微型流化床中焦油热裂解和水蒸气重整的反应特性及动力学对比

doi:10.11949/0438-1157.20211244

化工学报 ›› 2022, Vol. 73 ›› Issue (1): 362-375.DOI: 10.11949/0438-1157.20211244

微型流化床中焦油热裂解和水蒸气重整的反应特性及动力学对比

武鹏^1,³(),王芳^2,³(),曾玺^2,³,战洪仁¹,岳君容³,王婷婷³,许光文^1,³

^1.沈阳化工大学机械与动力工程学院，辽宁沈阳 110142
^2.北京工商大学生态环境学院，北京 100048
^3.中国科学院过程工程研究所多相复杂系统国家重点实验室，北京 100190

收稿日期:2021-08-27 修回日期:2021-10-19 出版日期:2022-01-05 发布日期:2022-01-18
通讯作者: 王芳
作者简介:武鹏(1995—)，男，硕士研究生，peng_w123@163.com
基金资助:
国家重点研发计划项目(2018YFF01011400);国家自然科学基金项目(21808227)

Comparison of reaction characteristics and kinetics between tar thermal cracking and steam reforming in a micro fluidized bed reaction analyzer

Peng WU^1,³(),Fang WANG^2,³(),Xi ZENG^2,³,Hongren ZHAN¹,Junrong YUE³,Tingting WANG³,Guangwen XU^1,³

^1.School of Mechanical and Power Engineering, Shenyang University of Chemical Technology, Shenyang 110142, Liaoning, China
^2.School of Ecology and Environment, Beijing Technology and Business University, Beijing 100048, China
^3.State Key Laboratory of Multi-phase Complex Systems, Institute of Process Engineering, Chinese Academy of Sciences, Beijing 100190, China

Received:2021-08-27 Revised:2021-10-19 Online:2022-01-05 Published:2022-01-18
Contact: Fang WANG

摘要/Abstract

摘要：

采用微型流化床反应分析仪(MFBRA)考察了不同温度(T，750~950℃)和水蒸气分压(SP，10%~30%)下生物质焦油水蒸气重整过程中的气体生成、气体产物中总碳转化和焦油转化等反应特性，求算反应动力学，并与焦油热裂解特性进行比较。在热裂解过程中，随温度增加，各气体(H₂、CH₄、CO、CO₂)产率和气体产物中的总碳转化率增加，反应时间缩短。而在焦油水蒸气重整过程中，等温下的反应时间明显延长，且H₂、CH₄、CO产率和气体产物中的总碳转化率显著提升，而CO₂产率在850℃时有最大值。在焦油水蒸气重整过程中，不仅有焦油裂解，还有裂解产物与水蒸气的反应，促进碳转化。在950℃、SP=30%条件下，气体产物中的总碳转化率达到92.34%。水蒸气作用下，气体组分的产率和气体产物中的总碳转化率增加，而等温条件下的反应速率下降。水蒸气分压对各气体组分的影响具有差异性。随分压增加，CO、CH₄的生成速率和气体产物中的总碳转化的反应速率增加；H₂生成速率逐渐下降，速率稳定段扩大；CO₂生成速率在850℃时有最大值。采用均相模型求取焦油水蒸气重整反应过程中的活化能，气体产物的生成活化能(H₂、CO、CO₂和CH₄)、气体产物中的总碳转化及焦油转化的活化能明显偏低，分别为90.10、42.01、58.56、64.92、61.44和63.26 kJ/mol，对应数值明显小于焦油热裂解，说明水蒸气对焦油重整反应的促进作用。最后，将焦油热裂解动力学数据与文献数据对比，验证了MFBRA对焦油水蒸气重整反应测试的可行性和分析结果的准确性。

关键词: 生物质, 焦油, 热裂解, 水蒸气重整, 微型流化床

Abstract:

