化工进展 ›› 2024, Vol. 43 ›› Issue (7): 3593-3612.DOI: 10.16085/j.issn.1000-6613.2024-0037
• 专栏:热化学反应工程技术 • 上一篇
丁路1,2(), 王培尧1,2(), 孔令学3(), 白进3, 于广锁1,2, 李文3, 王辅臣1,2
收稿日期:
2023-01-05
修回日期:
2024-04-07
出版日期:
2024-07-10
发布日期:
2024-08-14
通讯作者:
丁路,孔令学
作者简介:
丁路(1987—),男,教授,博士生导师,研究方向为含碳物料气化。E-mail:dinglu@ecust.edu.cn基金资助:
DING Lu1,2(), WANG Peiyao1,2(), KONG Lingxue3(), BAI Jin3, YU Guangsuo1,2, LI Wen3, WANG Fuchen1,2
Received:
2023-01-05
Revised:
2024-04-07
Online:
2024-07-10
Published:
2024-08-14
Contact:
DING Lu, KONG Lingxue
摘要:
煤炭是我国能源安全的压舱石,煤气化作为煤炭清洁高效利用的核心技术对实现“碳达峰、碳中和”的战略目标具有重要作用。基于动态原位表征揭示煤气化反应机理并建立煤气化模型,对拓展煤炭和生物质等含碳物料作为气化原料的适用性,开发新型高效的气化技术有重要的理论指导价值。同时,煤灰的流动性质是影响气化炉长周期稳定运行的关键指标。本文详细综述了煤气化过程的动力学模型、热力学模型、床层模型以及煤灰流动性的预测模型,对比了各类模型的优缺点、适用的条件以及描述气化过程的性能,指出了不同方法建立的模型存在的问题,为气化过程的总包反应模型建立提供了理论指导,并针对煤气化过程反应模型未来的研究重点进行了展望。
中图分类号:
丁路, 王培尧, 孔令学, 白进, 于广锁, 李文, 王辅臣. 煤气化过程反应模型研究进展[J]. 化工进展, 2024, 43(7): 3593-3612.
DING Lu, WANG Peiyao, KONG Lingxue, BAI Jin, YU Guangsuo, LI Wen, WANG Fuchen. Progress on reaction models for coal gasification processes[J]. Chemical Industry and Engineering Progress, 2024, 43(7): 3593-3612.
优点 | 缺点 |
---|---|
不需考虑气化炉形状 | 无论何种气化炉在低工作温度下都无法获得热力学平衡 |
不需要了解转换机制 | 结果不精确 |
设置操作条件不受限制 | 难以解释炭化和焦油的形成 |
可提供最大的反应物转化率和最大的产物收率 | 忽视了CO2和CH4的产生 |
可便捷地进行灵敏度分析 | 高估了H2、CO的产品收率 |
相对容易实现 | 气化炉的几何形状和设计未在模型中考虑 |
动力学模型与之相较计算更加密集 | 无法准确估计焦油含量 |
可以获得最佳条件 | 不考虑出口流中的焦油、焦炭和CH4 |
表1 热力学平衡模型优缺点
优点 | 缺点 |
---|---|
不需考虑气化炉形状 | 无论何种气化炉在低工作温度下都无法获得热力学平衡 |
不需要了解转换机制 | 结果不精确 |
设置操作条件不受限制 | 难以解释炭化和焦油的形成 |
可提供最大的反应物转化率和最大的产物收率 | 忽视了CO2和CH4的产生 |
可便捷地进行灵敏度分析 | 高估了H2、CO的产品收率 |
相对容易实现 | 气化炉的几何形状和设计未在模型中考虑 |
动力学模型与之相较计算更加密集 | 无法准确估计焦油含量 |
可以获得最佳条件 | 不考虑出口流中的焦油、焦炭和CH4 |
作者 | 年份 | 定义 |
---|---|---|
Reid和Cohen | 1944 | 降温过程中全液相流体变为塑性流体对应的温度 |
Corey | 1964 | 全流体与塑性流体的分界温度,也是降温过程中首次出现屈服应力的温度 |
Watt和Fereday | 1969 | 结晶相与流体开始发生相互作用时的温度 |
