The design of a fully integrated Chemical looping reforming (CLR), single adiabatic water gas shift reactor (WGSR) and Pressure swing adsorption (PSA) operated under dynamic conditions for small scale H generation with inherent pure CO production is carried out. The dynamically operated packed bed reactors taking part in the chemical looping process have been modelled, designed and simulated to operate with transient feeds from an integrated PSA unit used for the production of 130 Nm/h of pure H (99.9999% purity). As by-product, 51 Nm/h of pure CO (>98.8% purity) is also produced. A rapid cycle 8-bed configuration increases the H recovery by 4% whilst reducing the tail gas buffer tank volume requirement by 44%. The effect of the PSA dynamic tail gas composition used as fuel for the CLR reduction reactor stage was found negligible regarding the continuity of the process and the performance of the plant, as it affected only the reduction outlet gas composition profile but had little effect on the reactor bed temperature profile. With respect to the design of the chemical looping reactor beds, an analysis has been performed on the effect of heat losses showing that at higher heat transfer coefficient ( = 5.0 W∙m∙K) CH conversion decreased significantly (≈90% compared to adiabatic operation), therefore a different strategy was implemented. The overall study demonstrates the process design feasibility for producing blue H or renewable H from methane/bio-methane in decentralised and modular units.

中文翻译：

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小规模现场氢气和纯二氧化碳生产中变压吸附集成化学循环工艺的动态行为

设计了完全集成的化学循环重整（CLR）、单个绝热水煤气变换反应器（WGSR）和在动态条件下运行的变压吸附（PSA），用于小规模氢气生产和固有的纯二氧化碳生产。参与化学循环过程的动态运行的填充床反应器已经过建模、设计和模拟，可使用来自集成 PSA 装置的瞬态进料运行，该装置用于生产 130 Nm3/h 的纯 H（纯度为 99.9999%）。作为副产品，还产生了 51 Nm3/h 的纯 CO（纯度 >98.8%）。快速循环 8 床配置将 H 回收率提高了 4%，同时将尾气缓冲罐体积需求减少了 44%。发现用作 CLR 还原反应器阶段燃料的 PSA 动态尾气成分对于工艺的连续性和工厂性能的影响可以忽略不计，因为它仅影响还原出口气体成分分布，但对反应器床层温度曲线。关于化学循环反应器床的设计，对热损失的影响进行了分析，结果表明，在较高的传热系数（= 5.0 W∙m∙K）下，CH 转化率显着下降（与绝热相比约 90%）操作），因此实施了不同的策略。总体研究证明了在分散和模块化单元中从甲烷/生物甲烷生产蓝色氢气或可再生氢气的工艺设计可行性。