亚临界有机朗肯循环系统工质筛选及热经济性分析

doi:10.11949/0438-1157.20210245

摘要/Abstract

摘要：

针对开口热源与闭口热源两种热源类型，选取423.15和463.15 K两种热源温度，模拟分析采用非共沸混合工质亚临界有机朗肯循环（ORC）热力学及热经济性特性。四种热经济性指标［平均化发电成本（LEC）、单位净输出功换热器面积（APR）、单位时间成本（Z）以及净输出功指标（NPI）］结果具有一致性，具有相同的抛物线形变化趋势。随着选取工质临界温度的升高，各热经济性指标发生规律性变化，其中由热力学筛选准则筛选的工质具有较高热经济性能，表明热力学筛选准则在热经济性方面同样具有较高的适用性。

关键词: 亚临界有机朗肯循环, 非共沸混合工质, 工质筛选准则, 热经济性分析

Abstract:

For the two types of heat sources, open heat source and closed heat source, two heat source temperatures of 423.15 K and 463.15 K were selected, and the none-azeotropic mixed working fluid subcritical organic Rankine cycle (ORC) thermodynamic and thermal economic characteristics were used for simulation analysis. Four thermo-economic indexes are selected, such as levelized energy cost (LEC), area per unit of net power (APR), cost per unit of time (Z) and net power index (NPI). The results show that four thermo-economic indexes are consistent and show same parabolic change trend. With the increase of fluids critical temperature, thermo-economic indexes change regularly. The working fluids selected by the thermodynamic screening criteria have higher thermo-economic performance, indicating that the thermodynamic screening criteria also show high applicability in thermo-economic analysis.

Key words: sub-critical organic Rankine cycle, zeotropic mixtures, working fluid selection criteria, thermo-economic analysis

中图分类号:

TQ 028.8

李子航, 王占博, 苗政, 纪献兵. 亚临界有机朗肯循环系统工质筛选及热经济性分析[J]. 化工学报, 2021, 72(9): 4487-4495.

Zihang LI, Zhanbo WANG, Zheng MIAO, Xianbing JI. Working fluid selection and thermo-economic analysis of sub-critical organic Rankine cycle[J]. CIESC Journal, 2021, 72(9): 4487-4495.

图/表 8

图1 ORC系统设备流程及T-s图

Fig.1 Schematic diagram and T-s diagram of ORC

表1 烷烃工质基本参数（质量分数1~0变化）

Table 1 Fundamental parameters of alkane mixtures

工质名称	临界温度/K	临界压力/MPa
propane/isobutane	369.89~407.81	3.63~4.33
propane/butane	369.89~425.13	3.8~4.38
isobutane/isopentane	407.81~460.35	3.38~3.75
isobutane/pentane	407.81~469.7	3.37~3.82
butane/isopentane	425.13~460.35	3.38~3.8
butane/pentane	425.13~469.7	3.37~3.81
isopentane/hexane	460.35~507.82	3.03~3.41
pentane/hexane	469.7~507.82	3.03~3.37
hexane/heptane	507.82~540.13	2.74~3.03
heptane/octane	540.13~569.32	2.5~2.74
octane/nonane	569.32~594.55	2.28~2.5
R142b-R245fa	410.26~427.16	3.65~4.06
R245fa-R123	427.16~456.83	3.65~3.66
R123-R113	456.83~487.21	3.39~3.66
R113-MM	487.21~518.7	1.94~3.39

图2 ORC系统?效率变化趋势

Fig.2 Exergy efficiency variation of ORC system at different heat source temperature

图3 LEC随工质临界温度变化趋势

Fig.3 Variation of LECwith working fluid critical temperature

图4 非烷烃工质?效率及平均化发电成本

Fig.4 Exergy efficiency and LEC of other working fluids

图5 APR随工质临界温度变化曲线

Fig.5 Variation of APR with working fluid critical temperature

图6 单位时间成本随临界温度变化趋势

Fig.6 Variation of cost per unit of time with working fluid critical temperature

图7 净输出功指标随工质临界温度变化曲线

Fig.7 Variation of NPIwith working fluid critical temperature

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