本研究目的幫助胺液再生單元(Amine Regeneration Unit,ARU)達到節省蒸氣的使用量，降低成本支出，但因現場變數E的實驗室數據一天只有一筆，無法立即得知目前變數E是多少，藉此作為一個基準點來調整蒸氣用量，只能透過一段時間得知實驗室數據才能進行調整，如此一來，便導致一些不必要的蒸氣損失。
研究共分為三部分，第一部分是利用ASPEN PLUS軟體來建立ARU模型來模擬在不同進料條件下各個變數對蒸氣用量的影響程度推導出相關方程式，並模擬現場實際進料數據來與現場數據做比較，來對模型進行修正。第二部分則是利用主要變數每小時間的變化關係來建立變數E預測模型，藉此模型可以得到每小時變數E的預測值，以提供現場操作人員掌握目前變數E的情況，以此作為基準點適當地調高變數E來達到降低蒸氣用量的效果。第三部分則是探討加入磷酸等降低平衡常數物質對ARU蒸氣用量的影響。

The purpose of this study is to help the Amine Regeneration Unit(ARU) to save steam usage and reduce costs. In reality, however, the laboratory data of variable E is only one per day, which results in the process operating at non-optimal steam usage. Therefore, this study was divided three parts. First of all, we used Aspen Plus simulation software to build up the ARU model to find out how much each of the variables are affecting steam usage and then derive the equations of each of the variables. Secondly we developed a prediction model for variable E by which the model could obtain the predicted value of variable E per hour so as to provide operators to use it to adjust steam usage. Finally we discussed the effect of adding phosphoric acid or other substances that reduce the equilibrium constant on the steam usage of ARU.

摘要 i
Abstract ii
誌謝 iii
目錄 iv
圖目錄 vi
表目錄 viii
第一章 緒論 1
1.1 研究背景 1
1.2研究動機 2
1.3文獻回顧 3
第二章 研究方法 6
2.1 模擬軟體簡介 6
2.2 Aspen Plus基本架構 6
2.3 Aspen Plus模擬操作流程 7
2.3 化學平衡反應 10
2.4熱力學模型-Electrolyte NRTL Model 11
2.5平衡模型建立 13
2.6 有限差分法 15
2.7 現場數據描述 16
三、結果與討論 21
3.1修改平衡常數 21
3.2單元效率 23
3.3 主要變數效應 24
3.4蒸氣流量對主要變數的變化率 30
3.4.1蒸氣用量對A的變化率 30
3.4.2蒸氣用量對C的變化率 31
3.5 變數E預測結果 32
3.6節能預測 33
3.7加入H3PO4對胺液再生系統的影響 34
第四章 結論 40
參考文獻 41

[1] Khakdaman, H., et al., Revamping of gas refineries using amine blends. 2008.
[2] Butwell, K.F. and C.R. Perry. Performance of gas purification systems utilizing DEA solutions. in Gas Conditioning Conference. 1975.
[3] Donnelly, S.T. and D. Henderson. A new approach to amine selection. in CNGPA Third Quarterly Meeting. 1974.
[4] Blanc, C., M. Grall, and G. Demarais. Part played by degradation products in the corrosion of gas sweetening plants using DEA and MDEA. in Proc. Gas Cond. Conf.;(United States). 1982.
[5] Polasek, J. and J.J.E.P. Bullin, Selecting amines for sweetening units. 1984. 4(3): p. 146-149.
[6] Polasek, J.C., G. Inglesias-Silva, and J.A. Bullin. Using mixed amine solutions for gas sweetening. in Proceedings of the annual convention-gas processors association. 1992. Gas Processors Association.
[7] Idem, R., et al., Pilot plant studies of the CO2 capture performance of aqueous MEA and mixed MEA/MDEA solvents at the University of Regina CO2 capture technology development plant and the boundary dam CO2 capture demonstration plant. 2006. 45(8): p. 2414-2420.
[8] Spears, M.L., et al., Converting to DEA/MDEA mix UPS sweetening capacity. 1996. 94(33): p. 63-68.
[9] Huffmaster, M. and P. Nasir, Amine and Sulfinol treating system optimization. 1995, Gas Processors Association, Tulsa, OK (United States).
[10] Keller, A., et al., How efficient are refinery amine units? 1995. 74(4).
[11] Abry, R. and M. DuPart. Amine Plant Troubleshooting and Optimization: A Practical Operating Guide. in Proceedings of the 43rd Laurance Reid Gas Conditioning Conference, held in. 1993.
[12] Lunsford, K.M. and J.A. Bullin, Optimization of amine sweetening units. 1996: American Institute of Chemical Engineers.
[13] Austgen, D.M., et al., Model of vapor-liquid equilibria for aqueous acid gas-alkanolamine systems using the electrolyte-NRTL equation. 1989. 28(7): p. 1060-1073.
[14] Austgen, D.M., et al., Model of vapor-liquid equilibria for aqueous acid gas-alkanolamine systems. 2. Representation of H2S and CO2 solubility in aqueous MDEA and CO2 solubility in aqueous mixtures of MDEA with MEA or DEA. 1991. 30(3): p. 543-555.
[15] Mock, B., L. Evans, and C.C.J.A.J. Chen, Thermodynamic representation of phase equilibria of mixed‐solvent electrolyte systems. 1986. 32(10): p. 1655-1664.
[16] Pitzer, K.S.J.J.o.t.A.C.S., Electrolytes. From dilute solutions to fused salts. 1980. 102(9): p. 2902-2906.
[17] Rashin, A.A. and B.J.T.j.o.p.c. Honig, Reevaluation of the Born model of ion hydration. 1985. 89(26): p. 5588-5593.
[18] Optimized Gas Treating, I., Enhanced Treating Using MDEA with H3PO4. April, 2020. 14(4): p. 2.