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完整後設資料紀錄
DC 欄位 | 值 | 語言 |
---|---|---|
dc.contributor.advisor | 黃孝平(Hsiao-Ping Huang) | |
dc.contributor.author | Yi-Chen Lee | en |
dc.contributor.author | 李奕成 | zh_TW |
dc.date.accessioned | 2021-06-13T15:22:25Z | - |
dc.date.available | 2013-07-23 | |
dc.date.copyright | 2008-07-23 | |
dc.date.issued | 2008 | |
dc.date.submitted | 2008-07-23 | |
dc.identifier.citation | [中 文]
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F., “Design Method for Kinetically Controlled, Staged Reactive Distillation Columns.” Ind. Eng. Chem. Res., 37(7), 2821, (1998). [39] Olujic Z.; Fakhri F.; A. de Rijke, J. de Graauw, Jansens P. J., “Internal Heat Integration–the key to an energy-conserving distillation column.” J. Chem. Technol. Biotechnol. 78, 241, (2003). [40] Olujic Z.; Sun L.; A. de Rijke, J. de Graauw, Jansens P. J., “Conceptual Design of an Internally Heat Integrated Propylene and Propane Splitter.” Energ, 31, 3083, (2006). [41] Pöpken, T., Götze, L.; Gmehling, J., “Reaction Kinetics and Chemical Equilibrium of Homogeneously and Heterogneously Catalyzed Acetic Acid Esterification with Methanol and Methyl Acetate Hydrolysis.” Ind. Eng. Chem. Res., 39(7), 2601, (2000). [42] Pöpken, T.; Steinigeweg, S.; Gmehling, J., ”Synthesis and Hydrolysis of Methyl Acetate by Reactive Distillation Using Structured Catalytic Packings: Experiments and Simulation.” Ind. Eng. Chem. Res., 40(6), 1566, (2001). [43] Robinson, C. S.; Gilliland, R. E., Elements ofFractiona1 Distillation, McGraw-Hill: New York, 4th ed. (1950). [44] Song, W.; Venimadhavan, G.; Manning, J. M.; Malone, M. F.; Doherty, M. F., “Measurement of Residue Curve Maps and Heterogeneous Kinetics in Methyl Acetate Synthesis.” Ind. Eng. Chem. Res., 37(5), 1917, (1998). [45] Tang, Y. T.; Chen, Y. W.; Huang, H. P.; Yu, C. C.; Hung, S. B.; Lee, M. J., “Design of Reactive Distillations for Acetic Acid Esterification.”, AIChE J., 51(6), 1683, (2005). [46] Tyreus, B. D., “Control of Multi-Effect, Energy Conserving Distillation System”, Ph.D. Thesis. (1976). [47] Takamatsu T., Nakaiwa M., Huang K., Noda H., Nakanishi T., Aso K., “Simulation oriented development of a new heat-integrated distillation column and its characteristics for energy saving.” Comput. Chem Eng., 21,243, (1997). [48] Wankat, P. C.; “Multieffect Distillation Processes.” Ind. Eng. Chem. Res., 32(5), 894, (2001). | |
dc.identifier.uri | http://tdr.lib.ntu.edu.tw/jspui/handle/123456789/37247 | - |
dc.description.abstract | 本論文將介紹兩種利用加壓技術的熱整合反應蒸餾塔:內部熱整合反應蒸餾塔(r-HIDiC),與雙效熱整合反應蒸餾塔(r-FS),並實際應用於乙酸甲酯水解反應蒸餾系統(林禹德 2006)。在加壓的操作下,將可以使得反應蒸餾塔發生內部或外部的熱傳,進而達到熱整合的效果;乙酸甲酯水解係微吸熱反應,在操作壓力、溫度提高的條件下,亦加快系統的反應速率(reaction rate),並提升平衡常數(equilibrium constant),使得反應轉化率變好,而系統所需的觸媒量亦可以減少。
