加压循环流化床富氧燃烧中试研究

二氧化碳捕集和封存技术(CCUS)是减少温室气体排放,实现全球环境可持续发展的有效技术手段。加压富氧燃烧技术是一种低成本CCUS技术。循环流化床燃烧技术(CFB)是目前商业化程度最好的清洁煤燃烧技术之一,加压循环流化床富氧燃烧耦合了加压富氧燃烧和循环流化床燃烧的诸多优点,具有很强的工业应用前景。但加压循环流化床富氧燃烧系统结构复杂,燃烧工况的切换和烟气再循环导致其在启动、控制、运行等方面面临巨大挑战。目前对于加压循环流化床富氧燃烧的研究大多处于理论建模、机理研究和小试试验阶段。为了更深入地探究加压循环流化床富氧燃烧的启动和运行方法,中国科学院工程热物理研究所在MW级加压循环流化床富氧燃烧中试试验平台上进行了中试研究,实现了加压富氧燃烧的稳定运行,获得了中试尺度加压富氧燃烧运行模式,以及启动和运行过程中温度、压力、给煤量和风量的变化曲线。加压富氧燃烧工况运行中整体O₂体积分数为29%,压力为0.30 MPa,功率为0.84 MW,尾部烟气中CO₂体积分数达91%,可较好地实现CO₂产品的捕集和压缩纯化。中试尺度加压富氧燃烧启动和运行的主要流程为:启动阶段-常压O₂/N₂燃烧阶段-常压富氧燃烧-加压富氧燃烧阶段,各阶段切换平稳。     

Olive cake combustion in a circulating fluidized bed

In this study, a circulating fluidized bed of 125 mm diameter and 1800 mm height was used to find the combustion characteristics of olive cake (OC) produced in Turkey. A lignite coal that is most widely used in Turkey was also burned in the same combustor. The combustion experiments were carried out with various excess air ratios. The excess air ratio, λ, has been changed between 1.1 and 2.16. Temperature distribution along the bed was measured with thermocouples. On-line concentrations of O₂, SO₂, CO₂, CO, NO_x and total hydrocarbons were measured in the flue gas. Combustion efficiencies of OC and lignite coal are calculated, and the optimum conditions for operating parameters are discussed. The combustion efficiency of OC changes between 82.25 and 98.66% depending on the excess air ratio. There is a sharp decrease observed in the combustion losses due to hydrocarbons and CO as the excess air ratio increases. The minimum emissions are observed at λ=1.35. Combustion losses due to unburned carbon in the bed material do not exceed 1.4 wt% for OC and 1.85 wt% for coal. The combustion efficiency for coal changes between 82.25 and 98.66% for various excess air ratios used in the study. The ash analysis for OC is carried out to find the suitability of OC ash to be used as fertilizer. The ash does not contain any hazardous metal.     

Coal combustion characteristics in a circulating fast fluidized bed

The effect of coal size (0.73–1.03 mm), excess air ratio (1.0–1.4), operating bed temperature (750–900‡C), coal feeding rate (1–3 kg/h), and coal recycle rate (20–40 kg/h) on combustion efficiency, temperature profiles along the bed height and flue gas composition have been determined in a bubbling and circulating fluidized bed combustor (7.8 cm-ID x 2.6 m-high). Combustion efficiency increases with increasing excess air ratio and operating bed temperature and it decreases with increasing particle size in the bubbling and circulating fluidzing beds. In general, temperature profiles and combustion efficiency are more uniform and higher in a circulating bed than those in bubbling bed. Combustion efficiency also increases with increasing recycle rate of unburned coal in the circulating bed. The ratio of CO/CO₂ of flue gas decreases with increasing bed temperature and excess air ratio, whereas the ratio of O₂(CO + CO₂) decreases with bed temperature in both bubbling and circulating fluidized beds.     

