CO2跨临界热泵系统采暖工况下能效和经济对比分析

doi:10.16085/j.issn.1000-6613.2020-0905

摘要/Abstract

摘要：

为提高CO₂跨临界热泵采暖系统的性能，提出了双级压缩双气冷器中间补气回热系统。结合其他3种CO₂热泵系统和R134a单级压缩回热系统，通过建立热力学模型，分析各因素对系统能效的影响。此外，通过构建综合考虑初始投资成本和年运行成本的经济性评价模型，结合典型年气象参数，研究不同城市中各系统在运行周期内的总投资情况。结果表明，CO₂热泵系统中，双级压缩双气冷器中间补气回热系统最优COP_h最高且可以超过R134a单级压缩回热系统，在环境温度为0℃、出水/回水温度为65℃/40℃时，理论性能系数（COP_h）可达2.58，比R134a系统高9.1%，比CO₂单级压缩系统高22.5%，且排气温度不超过现有压缩机排气温度极限，是能效最优系统。在选定样本城市中，热泵系统运行周期内的总投资成本在上海最低，而在沈阳最高，可见总投资成本受气候区域影响较大。由于CO₂压缩机成本过高，CO₂热泵系统的总投资成本高于R134a系统。随着CO₂热泵技术的提高和生产规模的扩大，当压缩机成本降低80%，CO₂双级压缩双气冷器中间补气回热系统的总投资成本将低于R134a系统。

关键词: CO₂热泵, 跨临界, 采暖, 能效, 经济

Abstract:

In order to improve the performance of the CO₂ transcritical heat pump heating system, a heat recovery system with secondary air supply for two-stage compression and double gas cooler is proposed. Through the establishment of the thermodynamic model, the impact of various factors on the energy efficiency of the system is analyzed combined with the other three CO₂ heat pump systems and the R134a single-stage compression regenerative system. In addition, the total investment situation of each system in different cities during the operating cycle is studied based on typical annual meteorological parameters by an economic evaluation model, which comprehensively considers the initial investment cost and annual operating cost. The results show that the heat recovery system with secondary air supply for two-stage compression and double gas cooler is the optimal system scheme, which has the highest COP_h and exceeds that of R134a single-stage compression regenerative system. When the ambient temperature is 0℃ and the temperature of outlet/return water is 65℃/40℃, the theoretical COP_h can reach 2.58, which is 9.1% higher than that of the R134a system, and 22.5% higher than that of CO₂ single-stage compression system, and the compressor discharge temperature doesn't exceed the existing temperature limit. In the selected sampling cities, the total investment cost of all heat pump systems during the operating cycle is the lowest in Shanghai and the highest in Shenyang, which shows that it is greatly affected by the climate region. Due to the high cost of the CO₂ compressor, the total investment cost of the CO₂ heat pump system is higher than that of the R134a system. With the improvement of CO₂ heat pump technology and the expansion of production scale, when the cost of the compressor is reduced by 80%, the total investment cost of the heat recovery system with secondary air supply for two-stage compression and double gas cooler will be lower than that of R134a system.

Key words: CO₂ heat pump, transcritical, heating, energy efficiency, economy

中图分类号:

TK124

刘雪涛, 李敏霞, 马一太, 姚良, 詹浩淼. CO₂跨临界热泵系统采暖工况下能效和经济对比分析[J]. 化工进展, 2021, 40(3): 1315-1324.

LIU Xuetao, LI Minxia, MA Yitai, YAO Liang, ZHAN Haomiao. Comparative analysis of energy efficiency and economy of CO₂ transcritical heat pump system under heating condition[J]. Chemical Industry and Engineering Progress, 2021, 40(3): 1315-1324.

图/表 18

图1 单级压缩回热系统

图2 双级压缩双气冷器回热系统

图3 补气压缩回热系统

图4 双级压缩双气冷器中间补气回热系统

图5 压缩机效率与压比关系拟合曲线

表1 居民住宅供暖设计参数

参数	城市
参数	沈阳	北京	上海
供暖面积/m²	100	100	100
HLET/℃	18	18	18
设计采暖室外温度/℃	-16.9	-7.6	-0.3
建筑采暖热指标/W·m^-2	69	61.8	58

图6 环境温度所对应的热负荷及时长分布

表2 设备成本估算公式

设备	公式
CO₂压缩机	C_com(CO₂)=17547W^0.4488
R134a压缩机	C_com(R134a)=758.15W^0.8728
套管式换热器	C_HE,_tube-in-tube=1874.4W^0.9835
翅片管式换热器	C_HE,_fin-tube=331.7A^0.9390

表3 换热器结构参数

换热器类型	参数	数值/mm
套管式换热器	外管外径	19
	外管管壁厚度	2
	内管外径	7
	内管管壁厚度	1
翅片管式换热器	管外径	7
	管壁厚度	0.7
	翅片厚度	0.15
	翅片间距	2
	横向管间距	21
	纵向管间距	18.166
	迎风长度	400
	迎风宽度	170

