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完整後設資料紀錄
DC 欄位 | 值 | 語言 |
---|---|---|
dc.contributor.advisor | 郭修伯 | zh_TW |
dc.contributor.advisor | Hsiu-Po Kuo | en |
dc.contributor.author | 徐秉鈞 | zh_TW |
dc.contributor.author | Ping-Chu Hsu | en |
dc.date.accessioned | 2023-03-19T22:06:00Z | - |
dc.date.available | 2024-04-03 | - |
dc.date.copyright | 2022-09-30 | - |
dc.date.issued | 2022 | - |
dc.date.submitted | 2002-01-01 | - |
dc.identifier.citation | 1. Kunii, D. and O. Levenspiel, Fluidization engineering. 1991: Butterworth-Heinemann.
2. Geldart, D., Types of gas fluidization. Powder technology, 1973. 7(5): p. 285-292. 3. Geldart, D., Gas fluidization technology. 1986. 4. Davidson, J.F. and D. Harrison, Fluidised particles / by J.F. Davidson and D. Harrison. 1963, Cambridge: University Press. 5. Punčochář, M., et al., Evaluation of minimum fluidizing velocity in gas fluidized bed from pressure fluctuations. Chemical Engineering Communications, 1985. 35(1-6): p. 81-87. 6. Ergun, S., Fluid flow through packed columns. Chem. Eng. Prog., 1952. 48: p. 89-94. 7. Saxena, S. and G. Vogel, Segregation and fluidization characteristics of a dolomite bed with a range of particle sizes and shapes. Chem. Eng. J.(Lausanne);(Switzerland), 1977. 14. 8. Wen, C. and Y. Yu, A generalized method for predicting the minimum fluidization velocity. AIChE Journal, 1966. 12(3): p. 610-612. 9. Saxena, S. and V. GJ, The measurement of incipient fluidisation velocities in a bed of coarse dolomite at temperature and pressure. 1977. 10. Babu, S. and B. SP, Fluidization correlations for coal gasification materials-minimum fluidization velocity and fluidized bed expansion ratio. 1978. 11. Richardson, J.F. and M.A. da S. Jerónimo, Velocity-voidage relations for sedimentation and fluidisation. Chemical Engineering Science, 1979. 34(12): p. 1419-1422. 12. Doichev, K. and N. Akhmakov, Fluidisation of polydisperse systems. Chemical Engineering Science, 1979. 34(11): p. 1357-1359. 13. Hetsroni, G., Handbook of multiphase systems. 1982. 14. Yang, W.C., et al., A generalized methodology for estimating minimum fluidization velocity at elevated pressure and temperature. AIChE journal, 1985. 31(7): p. 1086-1092. 15. Llop, M., et al., Fluidization at vacuum conditions. A generalized equation for the prediction of minimum fluidization velocity. Chemical Engineering Science, 1996. 51(23): p. 5149-5157. 16. Reina, J., E. Velo, and L. Puigjaner, Predicting the minimum fluidization velocity of polydisperse mixtures of scrap-wood particles. Powder technology, 2000. 111(3): p. 245-251. 17. Subramani, H.J., M.M. Balaiyya, and L.R. Miranda, Minimum fluidization velocity at elevated temperatures for Geldart’s group-B powders. Experimental Thermal and Fluid Science, 2007. 32(1): p. 166-173. 18. Rao, A., et al., The effect of column diameter and bed height on minimum fluidization velocity. AIChE Journal, 2010. 56(9): p. 2304-2311. 