吸收式工质对R152a+DMETrEG的汽液相平衡特性

doi:10.11949/j.issn.0438-1157.20170516

摘要/Abstract

摘要：

R152a（ODP=0，GWP=124）对环境友好，热力性能完善，而吸收剂三乙二醇二甲醚（DMETrEG）沸点较高，毒性较弱，对较多制冷剂都有很好的溶解能力。因此，R152a与DMETrEG的二元混合物是一种具有潜在应用价值的吸收制冷工质对。采用气液双循环法，实验研究了R152a+DMETrEG在293.15~353.15 K温度范围内的汽液相平衡特性；分别采用NRTL模型和Wilson模型对测得的汽液相平衡（VLE）数据关联对比。实验结果与关联结果具有良好的一致性，NRTL模型拟合计算结果与实验结果的平均相对偏差为1.80%，而Wilson模型拟合计算结果与实验结果的平均相对偏差为1.83%。当混合溶液中R152a摩尔分数大于0.8时，R152a活度系数接近1，混合溶液可近似视为理想溶液。

关键词: 汽液平衡, R152a, 三乙二醇二甲醚, 吸收式工质对, 色谱, 活度系数

Abstract:

R152a (ODP=0, GWP=124) is environmentally friendly and has good thermal performance. The absorbent, triethylene glycol dimethyl ether (DMETrEG), is less toxic, has high boiling temperature and good dissolution ability for more refrigerants. Therefore, the mixture of R152a and DMETrEG is considered as a potential absorption working pair. The vapor-liquid equilibrium(VLE) of R152a+DMETrEG in the temperature range of 293.15-353.15 K was studied by gas-liquid double-cycle method. NRTL model and Wilson model were used to correlate the experimental results. The results were in good agreement with the correlated results. The average relative deviation between the calculated results and the experimental results is 1.80% for NRTL model, and the average deviation between the calculated results and the experimental results is 1.83% for Wilson model. When mole faction of R152a in the solution of R152a and DMETrEG is larger than 0.8, activity coefficient of R152a is close to 1, therefore, this solution can be considered as an ideal solution approximately.

Key words: vapor liquid equilibrium, R152a, DMETrEG, absorbent-refrigerant pair, chromatography, activity coefficient

中图分类号:

TB61⁺6

方一波, 管文洁, 华超, 王琰铚, 韩晓红, 陈光明. 吸收式工质对R152a+DMETrEG的汽液相平衡特性[J]. 化工学报, 2017, 68(11): 4025-4034.

FANG Yibo, GUAN Wenjie, HUA Chao, WANG Yanzhi, HAN Xiaohong, CHEN Guangming. Vapor liquid equilibrium of absorption working pair R152a+DMETrEG[J]. CIESC Journal, 2017, 68(11): 4025-4034.