在最適化的設計下,r-HIDiC約有27 %的節能效果而r-FS則有38 %。但由於r-HIDiC必須使用價格昂貴的設備裝置-氣體壓縮機且其耗費61.9 %的總設備成本與31.3 %的總水電、蒸氣費用,使得r-HIDiC之年總成本(TAC)高出傳統反應蒸餾塔約33 %,因此就經濟層面來看,r-HIDiC並無好處。相較之下,r-FS有較好的經濟效益並可以節省15.2 %的操作成本以及6.4 %的TAC;雖然r-FS是由兩根反應蒸餾塔所組成,但在加壓與進料負載量減半的操作下,每根反應蒸餾塔都較原來的小,所以其設備成本與傳統反應蒸餾塔相去不遠。 經由節能效益與經濟面的分析,對乙酸甲酯水解反應系統而言,r-FS係為較好的熱整合架構。因此,我們將探討r-FS的動態控制策略,其控制架構將有三種:CS1~CS3。為了達到產物的規格,我們將第二根分離塔底液位視為系統內水庫存量的大小,用來控制新鮮水入料流量,以滿足化學計量平衡。在溫度控制下將造成產品組成偏差;但是其偏差很小,亦在可以接受的範圍內。這些控制架構在進料組成擾動皆有良好的排除效果;此外,控制架構CS3在進料流量擾動的排除效果優於CS1與CS2。 關鍵詞:反應蒸餾塔、內部熱整合、雙效熱整合、乙酸甲酯水解、節能技術、壓力轉移。 | zh_TW |
dc.description.abstract | In this paper, two designs of heat-integrated reactive distillation for the hydrolysis of methyl acetate are studied. The first one employs internal heat-integrated reactive distillation column (r-HIDIC) and the other utilizes feed-split reactive distillation column (r-FS). The savings in energy consumption and total annual costs are focused on the reactive column only. The reference base case for comparison is the RD column in the work of Lin et al. (2006). In both cases, part of the reactive distillation utilizes a higher pressure. This is because a higher pressure makes heat transfers in the system possible. In fact, this higher pressure benefits the reaction taking place. Because, the hydrolysis reaction of methyl acetate is slightly endothermic, a higher operating pressure implies higher temperatures, faster reaction rates, and better equilibrium constants in the reaction part which, in turn, results in less catalyst requirement.
The energy conservation studies show that r-HIDIC can reduce energy saving up to 27%, and r-FS had 38% saving when the process conditions are both optimized. Nevertheless, as far as economic aspect is concerned, r-HIDIC has no benefit, because of 33% more total annual cost (TAC) than the original RD column is required. This is due to an expensive gas compressor which takes 61.9% total capital cost and 31.3% utility costs. On the other hand, r-FS has a better economical efficiency with 6.4% and 15.2% savings on TAC and operating cost. Although r-FS consisted of two columns, each column is smaller than original one under the higher operating pressure and half loading conditions. Thus, the capital cost of r-FS is almost same as RD. Based on the energy conservation ability and economical analysis, r-FS is the better heat-integrated structure than r-HIDiC for hydrolysis of Methyl acetate reactive distillation system. Then, the issue of control strategies for r-FS is studied. There are three control strategies (CS1 to CS3) to be considered. The system should keep stoichiometric balance for satisfying both product specifications. Therefore, in the control structure, fresh water feed is controlled by the liquid level of the second separation column. Since offsets in product