在常规生物质化学链气化工艺中，热解、气化、重整等众多复杂的反应过程被限制在同一个反应空间中，这些反应之间存在复杂的相互作用，导致碳转化率较低，且难以实现产物定向调控与系统自热运行。基于解耦策略的生物质热解与化学链重整相结合的工艺可实现上述复杂过程定向调控，从而一定程度上克服常规化学链气化面临的挑战。利用Aspen Plus软件对该工艺进行全流程模拟，并使用热解实验结果对模型进行验证。考察了热解反应器温度、重整反应器温度、蒸汽生物质质量比对工艺性能的影响规律。结果表明：热解温度在400～600 ℃所建立的工艺模型能够有效预测热解产物分布；随着热解温度的提升，合成气产量总体上呈现上升趋势，在550 ℃下获得最高的合成气产量为1 158.98 Nm³/kg生物质；在600 ℃热解温度下，热解半焦和载氧体氧化放热可满足重整反应器的热量需求，实现系统热自持； 重整反应器温度升高会增加合成气的产量，但是会降低合成气的氢碳比与能量效率，同时系统自热状态下运行所需的床料循环速率显著增加；蒸汽能够有效调节合成气产品的氢碳比，热解化学链重整工艺生产氢碳摩尔比为2.0的合成气，蒸汽生物质质量比仅为0.45，低于生物质化学链气化工艺所需的1.2～1.4。因此，综合考虑合成气产量及工艺性能，生物质热解结合化学链重整工艺操作条件以热解反应器温度550～600 ℃，重整反应器温度700 ℃，蒸汽生物质质量比为0.45较为适宜。

The biomass chemical looping gasification process involves various complex reaction processes, including pyrolysis, gasification, and reforming, which occur within the same reaction space. These reactions exhibit intricate interactions, posing challenges for achieving targeted control. Consequently, some issues arise, such as low carbon conversion, high tar yield, and difficulties in attaining auto thermal operation. The biomass pyrolysis chemical looping re-forming process, employing the decoupling strategy, aims to achieve an independent regulation of pyrolysis and reforming reactions, thereby mitigating the issues mentioned above. The process underwent simulation using the Aspen Plus software, and the model’s validity was confirmed by comparing it with the results of pyrolysis experiments. Using the established process model, the impact of pyrolysis reactor temperature, fuel reactor temperature, and steam-to-biomass mass ratio on process performance was examined. The results demonstrate the effective predictive capability of the established process model regarding the distribution of pyrolysis products within the temperature range of 400−600 ℃. As the pyrolysis temperature rises, the syngas yield exhibits a generally increasing trend, reaching its peak at 550 ℃ with a value of 1158.98 Nm³/kg biomass. At a pyrolysis temperature of 600 ℃, the heat demand of the reforming reactor is adequately met by the exothermic reactions of pyrolysis char and oxygen carrier oxidation without any surplus energy. Elevating the fuel reactor temperature augments the syngas yield but diminishes the H₂-to-CO ratio and energy efficiency of the syngas while also necessitating a substantial increase in the circulation rate of bed material for achieving auto thermal operation. Steam serves as an effective regulator for controlling the H₂-to-CO ratio in syngas. The pyrolysis chemical looping reforming process generates syngas with an H₂-to-CO ratio of 2.0 when the steam-to-biomass mass ratio is 0.45, lower than the ratio needed for the biomass chemical looping gasification process. Consequently, taking into account the syngas yield and process performance, the recommended operating conditions for the pyrolysis chemical looping reforming process are as follows: a pyrolysis reactor temperature ranging from 550 to 600 ℃, a fuel reactor temperature of 700 ℃, and a steam-to-biomass mass ratio of 0.45.