化學迴路燃燒系統具高效燃燒與分離二氧化碳的功能，其反應系統設計、載氧體流體化狀態及固氣接觸時間，均會影響反應效率。本研究以澳洲和巴西鐵礦為載氧體，以實場廢液異丙醇(IPA)與蝕刻後消除液(EKC)為燃料，於1kWth和100kWth交聯式流體化床進行化學迴路燃燒程序。藉由調整燃料反應器、空氣反應器與密封迴路的氣體流量，來改變載氧體流體化行為與其在系統內分佈，在不同的溫度下進行化學迴路燃燒反應，量測系統內壓力分佈，並以上升管的壓力差估算固體循環速率，並分析燃燒後尾氣的組成。此系統中燃料反應器與封閉迴路均為鼓泡床形式，空氣反應器為快速流體化床，載氧體在兩者間穩定運行可達到較高CO2選擇率和純度。
實驗結果顯示，在1kWth交聯式流體化床系統中，空氣流量為 5 L/min與封閉迴路氮氣流量為 3.5 L/min時，燃料反應器以液體流量 1 mL/min搭配氮氣流量4 L/min，以及實場廢液4 mL/min搭配氮氣流量1L/min為最佳參數，CO2 選擇率與純度可高於70%。在100kWth反應系統中空氣流量為 80 L/min與封閉迴路氮氣流量為 40 L/min時，燃料反應器分以液體流量 23 mL/min搭配氮氣流量50 mL/min為最佳參數，此時，出口氣體組成以甲烷濃度最高。操作程序的關鍵點為液體汽化率，若燃料經預熱器氣化程度愈高，其可使載氧體流體化越穩定，廢液裂解率可達100%且CO2 選擇率可高於70%。在液體進料量過多時，供氧量不足時，系統會產生積碳行為，此時整體系統可視為裂解爐，產生甲烷與氫氣比例可達60％以上，但仍可維持穩定流體化運行。載氧體的低磨耗性質顯示天然鐵礦適合運用在交聯式流體化床，壽命長達1000小時以上，顯示此載氧體與本系統具有商轉價值的潛力所在。

The chemical-looping combustion (CLC) is a novel combustion process with the high combustion efficiency and direct separation of carbon dioxide during combustion reaction. The reaction rate is affected by the design of the reaction system, the degree of fluidization of oxygen carrier, and the contact time between oxygen carrier and fuel gas significantly. In this study, two kinds of high-water-content organic waste, IPA and EKC, were selected as the fuel for chemical-looping combustion, which was carried out in the 1kWth and 100kWth interconnected fluidized bed with two kinds of oxygen carriers, Australian and Brazilian iron ore, respectively. The behavior of fluidization of the oxygen carrier and the distribution of the oxygen carrier in fuel and air reactors were affected by the gas flow rates of the fuel reactor, air reactor, and the loop seal. The pressure drop of air reactor was measured and applied to estimate the solids circulation rate. The composition of the exhaust gas for the chemical-looping combustion process was measured to determine the combustion efficiency and fuel conversion under different temperatures. In this system, the fuel reactor and loop seal were in the form of bubbling bed, and the air reactor was a fast fluidized bed. The oxygen carriers were transported stably between two reactors to achieve high CO2 selectivity and purity.
In 1kWth interconnected fluidized bed, the experimental results showed that the optimal operation parameters were obtained at 5 L/min of air to AR ,3.5 L/min of nitrogen to LS and 4L/min of nitrogen with 1mL/min of solvent to FR. The maximum solvent feeding rate was 4 mL/min with 1L/min of nitrogen as carrier gas. It was achieved with over 70% of CO2 selectivity and purity.
In 100kWth interconnected fluidized bed, the experimental results indicated that the optimal operation parameters were obtained at 80 L/min of air to AR, 40 L/min of nitrogen to LS, and 50 L/min of nitrogen with 23 mL/min of solvent to FR. The methane was the major product of exhaust as feeding 160 ml/min of solvent to FR. The vaporization rate of the solvent was the key step in this combustion process. The more complete vaporization of liquid fuel through the preheating device is, the more stable and smoother the degree of fluidization is.
In conclusion, the complete vaporization of solvent was achieved with over 70% of CO2 selectivity. As the feeding rate of liquid fuel was too large, the oxygen-supply rate by oxygen carriers was insufficient, resulting in the generation of coke. The entire system thus played a role as thermal cracking system, and the molar fraction of methane and hydrogen was higher than 60%. The system could still be kept at a stable fluidization condition. The analysis results of physic characteristics for oxygen carriers indicated that the iron ore was suitable material for interconnected fluidized beds with a lifetime over 1000 h. The whole results showed the practicality of the chemical-looping combustion process for treatment of high-water-content organic waste.

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