• •
收稿日期:
2023-12-28
修回日期:
2024-03-26
出版日期:
2024-03-29
通讯作者:
鲁波娜
作者简介:
卢飞(1997—),男,硕士研究生,flu@ipe.ac.cn
基金资助:
Fei LU1,2(), Bona LU2,3(), Guangwen XU1
Received:
2023-12-28
Revised:
2024-03-26
Online:
2024-03-29
Contact:
Bona LU
摘要:
微型流化床因具有气体返混小和可操作性强等优点,在反应动力学测量等领域备受关注。获得流型随操作参数的变化规律,才能实现微型流化床理想流型的有效调控。采用双流体模型耦合考虑结构的相间曳力(又称多尺度CFD)模拟了一系列A类和B类颗粒在不同操作条件下的流化行为,结合颗粒浓度和气体停留时间分布(RTD)特征考察气速、床径和初始床高对气体返混行为的影响。研究表明,当微型流化床在初始鼓泡到湍动流态化之间操作时,才逼近颗粒全混流和气体近似平推流的运动状态。进一步分析气体RTD曲线形状特征(如拖尾、多峰等),提出采用斜度S < 0.6作为微型流化床平推流判据,弥补了原判据(满足方差σt2 < 0.25且峰高E(t)h > 1)的不足,为微型反应分析仪的流型调控奠定了基础。
中图分类号:
卢飞, 鲁波娜, 许光文. 气固微型流化床反应分析仪的理想流型判据分析[J]. 化工学报, DOI: 10.11949/0438-1157.20231386.
Fei LU, Bona LU, Guangwen XU. Analysis of criteria for ideal flow patterns in gas-solid micro fluidized bed reaction analyzer[J]. CIESC Journal, DOI: 10.11949/0438-1157.20231386.
Parameter | Value |
---|---|
Particle diameter dp/µm | 53 |
Particle density ρp/kg·m-3 | 1400 |
Gas density ρg/kg·m-3 | 1.225 |
Gas viscosity µg/Pa·s | 1.7894×10-5 |
Minimum fluidization velocity Umf/mm·s-1 | 4.9 |
Operating gas velocity Ug/mm·s-1 | 4 ~ 40 |
表1 模拟验证采用的物性及操作参数
Table 1 Physical properties and operating parameters used for simulation validation
Parameter | Value |
---|---|
Particle diameter dp/µm | 53 |
Particle density ρp/kg·m-3 | 1400 |
Gas density ρg/kg·m-3 | 1.225 |
Gas viscosity µg/Pa·s | 1.7894×10-5 |
Minimum fluidization velocity Umf/mm·s-1 | 4.9 |
Operating gas velocity Ug/mm·s-1 | 4 ~ 40 |
Type of particles | Ug/Umf | Dt/mm | Hs/mm |
---|---|---|---|
Geldart A(dp=92 μm, ρp=1200 kg·m-3, Ar=35.0341) | 2,3,4,5,6,7 | 5,10,15,20,30 | 10,15,20,25,30,35,40 |
Geldart B(dp=240 μm, ρp=2644 kg·m-3, Ar=1371.1474) | 1,2,3,4,5,6 | 5,10,15,20,30 | 10,15,20,25,30,35,40 |
表2 用于流型分析的各参数变化范围
Table 2 The range of variation of various parameters used for flow pattern analysis
Type of particles | Ug/Umf | Dt/mm | Hs/mm |
---|---|---|---|
Geldart A(dp=92 μm, ρp=1200 kg·m-3, Ar=35.0341) | 2,3,4,5,6,7 | 5,10,15,20,30 | 10,15,20,25,30,35,40 |
Geldart B(dp=240 μm, ρp=2644 kg·m-3, Ar=1371.1474) | 1,2,3,4,5,6 | 5,10,15,20,30 | 10,15,20,25,30,35,40 |
图2 时均颗粒浓度的轴向分布(dp = 53 µm, ρp = 1400 kg·m-3, ρg = 1.225 kg·m-3, μg = 1.7894×10-5 Pa·s, Ug = 15 mm·s-1)
Fig.2 The axial profiles of time-average solid concentration (dp = 53 µm, ρp = 1400 kg·m-3, ρg = 1.225 kg·m-3, μg = 1.7894×10-5 Pa·s, Ug = 15 mm·s-1)
图3 起始鼓泡速度Umb随网格尺寸的变化(dp = 53 µm, ρp = 1400 kg·m-3, ρg = 1.225 kg·m-3, μg = 1.7894×10-5 Pa·s)