In this study, a micro fluidized bed reaction analyzer (MFBRA) was used to examine the reaction characteristics of tar steam reforming and thermal cracking in the temperature range of 750—950℃ and steam partial pressure (SP) of 10%—30%. The production of gaseous products and the conversion of total carbon in the gaseous products and the conversion of tar were completely analyzed. The reaction kinetics was also calculated. The results show that during tar thermal cracking, with the increase of reaction temperature, the yields of H₂, CH₄, CO and CO₂ and the conversion of total carbon in the gaseous products increased, and the reaction time decreased. However, in the process of tar steam reforming, by raising the reaction temperature, the reaction time was prolonged largely, and the yields of H₂, CH₄, CO and the conversion of total carbon in the gaseous products increased significantly, while that of CO₂ reached the maximum value at 850℃. During this process, it included not only tar thermal cracking but also the reforming reaction between tar components and the reaction intermediates. At 950℃ and SP of 30%, the conversion of total carbon in the gaseous products reached 92.34%. For the tar steam reforming, with the increase of SP, although the yields of gas components and the conversion of total carbon in the gaseous products increased, the corresponding reaction rate decreased. At the same reaction temperature, with the increase of SP, the generation rates of CO, CH₄ and the rate of total carbon conversion in the gaseous products increased, the H₂ reaction rate gradually decreased with a long stable zone, while the CO₂reaction rate reached its maximum value at 850℃. The activation energy (E_a) of the gaseous products (H₂, CO, CO₂ and CH₄), the conversion of total carbon in the gaseous products and the tar conversion were 90.10, 42.01, 58.56, 64.92, 61.44 and 63.26 kJ/mol, respectively. The corresponding values were obviously less than that of tar thermal cracking. It indicated the promotion effect of steam on tar conversion. Finally, the tar thermal cracking kinetics data was compared with the literature data to verify the feasibility of the MFBRA tar steam reforming reaction test and the accuracy of the analysis results.

Key words: biomass, tar, thermal cracking, steam reforming, micro fluidized bed

中图分类号:

TQ 522.64

武鹏, 王芳, 曾玺, 战洪仁, 岳君容, 王婷婷, 许光文. 微型流化床中焦油热裂解和水蒸气重整的反应特性及动力学对比[J]. 化工学报, 2022, 73(1): 362-375.

Peng WU, Fang WANG, Xi ZENG, Hongren ZHAN, Junrong YUE, Tingting WANG, Guangwen XU. Comparison of reaction characteristics and kinetics between tar thermal cracking and steam reforming in a micro fluidized bed reaction analyzer[J]. CIESC Journal, 2022, 73(1): 362-375.

图/表 15

图1 焦油水蒸气重整反应路径

Fig.1 Simplified reaction diagram of tar steam reforming

表1 焦油水蒸气重整过程中涉及到的化学反应

Table 1 Reactions involved in the tar steam reforming process

序号	反应方程式	反应类型
R1	tar $→$ char + gas + tar	热裂解反应
R2	C_nH_m + n H₂O $? ????????????$ n CO + (n + m/2) H₂	重整反应
R3	C_nH_x + CO₂ $→$ H₂ + CO	干重整反应
R4	CO + H₂O $?$ CO₂ + H₂	水煤气变换反应
R5	C_nH_x $? ????????????$ n C + (x/2) H₂	积炭反应
R6	C + H₂O $?$ CO + H₂	炭气化反应
R7	C + CO₂ $?$ 2CO	二氧化碳还原反应
R8	CH₄ + H₂O $?$ CO + 3H₂	甲烷蒸气重整

表1 焦油水蒸气重整过程中涉及到的化学反应

Table 1 Reactions involved in the tar steam reforming process

序号	反应方程式	反应类型
R1	tar $→$ char + gas + tar	热裂解反应
R2	C_nH_m + n H₂O $? ????????????$ n CO + (n + m/2) H₂	重整反应
R3	C_nH_x + CO₂ $→$ H₂ + CO	干重整反应
R4	CO + H₂O $?$ CO₂ + H₂	水煤气变换反应
R5	C_nH_x $? ????????????$ n C + (x/2) H₂	积炭反应
R6	C + H₂O $?$ CO + H₂	炭气化反应
R7	C + CO₂ $?$ 2CO	二氧化碳还原反应
R8	CH₄ + H₂O $?$ CO + 3H₂	甲烷蒸气重整

图2 实验装置原理图(a)和微型流化床反应器结构图(b)

Fig.2 Schematic diagram of experimental device (a) and structure of micro-fluidized bed reactor (b)

图3 焦油水蒸气重整反应的数据处理方法

Fig.3 Data treating approch of tar reforming in steam

图4 焦油热裂解(a)和水蒸气重整[(b)~(d)]过程中H2产率变化

Fig.4 Variation of H2 yield in tar thermal cracking (a) and steam reforming [(b)—(d)]

