低温管路预冷两相流瞬变规律仿真研究

李卓伦; 应媛媛; 王磊; 张淇栋; 厉彦忠

doi:10.13224/j.cnki.jasp.20230737

低温管路预冷两相流瞬变规律仿真研究

doi: 10.13224/j.cnki.jasp.20230737

李卓伦^1,,
应媛媛²,
王磊^1,*, ,,
张淇栋¹,
厉彦忠¹

1.
西安交通大学制冷与低温工程系，西安 710049
2.
中国航天科技集团有限公司北京航天试验技术研究所，北京 100074

基金项目: 国家自然科学基金（52332012，52495001）

详细信息

作者简介:
李卓伦（2000-），男，硕士生，主要从事航天低温领域研究。E-mail：lizhuolun2000@stu.xjtu.edu.cn

通讯作者:
王磊（1985-），男，教授、博士生导师，博士，主要从事航天低温领域研究。E-mail：wanglei-epe@xjtu.edu.cn

中图分类号: V434
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出版历程
- 收稿日期: 2023-11-24
- 网络出版日期: 2025-04-16

Simulation study on transient two phase flow in cryogenic tube chill-down process

1.
Institute of Refrigeration and Cryogenic Engineering，Xi’an Jiaotong University，Xi’an 710049，China
2.
Beijing Institute of Aerospace Testing Technology，China Aerospace Science and Technology Corporation，Beijing 100074，China

摘要

摘要:
为揭示低温管路预冷两相流态与沸腾换热的瞬变规律，建立了低温管路预冷瞬变过程的计算流体动力学（CFD）数值模型，采用不同传热模型考虑预冷不同阶段的流-固耦合换热速率。研究发现，低温管路预冷根据管内流态可分为液面抬升、膜态沸腾、过渡及核态沸腾、液面上涨至满液共4个阶段。在管内两相流发展过程中，受重力影响，管截面表现为局部“上翘”式反环状流、主体分层流的流型特征，其中，底部与侧壁气膜厚度分别由0.093 mm和0.124 mm波动减薄。截面内最大温差达90 K，进出口最大温差约50 K。由于管内存在膜态沸腾向过渡沸腾、核态沸腾转变区，可能造成局部含气率突增。
- 两相流型 /
- 低温管路预冷 /
- 流-固耦合换热 /
- 反环状流 /
- 分层流
Abstract:
To reveal the transient properties of two-phase flow and boiling heat transfer in cryogenic tube chill-down process, a computational fluid dynamics (CFD) model to account for transient variations in the cryogenic chill-down event was developed. In this CFD model, different heat transfer models were selected to calculate fluid-solid coupling heat transfer rates at different stages of chill-down. The results showed that the flow patterns inside the tube could be divided into four stages, including liquid level rising, film boiling, transition and nucleate boiling, and pipe flooding. Due to the influence of gravity in the development of the interior two-phase flow, the distribution of a general stratified flow with local “upwarped” appeared at the liquid surface position near the tube wall. The thicknesses of the vapor film at the bottom and side wall decreased fluctuatingly from 0.093 mm and 0.124 mm, respectively. Moreover, it was found that the maximum temperature difference at the cross section was about 90 K, and the temperature difference between the tube inlet and outlet reached about 50 K. Owing to the transition from film boiling to transition and nucleate boiling, the local void fraction could increase significantly.
- two-phase flow pattern /
- cryogenic tube chill-down /
- fluid-solid coupling heat transfer /
- inversed annular flow /
- stratified flow

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图 1 低温管路预冷两相流型示意图

Figure 1. Schematic diagram of two-phase flow pattern in cryogenic tube chill-down process

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图 2 液氮池沸腾曲线^[25]

Figure 2. Boiling curve of liquid nitrogen^[25]

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图 3 流-固间换热热流求解框图

Figure 3. Solution flow chart for fluid-solid coupling heat transfer

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图 4 低温管路网格模型示意图

Figure 4. Schematic diagram of cryogenic tube grid model

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图 5 网格数对预测结果的影响

Figure 5. Influence of grid numbers on predicted results

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图 6 管内壁降温曲线对比

Figure 6. Comparison of temperature decrease curves of tube inner wall

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图 7 低温管路预冷相分布及流线特征

Figure 7. Phase distribution and streamline characteristics during cryogenic tube chill-down process

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图 8 距入口0.149 m处截面管壁降温过程

Figure 8. Temperature decrease performance at 0.149 m away from inlet

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图 9 距入口0.149 m处内壁温度与热流随时间变化

Figure 9. Variation of inner wall temperature and heat flux with time at 0.149 m away from inlet

