化工学报 ›› 2020, Vol. 71 ›› Issue (2): 584-593.doi: 10.11949/0438-1157.20190812

• 流体力学与传递现象 • 上一篇    下一篇

聚合釜传热性能的实验研究及数值模拟

王修纲1,2,3(),吴裕凡1,2,郭潞阳1,2,路庆华3,叶晓峰1,2,曹育才1,2()   

  1. 1.上海化工研究院有限公司聚烯烃催化技术与高性能材料国家重点实验室，上海 200062
    2.上海化工研究院有限公司 上海市聚烯烃催化技术重点实验室，上海 200062
    3.上海交通大学化学化工学院，上海 200240
  • 收稿日期:2019-07-12 修回日期:2019-10-11 出版日期:2020-02-05 发布日期:2019-11-02
  • 通讯作者: 曹育才 E-mail:xgwang@sjtu.edu.cn;caoyc@srici.cn
  • 作者简介:王修纲（1986—），男，博士，工程师， xgwang@sjtu.edu.cn
  • 基金资助:
    上海市科委科技发展基金项目(16DZ2290700)

Experimental study and CFD simulation of heat transfer in polymerization reactor

Xiugang WANG1,2,3(),Yufan WU1,2,Luyang GUO1,2,Qinghua LU3,Xiaofeng YE1,2,Yucai CAO1,2()   

  1. 1.State Key Laboratory of Polyolefins and Catalysis, Shanghai Research Institute of Chemical Industry Co. , Ltd. , Shanghai 200062, China
    2.Shanghai Key Laboratory of Catalysis Technology for Polyolefins, Shanghai Research Institute of Chemical Industry Co. , Ltd. , Shanghai 200062, China
    3.School of Chemistry and Chemical Engineering, Shanghai Jiao Tong University, Shanghai 200240, China
  • Received:2019-07-12 Revised:2019-10-11 Online:2020-02-05 Published:2019-11-02
  • Contact: Yucai CAO E-mail:xgwang@sjtu.edu.cn;caoyc@srici.cn

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摘要：

基于CFD模拟与传热实验相结合的方法对5 L夹套聚合釜的传热性能进行研究。建立聚合釜的液固耦合稳态传热模型，获得釜内流体、夹套内流体及金属固体域内温度分布。开展传热实验对模拟结果进行验证，各对比点温度的最大相对误差在1%~5%范围内。通过模拟获得釜内外壁面传热系数及总传热系数，并关联出釜侧及夹套侧 Nu的经验式。结果表明：釜内流体温度分布方差始终在0.002以下，固体域内和传热边界层温度梯度较大，传热边界层厚度约3.8 mm；实验范围内，入口温度和反应放热量对釜内温度的影响显著，入口流速次之，搅拌转速影响最弱；夹套侧传热系数远小于釜侧传热系数，提高夹套侧传热系数是提升传热性能的关键；实验用聚合釜外表面散热量与内外温差呈正比，比例系数约为3.031 W·K -1。

关键词: 计算流体力学, 搅拌容器, 传热, 数值模拟, 聚合, 流固耦合

Abstract:

The heat transfer performance of 5 L jacketed polymerizer was studied based on the combination of CFD simulation and heat transfer experiments. The liquid-solid coupled steady-state heat transfer model of the polymerizer was established to obtain the temperature distribution of the metal solid and the fluid in the reactor and the jacket. The CFD simulation results were validated by heat transfer experiments, and the maximum relative error of temperature at each test point was within 1%—5%. The convective heat transfer coefficients of the inner and outer walls of the reactor and the total heat transfer coefficients were obtained by simulation, and the empirical formulas of Nu on the reactor side and the jacket side were correlated. The results show that the variance of the fluid temperature distribution in the reactor is always below 0.002 in the three calculation domains. Among them, the temperature gradients in the solid domain and the heat transfer boundary layer are larger, and the thickness of the boundary layer is about 3.8 mm. In the experiment range, the inlet temperature and reaction exothermic have a significant influence on the reactor temperature, followed by the inlet flow rate, and the stirring speed has the weakest influence. The heat transfer coefficient on the jacket side is much smaller than the heat transfer coefficient on the side of the kettle. Increasing the heat transfer coefficient on the jacket side is the key to improving the heat transfer performance. The heat dissipation on the outer surface of the reactor is proportional to the temperature difference between the inside and outside, and the proportional coefficient is about 3.031 W·K -1.

Key words: CFD, stirred vessel, heat transfer, numerical simulation, polymerization, fluid-structure interaction

中图分类号: 

  • TQ 021.3

图1

实验聚合釜安装图"

图2

实验流程原理"

图3

物理模型与网格"

表1

网格无关检验"

Mesh numberTr /K Ql /(W·m -2)
92×10 455.3291.79
206×10 454.8690.53
393×10 454.7390.12
788×10 454.7290.09

表2

丙烯物性参数多项式系数"

多项式系数ρ/(kg·m -3) c p /(J·kg -1·K -1) μ /(mPa·s) λ/(W·m -1·K -1)
a5.4611×10 22.4810×10 31.0909×10 -19.9055×10 -2
b-1.14149.7721-1.2086×10 -3-3.1159×10 -4
c-1.2857×10 -21.8036×10 -22.8571×10 -6-4.4643×10 -7

表3

导热油物性参数多项式系数"

多项式系数ρ/(kg·m -3) c p /(J·kg -1·K -1) μ /(mPa·s) λ/(W·m -1·K -1)
a7.7717×10 22.0175×10 31.72501.3152×10 -1
b-7.0114×10 -13.7815-2.1955×10 -2-2.0679×10 -4
c-5.7114×10 -42.0930×10 -39.1518×10 -5-2.4187×10 -8

图4

聚合釜的速度分布"

表4

模拟方法的实验验证"

条件测温点实验值/℃模拟值/℃绝对误差/℃相对误差/%
① Tji=87.64℃, uin=1.0 m·s -1, N=200 r·min -1, Qr=0 Tr83.0182.660.350.42
Tjo86.8286.760.060.07
Ta42.1243.98-1.86-4.42
Tb47.1248.50-1.38-2.93
②Tji =56.86℃, uin =1.5 m·s -1, N=200 r·min -1, Qr=0 Tr55.1154.730.380.69
Tjo56.5056.480.020.04
Ta32.1133.25-1.14-3.55
Tb36.8938.71-1.82-4.93
③Tji =65.66℃, uin =2.0 m·s -1, N=200 r·min -1, Qr=250 W Tr68.0267.600.420.62
Tjo65.6965.640.050.08
Ta36.8838.68-1.80-4.88
Tb42.3444.01-1.67-3.94

图5

聚合釜的温度分布"

图6

三计算域内温度分布方差"

图7

线上（ X=0, Y=300 mm）温度分布及边界层厚度估计 "

图8

影响釜内温度的单因素分析"

表5

不同条件下传热系数模拟值与实验值"

uin/(m·s -1) N/(r·min -1) αo/(W·m -2·K -1) αi/(W·m -2·K -1) K-calc /(W·m -2·K -1) K-exp/(W·m -2·K -1) Error/%
1.020071.67255666.1162.385.64
1.520075.80255669.6171.96-3.38
2.020078.87255672.1978.09-8.17
4.010086.79132976.3376.66-0.44
1.540075.80491570.6573.57-4.13
1.080071.67945367.5561.469.01

图9

计算 K值与实验 K值对比 "

图10

表面散热量的线性拟合"

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