Modelling of circulating fluidized bed combustion of a char

The combustion of a char in the 41 mm ID riser of a laboratory circulating fluidized bed combustor has been investigated at different air excesses and rates of solids (char and sand) circulating in the loop. Riser performance was characterized by an axial oxygen concentration profile as well as by the overall carbon content and particle size distribution. The proposed model accounts for carbon surface reaction, intraparticle and external diffusion, and attrition. External diffusion effects were relevant in the riser dense region where char was potentially entrapped in large clusters of inert solids. Experimental data and results of the model calculations are in satisfactory agreement.     

Oxy-fuel circulating fluidized bed combustion in a small pilot-scale test rig

Coal combustion under the elevated partial pressure of oxygen in a circulating fluidized bed environment was investigated. The fuel used was bituminous coal. The concentration of oxygen in the air was increased to 35% per volume. Excess oxygen ranged from 1.1 to 1.3 and the temperature ranged from ca. 1073 K to 1273 K. A 0.1 MW_th CFB combustor was adapted for oxy-combustion. The conversion ratios respectively studied were: carbon, sulfur and nitrogen to CO, SO₂ and NO_X. An increase of nitrogen and sulfur conversion ratios and a strong decrease of incomplete combustion losses were found under the oxygen-enriched conditions. Moreover, a strong increase in temperature was noticed during oxy-combustion.     

Experimental trends of NO in circulating fluidized bed combustion

Experimental trends for the dependence of CO, NO and N₂O emissions on bed temperature and oxygen concentration in circulating fluidized bed combustion (CFB) are presented. The main focus is on the nitrogen emission formation in the lower furnace area. A test campaign including seven tests with a laboratory scale CFB test rig were carried out to produce appropriate data of the phenomena. These experiments show that NO emissions above the dense bed decrease with decreasing temperature or oxygen concentration. Instead, N₂O emissions increase when the bed temperature is decreased and decrease when the oxygen concentration is decreased. These trends can partly be explained by heterogeneous reactions between NO and char, since decrease in temperature or oxygen concentration increases the bed char inventory. However, oxygen and temperature also affect directly on NO emissions. Correlations for the CO, NO, N₂O, NH₃ and HCN concentrations at the exit of dense bed were developed. This type of correlations can, among other things, be applied as boundary conditions to the more sophisticated CFD models that are usually applied to modelling of diluted part of the furnace. CFD modelling of the dense bed area is complicated and accuracy is not sufficient, thus simplified experimental correlations can aid in the development of furnace design towards better emission performance.     

Countermeasures against alkali-related problems during combustion of biomass in a circulating fluidized bed boiler

The purpose of this work was to study different ways to mitigate alkali-related problems during combustion of biomass in circulating fluidized beds. Wood chips and wood pellets were fired together with straw pellets, while the tendency to agglomerate and form deposits was monitored. In addition to a reference case, a number of countermeasures were applied in related tests. Those were addition of elemental sulphur, ammonium sulphate and kaolin to a bed of silica sand, as well as use of olivine sand and blast-furnace slag as alternative bed materials. The agglomeration temperature, composition and structure of bed-ash samples were examined. The flue-gas composition, including gaseous alkali chlorides, was measured in the hot flue gases and in the stack. Particles in the flue gas were collected and analysed for size distribution and composition. Deposits were collected on a probe in hot flue gases and their amount and composition were analysed. Addition of kaolin was found to be the best method to counteract the agglomeration problem. The deposition problem is effectively counteracted with addition of ammonium sulphate, while kaolin is too expensive to be used commercially against deposits, and sulphur is less effective than ammonium sulphate.     

