Investigation progress on the synergy between coal and biomass during co-gasification
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摘要: 煤与生物质共气化作为实现这两种含碳资源高效清洁利用的重要技术路径,对于实现“碳中和”、“碳达峰”有着积极促进的作用。共气化不仅有助于克服煤单独气化衍生的系列问题,减少SOx、NOx等有害物质的排放,提高煤反应活性,也有利于克服生物质单独气化存在的能量密度低、气化效率差、焦油产率高等问题。基于此,文章从共气化过程的影响因素、协同反应机制等方面出发,总结了原料类型及预处理方法、工艺参数和气化炉类型对共气化过程的影响,阐述了共气化过程中的催化协同机理,简要概述了共气化过程中非催化因素的协同机理,讨论了研究共气化过程的新方法。文章对煤与生物质共气化研究近年重点关注的方向进行了梳理,对借助现代原位表征技术构建完整协同反应路径、结合密度泛函理论计算及理论建模解析共气化过程多反应耦合作用机制做出了展望。Abstract: Co-gasification of coal and biomass, as one of the means to achieve efficient and clean utilization of coal, has a positive contribution to achieving carbon neutrality and carbon peaking. Co-gasification not only helps to overcome a series of problems derived from coal gasification alone, reduces the emission of SOx, NOx and other harmful substances, and improves coal reactivity but also helps to overcome the problems of low energy density, poor gasification efficiency and high tar yield existing in biomass gasification alone. Based on this, the progress in the research of influencing factors and synergetic reaction mechanism is reviewed in this work. The effects of feedstock type and pretreatment method, process parameters and gasifier type on the co-gasification process are summarized, the catalytic synergistic mechanism in the co-gasification process of coal and biomass is systematically described, the synergistic mechanism of non-catalytic factors in the co-gasification process is briefly outlined, and new methods to study the co-gasification process are comprehensively discussed. The main concern of the co-gasification process is sorted out, and prospects are made for constructing the synergistic pathway with the help of the new in situ technique and revealing the reaction mechanism in coupling the chemical reaction system with the combination of density functional theory and gasification dynamics models.
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Key words:
- coal /
- biomass /
- co-gasification /
- synergistic effect /
- gasifier
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表 1 气化反应器的特性与性能
Table 1 Characteristics and performance of gasification reactors
Gasifier type Operation conditions Material type Gasification agent type Temp. /℃ Cold gas efficiency [a]/% Carbon conversion rate[b]/% Tar content /
(g·m−3)Ref. Updraft fixed
bed gasifiermaterial
mixing ratio 7∶3palm kernel shell; bituminous coal air 800−900 45 46 − [32] Downdraft fixed bed gasifier material
mixing ratio 85∶15wood; indian coal air; steam 1000 65 94 − [33] fluidized bed gasifier − lignite; wood; plastic air; steam 850 <50 − 48 (ER= 0.2),
21 (ER = 0.3)[34] Dual fluidized bed gasifier material
mixing ratio 1∶1coal; wood steam 900 60 80 2.9 [35] [a] Ratio of the chemical energy of gasification to produce gas to the chemical energy of the feedstock used for gasification;[b] Carbon in feedstock generation gas as a percentage of carbon in feedstock 表 2 协同效应的量化指标
Table 2 Quantitative indicators of synergy effects