19. Escudero, D. and T.J. Heindel, Bed height and material density effects on fluidized bed hydrodynamics. Chemical Engineering Science, 2011. 66(16): p. 3648-3655. 20. Hilal, N., M.T. Ghannam, and M.Z. Anabtawi, Effect of Bed Diameter, Distributor and Inserts on Minimum Fluidization Velocity. Chemical Engineering & Technology, 2001. 24(2): p. 161-165. 21. Dong, S., et al., Effect of Perforated Ratios of Distributor on the Fluidization Characteristics in a Gas− Solid Fluidized Bed. Industrial & Engineering Chemistry Research, 2009. 48(1): p. 517-527. 22. Yogendrasasidhar, D., G. Srinivas, and Y. Pydi Setty, Effect of distributor on performance of a continuous fluidized bed dryer. Heat and Mass Transfer, 2018. 54(3): p. 641-649. 23. Zhang, H., et al., Effects of internals and distributors on the distribution and growth of bubbles in the conventional gas–solid fluidized bed. Particuology, 2021. 55: p. 1-15. 24. Karri, S.R. and J. Werther, Gas distributor and plenum design in fluidized beds. Chemical industries-new york-marcel dekker-, 2003: p. 155-170. 25. Geldart, D. and J. Baeyens, The design of distributors for gas-fluidized beds. Powder technology, 1985. 42(1): p. 67-78. 26. Qureshi, A.E. and D.E. Creasy, Fluidised bed gas distributors. Powder Technology, 1979. 22(1): p. 113-119. 27. Yang, W.-c., Handbook of fluidization and fluid-particle systems. 2003: CRC press. 28. Mirek, P., Air Distributor Pressure Drop Analysis in a Circulating Fluidized-Bed Boiler for Non-reference Operating Conditions. Chemical Engineering & Technology, 2020. 43(11): p. 2233-2246. 29. Luo, Z., et al., Effect of gas distributor on performance of dense phase high density fluidized bed for separation. International Journal of Mineral Processing, 2004. 74(1): p. 337-341. 30. Shukrie, A., S. Anuar, and A.N. Oumer, Air distributor designs for fluidized bed combustors: A review. Engineering, Technology & Applied Science Research, 2016. 6(3): p. 1029-1034. 31. Chyang, C.-S. and C.-C. Huang, Pressure Drop across a Perforated-Plate Distributor in a Gas-Fluidized Bed. Journal of chemical engineering of japan, 1991. 24(2): p. 249-252. 32. Yudin, A.S.M., S. Anuar, and A.N. Oumer, Improvement on particulate mixing through inclined slotted swirling distributor in a fluidized bed: An experimental study. Advanced Powder Technology, 2016. 27(5): p. 2102-2111. 33. Sathiyamoorthy, D. and A. Vogelpohl, On the Distributors and Design Criteria for Gas-Solid and, Gas-Liquid-Solid Fluidized Beds. Mineral Processing and Extractive Metallurgy Review, 1993. 12(2-4): p. 125-163. 34. Institution, B.S.I.B.S., BS EN ISO 5167-1 Measurement of fluid flow by means of pressure differential devices inserted in circular cross-section conduits running full- Part 1: General principles and requirements. 2003: British Standards Institution. 35. Baker, R.C., Flow measurement handbook. Vol. 99. 2000: Cambridge University Press Cambridge. 