参考文献 36

[1]	ZHAI X Q, QU M, LI Y, et al. A review for research and new design options of solar absorption cooling systems[J]. Renewable and Sustainable Energy Reviews, 2011, 15(9):4416-4423.
[2]	IBARRA-BAHENA J, ROMERO R. Performance of different experimental absorber designs in absorption heat pump cycle technologies:a review[J]. Energies, 2014, 7(2):751-766.
[3]	陈国邦, 陈光明. 制冷与低温原理[M]. 2版. 北京:机械工业出版社, 2012:126-238. CHEN G B, CHEN G M. Principles of Refrigeration and Cryogenics[M]. 2nd ed. Beijing:China Macine Press, 2012:126-238.
[4]	孟学林. 热功复合驱动逆循环机理与HFC/酰胺类工质对汽液相平衡研究[D]. 北京:北京化工大学, 2013. MENG X L. Mechanisms of hybrid reverse cycle and vapor-liquid equilibrium of HFC/amides working pairs[D]. Beijing:Beijing University of Chemical Technology, 2013.
[5]	陈曙辉, 陈光明, 郑飞. 吸收式制冷工质的发展[J]. 制冷学报, 1998, (2):45-52. CHEN S H, CHEN G M, ZHENG F. Development of working pair in absorption refrigeration[J]. Journal of Refrigeration, 1998, (2):45-52.
[6]	洪大良. 新型吸收式制冷循环构建理论及其应用研究[D]. 杭州:浙江大学, 2013. HONG D L. Fundamentals and applications for creating novel absorption refrigeration cycles[D]. Hangzhou:Zhejiang University, 2013.
[7]	李国栋. 添加纳米颗粒的溴化锂溶液热物性及换热特性的实验研究[D]. 北京:北京建筑工程学院, 2009. LI G D. Experimental investigation on thermophysical properties and heat transfer characteristics of LiBr solution adding nano-particles[D]. Beijing:Beijing University of Civil Engineering and Architecture, 2009.
[8]	SARAVANAN R, MAIYA M P. Comparison of methanol-based working fluid combinations for a bubble pump-operated vapour absorption refrigerator[J]. International Journal of Energy Research, 1998, 22(8):715-731.
[9]	LI M, WANG L, WANG K, et al. Experimental measurement and modeling of solubility of LiBr and LiNO3 in methanol, ethanol, 1-propanol, 2-propanol and 1-butanol[J]. Fluid Phase Equilibria, 2011, 307(1):104-109.
[10]	GENSSLE A, STEPHAN K. Analysis of the process characteristics of an absorption heat transformer with compact heat exchangers and the mixture TFE-E181[J]. International Journal of Thermal Sciences, 2000, 39(1):30-38.
[11]	NOWACZYK U S F. Thermophysical properties of new working fluid systems for absorption processes[J]. International Journal of Refrigeration, 1992, 1(15):10-15.
[12]	李逍霄, 张敏, 李喆, 等. 吸收式动力循环工质R245fa+DMF体系汽液相平衡实验研究[J]. 工程热物理学报, 2014, (7):1260-1264. LI X X, ZHANG M, LI Z, et al. Measurement of vapor-liquid equilibria of a potential working pair of absorption power cycle-1,1,1,3,3-pentafluoropropane+N,N-dimethyl formamide[J]. Journal of Engineering Thermophysics, 2014, (7):1260-1264.
[13]	TSEREGOUNIS S I, RILEY M J. Solubility of HFC-134a refrigerant in glycol-type compounds:effects of glycol structure[J]. AIChE Journal, 1994, 40(4):726-737.
[14]	HAN X, GAO Z, XU Y, et al. Solubility of refrigerant 1,1,1,2-tetrafluoroethane in the N,N-dimethyl formamide in the temperature range from (263.15 to 363.15) K[J]. Journal of Chemical & Engineering Data, 2011, 56(5):1821-1826.
[15]	HAN X H, XU Y J, GAO Z J, et al. Vapor-liquid equilibrium study of an absorption heat transformer working fluid of (HFC-32+ DMF)[J]. Journal of Chemical & Engineering Data, 2011, 56(4):1268-1272.
[16]	GAO Z, XU Y, LI P, et al. Solubility of refrigerant trifluoromethane in N,N-dimethyl formamide in the temperature range from 283.15 K to 363.15 K[J]. International Journal of Refrigeration, 2012, 35(5):1372-1376.
[17]	ZEHIOUA R, COQUELET C, MENIAI A, et al. p-T-x measurements for some working fluids for an absorption heat transformer:1,1,1,2-tetrafluoroethane (R134a) + dimethylether diethylene glycol (DMEDEG) and dimethylether triethylene glycol (DMETrEG)[J]. Journal of Chemical & Engineering Data, 2010, 55(8):2769-2775.
[18]	李新如, 沈彦曙, 孟学林, 等. R152a-DMF体系汽液相平衡研究[J]. 工程热物理学报, 2013, (3):389-392. LI X R, SHEN Y S. MENG X L, et al. Vapor-liquid equilibrium (VLE) for the system 1,1-difluoroethane-N,N-dimethylformamide[J]. Journal of Engineering Thermophysics, 2013, (3):389-392.
