近年來經濟活動的快速成長，使人類對化石燃料的依賴性日趨增加，大量燃燒化石燃料的結果使得二氧化碳大量被排出，更加劇了全球暖化的腳步。如何捕捉二氧化碳使其減量，成為二十一世紀全球公民所需面對的共同議題。純氧燃燒系統是一種二氧化碳濃縮技術，排放的高濃度二氧化碳更利於捕獲，並降低捕獲成本、易於改建，因此近期獲得化石燃料發電廠高度重視。而流體化床反應器具有高熱傳及高質傳係數，易達到等溫狀態，符合可降低發電及環保成本之高溫乾式淨化系統。以脫硫渣當作高溫固態吸收劑，可降低吸收劑成本與增加爐石再利用性，因此本實驗模擬純氧燃燒之煙道氣條件，以脫硫渣作為吸收劑，探討在流體化床系統中與二氧化碳在高溫下反應形成金屬碳酸鹽之研究。
本研究操作條件及研究成果分為下列幾部分說明：
1. 隨著溫度上升，不管是實驗結果或者是經驗公式結果，其最小流體化速度都隨之減小。然而，當溫度達到700oC時，因為燒結現象導致其最小流體化速度略高於600oC的最小流體化速度。此外，由於Ergun equation之假設未考慮粒子間作用力，高溫下粒子黏滯性與凡得瓦力隨溫度提高而增加，因此本實驗最小流體化速度略高於經驗公式估計值。
2. 根據ICP及XRD定性及定量結果顯示，150-300 μm及75-106 μm脫硫渣中之鈣化合物以氫氧化鈣為主，含量分別為15.76%及18.86%，此外，由TGA結果可知：不管是粒徑範圍在150-300 μm之大顆粒脫硫渣，抑或是75-106 μm之小顆粒脫硫渣，在450-580oC下其利用率皆有一定量，24.5~34.09%。
3. 當氣流速度由0.5倍最小流體化速度上升至最小流體化速度時，其利用率由28.7%上升至41.2%，證實和固定床相比，流體化床有較好之碳酸化效果。在流體化床系統中，隨著空床速度上升，利用率會隨之下降；較小顆粒之脫硫渣有較好的利用率，但實驗操作參數仍須考量操作之經濟成本。
4. 在流體化床系統中，採用1.5倍Umf，以150-300 μm脫硫渣進行CO2吸收實驗，最佳操作溫度為600oC，此外，當水氣含量達到5%時，有助於脫硫渣之碳酸化反應，利用效率可達到42%，然而，若水氣濃度超過5%時，則會因為競爭吸收以及燒結作用造成利用率下降。
5. 由XRD、SEM、EDS、Mapping及FTIR結果可知脫硫渣在反應前後之各項特性轉變，也說明脫硫渣在流體化床中吸收CO2，並與其反應導致CaCO3之形成及堆積。
6. 由反應動力研究發現，衰退模式較適合用來描述此結果，其迴歸分析顯示在不同溫度下之實驗貫穿曲線與模擬結果符合，R2 可達到 0.99，脫硫渣反應活化能Ea= 58.9 kJ mol−1，衰退活化能Ea= 8.7 kJ mol−1。

In recent years, human being rely on the fossil fuel due to the booming economy. A great amount of carbon dioxide releasing from fossil fuel combustion cause the global warming. As a result, it is a serious issue to capture carbon dioxide for global citizens today. Oxy-fuel combustion system is a carbon dioxide capture technology, contributing to higher capture efficiency due to concentrated CO2, decreasing processing cost, and constructing easily. Recently, it is considered as a new option for power generation. In fluidized bed system, it has high heat transfer and mass transfer coefficient and it is easy to reach isothermal condition which fits the high temperature carbonation by dry techniques. Utilizing desulfurization slag as sorbent not only reuses the waste but also reduces cost. In this study, desulfurization slag was used to absorb carbon dioxide from oxy-fuel combustion in a fluidized bed reactor.
Results of this study are described as follows：
1. The minimum fluidized velocity decreases along with the increasing temperature both for empirical model prediction and experimental results. However, the minimum fluidized velocity at 700oC is slight higher than at 600 oC due to slag sintering. Besides, the assumption of Ergun equation neglects the interparticle force causing that the experimental results are higher than empirical results.
2. According to the results of ICP and XRD analysis, the contents of calcium hydroxide in desulfurization slag of 150-300 μm and 75-106 μm are 15.76% and 18.86%, respectively. From TGA analysis, the desulfurization slags of both 150-300 μm and 75-106 μm have a considerable slag utilization (24.5-34.09%) from 450oC to 580oC.
3. When the gas velocity reaches minimum fluidized velocity, the utilization of the slag with size 150-300 μm will increase from 28.7% of a fixed bed mode to 41.2%. Fluidized bed reactor is better than a fixed bed reactor due to the high heat transfer and mass transfer rate. In a fluidized bed reactor, as the weight hourly space velocity becomes higher, the slag utilization decreases as a result of the short residence time. Besides, the smaller size of the desulfurization slag, the higher of the utilization.
4. The optimal operating temperature is about 600oC for the CO2 removal with desulfurization slag of 150-300 μm. Furthermore, the effects of adding water vapor on the carbonation of desulfurization slag were conducted. The results illustrate that the water vapor content can enhance the carbonation reaction and its optimal content is 5% which the slag utilization is 42.2% with 1.5 Umf. However, the slag utilization decreases as the water vapor content is greater than 5%, resulting from competitive sorption and sintering.
5. The results of XRD, SEM, EDS, Mapping and FTIR analyses indicate the structure and bonding for desulfurization slags before and after carbonation. It confirms the appearance of CaCO3 after carbonation reaction.
6. The deactivation model regressions of the experimental breakthrough curves have been conducted and the results show that the model is in good agreement with the experimental data. The activation energies for the reaction and deactivation are 58.9 and 8.7 kJ mol−1, respectively.

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