36. Malavasi, S., et al., On the pressure losses through perforated plates. Flow measurement and instrumentation, 2012. 28: p. 57-66. 37. Fakhimi, S., S. Sohrabi, and D. Harrison, Entrance effects at a multi‐orifice distributor in gas‐fluidised beds. The Canadian Journal of Chemical Engineering, 1983. 61(3): p. 364-369. 38. Kassim, W., Flowback of solids through distribution plates of gas fluidized beds and associated phenomena. 1972, Aston University. 39. Davidson, J.F., R. Clift, and D. Harrison, Fluidization / edited by J.F. Davidson, R. Clift, D. Harrison. 2nd ed. ed. 1985, London ;: Academic Press. 40. Paiva, J., C. Pinho, and R. Figueiredo, The influence of the distributor plate on the bottom zone of a fluidized bed approaching the transition from bubbling to turbulent fluidization. Chemical Engineering Research and Design, 2004. 82(1): p. 25-33. 41. Barros Filho, J.A., et al., Pressure drop of flow through perforated plates. 2007. 42. Narsimhan, G., On a generalized expression for prediction of minimum fluidization velocity. AIChE Journal, 1965. 11(3): p. 550-554. 43. Shaaban, S., On the performance of perforated plate with optimized hole geometry. Flow Measurement and Instrumentation, 2015. 46: p. 44-50. 44. Svensson, A., F. Johnsson, and B. Leckner, Bottom bed regimes in a circulating fluidized bed boiler. International Journal of Multiphase Flow, 1996. 22(6): p. 1187-1204. 45. La Rosa, D.M., et al., On the pressure losses through multistage perforated plates. Journal of Fluids Engineering, 2021. 143(6). 46. Zenz, F., The fluid mechanics of bubbling beds. Fibonacci Quarterly, 1978. 16(2): p. 171-183. 47. Şahi̇n, B.r., Pressure losses in an isolated perforated plate and jets emerging from the perforated plate. International journal of mechanical sciences, 1989. 31(1): p. 51-61. 48. Qureshi, A. and D. Creasy, Fluidised bed gas distributors. Powder Technology, 1979. 22(1): p. 113-119. | - |
dc.identifier.uri | http://tdr.lib.ntu.edu.tw/jspui/handle/123456789/84188 | - |
dc.description.abstract | 流體化床擁有廣大的非勻相接觸面積,提供優異的質傳以及熱傳效率,因此被廣泛利用於工業製造。最小流體化床速度的決定對於流體化床是否良好運作佔有重要的地位。雖然前人已提出許多估計最小流體化床速度的經驗式,但多數僅考慮床質物性、流體黏度與密度。實際操作時,最小流體化床速度亦受到分散板設計、床高床徑比等的影響。本研究使用內徑11 cm的圓柱流化床,以四種分散板、五種床重,探討分散板以及床重對最小流體化床速度之影響。
使用不同分散板分析時,實驗結果所得的最小流體化床速度與經驗式預測結果不同。對於粒徑為595.7 μm的玻璃珠,經驗式高估最小流體化速度;對於粒徑為1059 μm的玻璃珠,經驗式低估最小流體化速度。分散板開孔率越大,經驗式與實驗所得最小流體化床速度差距越大。使用不同床重分析時,實驗所得最小流體化床速度並非隨著床重的增加而單調遞增或遞減。 除了可藉由流化床整體壓降隨流速變化曲線判斷最小流體化床速度外,吾人提出並以實驗驗證可藉由氣體通過分散板壓降隨流速變化曲線,或是由空氣通過系統上游的銳孔壓降隨流速變化曲線判斷最小流體化床速度。在不同實驗系統中,若以氣體通過上游銳孔壓降出現劇烈變化判斷最小流體化床速度,更具有便利性。 | zh_TW |