图5 焦油热裂解(a)和水蒸气重整[(b)~(d)]过程中CO产率变化

Fig.5 Variation of CO yield in tar thermal cracking (a) and steam reforming [(b)—(d)]

图6 焦油热裂解(a)和水蒸气重整(b)~(d)过程中CO2产率变化

Fig.6 Variation of CO2 yield in tar thermal cracking (a) and steam reforming [(b)—(d)]

图7 焦油热裂解(a)和水蒸气重整(b)~(d)过程中CH4产率变化

Fig.7 Variation of CH4 yield in tar thermal cracking (a) and steam reforming [(b)—(d)]

图8 焦油热裂解(a)和水蒸气重整[(b)~(d)]过程中气体产物中的总碳转化率变化

Fig.8 Variation of carbon conversion in the gaseous products during tar thermal cracking (a) and steam reforming [(b)—(d)]

图9 不同条件下气体产率及气体产物中碳转化率与反应速率之间的关系

Fig.9 Relationship of reaction rate vs. gas generation yield and carbon conversion at different conditions

图10 不同水蒸气分压下气体产率/气体产物中碳转化率与反应速率曲线的变化

Fig.10 Variation of reaction rate vs. gas yield or carbon conversion at different SP

图11 不同温度下各气体和气体产物中总碳转化的均相模型数据拟合

Fig.11 Fitting of homogeneous model data of gas generation and total carbon conversion in gaseous products at different temperatures

图12 不同水蒸气分压下速率常数与温度倒数的线性拟合

Fig.12 Linear fitting of rate constant vs. 1/T at different SP

表2 焦油热裂解和水蒸气重整的反应动力学数据

Table 2 Reaction kinetics data of tar thermal cracking and steam reforming

气体	水蒸气分压	E_a/(kJ/mol)	A/s^-1	R²
H₂	Ar	117.05	427.32	0.993
	SP=10%	86.40	13.14	0.997
	SP=20%	89.40	17.44	0.996
	SP=30%	94.49	26.87	0.999
	average (10%—30%)	90.10	19.15	0.997
CO	Ar	45.28	23.60	0.987
	SP=10%	44.87	12.39	0.999
	SP=20%	39.67	6.25	0.989
	SP=30%	41.49	7.11	0.995
	average (10%—30%)	42.01	8.58	0.994
CO₂	Ar	62.24	94.66	0.982
	SP=10%	56.33	10.79	0.991
	SP=20%	59.45	17.79	0.999
	SP=30%	59.91	11.92	0.990
	average (10%—30%)	58.56	13.50	0.993
CH₄	Ar	62.55	46.89	0.995
	SP=10%	62.90	24.12	0987
	SP=20%	67.51	37.77	0.993
	SP=30%	64.36	26.36	0.999
	average (10%—30%)	64.92	29.42	0.993
C	Ar	69.64	725.83	0.998
	SP=10%	62.51	101.79	0.998
	SP=20%	60.55	125.24	0.989
	SP=30%	61.26	78.63	0.991
	average (10%—30%)	61.44	101.87	0.996
Total	Ar	71.14	706.32	0.992
	SP=10%	63.55	105.14	0.993
	SP=20%	62.81	163.92	0.988
	SP=30%	63.42	99.67	0.999
	average (10%—30%)	63.26	122.91	0.993

表3 焦油热裂解活化能与文献数据对比

Table 3 Comparison of Ea between tar thermal cracking in this study and literatures

产物	仪器	原料	T/K	E_a/(kJ/mol)	文献
total	MFB	biomass tar	1023—1223	69.64	this study
	MFB	biomass tar	1023—1223	78.2	[38]
	fixed bed	biomass tar	773—1073	70.5	[39]
	TGA	biomass tar	1223	79.6	[40]
	fixed bed	biomass tar	773—1373	76.6	[41]
H₂	MFB	biomass tar	1023—1223	117.05	this study
	fixed bed	biomass tar	773—1073	129	[42]
CO	MFB	biomass tar	1023—1223	45.28	this study
	MFB	model compound	1023—1223	53.35	[43]
CH₄	MFB	biomass tar	1023—1223	62.55	this study
	MFB	biomass tar	1023—1223	63.19	[38]

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微型流化床中焦油热裂解和水蒸气重整的反应特性及动力学对比

Comparison of reaction characteristics and kinetics between tar thermal cracking and steam reforming in a micro fluidized bed reaction analyzer

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