Fig.3 The variation of incipient bubbling fluidization velocity Umb with grid size (dp = 53 µm, ρp = 1400 kg·m-3, ρg = 1.225 kg·m-3, μg = 1.7894×10-5 Pa·s)
图5 不同操作气速时的床层空隙率模拟值与实验值的对比(dp = 53 µm, ρp = 1400 kg·m-3, ρg = 1.225 kg·m-3, μg = 1.7894×10-5 Pa·s, Umf = 4.9 mm·s-1)
Fig.5 Comparison between simulated and experimental values of bed porosity at different gas velocities (dp = 53 µm, ρp = 1400 kg·m-3, ρg = 1.225 kg·m-3, μg = 1.7894×10-5 Pa·s, Umf = 4.9 mm·s-1)
Ug/mm-1 | εο(Exp.) | εο(Gidaspow) | relative error/% | εο(EMMS-bubbling) | relative error/% |
---|---|---|---|---|---|
10 | 0.4728 | 0.5912 | 25.03 | 0.4938 | 4.43 |
15 | 0.5168 | 0.6237 | 20.69 | 0.5230 | 2.55 |
25 | 0.5811 | 0.6747 | 16.11 | 0.5948 | 2.35 |
30 | 0.5970 | 0.6910 | 15.74 | 0.6181 | 3.53 |
表3 采用不同曳力模型时的床层空隙率模拟值与实验值的相对误差
Table 3 The relative error between simulated bed porosity and experiment using different drag models
Ug/mm-1 | εο(Exp.) | εο(Gidaspow) | relative error/% | εο(EMMS-bubbling) | relative error/% |
---|---|---|---|---|---|
10 | 0.4728 | 0.5912 | 25.03 | 0.4938 | 4.43 |
15 | 0.5168 | 0.6237 | 20.69 | 0.5230 | 2.55 |
25 | 0.5811 | 0.6747 | 16.11 | 0.5948 | 2.35 |
30 | 0.5970 | 0.6910 | 15.74 | 0.6181 | 3.53 |
Type of particles | Ug/Umf | S | |||||
---|---|---|---|---|---|---|---|
Geldart A (dp=92 μm, ρp=1200 kg·m-3, Umf=0.0091 m/s, Dt/dp=109) | 2 | 3.9100 | 0.7209 | 0.8944 | 0.4498 | 0.0585 | 1.7587 |
3 | 2.5921 | 0.6298 | 0.3261 | 0.7338 | 0.0485 | 1.9021 | |
4 | 1.9510 | 0.6338 | 0.1820 | 0.9837 | 0.0478 | 1.9192 | |
5 | 1.5519 | 0.5924 | 0.1166 | 1.2138 | 0.0484 | 1.8837 | |
6 | 1.3086 | 0.5735 | 0.0840 | 1.4261 | 0.0491 | 1.8662 | |
7 | 1.1244 | 0.5515 | 0.0628 | 1.6330 | 0.0497 | 1.8361 | |
Geldart B (dp=240 μm, ρp=2644 kg·m-3, Umf=0.1032 m/s, Dt/dp=42) | 1 | 0.7061 | 0.5523 | 0.0233 | 2.6343 | 0.0468 | 1.8601 |
2 | 0.3793 | 0.5826 | 0.0083 | 4.2471 | 0.0576 | 1.6109 | |
3 | 0.2498 | 0.6218 | 0.0047 | 5.6837 | 0.0753 | 1.4198 | |
4 | 0.1881 | 0.5986 | 0.0035 | 6.3570 | 0.0992 | 1.1958 | |
5 | 0.1558 | 1.0118 | 0.0026 | 10.2803 | 0.1087 | 1.6017 | |
6 | 0.1296 | 0.8004 | 0.0011 | 12.8732 | 0.0662 | 1.6684 |
表4 不同Ug时的微型流化床内气体RTD特征参数(Dt = 10 mm, Hs = 20 mm)
Table 4 The gas RTD characteristic parameters in micro fluidized beds at different operating gas velocities (Dt = 10 mm, Hs = 20 mm)
Type of particles | Ug/Umf | S | |||||
---|---|---|---|---|---|---|---|
Geldart A (dp=92 μm, ρp=1200 kg·m-3, Umf=0.0091 m/s, Dt/dp=109) | 2 | 3.9100 | 0.7209 | 0.8944 | 0.4498 | 0.0585 | 1.7587 |
3 | 2.5921 | 0.6298 | 0.3261 | 0.7338 | 0.0485 | 1.9021 | |
