Thermodynamic study of liquid air energy storage with air purification unit

doi:10.11949/0438-1157.20191131

Abstract

Abstract:

In the current research on liquid air energy storage (LAES), it is found that the performance of LAES system is generally overestimated without considering the power consumption of air purification. This paper therefore proposes a complete LAES system with air purification unit.The LAES system consists of three parts: charging cycle, discharging cycle and TSA process.The whole system is verified to be feasible by the simulation in the Aspen Plus^? version 8.4, and the thermodynamic analysis of this system is carried out. The results show that the thermodynamic performance of the system can be effectively improved by increasing the discharging pressure, the air turbine inlet temperature and the proportion of the thermal oil used in the discharging cycle. About 36% of the stored heat of compression is not fully used, if it is totally recycled, the exergy efficiency of the whole system can reach 0.623. The electricity storage efficiency of the LAES system with air purification unit is 0.471, which is 6.8% lower than that of the baseline LAES system.

Key words: liquid air energy storage, adsorption, desorption, heat of compression, thermodynamics

摘要：

针对现今液态空气储能（LAES）研究中普遍存在忽略空气净化过程能耗而使LAES系统能效被高估的问题，提出了一种含空气净化过程的LAES系统。该系统包含空气液化过程、液态空气释能过程和TSA纯化过程，通过全流程的仿真模拟验证系统可行性，并对其进行热力学分析。结果显示：提高液态空气释能压力、空气透平进口温度和储热油使用比例，可以有效提升系统的热力学性能；储存的压缩热仍有约36%未被完全使用，若将其全部回收利用，全系统效率可达0.623；该含空气纯化过程的LAES系统储电效率为0.471，比基线LAES系统低6.8%。

关键词: 液态空气储能, 吸附, 脱附, 压缩热, 热力学

CLC Number:

TK 02

Chen WANG, Xiaohui SHE, Xiaosong ZHANG. Thermodynamic study of liquid air energy storage with air purification unit[J]. CIESC Journal, 2020, 71(S1): 23-30.

王晨, 折晓会, 张小松. 含空气净化过程的液态空气储能热力学研究[J]. 化工学报, 2020, 71(S1): 23-30.

Figures/Tables 9

References 32

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参数	数值
加压压力P _c	9×10⁶ Pa
热油初始温度T ₁₇	293 K
丙烷初始温度T ₃₄	214 K
甲醇初始温度T ₃₆	293 K
液态空气温度T ₁₃	78.54 K
液态空气压力P ₁₃	1×10⁵ Pa
释能压力P _d	1.2×10⁷ Pa
透平进口温度P ₄₁	458.5 K
透平出口最终压力P ₄₆	1×10⁵ Pa
吸附温度	298 K
吸附压力	5.8×10⁵ Pa
脱附压力	1×10⁵ Pa
热吹温度P ₄₇	443 K
冷吹温度P ₄₇ _’	296 K
压缩机等熵效率	0.89
透平等熵效率	0.9
制冷膨胀机等熵效率	0.8
低温泵效率	0.7

参数	数值
加压压力P _c	9×10⁶ Pa
热油初始温度T ₁₇	293 K
丙烷初始温度T ₃₄	214 K
甲醇初始温度T ₃₆	293 K
液态空气温度T ₁₃	78.54 K
液态空气压力P ₁₃	1×10⁵ Pa
释能压力P _d	1.2×10⁷ Pa
透平进口温度P ₄₁	458.5 K
透平出口最终压力P ₄₆	1×10⁵ Pa
吸附温度	298 K
吸附压力	5.8×10⁵ Pa
脱附压力	1×10⁵ Pa
热吹温度P ₄₇	443 K
冷吹温度P ₄₇ _’	296 K
压缩机等熵效率	0.89
透平等熵效率	0.9
制冷膨胀机等熵效率	0.8
低温泵效率	0.7