dc.description.abstract | A fluidized bed has a large contact area between different phases, and high mass and heat transfer rates, leading to its wide applications in industry. Whether a fluidized bed operated efficiently depends on the accurate determination of the minimum fluidization velocity. Although there are several empirical equations for the minimum fluidization velocity prediction, most of them are only functions of the particle and fluid physical properties. In reality, the minimum fluidization velocity also depends on the design of the system, such as the distributor design and the bed aspect ratio. In the current study, experiments are performed in a cylindrical fluidized bed with a 11 cm inner diameter. Four different gas distributor designs and five different particle weights are employed to study their effects on the minimum fluidization velocity.
The results show that there is difference between the empirical equation predicted minimum fluidization velocity and that from the experimental observation. The empirical equation presents a higher minimum fluidization velocity for glass beads having a diameter of 595.7 μm, and a lower minimum fluidization velocity for glass beads having a diameter of 1059 μm. For the design of the distributor, the higher the open area ratio is, the larger the difference between the empirical equation prediction and the experimental observed velocity. Except from the bed pressure drop versus the superficial gas velocity (Us) diagram, we propose and prove two new methods to determine the minimum fluidization velocity. The minimum fluidization velocity can be determined from the distributor pressure drop versus Us diagram, and from the upstream orifice pressure drop versus Us diagram. Among them, the upstream orifice pressure drop monitoring is a more convenient method to determine the minimum fluidization velocity. | en |
dc.description.provenance | Made available in DSpace on 2023-03-19T22:06:00Z (GMT). No. of bitstreams: 1 U0001-2609202211354700.pdf: 9748003 bytes, checksum: f9c7101cd068ecbd22cd44e6d9bf05c5 (MD5) Previous issue date: 2022 | en |
dc.description.tableofcontents | 目錄 I
圖表目錄 V 第一章 緒論 1 第二章 文獻回顧 2 2.1 流體化床 2 2.2 粒子的分類 3 2.3 最小流體化速度 UMF 5 2.4 氣體分散板 10 2.5 銳孔流量計 12 第三章 實驗方法 15 3.1 實驗裝置 15 3.1.1 流體化床主體 15 3.1.2 分散板 16 3.1.3 空氣供應系統 18 3.1.4 壓力轉換器及數據擷取系統 18 3.1.5 熱線型氣體質量流量計 18 3.2 實驗參數設計 19 3.3 實驗步驟 19 第四章 結果與討論 22 4.1 床重以及分散板與最小流體化速度關係 22 4.1.1 以經驗式計算之最小流體化速度 22 4.1.2 以現象觀察得到之最小流體化速度 22 4.1.3 床整體壓降(ΔPB)與氣體表觀速度(Us)關係討論 25 4.1.3.1 不同床重下床整體壓降(ΔPB)與氣體表觀速度(Us)關係討論 30 4.1.3.2 不同分散板下床整體壓降(ΔPB)與氣體表觀速度(Us)關係 33 4.1.3.3 不同粒徑下床整體壓降(ΔPB)與氣體表觀速度(Us)關係 36 4.1.3.4 以Davidson & Harrison method [4]計算的最小流體化速度(Umf)與現象觀察結果比較 38 4.2 分散板壓降(ΔPDISTRIBUTOR)與最小流體化速度(UMF)關係 40 4.2.1 分散板兩側壓降(ΔPD)與氣體表觀速度(Us) 40 4.2.1.1 不同床重下分散板兩側壓降(ΔPD)與氣體表觀速度(Us)關係 42 4.2.1.2 不同分散板下分散板兩側壓降(ΔPD)與氣體表觀速度(Us)關係 45 4.2.1.3 不同粒徑下分散板兩側壓降(ΔPD)與氣體表觀速度(Us)關係 48 4.2.1.4 以Davidson & Harrison method [4]計算的最小流體化速度(Umf)與現象觀察結果比較 50 4.2.2 分散板壓降(ΔPdistributor)與氣體表觀速度(Us)關係討論 52 4.2.2.1空床分散板壓降(ΔPdistributor,empty)與氣體表觀速度(Us)關係 61 4.2.2.1.1 不同分散板下空床分散板壓降(ΔPdistributor,empty)與氣體表觀速度(Us)關係 61 4.2.2.2 實驗數據計算出的分散板壓降(ΔPdistributor, exp.)對氣體表觀速度(Us)關係 64 4.2.2.2.1 不同床重下實驗數據計算出的分散板壓降(ΔPdistributor, exp.)對氣體表觀速度(Us)關係 64 4.2.2.2.2 不同分散板下實驗數據計算出的分散板壓降(ΔPdistributor, exp.)