共查询到16条相似文献，搜索用时 187 毫秒
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发酵柑桔皮渣流化干燥传热传质分析 总被引：1，自引：1，他引：0
为了开发高效合理的柑桔皮渣发酵—干燥成套设备,需要进行发酵柑桔皮渣的干燥机理分析、传热传质的研究。该文采用流化干燥方法对发酵柑桔皮渣的干燥进行试验研究,建立了小型的流化床干燥试验台,分析了风速、颗粒粒径、初始含水率等对发酵柑桔皮渣流化干燥过程中传热传质的影响。试验表明：流化床的传热传质性能与流体的物理性质、操作参数、颗粒本身的物理性质以及流化床的特性密切相关。试验结果表明,传热系数沿流化床床高增加而减小,在床高4～6 cm之间,传热系数减小的幅度较大;在风速、颗粒粒径、初始含水率3个影响因素中,风速对传热系数的影响最大,当风速从2.06 m/s增大到2.75 m/s时,床高2～4 cm区域的平均局部传热系数增大了近92%。根据试验结果建立了传热传质数学模型并获得了传热无因次准则方程式,为强化传热传质以提高干燥效果提供了理论依据。 相似文献
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狭缝型分布板流化床提高核桃壳颗粒的流化效果 总被引：1，自引：1，他引：0
为了提高Geldart D类大颗粒物料在流化床中的流化效果,该文设计了一种结构简单的狭缝型气体分布板,进行了核桃壳颗粒(2~2.8 mm)的流态化试验,结果表明狭缝型分布板比传统多孔分布板提高床层膨胀率约5%,降低最小流化速率约8%。在欧拉-欧拉法的双流体模型和颗粒动力学理论基础上,建立流化床内气固两相流的数学模型并对模型进行验证,模拟值与试验值的误差在8%以内。利用数学模型对2种分布板流化床内大颗粒流化过程进行数值模拟,比较了2种分布板结构对流化床内床层压降、床层膨胀率、颗粒相体积分数及气固两相的流化速度的影响。模拟结果表明:狭缝型分布板的"V"型气流通道结构,使得气流易于集束向上运动,形成大气泡对床层造成扰动,从而增大床层压降波动幅度,提高床层膨胀率,并在流化床内形成4个小环流,促进气体相和颗粒相之间的混合,使得核桃壳颗粒流化均匀。该研究为大颗粒物料处理过程中流化床分布板的设计和选用提供参考。 相似文献
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中国西南石漠化地区农村能源消费结构研究 总被引：4，自引：4，他引：0
为考察烘焙林业废弃物生物质与煤粉二元混合物的流化特性,在自行搭建的流化试验装置上,进行不同质量配比的烘焙生物质与煤粉二元混合颗粒系统的流化试验,获得该系统的流化特性曲线,并在此基础上确定二元混合颗粒的起始流化速度、最小流化速度和完全流化速度等特征速度,进而获得"组分-特征速度"的相平衡图,探讨烘焙生物质质量分数(0,20%,40%,60%,80%和100%)对二元混合颗粒流化特性的影响规律,并提出了预测烘焙生物质与煤粉二元混合颗粒最小流化速度的经验公式。结果表明,煤粉颗粒与烘焙生物质颗粒单独流化时,流化曲线可以划分为4个区域:I固定床区域,II过渡区域,III起始流化区域和IV完全流化区域。完全流化区域标准化床层比压降值的大小依次为:无烟煤1(0.90)无烟煤2(0.86)烘焙生物质1(0.84)烘焙生物质2(0.53),流化质量依次变差。烘焙生物质与煤粉二元混合颗粒的流化曲线与其单组分颗粒的流化曲线近似,但区域II和III所对应的气速的范围明显缩小。随着烘焙生物质质量分数的增加,完全流化区域的标准化床层比压降值呈现出逐渐减小的趋势,混合颗粒的流化质量逐渐变差,起始流化速度先增大后减小,完全流化速度先减小后增大,最小流化速度逐渐减小。不同特征速度对应着不同流化阶段间的过渡,通过流化气速所处的区间并结合"组分-特征速度"相平衡图,可以对二元混合颗粒所处的流化状态进行预判,并可根据实际工程应用需要对操作流化气速进行相应的调节。该文所获得的不同配比烘焙生物质与煤粉二元混合颗粒最小流化速度经验公式可以在–25%～+20%的误差范围内对烘焙生物质与煤粉二元混合颗粒的最小流化速度进行较好地预测。研究结果可为生物质与煤流化床共气化工艺中的气化炉等相关工艺设备的设计和安全稳定运行提供参考。 相似文献
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流化床流态化质量影响因素(简报) 总被引：2，自引：1，他引：1
以石英砂为原料,在底部开孔进气和敞口进气两种类型的小型流化床上研究了在流化过程中生物质粒径、开孔率大小、进气方式3个主要参数对流态化质量的影响。由0.2～0.45 mm和0.45～0.6 mm两种粒径的红松木和白松木两种物料与石英砂（0.2～0.45 mm）在常温下混合的流态化曲线可以看出,各个混合情况均达到了良好的流态化质量;流化床开孔率在0.5%～3%之间变化时,开孔率越低,流态化质量越好。敞口式进气流态化质量比底部进气更好。 相似文献
