灰熔聚气化炉内气体与固体混合特性的研究

气化炉内的气化剂与煤粉的混合特性直接影响着气化炉内的碳转化率和灰熔聚流化床气化炉的热效率。研究气化炉内气体和固体颗粒的混合特性,掌握炉内气体和固体颗粒的轴向和径向的运动规律,对认识床内传热和传质机理具有重要的意义。基于欧拉双流体模型,结合颗粒动力学理论,应用商用FLUENT软件,对太原化学工业集团有限公司运行的灰熔聚流化床气化炉内的气体与固体的混合特性进行了数值模拟。     

基于FLUENT的粉浆配比对气化性能的影响

以单喷嘴粉浆气化炉为研究对象,深入了解了气化反应机理,基于FLuent软件分别建立了气化炉的热力学模型和动力学模型;对气化炉内粉浆气化过程进行了数值模拟,详细分析了投煤量为1 500 t/d的单喷嘴粉浆气化炉采用不同粉浆配比时对气化炉性能的影响;结果表明:在氧煤比一致的条件下,随着粉浆配比的增加,气化炉温度升高,有效气组分和产量随之增加,碳转化率略有提升。     

GSP气化炉内多相湍流反应流动模拟研究

采用涡耗散概念(EDC)模型,对某化工厂的GSP气化炉内多相反应流场进行了数值模拟研究.计算中采用Realizable k-ε湍流模型对雷诺平均后的N-S方程进行封闭;采用离散相随机轨道模型来模拟气化炉内煤颗粒的弥散运动;采用P1模型对燃烧的辐射传热进行模拟.计算结果表明:气化炉内为强旋射流流场,颗粒在气化炉顶部回流区...     

气流床气化炉的CPFD数值模拟

利用CPFD(computational particle fluid dynamics)模拟方法对三维、全尺寸的气流床气化炉进行了模拟计算,建立起了适用于CPFD模拟方法的气化模拟模型。模拟结果与实验数据相一致,说明模型基本准确且CPFD模拟方法适用于气流床气化过程的模拟。借由CPFD模拟方法给出了颗粒相在气化炉中的具体反应历程及颗粒停留时间的概率分布;结果表明,在单喷嘴顶喷的气化炉中,同时存在颗粒相的轴向流动短路及返混,短路主要发生在炉中心区域;颗粒在炉中心区域反应剧烈而边壁区域反应则很缓慢,而且从气化炉流出的第一股短路颗粒主要由充分反应了的粉煤颗粒构成。     

下吸式固定床气化炉的气化过程及气化特性模拟分析

为研究下吸式固定床气化炉内多相反应流场对气化过程的影响,基于Fluent软件,建立欧拉-拉格朗日模型追踪秸秆颗粒运动,P1模型模拟气化过程的辐射传热过程,同时耦合化学反应,对下吸式秸秆气化炉气化特性进行了分析.结果表明:燃料系数0.26,秸秆颗粒粒径13 mm,在距离燃烧器底部出口 4.85 m处,秸秆挥发分开始与气化...     

气流床气化炉的CPFD数值模拟

利用CPFD (computational particle fluid dynamics)模拟方法对三维、全尺寸的气流床气化炉进行了模拟计算,建立起了适用于CPFD模拟方法的气化模拟模型。模拟结果与实验数据相一致,说明模型基本准确且CPFD模拟方法适用于气流床气化过程的模拟。借由CPFD模拟方法给出了颗粒相在气化炉中的具体反应历程及颗粒停留时间的概率分布;结果表明,在单喷嘴顶喷的气化炉中,同时存在颗粒相的轴向流动短路及返混,短路主要发生在炉中心区域;颗粒在炉中心区域反应剧烈而边壁区域反应则很缓慢,而且从气化炉流出的第一股短路颗粒主要由充分反应了的粉煤颗粒构成。     