Reference Expression Parameter interpretation Wei et al.[49] $ {D}\left({{R}}_{0.5}\right)=\dfrac{{{R}}_{0.5,\mathrm{e}\mathrm{x}\mathrm{p}}-{{R}}_{0.5,\mathrm{c}\mathrm{a}\mathrm{l}}}{{R}_{0.5,{\rm{cal}}}}\times 100\mathrm{\%} $ ${{R} }_{0.5,\mathrm{e}\mathrm{x}\mathrm{p} }$ and $ {{R}}_{0.5,\mathrm{c}\mathrm{a}\mathrm{l}} $ are the overall gasification reactivity of the mixture material experimentally and theoretically calculated, and denote the calculated and experimental times required for co-gasification conversion at a gasification conversion rate of X Chen et al.[50] $ {{A}}_{\mathrm{X},\mathrm{T}}=\dfrac{{t}_{X,T,{\rm{cal}}}}{{t}_{X,T,{\rm{exp}}}} $ $ {t}_{X,T,{\rm{cal}}} $ and $ {t}_{X,T,{\rm{exp}}} $ denote the calculated and experimental time required for
co-gasification conversion at gasification conversion of XWei et al.[51] $ \mathrm{S}\mathrm{F}=\dfrac{{R}_{0.9,{\rm{exp}}}}{{R}_{0.9,{\rm{cal}}}} $ $ {R}_{0.9,{\rm{exp}}} $ and $ {R}_{0.9,{\rm{cal}}} $ are the experimental and theoretically calculated overall gasification reactions of pyrolytic mixed coke alone Jeong et al.[52] $ \mathrm{S}\mathrm{F}={{k}}_{\mathrm{e}\mathrm{x}\mathrm{p}}-{{k}}_{\mathrm{c}\mathrm{a}\mathrm{l}} $ $ {{k}}_{\mathrm{e}\mathrm{x}\mathrm{p}} $ and $ {{k}}_{\mathrm{c}\mathrm{a}\mathrm{l}} $ are the initial gasification reaction rates of co-pyrolysis coke and the theoretically calculated initial gasification reaction rates of individually pyrolyzed mixed coke Wang et al.[53] $ \mathrm{S}\mathrm{F}=\dfrac{{X}_{{\rm{exp}}}}{{X}_{{\rm{cal}}}} $ $ {X}_{{\rm{exp}}} $ and $ {X}_{{\rm{cal}}} $ are the experimental and theoretical calculated conversions for the same gasification time of pyrolysis mixed coke alone He et al.[54] $ \mathrm{S}\mathrm{F}=\dfrac{{t}_{X,{\rm{pre}}}}{{t}_{X,{\rm{exp}}}} $ $ {t}_{X,{\rm{pre}}} $ and $ {t}_{X,{\rm{exp}}} $ are the time required for theoretical calculation and co-pyrolysis coke conversion at X for separate pyrolysis mixture conversion and X for co-pyrolysis coke conversion Zhang et al.[55] $ \mathrm{S}\mathrm{F}=\dfrac{{{t}_{{\rm{se}}}}^{X=0.95}}{{{t}_{{\rm{bl}}}}^{X=0.95}} $ $ {{t}_{{\rm{se}}}}^{X=0.95} $ and $ {{t}_{{\rm{bl}}}}^{X=0.95} $ are the time required when the gasification
conversion of separated coke and co-pyrolysis coke is 0.95表 3 不同原料的灰分组成
Table 3 Analysis of ash composition of different raw materials
Raw material Content w/% K2O Na2O MgO CaO Fe2O3 TiO2 Al2O3 SiO2 P2O5 SO3 Peanut shell 14.80 1.70 4.30 6.80 3.10 0.60 8.60 48.60 5.50 3.60 Rice straw 17.81 0.96 2.33 7.68 0.84 0.04 0.91 51.99 2.49 6.50 Corn straw 25.14 0.68 3.55 6.48 0.59 0.03 1.75 40.97 5.81 3.74 Wood chip 7.76 12.84 5.56 24.89 4.57 0.58 6.50 16.47 2.42 7.64 Lignite coal 1.71 1.04 1.44 4.33 2.67 0.50 14.73 65.79 0.97 6.67 Subbituminous coal 0.80 2.60 1.30 5.60 2.80 0.50 23.60 57.60 0.10 2.30 Bituminous coal 1.52 0.74 0.94 3.56 3.66 1.01 28.72 57.3 0.19 2.32 Meagre coal 1.56 2.97 0.88 4.07 3.22 1.82 28.44 53.99 0.97 4.33 Raw material Mass
fraction of
K /%Mass fraction of K in
different compounds /%H2O soluble NH4Ac soluble acid soluble insoluble matter Wood 0.369 94.00 4.50 0.40 1.00 Straw 0.238 92.80 3.20 2.00 2.00 Rice stalk − 93.70 2.90 0.60 2.80 Lignite coal 0.028 46.50 12.90 12.90 27.70 Anthracite − 6.72 6.55 8.04 78.69 -
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