表4 换热关联式

类别	关联式
CO₂蒸发侧^[17]	$N u = 0.00061 S + F × R e L × F a 0.01 × P r L 0.4 l n 1.024 μ L, b μ L, w$ ， $S = 41000 × B o 1.13 - 0.275$ ， $F = x 1 - x a ρ L ρ V 0.4$ ， $a = 0.48 + 0.00524 R e L × F a 0.11 0.85 - 5.9 × 10 - 6 R e L × F a 0.11 1.85 R e L × F a 0.11 < 600 0.87 600 ≤ R e L × F a 0.11 ≤ 6000 160.8 R e L × F a 0.11 0.6 R e L × F a 0.11 > 6000$
CO₂气冷侧^[18]	$N u = f f 8 R e b - 1000 × P r 1.07 + 12.7 f f 8 × P r 2 / 3 - 1$ ， $P r = c p, b μ b λ b c p, b ≥ c ˉ p c ˉ p μ b λ b c p, b < c ˉ p ? 和 ??? μ b λ b ≥ μ f λ f c ˉ p μ f λ f c p, b < c ˉ p ? 和 ??? μ b λ b ≥ μ f λ f$
R134a蒸发侧^[19]	$h = 0.55 h f m 1 + 3000 × B o 0.86 + 1.12 x 1 - x 0.7 ρ L ρ V 0.41 × F a 0.48$ $h f m = 0.023 G 1 - x D h μ L 0.9 × P r L 0.4 × λ L D h$ ， $F a = 1 x ≤ 0.7 1 + 0.2 x 1.2 c o s 15 ° x > 0.7$
R134a冷凝侧^[20]	$N u = 0.05 × R e e q 0.8 × P r L 0.33$ ， $R e e q = R e V × μ V μ L ρ L ρ V 0.5 + R e L$
空气侧^[21]	$h = h 4 ρ a ω m a x c p, a P r a 2 / 3$ ， $h 4 = 0.0014 + 0.2618 × R e d - 0.4 × A A t - 0.15$
单相工质流动^[22]	$N u = f 8 R e - 1000 × P r 1.07 + 12.7 f 8 × P r 2 / 3 - 1$

表4 换热关联式

类别	关联式
CO₂蒸发侧^[17]	$N u = 0.00061 S + F × R e L × F a 0.01 × P r L 0.4 l n 1.024 μ L, b μ L, w$ ， $S = 41000 × B o 1.13 - 0.275$ ， $F = x 1 - x a ρ L ρ V 0.4$ ， $a = 0.48 + 0.00524 R e L × F a 0.11 0.85 - 5.9 × 10 - 6 R e L × F a 0.11 1.85 R e L × F a 0.11 < 600 0.87 600 ≤ R e L × F a 0.11 ≤ 6000 160.8 R e L × F a 0.11 0.6 R e L × F a 0.11 > 6000$
CO₂气冷侧^[18]	$N u = f f 8 R e b - 1000 × P r 1.07 + 12.7 f f 8 × P r 2 / 3 - 1$ ， $P r = c p, b μ b λ b c p, b ≥ c ˉ p c ˉ p μ b λ b c p, b < c ˉ p ? 和 ??? μ b λ b ≥ μ f λ f c ˉ p μ f λ f c p, b < c ˉ p ? 和 ??? μ b λ b ≥ μ f λ f$
R134a蒸发侧^[19]	$h = 0.55 h f m 1 + 3000 × B o 0.86 + 1.12 x 1 - x 0.7 ρ L ρ V 0.41 × F a 0.48$ $h f m = 0.023 G 1 - x D h μ L 0.9 × P r L 0.4 × λ L D h$ ， $F a = 1 x ≤ 0.7 1 + 0.2 x 1.2 c o s 15 ° x > 0.7$
R134a冷凝侧^[20]	$N u = 0.05 × R e e q 0.8 × P r L 0.33$ ， $R e e q = R e V × μ V μ L ρ L ρ V 0.5 + R e L$
空气侧^[21]	$h = h 4 ρ a ω m a x c p, a P r a 2 / 3$ ， $h 4 = 0.0014 + 0.2618 × R e d - 0.4 × A A t - 0.15$
单相工质流动^[22]	$N u = f 8 R e - 1000 × P r 1.07 + 12.7 f 8 × P r 2 / 3 - 1$

图7 COPh、回热器1窄点温差随补气流量比的变化

图8 COPh随高压侧运行压力的变化

图9 最优COPh随环境温度的变化

图10 压缩机排气温度随环境温度的变化

图11 各热泵系统的初始投资成本

图12 各热泵系统的年运行成本

图13 总投资成本在运行周期内的变化

图14 与R134a系统总投资成本相同时各系统压缩机成本及其降低的百分比

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CO₂跨临界热泵系统采暖工况下能效和经济对比分析

Comparative analysis of energy efficiency and economy of CO₂ transcritical heat pump system under heating condition

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