Hydrodynamic modeling of a circulating fluidized bed

Hydrodynamics plays a crucial role in defining the performance of circulating fluidized beds (CFB). The numerical simulation of CFBs is very important in the prediction of its flow behavior. From this point of view, in the present study a dynamic two dimensional model is developed considering the hydrodynamic behavior of CFB. In the modeling, the CFB riser is analyzed in two regions: The bottom zone in turbulent fluidization regime is modeled in detail as two-phase flow which is subdivided into a solid-free bubble phase and a solid-laden emulsion phase. In the upper zone core-annulus solids flow structure is established. Simulation model takes into account the axial and radial distribution of voidage, velocity and pressure drop for gas and solid phase, and solids volume fraction and particle size distribution for solid phase. The model results are compared with and validated against atmospheric cold bed CFB units' experimental data given in the literature for axial and radial distribution of void fraction, solids volume fraction and particle velocity, total pressure drop along the bed height and radial solids flux. Ranges of experimental data used in comparisons are as follows: bed diameter from 0.05-0.418 m, bed height from 5-18 m, mean particle diameter from 67-520 μm, particle density from 1398 to 2620 kg/m³, mass fluxes from 21.3 to 300 kg/m²s and gas superficial velocities from 2.52-9.1 m/s.As a result of sensitivity analysis, the variation in mean particle diameter and superficial velocity, does affect the pressure especially in the core region and it does not affect considerably the pressure in the annulus region. Radial pressure profile is getting flatter in the core region as the mean particle diameter increases. Similar results can be obtained for lower superficial velocities. It has also been found that the contribution to the total pressure drop by gas and solids friction components is negligibly small when compared to the acceleration and solids hydrodynamic head components. At the bottom of the riser, in the core region the acceleration component of the pressure drop in total pressure drop changes from 0.65% to 0.28% from the riser center to the core-annulus interface, respectively; within the annulus region the acceleration component in total pressure drop changes from 0.22% to 0.11% radially from the core-annulus interface to the riser wall. On the other hand, the acceleration component weakens as it moves upwards in the riser decreasing to 1% in both regions at the top of the riser which is an important indicator of the fact that hydrodynamic head of solids is the most important factor in the total pressure drop.     

Hydrodynamic characteristics of a circulating fluidized bed

In a circulating fluidized bed (7.8 cm-ID x 260 cm-high), flow regime of coal-air system at room temperature has been determined. Bituminous coal particles used were either 0.73 mm or 1.03 mm in the mean diameter having density of 1400 Kg/m³. The transition velocities from bubbling to turbulent beds and the transport velocities between turbulent and fast beds have been determined. The resulting transition velocities between bubbling and turbulent beds were 103 cm/s for 0.73 mm and 130 cm/s for 1.03 mm coal particles, respectively. The transport velocities between turbulent and fast beds were 180 and 209 cm/s for 0.73 and 1.03 mm particles, respectively. In addition, chocking velocities were determined at different solid feeding rates. The resulting values were in the range of 2.55-2.65 m/s for 0.73 mm particle and of 2.77-2.84 m/s for 1.03 mm particle, respectively. The published literature data of the transition velocity between bubbling and turbulent bed have been correlated with particle properties.     

Sulfur fate during bituminous coal combustion in an oxy-fired circulating fluidized bed combustor

To clarify the sulfur transformation behavior during oxy-fired circulating fluidized bed (CFB) combustion, experiments on SO₂ emission characteristics were carried out in a 50 kWth CFB combustor. Results show that SO₂ emission is quite dependent on the bed temperature in different atmospheres without limestone injection. With Ca/S=2.5, SO₂ emission in 21%O₂/79%CO₂ atmosphere is smaller than that in air atmosphere, but SO₂ emission decreases with the increase of O₂ concentration. The calcium forms in the ash prove the combination of calcination/carbonation and direct sulfation mechanism of limestone under oxy-combustion conditions. And the desulfurization efficiency of limestone (as deducting the self-retention efficiency from the total sulfur removal efficiency) increases from 40% to 52% as the O₂ concentration increases from 21% to 40%.     