[19]	JING X, DENG R, ZHENG D. Measurement and correlation of isothermal vapor-liquid equilibrium of fluoroethane +N,N-dimethylacetamide, fluoroethane + N-methyl-2-pyrrolidone, and 1,1,1,2-tetrafluoroethane +N,N-dimethylacetamide systems[J]. Journal of Chemical & Engineering Data, 2013, 58(11):3289-3296.
[20]	ZHANG M, ZHENG D, YANG W, et al. Measurement and correlation of isothermal vapor-liquid equilibrium of 1,1,1,3,3-pentafluoropropane +N,N-dimethylacetamide and 1,1,1,3,3,3-hexafluoropropane +N,N-dimethylacetamide/diethylene glycol dimethyl ether systems[J]. Journal of Chemical & Engineering Data, 2014, 59(11):3912-3919.
[21]	CORONAS A, MAINAR A M, PATIL K R, et al. Solubility of 1,1,1,2-tetrafluoroethane in triethylene glycol gimethyl ether[J]. Journal of Chemical & Engineering Data, 2002, 47(1):56-58.
[22]	DENG R, JING X, ZHENG D, et al. Vapor-liquid equilibrium measurements and assessments of fluoroethane +N,N-dimethylformamide and fluoroethane + dimethylether diethylene glycol systems for the hybrid refrigeration cycle[J]. International Journal of Refrigeration, 2014, 43:176-186.
[23]	SHARIATI A, GUTKOWSKI K, PETERS C J. Comparison of the phase behavior of some selected binary systems with ionic liquids[J]. AIChE Journal, 2005, 51(5):1532-1540.
[24]	SHIFLETT M B, YOKOZEKI A. Solubility and diffusivity of hydrofluorocarbons in room-temperature ionic liquids[J]. AIChE Journal, 2006, 52(3):1205-1219.
[25]	SHIFLETT M B, YOKOZEKI A. Phase equilibria of hydrofluorocarbon-4310mee mixtures with ionic liquids:miscibility ofthreo-anderythro-diastereomers in ionic liquids[J]. Industrial & Engineering Chemistry Research, 2008, 47(3):926-934.
[26]	REN W, SCURTO A M. Phase equilibria of imidazolium ionic liquids and the refrigerant gas, 1,1,1,2-tetrafluoroethane(R-134a)[J]. Fluid Phase Equilibria, 2009, 286(1):1-7.
[27]	DONG L, ZHENG D, SUN G, et al. Vapor-liquid equilibrium measurements of difluoromethane +[Emim]OTf, difluoromethane +[Bmim]OTf, difluoroethane +[Emim]OTf, and difluoroethane +[Bmim]OTf systems[J]. Journal of Chemical & Engineering Data, 2011, 56(9):3663-3668.
[28]	LIU X, HE M, LV N, et al. Vapor-liquid equilibrium of three hydrofluorocarbons with[HMIM] [Tf2N] [J]. Journal of Chemical & Engineering Data, 2015, 60(5):1354-1361.
[29]	王旭阳. R152a在微圆管内凝结流型与换热的研究[D]. 北京:清华大学, 2012. WANG X Y. Study on condensation flow regime and heat transfer of R152a in micro-tubes[D]. Beijing:Tsinghua University, 2012.
[30]	WANG Q, XU Y J, CHEN X, et al. Experimental studies on a mixture of HFC-32/125/161 as an alternative refrigerant to HCFC-22 in the presence of polyol ester[J]. Fluid Phase Equilibria, 2010, 293(1):110-116.
[31]	HAN X, GAO Z, LEI J, et al. Isothermal vapor-liquid equilibrium of the ternary mixture of 1,1,1,2-tetrafluoroethane +2,3,3,3-tetrafluoroprop-1-ene + dimethyl ether at temperatures from 253.15 K to 323.15 K[J]. Journal of Chemical & Engineering Data, 2015, 60(8):2219-2225.
[32]	韩晓红. 状态方程混合法则及混合制冷剂相平衡研究[D]. 杭州:浙江大学, 2005. HAN X H. Study of mixing rules for equation of state and vapor-liquid equilibrium of mixture refrigerants[D]. Hangzhou:Zhejiang University, 2005.
[33]	MARCHI P, SCALABRIN G, IHMELS E C, et al. Bubble pressure measurements for the (1,1,1,2-tetrafluoroethane+triethylene glycol dimethyl ether) system[J]. The Journal of Chemical Thermodynamics, 2006, 38(11):1247-1253.
[34]	HAN X H, YANG Z Z, GAO Z J, et al. Isothermal vapor-liquid equilibrium of HFC-161+ DMETrEG within the temperature range of 293.15-353.15 K and comparison for HFC-161 combined with different absorbents[J]. Journal of Chemical & Engineering Data. 2016, 61(3):1321-1327.
[35]	HURON M J, VIDAL J. New mixing rules in simple equations of state for representing vapour-liquid equilibria of strongly non-ideal mixtures[J]. Fluid Phase Equilibria, 1979, 3(4):255-271.
[36]	WONG D S H, SANDLER S I. A theoretically correct mixing rule for cubic equations of state[J]. AIChE Journal, 1992, 38(5):671-680.