4 | 1.9510 | 0.6338 | 0.1820 | 0.9837 | 0.0478 | 1.9192 | |
5 | 1.5519 | 0.5924 | 0.1166 | 1.2138 | 0.0484 | 1.8837 | |
6 | 1.3086 | 0.5735 | 0.0840 | 1.4261 | 0.0491 | 1.8662 | |
7 | 1.1244 | 0.5515 | 0.0628 | 1.6330 | 0.0497 | 1.8361 | |
Geldart B (dp=240 μm, ρp=2644 kg·m-3, Umf=0.1032 m/s, Dt/dp=42) | 1 | 0.7061 | 0.5523 | 0.0233 | 2.6343 | 0.0468 | 1.8601 |
2 | 0.3793 | 0.5826 | 0.0083 | 4.2471 | 0.0576 | 1.6109 | |
3 | 0.2498 | 0.6218 | 0.0047 | 5.6837 | 0.0753 | 1.4198 | |
4 | 0.1881 | 0.5986 | 0.0035 | 6.3570 | 0.0992 | 1.1958 | |
5 | 0.1558 | 1.0118 | 0.0026 | 10.2803 | 0.1087 | 1.6017 | |
6 | 0.1296 | 0.8004 | 0.0011 | 12.8732 | 0.0662 | 1.6684 |
Type of particles | Dt/mm | Dt/dp | S | |||||
---|---|---|---|---|---|---|---|---|
Geldart A (dp=92 μm, ρp=1200 kg·m-3, Ug= 4Umf, Hs=20 mm) | 5 | 54 | 0.5778 | 0.6614 | 0.0129 | 3.7417 | 0.0387 | 2.1620 |
10 | 109 | 1.9510 | 0.6338 | 0.1820 | 0.9837 | 0.0478 | 1.9192 | |
15 | 163 | 2.8654 | 0.6841 | 0.4930 | 0.6024 | 0.0601 | 1.7262 | |
20 | 217 | 3.4392 | 0.7599 | 0.8653 | 0.4592 | 0.0732 | 1.5793 | |
30 | 326 | 4.1145 | 0.9198 | 1.6549 | 0.3429 | 0.0978 | 1.4109 | |
Geldart B (dp=240 μm, ρp=2644 kg·m-3, Ug= 1Umf, Hs=20 mm) | 5 | 21 | 0.1858 | 0.4273 | 0.0015 | 10.3461 | 0.0428 | 1.9223 |
10 | 42 | 0.7061 | 0.5523 | 0.0233 | 2.6343 | 0.0468 | 1.8601 | |
15 | 63 | 1.0042 | 0.6624 | 0.0636 | 1.5990 | 0.0630 | 1.6057 | |
20 | 83 | 1.1938 | 0.7697 | 0.1053 | 1.2529 | 0.0739 | 1.4957 | |
30 | 125 | 1.4222 | 0.9441 | 0.1785 | 1.1184 | 0.0883 | 1.5906 |
表5 不同Dt时的微型流化床内气体RTD特征参数(Hs = 20 mm)
Table 5 The gas RTD characteristic parameters in micro fluidized beds at different bed diameters (Hs = 20 mm)
Type of particles | Dt/mm | Dt/dp | S | |||||
---|---|---|---|---|---|---|---|---|
Geldart A (dp=92 μm, ρp=1200 kg·m-3, Ug= 4Umf, Hs=20 mm) | 5 | 54 | 0.5778 | 0.6614 | 0.0129 | 3.7417 | 0.0387 | 2.1620 |
10 | 109 | 1.9510 | 0.6338 | 0.1820 | 0.9837 | 0.0478 | 1.9192 | |
15 | 163 | 2.8654 | 0.6841 | 0.4930 | 0.6024 | 0.0601 | 1.7262 | |
20 | 217 | 3.4392 | 0.7599 | 0.8653 | 0.4592 | 0.0732 | 1.5793 | |
30 | 326 | 4.1145 | 0.9198 | 1.6549 | 0.3429 | 0.0978 | 1.4109 | |
Geldart B (dp=240 μm, ρp=2644 kg·m-3, Ug= 1Umf, Hs=20 mm) | 5 | 21 | 0.1858 | 0.4273 | 0.0015 | 10.3461 | 0.0428 | 1.9223 |
10 | 42 | 0.7061 | 0.5523 | 0.0233 | 2.6343 | 0.0468 | 1.8601 | |
15 | 63 | 1.0042 | 0.6624 | 0.0636 | 1.5990 | 0.0630 | 1.6057 | |
20 | 83 | 1.1938 | 0.7697 | 0.1053 | 1.2529 | 0.0739 | 1.4957 | |