Coal combustion characteristics in a pressurized fluidized bed

The characteristics of emission and heat transfer coefficient in a pressurized fluidized bed combustor are investigated. The pressure of the combustor is fixed at 6 atm. and the combustion temperatures are set to 850, 900, and 950 °C. The gas velocities are 0.9, 1.1, and 1.3 m/s and the excess air ratios are 5, 10, and 20%. The desulfurization experiment is performed with limestone and dolomite and Ca/S mole ratios are 1,2, and 4. The coal used in the experiment is Cumnock coal from Australia. All experiments are executed at 2 m bed height. In this study, the combustion efficiency is higher than 99.8% through the experiments. The heat transfer coefficient affected by gas velocity, bed temperature and coal feed rate is between 550-800 W/m² °C, which is higher than those of AFBC and CFBC. CO concentration with increasing freeboard temperature decreases from 100 ppm to 20 ppm. NO_x concentration in flue gas is in the range of 5-130 ppm and increases with increasing excess air ratio. N₂O concentration in flue gas decreases from 90 to 10 ppm when the bed temperature increases from 850 to 950 °C.     

循环流化床生物质直燃发电技术研究进展

循环流化床农林生物质直燃发电是农林生物质能源化利用的主要途径,在我国碳达峰和碳中和的战略目标下,产业发展将迎来更大的机遇,同时也面临更多的问题和挑战。为了促进循环流化床锅炉生物质发电产业的稳定、健康发展,调研了生物质直燃发电产业发展现状,梳理了循环流化床锅炉在生物质发电产业应用的技术优势,系统分析了生物质循环流化床锅炉的发展历程和关键技术突破。生物质直燃发电产业近年来在我国乃至世界范围内都得到了高速发展,“十三五”以来,我国生物质发电装机年均增长率约20.3%。循环流化床燃烧技术由于其特有的燃料适应性、较高的燃烧效率和较低的污染物排放,适用于生物质直燃发电,目前新建的生物质发电厂普遍采用高压和超高压参数循环流化床锅炉,部分先进机组带有一次再热循环。流态重构技术在生物质循环流化床锅炉上的应用,能大幅降低机组厂用电率,进一步提高锅炉效率;通过优化燃烧温度及风量配比,NO_x原始排放得到有效控制;针对生物质燃料碱金属含量高,易于结渣沾污的问题,通过优化对流受热面,控制燃烧温度,可以有效减缓受热面沾污堵塞等问题,锅炉可用率大幅提高。目前限制生物质发电产业发展的主要因素包括运...     

黄磷尾气在循环流化床锅炉中的掺烧使用

国内大部分中小型黄磷企业受制于矿、电因素无法连续稳定生产,给黄磷尾气的净化和规模化综合利用造成很大困难。为适应这一工况,提高黄磷尾气的利用率,分析黄磷尾气对热工设备的腐蚀机制,在降低投资和净化成本的基础上,探索出在循环流化床锅炉中掺烧黄磷尾气的方法,并辅以脱硫固磷、超音速喷涂等防腐蚀措施,并对防腐机理进行分析。锅炉近十年运行安全平稳,达到了节能减排的目的。     

Fluidized bed pyrolysis of distilled spirits lees for adapting to its circulating fluidized bed decoupling combustion

Distilled spirits Lees, rich in cellulose, water and N element, are difficult to burn efficiently and cleanly in grate chain stock boiler. The circulating fluidized bed decoupling combustion (CFBDC) was therefore proposed to burn the distilled spirits lees efficiently and with low-NOx emission. The pyrolysis behavior of the distilled spirits lees was investigated in a fluidized bed reactor for optimizing the pyrolysis conditions of the pyrolyzer in CFBDC. The results showed that the distilled spirits lees began to devolatize at 250 °C and at 350–450 °C the tar yield reached its maximum of about 16.3 wt.% (dry base). The chemical oxygen demand (COD) value of the condensed liquid reached its maximum of about 50,000 mg/L at 450 °C. With raising temperature the pyrolysis gas tended to contain more CO and H₂ and less CO₂. The functional groups H-O, aliphatic C-H, aromatic ring, C=O and C-O were all presented in the char generated at low-temperatures, while only the C-O group was identified for the char from the pyrolysis at 650 °C. The article suggested that the pyrolysis for the CFBDC was better around 500 °C so that certain volatiles could remain in the char to sustain stable combustion.     