Winegartner | 1974 | 熔渣由牛顿流体变为假塑性流体的温度 |
Singer(editor) | 1991 | 固相开始结晶和从液相中析出的温度 |
Nowok和Benson | 1991 | 熔体的流动性由牛顿流体变为非牛顿流体特性的温度 |
Nowok等 | 1993 | 熔渣由均相变为多相混合时的温度 |
Mills和Broadbent | 1994 | 黏度快速上升时对应的温度 |
Seggiani | 1999 | 熔渣由牛顿流体变为假塑性流体的温度 |
Vargas等 | 2001 | 晶体开始影响熔渣黏度的温度 |
Stultz和Kitto | 2005 | 黏度的对数与温度不为线性的温度 |
Spliethoff | 2010 | 黏度达到250P的温度 |
Massoudi和Wang | 2011 | 熔渣由牛顿流体变为非牛顿流体的温度 |
表2 临界黏度温度的定义
作者 | 年份 | 定义 |
---|---|---|
Reid和Cohen | 1944 | 降温过程中全液相流体变为塑性流体对应的温度 |
Corey | 1964 | 全流体与塑性流体的分界温度,也是降温过程中首次出现屈服应力的温度 |
Watt和Fereday | 1969 | 结晶相与流体开始发生相互作用时的温度 |
Winegartner | 1974 | 熔渣由牛顿流体变为假塑性流体的温度 |
Singer(editor) | 1991 | 固相开始结晶和从液相中析出的温度 |
Nowok和Benson | 1991 | 熔体的流动性由牛顿流体变为非牛顿流体特性的温度 |
Nowok等 | 1993 | 熔渣由均相变为多相混合时的温度 |
Mills和Broadbent | 1994 | 黏度快速上升时对应的温度 |
Seggiani | 1999 | 熔渣由牛顿流体变为假塑性流体的温度 |
Vargas等 | 2001 | 晶体开始影响熔渣黏度的温度 |
Stultz和Kitto | 2005 | 黏度的对数与温度不为线性的温度 |
Spliethoff | 2010 | 黏度达到250P的温度 |
Massoudi和Wang | 2011 | 熔渣由牛顿流体变为非牛顿流体的温度 |
作者 | 年份 | 公式 |
---|---|---|
Reid | 1944 | TCV=TS |
Sage | 1960 | TCV=HT+111K |
Watt | 1963 | TCV=3263-1470×(SiO2/Al2O3)+360×(SiO2 /Al2O3)2-14.7×(Fe2O3+CaO+MgO)+0.15×( Fe2O3+CaO+MgO)2 |
Corey | 1964 | TCV=ST |
Marshak | 1969 | TCV=0.75×HT+548K |
Song | 2011 | TCV=118+0.894Tliq |
Kong | 2013 | TCV=0.98Tmax +17.33 |
Hsieh | 2016 | TCV=FT,TCV=1900-148.3×(SiO2/Al2O3)-8.04×(Fe2O3+1.1FeO+1.43Fe) |
Ge | 2020 |
表3 临界黏度温度预测公式
作者 | 年份 | 公式 |
---|---|---|
Reid | 1944 | TCV=TS |
Sage | 1960 | TCV=HT+111K |
Watt | 1963 | TCV=3263-1470×(SiO2/Al2O3)+360×(SiO2 /Al2O3)2-14.7×(Fe2O3+CaO+MgO)+0.15×( Fe2O3+CaO+MgO)2 |
Corey | 1964 | TCV=ST |
Marshak | 1969 | TCV=0.75×HT+548K |
Song | 2011 | TCV=118+0.894Tliq |
Kong | 2013 | TCV=0.98Tmax +17.33 |
Hsieh | 2016 | TCV=FT,TCV=1900-148.3×(SiO2/Al2O3)-8.04×(Fe2O3+1.1FeO+1.43Fe) |
Ge | 2020 |
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