下吸式固定床气化炉的气化过程及气化特性模拟分析

doi:10.3969/j.issn.1673-5854.2021.02.002

Abstract

Abstract:

In order to study the effect of the multiphase reaction flow field on the gasification process in downdraft fixed-bed gasifier, based on Fluent software, Euler Langrange model was established to track the movement of straw particles. P1 model was used to simulate the radiation heat transfer process of gasification process. At the same time, the gasification characteristics of straw downdraft gasifier were analyzed by coupling chemical reactions.The results showed that when the fuel coefficient was 0.26 and the particle size of straw was 13 mm, the volatiles of straw begin to react with the gastifier at the distance of 4.85 m from the bottom outlet of the burner. The flame temperature at the center of the gasifier increased, and then decreased with the depletion of volatiles. When the particle size of straw particles increased from 10 mm to 30 mm, the flammable gas content gradually decreased, but the content gap was not large.When the particle size of straw reached 40 mm, the temperature in gasifier dropped rapidly, then the serious phenomenon of incomplete dry volatilization would happen.

Key words: coupling reaction, fixed bed, flow field analysis, gasification characteristics

CLC Number:

TQ35

Xiangwen CHENG, Lizhi LIU, Rong WEI. Analysis of Gasification Process and Gasification Characteristics of Downdraft Fixed Bed Gasifier[J]. Biomass Chemical Engineering, 2021, 55(2): 9-15.

Figures/Tables 10

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References 15

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均相反应式 homogeneous reaction formula	反应速率表达式 expression of reaction rate
CO+0.5O₂→CO₂	$R_{1}=2.239 \times 10^{12} \exp \left(-\frac{1.674 \times 10^{8}}{R T_{\mathrm{g}}}\right) C(\mathrm{CO}) C\left(\mathrm{O}_{2}\right)^{0.25}$
H₂+0.5O₂→H₂O	$R_{2}=6.8 \times 10^{5} \exp \left(-\frac{1.67 \times 10^{8}}{R T_{\mathrm{g}}}\right) C\left(\mathrm{H}_{2}\right)^{0.25} C\left(\mathrm{O}_{2}\right)^{1.5}$
CO+2H₂O→2H₂+CO₂	$R_{3}=2.34 \times 10^{10} \exp \left(-\frac{2.883 \times 10^{8}}{R T_{\mathrm{g}}}\right) C(\mathrm{CO})^{0.5} C\left(\mathrm{H}_{2} \mathrm{O}\right)$
CH₄+2O₂→CO₂+2H₂O	$R_{4}=4.4 \times 10^{11} \exp \left(-\frac{1.25 \times 10^{8}}{R T_{\mathrm{g}}}\right) C\left(\mathrm{CH}_{4}\right)^{0.5} C\left(\mathrm{O}_{2}\right)^{1.25}$
CH₄+H₂O→CO+3H₂	$R_{5}=8.0 \times 10^{7} \exp \left(-\frac{2.51 \times 10^{8}}{R T_{\mathrm{g}}}\right) C(\mathrm{CO}) C\left(\mathrm{H}_{2}\right)$

反应式 reaction equation	指前因子(A) pre-exponential factor	活化能(E)/(J·mol^-1) activation energy
C+O₂→CO₂	267	1.26×10⁸
C+CO₂→2CO	2100	2.6×10⁸
C+H₂O→ CO+H₂	36	1.54×10⁸

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Analysis of Gasification Process and Gasification Characteristics of Downdraft Fixed Bed Gasifier

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