of the relative deviation of calculation results and the experimental data are less than 2%, and those are less than 0.7% at 220 K, proving the accuracy of the correlation.

参考文献/References:

[1] Theunissen T, Golombok M, Brouwers J J H, et al. Liquid CO2 droplet extraction from gases [J]. Energy, 2011, 36(5):2961-2967. DOI:10.1016/j.energy.2011.02.040.
[2] Zanganeh K E, Shafeen A. A novel process integration, optimization and design approach for large-scale implementation of oxy-fired coal power plants with CO2 capture [J]. International Journal of Greenhouse Gas Control, 2007, 1(7):47-54.
[3] Vrabec J, Kedia G K, Buchhauser U, et al. Thermodynamic models for vapor-liquid equilibria of nitrogen+oxygen+carbon dioxide at low temperatures [J]. Cryogenics, 2009, 49(2):72-79.
[4] Thiery R, Vidal J, Dubessy J. Phase equilibria modelling applied to fluid inclusions: Liquid-vapor equilibria and calculation of the molar volume in the CO2-CH4-N2 system [J]. Geochim Cosmochim Acta, 1994, 58(3):1073-1082. DOI:10.1016/0016-7037(94)90573-8.
[5] Li H, Yan J. Evaluating cubic equations of state for calculation of vapor-liquid equilibrium of CO2 and CO2-mixtures for CO2 capture and storage processes [J]. Applied Energy, 2009, 86(6):826-836. DOI:10.1016/j.apenergy.2008.05.018.
[6] 李舒宏, 李献亮, 杨文超, 等. 基于不同状态方程模型的N2/O2/CO2相平衡特性分析[J]. 化工学报, 2014, 65(S2):25-32. DOI:10.3969/j.issn.0438-1157.2014.z2.004.
  Li Shuhong,Li Xianliang,Yang Wenchao, et al. Phase equilibrium property analysis of N2/O2/CO2 based on several state equation models [J]. CIESC Jorunal, 2014, 65(S2):25-32. DOI:10.3969/j.issn.0438-1157.2014.z2.004.(in Chinese)
[7] Touret J. An empirical phase diagram for a part of the N2-CO2 system at low temperature[J]. Chemical Geology, 1982, 37(1):49-58. DOI:10.1016/0009-2541(82)90066-3.
[8] Graboski M S, Daubert T E. A modified soave equation of state for phase equilibrium calculations. 1.hydrocarbon systems[J]. Industrial & Engineering Chemistry Process Design and Development, 1978, 17(4):443-448. DOI:10.1021/i260068a009.
[9] 董军航, 汪朝晖, 徐南平,等. 方型状态方程在高压相平衡中的研究及应用 [J]. 南京化工大学学报,1997, 19(1):86-93.
  Dong Junhang, Wang Zhaohui, Xu Nanping, et al. Researches and applications of cubic equation of state for high pressure phase equilibria [J]. Journal of Nanjing University of Chemical Technology, 1997, 19(1):86-93.(in Chinese)
[10] 石玉美,顾安忠,鲁雪生,等.甲烷-氮气气液相平衡试验研究[J].天然气工业, 2000,20(4):80-82. DOI:10.3321/j.issn:1000-0976.2000.04.023.
  Shi Yumei,Gu Anzhong,Lu Xuesheng,et al. A study of methane-nitrogen gas-liquid phase equilibrium test [J].Natural Gas Industry, 2000,20(4):80-82. DOI:10.3321/j.issn:1000-0976.2000.04.023.(in Chinese)
[11] 石玉美,顾安忠,汪荣顺,等.CH4-N2-CO2三元汽液相平衡试验研究[J].天然气工业,2002, 22(5):84-87. DOI:10.3321/j.issn:1000-0976.2002.05.024.
  Shi Yumei,Gu Anzhong,Wang Rongshun,et al. An experiment on vapor-liquid equilibrium of CH4-N2-CO2 [J]. Natural Gas Industry, 2002, 22(5):84-87. DOI:10.3321/j.issn:1000-0976.2002.05.024.(in Chinese)
[12] Brown T S, Sloan E D, Kidnay A J. Vapor-liquid equilibria for the ternary system N2+CO2+nC4H10 at 250 and 270 K[J]. International Journal of Thermophysics, 1994, 15(6):1211-1219. DOI:10.1007/bf01458829.
[13] Brown T S, Niesen V G, Sloan E D, et al. Vapor-liquid equilibria for the binary systems of nitrogen, carbon dioxide, and n-butane at temperatures from 220 to 344 K[J]. Fluid Phase Equilibria, 1989, 53: 7-14. DOI:10.1016/0378-3812(89)80067-6.
[14] Mantovani M, Chiesa P, Valenti G, et al. Supercritical pressure-density-temperature measurements on CO2-N2,CO2-O2 and CO2-Ar binary mixtures[J]. Journal of Supercritical Fluids, 2012, 61(2):34-43. DOI:10.1016/j.supflu.2011.09.001.
[15] Xu N, Dong J, Wang Y, et al. High pressure vapor liquid equilibria at 293 K for systems containing nitrogen, methane and carbon dioxide[J]. Fluid Phase Equilibria, 1992, 81:175-186. DOI:10.1016/0378-3812(92)85150-7.
[16] Ahmad M, Gernert J, Wilbers E. Effect of impurities in captured CO2 on liquid-vapor equilibrium[J]. Fluid Phase Equilibria, 2013, 363(4):149-155. DOI:10.1016/j.fluid.2013.11.009.
[17] Peng D Y, Robinson D B. A new two-constant equation of state [J]. Industrial and Engineering Chemistry Fundamentals, 1976, 15(1): 59-64. DOI:10.1021/i160057a011.
[18] Soave G. Equilibrium constants from a modified Redlich-Kwong equation of state [J]. Chemical Engineering Science, 1972, 27(6): 1197-1203. DOI:10.1016/0009-2509(72)80096-4.
[19] 韦钦胜. 复杂体系化学平衡及相平衡计算方法的研究[D]. 青岛:中国海洋大学化学化工学院, 2007.
[20] Thiery R, Dubessy J. Improved modelling of vapour-liquid equilibria up to the critical region: Application to the CO2-CH4-N2 system [J]. Fluid Phase Equilibria, 1996, 121(1):111-123. DOI:10.1016/0378-3812(96)03029-4.

备注/Memo

备注/Memo:
收稿日期: 2015-12-13.
作者简介: 杨文超(1990—),男,硕士生;李舒宏(联系人),男,博士,教授,博士生导师,equart@seu.edu.cn.
基金项目: 江苏省“六大人才高峰”资助项目(2013-JNHB-014).
引用本文: 杨文超,李舒宏,冯义康,等.N2在液态CO2中的溶解度分析[J].东南大学学报(自然科学版),2016,46(4):776-781. DOI:10.3969/j.issn.1001-0505.2016.04.017.
更新日期/Last Update: 2016-07-20