气流床气化炉综合模型及颗粒粒径对气化结果的影响研究

采用颗粒停留时间分布表征炉内颗粒流动,建立了一种考虑了炉体结构、颗粒粒径以及煤焦反应动力学的气流床气化炉综合模型,其中包含了煤脱挥发份、均相反应、非均相反应、气-固相能量方程、相间传热等子模型。模拟结果与多喷嘴对置式水煤浆气化炉工业运行数据吻合良好,考察了气相组分、温度以及不同粒径颗粒的碳转化率和温度在炉内的一维无因次分布。对模拟结果的分析表明:煤颗粒的预热、脱挥发份和燃烧过程在约30 ms内完成,气化过程占颗粒反应历程的绝大部分;气化炉内100μm以下的小颗粒升温速率快,且温度较高,碳转化率基本接近100%;而200μm以上的大颗粒升温速率较慢,碳转化率较低,影响了气化炉整体碳转化率。     

水煤浆气化炉的形式和新型气化炉的开发

对目前世界上3种主要的气化炉--德士古(Texaco)水煤浆气化炉、道(Dow)水煤浆气化炉和多喷嘴对置式水煤浆气化炉,从工艺流程到气化炉内流场结构都进行了比较说明,同时分析了各种气化炉的优缺点,在此基础上,结合各种气化炉的优点,自行开发设计了一种新型水煤浆气化炉.后期的冷态和热态数值模拟计算以及实验测试结果表明,该气化炉具有流场分布合理、颗粒平均停留时间长、出口粗煤气有效气成分高等优点.     

气固颗粒系统模拟的研究进展

综述了气固颗粒系统模拟方法的发展状况。首先,从宏观、中观及直接数值模拟角度对基于欧拉-欧拉架构下的双流体模型、拉格朗日-欧拉架构下的离散气泡模型以及欧拉-拉格朗日架构下的计算流体力学和离散单元法耦合模型(CFD-DEM)及直接数值模拟方法就模型基本原理、计算量、预测精度以及应用前景等方面进行对比和分析。接着,针对工程应用前景较强的双流体模型和CFD-DEM模型进行了详细阐述,着重强调了欧拉架构下的模型植入过程,颗粒相的动力学过程和微观行为描述、两相耦合作用及相间耦合模型描述。基于欧拉-拉格朗日架构下的多相耦合模型的普适性,模型的应用已经从研究尺度的模拟逐渐走向工程尺度的模拟,成为今后研究多相颗粒系统的热点。     

典型气流床煤气化炉气化过程的建模

利用Aspen Plus、基于热力学平衡模型对GSP煤粉气化炉、GE水煤浆气化炉及四喷嘴对置式水煤浆气化炉的气化过程建模。根据煤颗粒热转化的历程,将煤气化过程划分为热解、挥发分燃烧、半焦裂解及气化反应4个阶段,利用David Merrick模型计算热解过程,采用Beath模型校正压力对热解过程的影响,选用化学计量反应器模拟挥发分燃烧反应,编制Fortran程序计算半焦裂解产物收率,最后基于Gibbs自由能最小化方法计算气化反应。结果表明,采用建立的气流床气化过程模型模拟工业气化过程的结果与生产数据基本吻合,对GSP煤粉气化炉、GE水煤浆气化炉及四喷嘴对置式水煤浆气化炉等3种气化炉有效气成分（CO+H₂）体积分数模拟结果的误差均不超过2%,建立模型的可靠性得到验证。     

Co‐gasification of woody biomass and sewage sludge in a fixed‐bed downdraft gasifier

Experimental and numerical studies of cogasification of woody biomass and sewage sludge have been carried out. The gasification experiments were performed in a fixed‐bed downdraft gasifier and the experimental results show that 20 wt % dried sewage sludge in the feedstock was effectively gasified to generate producer gas comprising over 30 vol % of syngas with an average lower heating value of 4.5 MJ/Nm³. Further increasing sewage sludge content to 33 wt % leads to the blockage of gasifier, which is resulted from the formation of agglomerated ash. The numerical models were then developed to simulate the reactions taking place in four different zones of the gasifier (i.e., drying, pyrolysis, combustion, and reduction zones) and to predict the producer gas composition and cold gas efficiency. The deviation between the numerical and experimental results obtained was lower than 10%. © 2015 American Institute of Chemical Engineers AIChE J, 61: 2508–2521, 2015     