工况点	流量/(kg/s)	温度/K	压力×10^-5/Pa	介质
1	129.74	293.00	1.00	空气
2	200.00	506.79	5.80	空气
3	200.00	309.00	5.80	空气
4	200.00	298.00	5.80	空气
5	199.84	298.00	5.80	空气
6	199.84	446.19	20.85	空气
7	199.84	309.00	20.85	空气
8	199.84	490.20	90.00	空气
9	199.84	309.00	90.00	空气
10	199.84	221.38	90.00	空气
11	199.84	123.80	90.00	空气
12	199.84	78.74	1.00	空气
13	129.74	78.54	1.00	空气
14	70.10	79.24	1.00	空气
15	70.10	216.90	1.00	空气
16	70.10	293.00	1.00	空气
17	380.00	293.00	1.00	储热油
18	129.20	293.00	1.00	储热油
19	129.20	479.90	1.00	储热油
20	125.40	293.00	1.00	储热油
21	125.40	434.47	1.00	储热油
22	125.40	293.00	1.00	储热油
23	125.40	481.61	1.00	储热油
24	380.00	465.85	1.00	储热油
25	243.20	465.85	1.00	储热油
26	86.82	465.85	1.00	储热油
27	86.82	293.87	1.00	储热油
28	79.04	465.85	1.00	储热油
29	79.04	309.63	1.00	储热油
30	77.34	465.85	1.00	储热油
31	77.34	312.04	1.00	储热油
32	243.20	304.86	1.00	储热油
33	120.00	87.20	1.00	丙烷
34	120.00	214.00	1.00	丙烷
35	55.00	215.00	1.00	甲醇
36	55.00	293.00	1.00	甲醇
37	129.74	78.74	1.00	空气
38	129.74	86.11	120.00	空气
39	129.74	206.86	120.00	空气
40	129.74	290.42	120.00	空气
41	129.74	458.50	120.00	空气
42	129.74	304.51	24.33	空气
43	129.74	458.50	24.33	空气
44	129.74	306.77	4.93	空气
45	129.74	458.50	4.93	空气
46	129.74	307.53	1.00	空气

工况点	流量/(kg/s)	温度/K	压力×10^-5/Pa	介质
1	129.74	293.00	1.00	空气
2	200.00	506.79	5.80	空气
3	200.00	309.00	5.80	空气
4	200.00	298.00	5.80	空气
5	199.84	298.00	5.80	空气
6	199.84	446.19	20.85	空气
7	199.84	309.00	20.85	空气
8	199.84	490.20	90.00	空气
9	199.84	309.00	90.00	空气
10	199.84	221.38	90.00	空气
11	199.84	123.80	90.00	空气
12	199.84	78.74	1.00	空气
13	129.74	78.54	1.00	空气
14	70.10	79.24	1.00	空气
15	70.10	216.90	1.00	空气
16	70.10	293.00	1.00	空气
17	380.00	293.00	1.00	储热油
18	129.20	293.00	1.00	储热油
19	129.20	479.90	1.00	储热油
20	125.40	293.00	1.00	储热油
21	125.40	434.47	1.00	储热油
22	125.40	293.00	1.00	储热油
23	125.40	481.61	1.00	储热油
24	380.00	465.85	1.00	储热油
25	243.20	465.85	1.00	储热油
26	86.82	465.85	1.00	储热油
27	86.82	293.87	1.00	储热油
28	79.04	465.85	1.00	储热油
29	79.04	309.63	1.00	储热油
30	77.34	465.85	1.00	储热油
31	77.34	312.04	1.00	储热油
32	243.20	304.86	1.00	储热油
33	120.00	87.20	1.00	丙烷
34	120.00	214.00	1.00	丙烷
35	55.00	215.00	1.00	甲醇
36	55.00	293.00	1.00	甲醇
37	129.74	78.74	1.00	空气
38	129.74	86.11	120.00	空气
39	129.74	206.86	120.00	空气
40	129.74	290.42	120.00	空气
41	129.74	458.50	120.00	空气
42	129.74	304.51	24.33	空气
43	129.74	458.50	24.33	空气
44	129.74	306.77	4.93	空气
45	129.74	458.50	4.93	空气
46	129.74	307.53	1.00	空气

参数	数值
压缩机耗功	109243.864 kW
制冷膨胀机输出功率	4311.376 kW
空气液化过程效率	0.814
低温泵耗功	2527.568 kW
空气透平输出功率	59068.701 kW
液态空气释能过程效率	0.873
液体收率	0.65
基线系统储电效率	0.539