composition may result in temperature control, the deviations are small and under acceptable range. These schemes all have good results for feed composition disturbance rejections. Beside, CS3 has a better result for feed flow rate disturbance rejections than CS1 and CS2. Keywords: reactive distillation, internally heat-integrated distillation column (HIDiC), feed-split columns, hydrolysis of methyl acetate, energy saving, pressure swing. | en |
dc.description.provenance | Made available in DSpace on 2021-06-13T15:22:25Z (GMT). No. of bitstreams: 1 ntu-97-R95524041-1.pdf: 3403646 bytes, checksum: c4260b6ebb90a56206ca518671b239b8 (MD5) Previous issue date: 2008 | en |
dc.description.tableofcontents | 致謝 I
摘要 II Abstract IV 目錄 VI 圖索引 VIII 表索引 X 1. 緒論 1 1.1. 前言 1 1.2. 文獻回顧 6 1.3. 研究動機與目的 9 1.4. 組織章節 10 2. 熱力學及動力學模式 11 2.1. 前言 11 2.2. 熱力學模式 12 2.2.1. 液相之熱力學模式 13 2.2.2. 氣相之熱力學模式 14 2.2.3. 兩相區分布之探討 15 2.2.4. 乙酸甲酯反應蒸餾系統之蒸餘曲線圖分析 16 2.2.5. 高壓下物性之探討 21 2.3. 動力學模式 23 3. 穩態設計I 內部熱整合反應蒸餾塔(r-HIDiC) 25 3.1. 前言 25 3.2. 熱力學分析 26 3.3. 應用於乙酸甲酯水解製程 32 3.4. 最適化設計 36 3.4.1. 內部熱傳的模擬流程 36 3.4.2. 最適化步驟 39 3.4.3. 反應段與汽提段總板數的影響 41 3.4.4. 反應段中反應板數的影響 42 3.4.5. 氣體壓縮機設定之壓力差的影響 43 3.4.6. 內部熱整合反應蒸餾塔之最適化設計與比較 45 3.5. 溫度、濃度分佈以及氣、液流量探討 48 3.5.1. 溫度、濃度分佈探討 48 3.5.2. 氣、液流量探討 50 3.6. 最小回收年限之探討 51 3.7. 結果與討論 54 4. 穩態設計II雙效熱整合反應蒸餾塔(r-FS) 55 4.1. 前言 55 4.2. 應用於乙酸甲酯水解製程 56 4.3. 最適化設計 60 4.3.1. 最適化步驟 60 4.3.2. 系統中各設計變數的影響 62 4.3.3. 雙效熱整合反應蒸餾塔之最適化設計與比較 64 4.4. 溫度分佈及濃度分佈探討 68 4.4.1. 溫度分佈探討 68 4.4.2. 濃度分佈探討 69 4.5. 與內部熱整合架構之比較與討論 71 5. 動態模擬與控制 73 5.1. 前言 73 5.2. 控制環路設計 73 5.3. 控制架構的探討 74 5.3.1. 控制架構分類(CS1~CS3) 74 5.3.2. 系統所承受的干擾 76 5.4. CS1 三點溫度控制 76 5.4.1. 溫度靈敏度測試分析 77 5.4.2. 控制器參數調諧方法 82 5.4.3. CS1三點溫度控制動態模擬結果 83 5.5. CS2三點溫度控制 87 5.5.1. 溫度靈敏度測試分析及控制器參數 89 5.5.2. CS2三點溫度控制動態模擬結果 91 5.6. CS3四點溫度控制 94 5.6.1. 溫度靈敏度測試分析 94 5.6.2. 非方形相對增益(NRG)與RGA配對分析 97 5.6.3. CS3四點溫度控制動態模擬結果 99 6. 結論 103 附錄A 年總成本計算公式 105 附錄B 庫存控制環路控制器參數 107 參考文獻 109 | |
dc.language.iso | zh-TW | |
dc.title | 熱整合反應蒸餾塔應用於乙酸甲酯水解系統 | zh_TW |
dc.title | Heat Integrated Reactive Distillation Column Applied to Hydrolysis of Methyl Acetate System | en |
dc.type | Thesis | |
dc.date.schoolyear | 96-2 | |
dc.description.degree | 碩士 | |
dc.contributor.oralexamcommittee | 余政靖(Cheng-Ching Yu),陳誠亮(Cheng-Liang Chen),錢義隆(I-Lung Chien),黃琦聰 | |
dc.subject.keyword | 反應蒸餾塔,內部熱整合,雙效熱整合,乙酸甲酯水解,節能技術,壓力轉移, | zh_TW |
dc.subject.keyword | reactive distillation,internally heat-integrated distillation(HIDiC),feed-split columns,hydrolysis of methyl acetate,energy saving,pressure swing, | en |
dc.relation.page | 114 | |
dc.rights.note | 有償授權 | |
dc.date.accepted | 2008-07-23 | |
dc.contributor.author-college | 工學院 | zh_TW |
dc.contributor.author-dept | 化學工程學研究所 | zh_TW |
顯示於系所單位: | 化學工程學系 |
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