Process characteristics investigation of simulated circulating fluidized bed combustion combined with coal pyrolysis

A poly-generation process of simulated circulating fluidized bed (CFB) combustion combined with coal pyrolysis was developed in a laboratory scale. Pyrolysis characteristics of three bituminous coals with high volatile contents were investigated in a fixed bed with capacity of 10 kg solid samples. The effects of initial temperature of solid heat carrier, pyrolysis holding time, blending (ash/coal) ratio and coal particle size on gas and tar yields were studied experimentally. The results indicate that the initial temperature of the heat carrier is the key factor that affects the gas and tar yield, and the gas composition. Most of the gas and the tar are released during the first few minutes of the pyrolysis holding time. For caking coal, the amount of char agglomerating on the pyrolyzer inner wall is reduced by enhancing the blending ratio. The experimental results may provide basic engineering data or information for the process design of CFB combustion combined with coal pyrolysis in a large scale.     

Bed-to-wall heat transfer characteristics in a circulating fluidized bed

The bed-to-wall heat transfer coefficients were measured in a circulating fluidized bed of FCC particles (d_p = 65 μm). The effects of gas velocity (1.0–4.0 m/s), solid circulation rate (10–50 kg/m²s) and particle suspension density (15–100 kg/m³) on the bed-to-wall heat transfer coefficient have been determined in a circulating fluidized bed (0.1 m-ID x 5.3 rn-high). The heat transfer coefficient strongly depends on particle suspension density, solid circulation rate, and gas velocity. The axial variation of heat transfer coefficients is a strong function of the axial solid holdup profile in the riser. The obtained heat transfer coefficient in terms of Nusselt number has been correlated with the pertinent dimensionless groups     

循环流化床燃烧在高过剩空气下的NOx排放

提出了借助循环流化床在高过剩空气系数下燃烧的技术提供高温空气的新构思。搭建了循环流化床燃烧热态试验台,完成了循环流化床燃烧在高过剩空气系数下的NOx排放特性试验,结果表明:循环流化床在高过剩空气系数下燃烧温度分布均匀,燃烧稳定性好;过剩空气系数增大,氮氧化物排放增加;提升管二次风高度的增加和还原区系数的减小有利于控制氮氧化物的排放水平和减少煤中的N向NOx的转化比。在过剩空气系数为1.6、还原区系数为0.72和二次风高度为1 500 mm时,循环流化床NOx排放为339 mg/m3,煤中的N向NOx转化比为21%。循环流化床高温空气NOx的浓度对燃料高温燃烧NOx排放的影响需要进一步研究。     

Axial dispersion of gas in a circulating fluidized bed

An axial dispersion of gas in a circulating fluidized bed was investigated in a fluidized bed of 4.0 cm I.D. and 279 cm in height. The axial dispersion coefficient of gas was determined by the stimulus-response method of trace gas of CO₂. The employed particles were 0.069 mm and 0.147 mm silica-sand. The results showed that axial dispersion coefficients were increased with gas velocity and solid circulation rates as well as suspension density. The experimentally determined axial dispersion coefficients in this study were in the range of 1.0-3.5 m²/s.     

Sulfate decomposition from circulating fluidized bed combustors bottom ash

The decomposition of sulfates present within bottom ashes produced during operation of a fluidized bed combustor is not complete under continuously reducing conditions (2% CO) at . The product CaS accumulates within the particles. Under alternatively reducing and oxidizing conditions, a complete sulfur release can be obtained. The reduction product CaS is oxidized to SO₂ during the oxidizing step. This prevents sulfate accumulation within the particles during the reducing step. Under these cycling conditions, the rate of sulfate decomposition is increased by using a high CO concentration during the reduction phase. The duration of the reduction phase must be optimized to avoid the formation of too much CaS within the particle.