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图 10 壁面平均温度沿管长分布

Figure 10. Average wall temperature distribution along cryogenic tube

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图 11 截面含气率沿管长分布

Figure 11. Void fraction distribution along cryogenic tube

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表 1 低温管路预冷仿真所采用换热模型

Table 1. Heat transfer models in cryogenic tube chill-down calculation

物理量	模型	公式	备注
f （α_l）	Ioilev模型^[28]	$ f （{{\alpha _{\text{l}}}} ） = 1 - \max \left[ {0,\min \left( {\dfrac{{0.1 - {\alpha _{\text{l}}}}}{{0.05}},1} \right)} \right] $	判断液相或气相换热
q_c，q_v	Jayatilleke模型^[29]	${q_{\text{c}}} = \dfrac{{{\rho _{\text{l}}}{c_{{{p{\mathrm{l}}}}}}{u_{{\text{lw}}}}}}{{{T_{{\text{lw}}}}}}\quad\quad{q_{\text{v}}} = \dfrac{{{\rho _{\text{v}}}{c_{{{p{\mathrm{v}}}}}}{u_{{\text{vw}}}}}}{{{T_{{\text{vw}}}}}}$	基于对流换热原理提出
T_MHF	Darr模型^[30]	${T_{{\text{MHF}}}} = 0.844{T_{{\text{cr}}}}\left[ {1 + 0.06\left( {\dfrac{{{\rho _{\text{l}}}{u_{\text{l}}}{D_{\text{i}}}}}{\sigma }} \right)} \right]$	适用于液氮
T_CHF	Kalinin模型^[31]	$\dfrac{{{T_{{\text{CHF}}}} - {T_{{\text{sat}}}}}}{{{T_{{\text{cr}}}} - {T_{\text{l}}}}} = 0.1 + 1.5\sqrt \beta + 0.6{\beta ^2}\quad\quad \beta = \sqrt {\dfrac{{{k_{\text{l}}}{\rho _{\text{l}}}{c_{{{p{\mathrm{l}}}}}}}}{{{k_{\text{w}}}{\rho _{\text{w}}}{c_{{{p{\mathrm{w}}}}}}}}} $	适用于液氮
h_film	Breen-Westwater 修正模型^[32]	$\begin{gathered} {h_{{\text{film}}}} = \left[ {0.37 + 0.28{{\left( {\dfrac{\sigma }{{gD_{\text{i}}^{\text{2}}\Delta \rho }}} \right)}^{0.5}}} \right]{\left( {\dfrac{\sigma }{{g\Delta \rho }}} \right)^{ - 0.125}}{\left[ {\dfrac{{{\mu _{\text{v}}} （ {{T_{\text{w}}} - {T_{{\text{sat}}}}} ） }}{{k_{\text{v}}^{\text{3}}{\rho _{\text{v}}}\Delta \rho g{\lambda '}}}} \right]^{ - 0.25}} \\ {\lambda '} = \dfrac{{{{\left[ {\lambda + 0.34{c_{{{p{\mathrm{v}}}}}} （{{T_{\text{w}}} - {T_{{\text{sat}}}}} ） } \right]}^2}}}{\lambda } \\ \end{gathered} $	适用于液氮
q_CHF	Wang模型^[16], Tatsumoto修正模型^[33]	$\begin{gathered} {q_{{\text{CHF}}}} = 0.486G\lambda {\left( {\dfrac{{{\rho _{\text{v}}}}}{{{\rho _{\text{l}}}}}} \right)^{0.635\;3}}{\left( {\dfrac{{{\rho _{\text{l}}}\sigma }}{{{G^2}L}}} \right)^{0.498\;7}}{\left( {\dfrac{L}{{{D_{\text{i}}}}}} \right)^{0.311\;2}} \\ {q_{{\text{CHF,sub}}}} = \left[ {1 + 0.23{{\left( {\dfrac{{{\rho _{\text{v}}}}}{{{\rho _{\text{l}}}}}} \right)}^{0.8}}\left( {\dfrac{{{c_{{{p{\mathrm{l}}}}}}\Delta {T_{{\text{sub}}}}}}{\lambda }} \right)} \right]{q_{{\text{CHF}}}} \\ \end{gathered} $	适用于液氮^[34]
q_MHF	Jeschar模型^[35]	${q_{{\text{MHF}}}} = 0.16{\rho _{\text{v}}}\lambda {\left[ {\dfrac{{g\sigma \Delta \rho }}{{{{ （ {{\rho _{\text{l}}} + {\rho _{\text{v}}}} ） }^2}}}} \right]^{0.25}}$	适用于液氮^[32]
d_b	He模型^[36]	${d_{\text{b}}} = 7.2 \times {10^{ - 0.433}}{\left( {\dfrac{{{\rho _{\text{v}}}}}{{{\rho _{\text{l}}}}}} \right)^{ - 0.018}}{\left[ {\dfrac{{{c_{{{p{\mathrm{l}}}}}}\left( {{T_{\text{w}}} - {T_{{\text{sat}}}}} \right)}}{\lambda }} \right]^{0.32}}R{e^{ - 0.3}}$	适用于低温液体^[37]：水力直径为1～42.4 mm、质量流速为67～1927 kg/（m²·s）
$ \tilde n $	Kirichenko模型^[38]	$\tilde n = \left\{ \begin{gathered} {10^{ - 7}}{\left[ {\dfrac{{\lambda {\rho _{\text{v}}} （ {{T_{\text{w}}} - {T_{{\text{sat}}}}} ） }}{{\sigma {T_{{\text{sat}}}}}}} \right]^2}\quad\quad\quad\quad\quad p/{p_{{\text{cr}}}} \geqslant 0.04 \\ 625 \times {10^{ - 16}}{\left[ {\dfrac{{\lambda {\rho _{\text{v}}} （ {{T_{\text{w}}} - {T_{{\text{sat}}}}} ） }}{{\sigma {T_{{\text{sat}}}}}}} \right]^3}\quad\;\quad p/{p_{{\text{cr}}}} < 0.04 \\ \end{gathered} \right.$	适用于液氮^[39]
f_b	Cole模型^[40]	${f_{\text{b}}} = \sqrt {\dfrac{{4g （{{\rho _{\text{l}}} - {\rho _{\text{v}}}} ） }}{{3{\rho _{\text{l}}}{d_{\text{b}}}}}} $	确定气泡脱落频率^[22]

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表 2 模拟参数取值

Table 2. Values of simulation parameters

参数	数值或说明
管路内径D_i/mm	11.68
管路外径D_o/mm	12.70
管长L/m	0.572
入口压力/MPa	0.298
质量流速/（kg/（m²·s））	169
入口液氮过冷度ΔT_sub/K	0.9
管壁比定压热容c_pw/（J/（kg·K））	由式（4）确定
管壁热导率k_w/（W/（m·K））	由式（5）确定
重力加速度g/（m/s）	9.81

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