气液相变换热过程中界面腐蚀的基础研究进展

doi:10.16085/j.issn.1000-6613.2019-0536

摘要/Abstract

摘要：

由于两相之间会不断转换，相变换热被称为复杂的传热传质过程，其过程中会引起相变腐蚀，如冷凝液滴腐蚀、气泡腐蚀以及多相流流动腐蚀等。目前对于气液相变腐蚀的研究集中在对腐蚀产物的表征、分析，忽略了相变过程中由于能量传递引起的界面变化对腐蚀的影响。本文从相变腐蚀机理、腐蚀防护两方面出发，系统地总结管道内外冷凝液滴腐蚀、气泡腐蚀与多相流流动腐蚀等气液相变腐蚀领域的研究进展，并对其中存在的问题进行总结，同时归纳了用于研究相变腐蚀过程的腐蚀预测模型，分析其应用场合以及各种模型的优势与不足，以期为研究气液相变腐蚀监测与控制的学者提供参考，并指出气液相变换热过程中的气液两相界面腐蚀问题是未来相变腐蚀研究的重要方向。

关键词: 相变, 凝结, 沸腾, 界面, 腐蚀, 多相流

Abstract:

Phase change heat transfer is a complex process for the gas-liquid phase transition. This process will trigger the phase change corrosion such as condensate-droplet corrosion, bubble corrosion and multiphase flow corrosion. Almost present researches focused on the vapor-liquid phase change corrosion are carried out mainly through characterizing the corrosion products without consideration of the effect of latent heat variation and interface change on the corrosion during the phase change process. In this paper, the study on vapor-liquid phase change corrosion was systematically reviewed in terms of the mechanism of phase-change corrosion and the corrosion protection firstly to summarize the existing problems. Secondly, the corrosion prediction models were outlined with the differences of application conditions, advantages and disadvantages, in order to provide a reference or principle for corrosion determination and further control. Finally, it was pointed out that the problem of interface corrosion in the phase change heat exchange process was the hot spot of the future research.

Key words: phase change, condensation, boiling, interface, corrosion, multi-phase flow

中图分类号:

TK121

陈宏霞,刘霖,肖红洋,孙源. 气液相变换热过程中界面腐蚀的基础研究进展[J]. 化工进展, 2019, 38(12): 5225-5237.

Hongxia CHEN,Lin LIU,Hongyang XIAO,Yuan SUN. Basic research progress of interface corrosion in gas-liquid phase transformation heat process[J]. Chemical Industry and Engineering Progress, 2019, 38(12): 5225-5237.

图/表 14

图1 冷凝过程中腐蚀的诱发机理○蒸汽； ×腐蚀离子

图2 省煤器内腐蚀管道形貌图[3]

图3 两个参数对酸露点的影响[19]

表1 酸露点的主要预测模型

预测模型	备注	研究者
$T = 116.5515 + 16.06329 l g V S O 3 + 1.05377 (l g V S O 3) 2$	燃烧含硫2.5%的煤（未考虑水蒸气影响）	Islam等^[29]
$1000 T + 273.15 = 1.7842 + 0.0269 l g P H 2 O - 0.1029 l g P S O 3 +$ $0.0329 l g P H 2 O × l g P S O 3$	硫酸分压大于0.1013Pa	Verhoff和Branchero^[24]

$T = 113.0219 + 15.0777 l g V H 2 S O 4 + 2.0975 (l g V H 2 S O 4) 2$	硫酸蒸气分压为0～2Pa，水蒸气分压为0～14185.5Pa	Halstead等^[28]
$T = 203.35 + 27.6 l g P H 2 O + 10.83 l g P S O 3 + 1.06 (l g P S O 3 + 8) 2.19$	基于燃料成分和过量空气比估算烟气中硫酸	Okkes^[27]
$T = 20 l g P S O 3 + a - 80$	a取决于烟气中水蒸气的分压	Qin等^[25]
$T = β × S 3 1 . 05 a H × A + t d p$	β取决于锅炉的过量空气比	Feng等^[34]
$T = 186 + 20 l g C H 2 O + 26 l g C S O 2 × 127.65 (C * S O 2) - 0.585 + l g A a r x α f l y C * S O 2 12 ×$ $? (15.191 + 0.071 C F e + 0.044 C A l - 0.058 C C a - 0.117 C M g) × 10 - 2$	综合考虑水蒸气、SO₂含量、原煤灰分含量、粉煤灰比例以及粉煤灰中Fe含量等参数	Li等^[35]

表1 酸露点的主要预测模型

预测模型	备注	研究者
$T = 116.5515 + 16.06329 l g V S O 3 + 1.05377 (l g V S O 3) 2$	燃烧含硫2.5%的煤（未考虑水蒸气影响）	Islam等^[29]
$1000 T + 273.15 = 1.7842 + 0.0269 l g P H 2 O - 0.1029 l g P S O 3 +$ $0.0329 l g P H 2 O × l g P S O 3$	硫酸分压大于0.1013Pa	Verhoff和Branchero^[24]

$T = 113.0219 + 15.0777 l g V H 2 S O 4 + 2.0975 (l g V H 2 S O 4) 2$	硫酸蒸气分压为0～2Pa，水蒸气分压为0～14185.5Pa	Halstead等^[28]
$T = 203.35 + 27.6 l g P H 2 O + 10.83 l g P S O 3 + 1.06 (l g P S O 3 + 8) 2.19$	基于燃料成分和过量空气比估算烟气中硫酸	Okkes^[27]
$T = 20 l g P S O 3 + a - 80$	a取决于烟气中水蒸气的分压	Qin等^[25]
$T = β × S 3 1 . 05 a H × A + t d p$	β取决于锅炉的过量空气比	Feng等^[34]
$T = 186 + 20 l g C H 2 O + 26 l g C S O 2 × 127.65 (C * S O 2) - 0.585 + l g A a r x α f l y C * S O 2 12 ×$ $? (15.191 + 0.071 C F e + 0.044 C A l - 0.058 C C a - 0.117 C M g) × 10 - 2$	综合考虑水蒸气、SO₂含量、原煤灰分含量、粉煤灰比例以及粉煤灰中Fe含量等参数	Li等^[35]

图4 金属壁面多孔沉积

图5 空泡腐蚀形貌图[51]

图6 气泡破裂的速度场矢量图及压力云图[55][图6(f)为压力场及流线图]

图7 表面张力对空泡泡径变化的影响

图8 表面张力对空泡泡壁运动速度变化的影响[57]

图9 纯Ni涂层和Ni-TiO 2纳米复合涂层在不同溶液中的极化曲线

图10 相变换热中的不同流型以及对应的腐蚀形态示意图

图11 液滴电化学腐蚀实验装置图

图12 45#钢磨蚀量随泥沙含量变化关系[73]

图13 冷却水管管网模型[74]

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