Staged Catalytic Gasification/Steam Reforming of Pyrolysis Oil
Staged Catalytic Gasification/Steam Reforming of Pyrolysis Oil
复制标题
热解油的分级催化气化/蒸汽重整
DOI：
10.1021/ie900194j
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发表时间：
2009
影响因子：
4.2
通讯作者：
W. V. Swaaij
中科院分区：
文献类型：
--
作者：
G. V. Rossum;S. Kersten;W. V. Swaaij
采用分段反应器的概念对裂解油气化/水蒸气重整反应进行了研究，该反应器由惰性床和催化固定床组成。甲烷和C2−C3自由合成气在大气压下以约800°C的单一温度产生。通过降低沸腾床的温度(432−500°C)，其功能从气化器转变为蒸发器，这样，后续的催化剂床实际上可以看到蒸发的热解油化合物(而不是燃料气)，它可以更容易地将其转化为合成气。然而，固定床的温度不能太低(最低700°C)，以避免过度的碳沉积。系统计算表明，当考虑加压(30bar)裂解油气化/重整时，当合成气是理想产品时，催化剂出口床层温度应较高(900−1000°C)才能达到足够的甲烷转化率。当只在高压下加入蒸汽时，H2/CO比率很容易增加，这是制氢所需的。对于其他应用(例如，Fischer−Tropch)，二氧化碳可能必须循环使用，以使H2/CO比保持在2−3左右。裂解油气化/重整的较低热值效率与已报道的商业甲烷蒸汽重整范围的低端相当。
Gasification/steam reforming of pyrolysis oil was studied in a staged reactor concept, which consisted of an inert fluidized bed and a catalytic fixed bed. Methane and C2−C3 free syngas is produced at a single temperature around 800 °C at atmospheric pressure. By lowering the temperature of the fluidized bed (432−500 °C), its function is changed from a gasifier to an evaporator, and in this way the subsequent catalyst bed actually sees vaporized pyrolysis oil compounds (instead of a fuel gas), which it can more readily convert to syngas. However, the temperature of the fixed bed cannot be too low (min 700 °C) to avoid excessive carbon deposition. System calculations show that when pressurized (30 bar) pyrolysis oil gasification/reforming is considered, the catalytic exit bed temperature should be high (900−1000 °C) to reach sufficient enough methane conversion when syngas is the desired product. When only steam is added at elevated pressure, the H2/CO ratio readily increases, which is desired for hydrogen production. For other applications (e.g., Fischer−Tropsch), carbon dioxide probably has to be recycled to keep the H2/CO ratio around 2−3. The lower heating value efficiency of pyrolysis oil gasification/reforming is comparable to the lower end of the reported range of commercial methane steam reforming.