Mass transfer characteristics of gas-liquid two-phase flow in microchannels and applications

doi:10.11949/0438-1157.20190710

Abstract

Abstract:

The Taylor flow and bubbly flow in gas-liquid two phase systems in microchannels have the advantages of uniform bubble size, narrow residence time distribution, easy control, high specific surface area, and so on. These advantages facilitate them various applications and important implications. Based on the bubble dissolution and mass transfer process during Taylor flow and bubbly flow, this paper systematically reviews the research progress of bubble dissolution, mass transfer process and mass transfer/dissolution model at microscale, and introduces the above flow pattern in reaction or process. Finally, an outlook is given for further research directions in this field.

Key words: slug flow, microchannel, microreactor, bubble, mass transfer

摘要：

微通道内气-液两相体系中Taylor流和泡状流具有气泡尺寸均一、停留时间分布窄、可调控性强和比表面积高等优点，具有广泛的应用前景。从Taylor气泡和泡状气泡的传质过程出发，系统综述了微尺度下气泡的溶解规律、传质过程机理和传质/溶解模型等方面的研究进展，并介绍上述流型在反应或过程强化、基础物性及动力学数据测量和微纳材料合成方面的应用。最后总结并展望了技术领域的研究难点与研究方向。

关键词: 弹状流, 微通道, 微反应器, 气泡, 传质

CLC Number:

TK 124

Chaoqun YAO, Guangwen CHEN, Quan YUAN. Mass transfer characteristics of gas-liquid two-phase flow in microchannels and applications[J]. CIESC Journal, 2019, 70(10): 3635-3644.

尧超群, 陈光文, 袁权. 微通道内气-液两相传质过程行为及其应用[J]. 化工学报, 2019, 70(10): 3635-3644.

Figures/Tables 8

Fig.1 Typical concentration field in liquid slugs

Table 1 Typical correlations for gas-liquid mass transfer

文献	关联式
[29]	$k L a = 4.5 D j G / L U C 1 D H$
[30]	$k L a = 2 D H D U B D H L B L U C 0.3$
[24]	$k L a = E q . (8) × μ L 1 m P a ? s - 0.33$
[28]	$k L a = 0.111 j T P 1.19 [(1 - ε G) L U C] 0.57$
[31]	$k L a = 0.133 j T P 1.2 L S D D C H 4 0.5$ 标准单位
[3]	$S h L a D H = 0.084 R e G 0.213 R e L 0.912 S c L 0.5$
[32]	$S h L = 0.69 (1 + 0.724 R e T P 0.48 S c L 1 / 3)$
[17]	$S h L a D H = 1.367 R e G 0.421 R e L 0.717 S c L 0.64 C a T P 0.5$
[33]	$S h L = 0.1 R e T P 0.421 S c L 0.05$

Table 1 Typical correlations for gas-liquid mass transfer

文献	关联式
[29]	$k L a = 4.5 D j G / L U C 1 D H$
[30]	$k L a = 2 D H D U B D H L B L U C 0.3$
[24]	$k L a = E q . (8) × μ L 1 m P a ? s - 0.33$
[28]	$k L a = 0.111 j T P 1.19 [(1 - ε G) L U C] 0.57$
[31]	$k L a = 0.133 j T P 1.2 L S D D C H 4 0.5$ 标准单位
[3]	$S h L a D H = 0.084 R e G 0.213 R e L 0.912 S c L 0.5$
[32]	$S h L = 0.69 (1 + 0.724 R e T P 0.48 S c L 1 / 3)$
[17]	$S h L a D H = 1.367 R e G 0.421 R e L 0.717 S c L 0.64 C a T P 0.5$
[33]	$S h L = 0.1 R e T P 0.421 S c L 0.05$

Fig.2 Unit cell model for mass transfer[17]

Fig.3 Three-layer model for mass transfer[38]

Fig.4 Film-slug separate transfer model[39]

Fig.5 Intensification of oxidation using Taylor flow[2]

Fig.6 Determination of physical properties based on bubble dissolution[8]

Fig.7 Synthesis of micro-capsules material using microfluidics[61]

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