對氣體表觀速度(Us)關係 67 4.2.2.2.3 不同粒徑下實驗數據計算出的分散板壓降(ΔPdistributor, exp.)對氣體表觀速度(Us)關係 71 4.2.2.2.4 實驗數據計算出的分散板壓降(ΔPdistributor, exp.)對最小流體化速度(Umf)關係 73 4.2.2.3 Ergun equation [6]和床重計算出的分散板壓降(ΔPdistributor, theo.)對氣體表觀速度(Us)關係 76 4.2.2.3.1 不同床重下Ergun equation [6]和床重計算出的分散板壓降(ΔPdistributor, theo.)對氣體表觀速度(Us)關係 76 4.2.2.3.2 不同分散板下Ergun equation [6]和床重計算出的分散板壓降(ΔPdistributor, theo.)對氣體表觀速度(Us)關係 79 4.2.2.3.3 不同粒徑下Ergun equation [6]和床重計算出的分散板壓降(ΔPdistributor, theo.)對氣體表觀速度(Us)關係 83 4.2.2.3.4 Ergun equation [6]和床重計算出的分散板壓降(ΔPdistributor, theo.)對最小流體化速度(Umf)關係 85 4.2.3 分散板壓降對床整體壓降比值(ΔPdistributor/ΔPB)與氣體表觀速度(Us) 88 4.2.3.1 實驗數據計算出的分散板壓降對床整體壓降比值(ΔPdistributor, exp./ ΔPB)對氣體表觀速度(Us)關係 88 4.2.3.1.1 不同床重下實驗數據計算出的分散板壓降對床整體壓降比值(ΔPdistributor, exp./ ΔPB)對氣體表觀速度(Us)關係 88 4.2.3.1.2 不同分散板下實驗數據計算出的分散板壓降對床整體壓降比值(ΔPdistributor, exp./ ΔPB)對氣體表觀速度(Us)關係 90 4.2.3.1.3 不同粒徑下實驗數據計算出的分散板壓降對床整體壓降比值(ΔPdistributor, exp./ ΔPB)對氣體表觀速度(Us)關係 91 4.2.3.1.4 實驗數據計算出的分散板壓降對床整體壓降比值(ΔPdistributor, exp./ ΔPB)對最小流體化速度(Umf) 92 4.2.3.2 以Ergun equation和床重計算出的分散板壓降對床整體壓降比值(ΔPdistributor, theo./ ΔPB)對氣體表觀速度(Us)關係 95 4.2.3.2.1 不同床重下Ergun equation [6]和床重計算出的分散板壓降對床整體壓降比值(ΔPdistributor, theo./ ΔPB)對氣體表觀速度(Us)關係 95 4.2.3.2.2 不同分散板下Ergun equation [6]和床重計算出的分散板壓降對床整體壓降比值(ΔPdistributor, theo./ ΔPB)對氣體表觀速度(Us)關係 96 4.2.3.2.3 不同粒徑下Ergun equation [6]和床重計算出的分散板壓降對床整體壓降比值(ΔPdistributor, theo./ ΔPB)對氣體表觀速度(Us)關係 97 4.2.3.2.4 Ergun equation [6]和床重計算出的分散板壓降對床整體壓降比值(ΔPdistributor, theo./ ΔPB)對最小流體化速度(Umf) 98 4.3 銳孔壓降(ΔPORIFICE)與最小流體化速度(UMF)關係 101 4.3.1 銳孔壓降(ΔPorifice)對氣體表觀速度(Umf)關係 101 4.3.1.1 不同床高下銳孔壓降(ΔPorifice)對氣體表觀速度(Umf) 103 4.3.1.2 不同分散板下銳孔壓降(ΔPorifice)對氣體表觀速度(Umf)關係 106 4.3.1.3 不同粒徑下銳孔壓降(ΔPorifice)對氣體表觀速度(Umf)關係 107 4.3.1.4 以Davidson & Harrison method [4]計算銳孔壓降(ΔPorifice)對氣體表觀速度(Us)的最小流體化速度(Umf)與現象觀察結果比較 108 4.3.2 床整體壓降(ΔPB)與銳孔壓降(ΔPorifice)關係討論 110 4.3.2.1 不同床高下床整體壓降(ΔPB)對銳孔壓降(ΔPorifice)關係 113 4.3.3 銳孔壓降(ΔPorifice)與最小流體化速度(Umf)關係 118 4.3.3.1 由流化床轉變為固定床時床整體壓降(ΔPB)、銳孔壓降(ΔPorifice)以及氣體表觀速度(Us)關係 120 第五章 結論 123 參考文獻 125 附錄 129 | - |
dc.language.iso | zh_TW | - |
dc.title | 以分散板與銳孔流量計壓降探討B族粒子之最小流體化床速度 | zh_TW |
dc.title | An Approach to Determine the Minimum Fluidization Velocity of Geldart Group B Particles by Distributor Pressure Drop and Orifice Pressure Drop | en |
dc.type | Thesis | - |
dc.date.schoolyear | 110-2 | - |
dc.description.degree | 碩士 | - |
dc.contributor.oralexamcommittee | 廖英志;徐振哲 | zh_TW |
dc.contributor.oralexamcommittee | Ying-Chih Liao;Cheng-Che Hsu | en |
dc.subject.keyword | 流體化床,最小流體化速度,分散板,銳孔流量計, | zh_TW |
dc.subject.keyword | fluidized bed,minimum fluidization velocity,distributor,orifice meter, | en |
dc.relation.page | 152 | - |
dc.identifier.doi | 10.6342/NTU202204058 | - |
dc.rights.note | 同意授權(限校園內公開) | - |
dc.date.accepted | 2022-09-27 | - |
dc.contributor.author-college | 工學院 | - |
dc.contributor.author-dept | 化學工程學系 | - |
dc.date.embargo-lift | 2025-09-26 | - |
顯示於系所單位: | 化學工程學系 |
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