本研究之主要目的為藉由氧化銅的高還原速率與氧化鐵良好的熱穩定性來提升載氧體之反應性，並製備出適合應用於化學迴路燃燒與產氫程序之合成鐵-銅系複合載氧體。本研究為了製備出高反應特性之鐵銅複合載氧體，對於氧化鐵和氧化銅比例與有無添加澱粉做了探討，其實驗結果顯示出氧化鐵與氧化銅比例為3比1時，於合成氣反應具有良好的反應性。此外，為了製備出具有高機械強度之複合載氧體，分別將氧化鐵和氧化銅分別與氧化鋁、二氧化鈦混合，並利用壓錠方式製備成錠材，也針對不同的燒結溫度也做了研究，當鐵銅鋁載氧體和鐵銅鈦複合載氧體鍛燒溫度為1000oC，在反應前及經過10圈的氧化還原操作後，皆具有相當不錯的反應性。
本研究在固定床反應器之產氫程序中，對水蒸氣的滯留時間與濃度做了探討，其實驗結果顯示，濃度比滯留時間更容易影響產氫量。反應溫度在600oC到1000oC的操作溫度下亦藉由通入水蒸氣以鐵-銅系複合載氧體(鐵銅鋁、鐵銅鈦)同時使水蒸氣還原產氫，實驗結果顯示鐵-銅系複合載氧體(鐵銅鋁、鐵銅鈦)均會受到動力學與熱力學的影響，在低溫時主要受到動力學的影響；在高溫時主要受到熱力學的影響，並且得知鐵銅鋁載氧體相較於鐵銅鈦載氧體適合在較低溫的環境中產氫。此外，固定床反應器所得之產氫反應實驗數據及搭配反應機制模型的結果中顯示，相邊界控制模型適用於鐵銅鋁載氧體與鐵銅鈦複合載氧體，其鐵銅鋁載氧體產氫反應濃度驅動力之反應級數為1.65，產氫反應活化能為20.328kJ/mole；鐵銅鈦載氧體產氫反應濃度驅動力之反應級數為1.13，產氫反應活化能為40.423kJ/mole。

This study focused on Fe2O3 and CuO because of better thermal stability and high reduction rates, respectively. The Fe-Cu mixed oxygen carrier had higher oxygen transport capacity and reduction rate. The suitable oxygen carriers were selected by optimizing performance for the applications of Chemical Looping Combustion (CLC) and Chemical Looping Hydrogen Generation (CLHG) process. In order to increase the reactivity for Fe-Cu based oxygen carriers with syngas, the effect of Fe2O3/ CuO ratios was to investigate in this study. The results showed that Fe2O3/ CuO was 3/1 having better redox reactivity. Besides, in order to increase the mechanical strength of Fe-Cu based oxygen carrier, the Fe2O3 and CuO were not only prepared with Al2O3 or TiO2 as inert support by mechanical mixing and pelletized by tablet machine but also the different sintering temperature was also investigated. The results showed that FCA3110-S0 and FCT3110-S0 pellets sintered at 1000oC had proper mechanical strength and better reactivity during 10 redox cycle.
The CLHG process was conducted at the fixed reactor which the steam flow rate was to investigate in this study. The results showed that the steam concentration had more influence than intake gas velocity. Hydrogen generation was demonstrated to be feasible by steam oxidation with reduced FCA3110-S0 and FCT3110-S0 oxygen carriers which the reaction temperature from 600-1000oC in the fixed bed reactor. The results showed that there were two processes which had the significant influence the hydrogen generation rate, i.e., the thermodynamic equilibrium and the reaction kinetics. The hydrogen equilibrium was higher at a lower operating temperature. However, the reaction rate constant increased with the increase of temperature. Finally, the FCA3110-S0 oxygen carrier was more suitable than FCT3110-S0 oxygen carrier to produce hydrogen at lower temperature.
Besides, the fixed reactor experiments also provided that the reaction temperature influenced not only the reaction rate constant, k, but also the driving force in steam oxidization of FCA3110-S0 and FCT3110-S0 oxygen carriers. The kinetics analysis indicated that the steam oxidization of FCA3110-S0 and FCT3110-S0 oxygen carriers can be described as 3-D phase-boundary controlled model. The reaction order, α and energy of activation found for steam oxidation of FCT3110-S0 oxygen carriers were 1.65 and 20.328 kJ/mol, respectively. The reaction order, β and energy of activation found for steam oxidation of FCT3110-S0 oxygen carriers were 1.13 and 40.423 kJ/mol, respectively.

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