A comparison of the energy and product distribution from biomass gasifiers

A detailed analyses of the raw producer gas streams generated by a downdraft gasifier and by a fluidized-bed gasifier are presented and are discussed in terms of raw gas clean-up considerations and of energy conversion efficiency. The major gasifier operating parameters such as fuel/air ratio, carbon conversion efficiency, net energy conversion efficiency, and producer gas heating value are then compared between seven operational gasifiers and a computer simulation model of a fluidized-bed gasifier developed by Queen's University. It is concluded that the Queen's University model correctly predicts that the fuel/air ratio is the single most important parameter for determining gasifier performance. Downdraft gasifiers exhibit superior energy conversion efficiency and producer gas quality because they utilize a higher fuel/air ratio than do fluidized bed gasifiers.     

EQUILIBRIUM MODELING OF A DOWNDRAFT GASIFIER I—OVERALL GASIFIER

A model, based on the thermodynamic equilibrium of the C-H-O-Inert system and mass and energy balances, has been applied to the air-blown downdraft gasification of wood. The model predicts the temperature, gas composition and char yield at the exit of the gasifier for a specified set of heat loss and input condition. A parametric study has been conducted to simulate the influences of the air/feed mass ratio and moisture/feed mass ratio on the gasifier's performance. The model predictions are compared with a comprehensive set of experimental data obtained from the gasification of wood in a commercial-scale downdraft gasifier; the air/feed ratios range from 1.1 to 2.1 and the moisture/feed ratios range from 0.05 to 0.3. The predicted trends for variations in the operating parameters are in general agreement with the experimental data. The results of comparisons also indicate that the performance of the wood gasifier can be approximated reasonably well by the equilibrium model.     

Effect of biomass particle size and air superficial velocity on the gasification process in a downdraft fixed bed gasifier. An experimental and modelling study

A one-dimensional stationary model of biomass gasification in a fixed bed downdraft gasifier is presented in this paper. The model is based on the mass and energy conservation equations and includes the energy exchange between solid and gaseous phases, and the heat transfer by radiation from the solid particles. Different gasification sub-processes are incorporated: biomass drying, pyrolysis, oxidation of char and volatile matter, chemical reduction of H₂, CO₂ and H₂O by char, and hydrocarbon reforming. The model was validated experimentally in a small-scale gasifier by comparing the experimental temperature fields, biomass burning rates and fuel/air equivalence ratios with predicted results. A good agreement between experimental and estimated results was achieved. The model can be used as a tool to study the influence of process parameters, such as biomass particle mean diameter, air flow velocity, gasifier geometry, composition and inlet temperature of the gasifying agent and biomass type, on the process propagation velocity (flame front velocity) and its efficiency. The maximum efficiency was obtained with the smaller particle size and lower air velocity. It was a consequence of the higher fuel/air ratio in the gasifier and so the production of a gas with a higher calorific value.     

生物质下吸式气化炉气化制备富氢燃气实验研究

以制取富氢燃气为目标,在自热式下吸式气化炉反应器内,进行了生物质下吸式气化炉富氧/水蒸气及空气气化的制氢特性研究。实验结果表明,与空气气化相比,富氧/水蒸气气化可显著提高氢产率和产气热值。在实验条件范围内,最大氢产率达到45.16 g/kg;最大低位热值达到11.11 MJ/m3。在富氧/水蒸气气化条件下,燃气中H2+CO体积分数达到63.27%—72.56%,高于空气气化条件下的52.19%—63.31%。富氧/水蒸气气化条件下的H2/CO体积比比值为0.70—0.90,低于空气气化条件下的1.06—1.27。实验结果证实:生物质下吸式气化炉富氧/水蒸气气化是一种有效的制取可再生氢源的工艺路线。     

Deactivation of a Ni-Based Reforming Catalyst During the Upgrading of the Producer Gas, from Simulated to Real Conditions