30 | 125 | 1.4222 | 0.9441 | 0.1785 | 1.1184 | 0.0883 | 1.5906 |
Type of particles | Hs/mm | Hs/dp | S | |||||
---|---|---|---|---|---|---|---|---|
Geldart A (dp=92 μm, ρp=1200 kg·m-3, Ug= 4Umf, Dt=10 mm) | 10 | 109 | 2.4550 | 0.5731 | 0.2589 | 0.8171 | 0.0430 | 2.0060 |
15 | 163 | 2.1465 | 0.5754 | 0.2035 | 0.9209 | 0.0442 | 1.9767 | |
20 | 217 | 1.9510 | 0.6338 | 0.1820 | 0.9837 | 0.0478 | 1.9192 | |
25 | 272 | 1.7770 | 0.6331 | 0.1646 | 1.0288 | 0.0521 | 1.8282 | |
30 | 326 | 1.6204 | 0.6505 | 0.1605 | 1.0419 | 0.0611 | 1.6883 | |
35 | 380 | 1.5353 | 0.7716 | 0.1574 | 1.0896 | 0.0668 | 1.6729 | |
40 | 435 | 1.4118 | 0.8737 | 0.1493 | 1.1430 | 0.0749 | 1.6137 | |
Geldart B (dp=240 μm, ρp=2644 kg·m-3, Ug= 1Umf, Dt=10 mm) | 10 | 42 | 0.9550 | 0.5111 | 0.0405 | 2.0146 | 0.0444 | 1.9239 |
15 | 63 | 0.8087 | 0.5265 | 0.0299 | 2.3322 | 0.0457 | 1.8861 | |
20 | 83 | 0.7061 | 0.5523 | 0.0233 | 2.6343 | 0.0468 | 1.8601 | |
25 | 104 | 0.6222 | 0.5502 | 0.0188 | 2.9247 | 0.0487 | 1.8197 | |
30 | 125 | 0.5472 | 0.5480 | 0.0148 | 3.2993 | 0.0493 | 1.8054 | |
35 | 146 | 0.4666 | 0.4142 | 0.0129 | 3.6054 | 0.0593 | 1.6823 | |
40 | 167 | 0.4140 | 0.5820 | 0.0092 | 4.3143 | 0.0535 | 1.7861 |
表6 不同Hs时的微型流化床内气体RTD特征参数(Dt = 10 mm)
Table 6 The gas RTD characteristic parameters in micro fluidized beds at different static bed heights (Dt = 10 mm)
Type of particles | Hs/mm | Hs/dp | S | |||||
---|---|---|---|---|---|---|---|---|
Geldart A (dp=92 μm, ρp=1200 kg·m-3, Ug= 4Umf, Dt=10 mm) | 10 | 109 | 2.4550 | 0.5731 | 0.2589 | 0.8171 | 0.0430 | 2.0060 |
15 | 163 | 2.1465 | 0.5754 | 0.2035 | 0.9209 | 0.0442 | 1.9767 | |
20 | 217 | 1.9510 | 0.6338 | 0.1820 | 0.9837 | 0.0478 | 1.9192 | |
25 | 272 | 1.7770 | 0.6331 | 0.1646 | 1.0288 | 0.0521 | 1.8282 | |
30 | 326 | 1.6204 | 0.6505 | 0.1605 | 1.0419 | 0.0611 | 1.6883 | |
35 | 380 | 1.5353 | 0.7716 | 0.1574 | 1.0896 | 0.0668 | 1.6729 | |
40 | 435 | 1.4118 | 0.8737 | 0.1493 | 1.1430 | 0.0749 | 1.6137 | |
Geldart B (dp=240 μm, ρp=2644 kg·m-3, Ug= 1Umf, Dt=10 mm) | 10 | 42 | 0.9550 | 0.5111 | 0.0405 | 2.0146 | 0.0444 | 1.9239 |
15 | 63 | 0.8087 | 0.5265 | 0.0299 | 2.3322 | 0.0457 | 1.8861 | |
20 | 83 | 0.7061 | 0.5523 | 0.0233 | 2.6343 | 0.0468 | 1.8601 | |
25 | 104 | 0.6222 | 0.5502 | 0.0188 | 2.9247 | 0.0487 | 1.8197 | |
30 | 125 | 0.5472 | 0.5480 | 0.0148 | 3.2993 | 0.0493 | 1.8054 | |
35 | 146 | 0.4666 | 0.4142 | 0.0129 | 3.6054 | 0.0593 | 1.6823 | |
40 | 167 | 0.4140 | 0.5820 | 0.0092 | 4.3143 | 0.0535 | 1.7861 |
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