基于吸热反应的电子设备热耗散相关技术进展

doi:10.16085/j.issn.1000-6613.2024-1566

摘要/Abstract

摘要：

高热耗电子设备的散热问题已成亟待解决的关键工程问题。作为一种新型的散热技术，吸热化学反应因其高储存密度、可长期储存及在环境条件下储热等优势，受到广泛关注。为此，本文首先介绍了发生在不同温度下的高热耗场景特点与散热需要，接着结合吸热反应的原理，并根据生成物的不同，重点分析了现有吸热反应类型与特点，具体包括氢体系、氨分解体系、水体系与碳酸盐体系。在上述分析中，进一步讨论了这些吸热反应对应的应用场景与存在的潜在问题。通过回顾传统超高温区与高温区中的化学反应进展，讨论了中低温区高热耗设备对吸热反应的要求。最后，从反应过程控制、产物处理等角度对基于吸热反应的散热技术前景进行了展望，试图从化学视角为该领域的研究提供借鉴。

关键词: 吸热反应, 相变, 热解, 高热耗, 散热, 反应特点

Abstract:

The heat dissipation of high heat flux equipment has become a key engineering problem to be solved urgently. As a novelty heat dissipation technology, endothermic chemical reaction has thus received wide attention due to its advantages of high storage density, long-term storage, and heat storage under environmental conditions. Therefore, we first introduced the characteristics of scenes with high heat flux under various working temperatures and their unique requirement for heat dissipation. After discussion on the principle of endothermic chemical reactions, various reactions categorized by their product, including hydrogen generation-based system, ammonia generation-based system, water generation-based system, and carbonate system, were emphatically summarized from the perspective of their features. Meanwhile, the application scenarios corresponding to the above reactions and the potential difficulties confronted in their application were also introduced. In combination of reviewing the progress made in heat dissipation of scenarios under ultra-high temperature or high temperature via the endothermic chemical reactions, we further discussed the requirement from scenarios under middle or low temperature, which was relatively less studied currently. Finally, we proposed the prospects of this technology by listing some difficulties faced during the application, such as the reaction control and the tail gas treatment, with the attempts to provide references to the studies on the heat dissipation of high heat flux equipment.

Key words: endothermic reaction, phase change, pyrolysis, high heat flux, heat dissipation, reaction characteristics

中图分类号:

TK124

陶婷, 徐计元, 张露, 钱吉裕, 王志飞, 赵红. 基于吸热反应的电子设备热耗散相关技术进展[J]. 化工进展, 2025, 44(11): 6212-6230.

TAO Ting, XU Jiyuan, ZHANG Lu, QIAN Jiyu, WANG Zhifei, ZHAO Hong. Progress on heat dissipation technology via endothermic chemical reaction for high heat flux equipment[J]. Chemical Industry and Engineering Progress, 2025, 44(11): 6212-6230.

图/表 20

表1 飞船和导弹再入时表面总加热量[18]

飞行器名称	总加热量/kJ·m^-2
“双子星座”号宇宙飞船	144628~275044
“阿波罗”宇宙飞船	505780
中程导弹	535040
远程导弹	3009600
神舟飞船	117600

表2 航天飞机热防护方案

位置	耐受温度/℃	解决方案
前缘	1450~1626	增强碳-碳烧蚀防护
迎风面	800~1200	陶瓷瓦
背风面	300~450	纤维毡

图1 MgH2不同温度分解速度[39]

图2 MgH2的解离压力曲线[12]（1bar=0.1MPa）

图3 催化剂用量对反应的影响[47]

图4 温度对反应的影响[47]

图5 转化率与反应温度的关系[54]

图6 Ca(OH)2反应体系平衡线[69]

表3 水合盐相变储能参数

水合盐	相变温度/℃	相变潜热/J·g^-1
CaCl₂·6H₂O	29.6	191
LiNO₃·3H₂O	30	125
MgCl₂·6H₂O	117	167
CaBr₂·2H₂O	34.3	116
NaH₂PO₄·12H₂O	36.5	264
CH₃COONa·3H₂O	58	246
Na₂SO₄·10H₂O	32.4	251
Ba(OH)₂·8H₂O	78	265.7

图7 LiNO3·3H2O溶解曲线[75]

图8 MgCl2·6H2O分解曲线[76]

表4 成核剂对MgCl2·6H2O的影响[77]

序号	成核剂	质量分数	过冷度/℃
1	—	0	19.8
2	Ba(OH)₂	0.5	0
3	Ca(OH)₂	0.5	0.6
4	Mg(OH)₂	0.5	0.2
5	MgO	0.5	0
6	CaC₂O₄	0.5	0