The deactivation of a nickel reforming catalyst during the upgrading of the producer gas obtained by gasification of lignocellulosic biomass was studied. The research involved several steps: the selective deactivation of the catalyst in a laboratory scale; the streaming of the catalyst with the producer gas of a downdraft and an oxygen/steam circulating fluidized bed (CFB) gasifier; and tests in a reformer placed in a slipstream of the CFB gasifier. The information obtained allowed to elucidate the catalyst deactivation mechanisms taking place during the reforming of the producer gas: physical deactivation by deposition of fine ashes, aerosol particulate or carbon; poisoning by H₂S and HCl present in the gas phase and thermal sintering because of the high operation temperatures required to avoid the chemical deactivation. These physical and chemical effects depended on the composition of the biomass fuel.     

两段炉内的压降以及速度分布

化学热回收两段组合式气化炉有效地提高了高温合成气的显热回收。为进一步了解该新型两段炉内气体的流动规律,在自行搭建的冷模实验装置上,考察了该组合式两段炉内的二段床层压降以及速度分布情况。研究表明,采用Montiller经验公式能够准确预测二段固定床的床层压降,当气体达到二段床层表面时,将产生一个冲击区。拟合得到单喷嘴顶喷的轴向速度衰减公式以及四喷嘴撞击后的向下径向射流速度衰减公式。轴向速度的径向分布中,中心气速最大并且衰减最快,采用四喷嘴对喷的形式达到管流区所需的轴向距离较单喷嘴顶喷小1.8D。     

Identification of the reaction zones occurring in a commercial-scale Sasol–Lurgi FBDB gasifier

Gasification behaviour is particle dependent, whilst gasifier (reactor) behaviour is an averaging process of individual responses of each particle. It was hypothesized, that if it were possible to extract and analyze particles from different reaction zones within a gasifier, it may be likely to enhance the understanding of the contribution that these particles make towards gasification. This better understanding of the particle-type compositional responses could act as an enabler to further manipulate and improve gasifier performance.The primary focus of this study was to evaluate a sequential (axial) sampling “turn-out” methodology of a quenched fixed-bed commercial-scale Sasol–Lurgi gasifier, in order to present samples that accurately describe operational aspects occurring in the reaction zones within the reactor. Characterization of the chemical properties of the sample increments were expected to deliver distinct profiles of the drying, pyrolysis, reduction and combustion (ash-bed) zones, which could be used to advance the kinetic modeling capability of the process. In order to interpret the coal property transformational behaviour occurring within the commercial-scale gasifier, the proximate, Fischer tar, ultimate, and coal char CO₂ reactivity analysis were conducted.The pyrolysis zone was found to be the largest reaction zone situated below the drying zone within the gasifier, followed by the reduction zone, and combustion (ash-bed) zones. Whilst the boundaries of the pyrolysis zone were very clearly defined by the residual volatile matter distribution profile, distinctive regional overlap with a “slow pyrolysis with gasification” region was observed in the bottom half of the pyrolysis zone, above which a “rapid de-volatilization” region existed. The reduction zone was found to also exhibit an overlap in zonal fronts, i.e. a gasification region occurred below the pyrolysis zone and co-existed in equal proportions, with an oxidation frontal region occurring above the combustion zone. The combustion zone was found to be very shallow, below which the ash-bed region existed.The findings clearly suggest that text book pictures showing axially-depicted reaction zones occurring within the fixed-bed gasifier, i.e. drying, pyrolysis, gasification and combustion, inadequately describe the “real” situation and in practice, overlap of reaction regions within zones indeed also transpire.     

热管式生物质气化炉的模拟

从化学反应和传热两个方面考虑,建立了生物质间接供热气化模型,包括化学反应和传热两个子模型。化学反应子模型可以预测产气主要成分以及气化反应需要的热量,而传热子模型则可以估算热管的总热阻和传热功率。在模型分析基础上,开发设计了热管式生物质气化炉,并对化学反应子模型进行了验证。结果表明生物质间接供热气化模型成功地预测了产气主要成分,在利用热管间接供热的生物质气化产气中氢气含量在50%～60%之间,并且气体热值较高,可达10 MJ·m^-3