图9 NaH2PO4·12H2O相图[79]

图10 CH3COONa·3H2O相图[79]

图11 氢氧化钡-水体系相图[84]

图12 纯八水合氢氧化钡相图[89]

图13 双组分反应装置的设计[86]1—冷却装置；2—密封外壳；3—存储反应物质的分离隔膜；4—接触系统（触发两种反应物质接触）；5—激活接触系统的接口原件；6—热界面；7—导热金属底座；8—密封外壳内部的腔室（减少发生热化学反应的腔室内的超压）；9—将腔室内气体排出到冷却装置外部的机械元件；10—壁面；11—反应触发系统；12—触发元件与试剂R1组成的系统；E—冷却元件；S1—与冷却装置内部接触的界面；S2—与冷却装置外部接触界面；R1、R2—两种反应试剂；1B—冷却装置；2B—冷却装置外壳部分；3B—分离膜；4B—接触系统；5B—接口元件（R1被激活时，需通过接口元件5B）；6B—冷却装置底部；7B—金属底板（可将化学反应产生的冷通过金属底板传递到外表面）

图14 CaCO3的分解曲线[92]

表5 不同温度范围内的吸热反应

温度范围/℃	吸热反应
700~1000	CaCO₃(s) $→$ CaO(s)+CO₂(g)
700~1000	CH₄(g)+H₂O(g) $→$ CO(g)+3H₂(g)
900~1200	SrCO₃(s) $→$ SrO(s)+CO₂(g)
1200~1300	BaCO₃(s) $→$ BaO(s)+CO₂(g)

表5 不同温度范围内的吸热反应

温度范围/℃	吸热反应
700~1000	CaCO₃(s) $→$ CaO(s)+CO₂(g)
700~1000	CH₄(g)+H₂O(g) $→$ CO(g)+3H₂(g)
900~1200	SrCO₃(s) $→$ SrO(s)+CO₂(g)
1200~1300	BaCO₃(s) $→$ BaO(s)+CO₂(g)

表6 不同温度范围内的吸热反应

温度范围/℃	吸热反应	储能密度/kJ·kg^-1
29~80	CaCl₂·6H₂O(s) $→$ CaCl₂·4H₂O(s)+2H₂O(g)	191
30~40	LiNO₃·3H₂O(l) $→$ LiNO₃(s)+3H₂O(g)	274
80~90	(CH₃)₂CHOH(l) $→$ (CH₃)₂CO(g)+H₂(g)	1673
25~202	3NaAlH₄(s) $→$ Na₃AlH₆(s)+2Al(s)+3H₂(g)	2160
91~130	MgCl₂·6H₂O(s) $→$ MgCl₂·2H₂O(s)+4H₂O(g)	160
170~340	CaCl₂·2NH₃(s) $→$ CaCl₂(s)+2NH₃(g)	2333
300~400	MgH₂(s) $→$ Mg(s)+H₂(g)	2814
300~400	Mg(OH)₂(s) $→$ MgO(s)+H₂O(g)	1340
320~430	MgCO₃(s) $→$ MgO(s)+CO₂(g)	1410
400~600	Ca(OH)₂(s) $→$ CaO(s)+H₂O(g)	1406
800~900	CaCO₃(s) $→$ CaO(s)+CO₂(g)	1790

表6 不同温度范围内的吸热反应

温度范围/℃	吸热反应	储能密度/kJ·kg^-1
29~80	CaCl₂·6H₂O(s) $→$ CaCl₂·4H₂O(s)+2H₂O(g)	191
30~40	LiNO₃·3H₂O(l) $→$ LiNO₃(s)+3H₂O(g)	274
80~90	(CH₃)₂CHOH(l) $→$ (CH₃)₂CO(g)+H₂(g)	1673
25~202	3NaAlH₄(s) $→$ Na₃AlH₆(s)+2Al(s)+3H₂(g)	2160
91~130	MgCl₂·6H₂O(s) $→$ MgCl₂·2H₂O(s)+4H₂O(g)	160
170~340	CaCl₂·2NH₃(s) $→$ CaCl₂(s)+2NH₃(g)	2333
300~400	MgH₂(s) $→$ Mg(s)+H₂(g)	2814
300~400	Mg(OH)₂(s) $→$ MgO(s)+H₂O(g)	1340
320~430	MgCO₃(s) $→$ MgO(s)+CO₂(g)	1410
400~600	Ca(OH)₂(s) $→$ CaO(s)+H₂O(g)	1406
800~900	CaCO₃(s) $→$ CaO(s)+CO₂(g)	1790

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