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《农业工程学报》2019,(3)
为考察烘焙林业废弃物生物质与煤粉二元混合物的流化特性,在自行搭建的流化试验装置上,进行不同质量配比的烘焙生物质与煤粉二元混合颗粒系统的流化试验,获得该系统的流化特性曲线,并在此基础上确定二元混合颗粒的起始流化速度、最小流化速度和完全流化速度等特征速度,进而获得"组分-特征速度"的相平衡图,探讨烘焙生物质质量分数(0,20%,40%,60%,80%和100%)对二元混合颗粒流化特性的影响规律,并提出了预测烘焙生物质与煤粉二元混合颗粒最小流化速度的经验公式。结果表明,煤粉颗粒与烘焙生物质颗粒单独流化时,流化曲线可以划分为4个区域:I固定床区域,II过渡区域,III起始流化区域和IV完全流化区域。完全流化区域标准化床层比压降值的大小依次为:无烟煤1(0.90)无烟煤2(0.86)烘焙生物质1(0.84)烘焙生物质2(0.53),流化质量依次变差。烘焙生物质与煤粉二元混合颗粒的流化曲线与其单组分颗粒的流化曲线近似,但区域II和III所对应的气速的范围明显缩小。随着烘焙生物质质量分数的增加,完全流化区域的标准化床层比压降值呈现出逐渐减小的趋势,混合颗粒的流化质量逐渐变差,起始流化速度先增大后减小,完全流化速度先减小后增大,最小流化速度逐渐减小。不同特征速度对应着不同流化阶段间的过渡,通过流化气速所处的区间并结合"组分-特征速度"相平衡图,可以对二元混合颗粒所处的流化状态进行预判,并可根据实际工程应用需要对操作流化气速进行相应的调节。该文所获得的不同配比烘焙生物质与煤粉二元混合颗粒最小流化速度经验公式可以在–25%～+20%的误差范围内对烘焙生物质与煤粉二元混合颗粒的最小流化速度进行较好地预测。研究结果可为生物质与煤流化床共气化工艺中的气化炉等相关工艺设备的设计和安全稳定运行提供参考。 相似文献
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基于颗粒流理论的微灌砂滤层反冲洗过程砂粒速度场模拟 总被引：2，自引：2，他引：0
砂颗粒流在石英砂滤层反冲洗流场中的速度分布,对滤层流化状态的稳定性和反冲洗效果起决定性作用。为了对滤层反冲洗过程砂颗粒的速度场进行分析,并确定最佳反冲洗速度,该文以厚度为400 mm,粒径范围为1.0～1.18 mm的石英砂滤层为研究对象,基于颗粒流运动理论,采用Eulerian-Eulerian模型对滤层反冲洗过程砂粒的速度场进行3维动态模拟。为了验证模拟结果的准确性,作者开展了室内模型试验,并将模拟结果与试验结果进行对比,结果显示,滤层膨胀高度的最大模拟误差为9.8%,能够控制在10%以内,说明数值模拟结果是可信的。在此基础上,分析了反冲洗流化倍数为1.3、1.5、1.7和1.9时,滤层高度分别为15、25和35 cm 3个横截面上,在不同的反冲洗时间,砂粒的轴向速度沿横坐标的分布规律。根据砂粒在3个横截面上运动速度的大小和方向,判断砂滤层是否达到完全流化;根据砂粒在3个横截面上运动趋势是否一致,砂粒的上升区是否保持稳定,判断滤层流化状态是否稳定。结果显示,当反冲洗流化倍数不小于1.7时,滤层才能达到稳定的流化状态,从而达到比较理想的反冲洗效果,并得出滤层最佳反冲洗流化倍数为1.7。研究结论为砂过滤器的反冲洗研究提供了理论基础和技术支撑,为反冲洗性能参数的确定提供了参考。 相似文献
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微灌石英砂过滤器反冲洗数值模拟验证与流场分析 总被引：5，自引：4，他引：1
微灌石英砂滤层的反冲洗,是实现滤料再生的有效途径,为了对反冲洗过程流场进行分析,并确定合理的反冲洗速度。该文建立了石英砂过滤器几何模型并进行了网格划分,采用Eulerian模型作为石英砂滤层反冲洗数值模拟模型,分别对石英砂当量粒径为1.06、1.2和1.5 mm的3种滤层的反冲洗过程进行了瞬态模拟,并将滤层整体压降和整体密度的模拟结果与试验结果进行对比,结果显示,整体压降的最大模拟误差为7.03%,整体密度的最大模拟误差为1.93%,说明数值模拟准确可信。在此基础上,分析了石英砂滤层反冲洗过程压降的波动规律、压降均值和压降标准偏差随反冲洗速度的变化趋势;并分析了滤层密度的分布规律、密度均值和密度标准偏差随反冲洗速度的变化趋势。根据压降波动的稳定性,结合滤层密度分布的稳定性,确定了石英砂滤层反冲洗强度的合理范围,3种滤层分别为0.0149~0.0212、0.0146~0.0218和0.0191~0.0261 m/s。该研究为石英砂滤层反冲洗过程的机理研究提供了参考,为砂过滤器反冲洗性能参数的确定提供了依据。 相似文献
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基于砂滤层内水体积分数瞬态模拟的反冲洗速度优选 总被引：2，自引：2，他引：0
为了对石英砂滤层反冲洗过程水的体积分数波动规律进行分析,并确定合理的反冲洗速度范围,该文采用数值模拟手段对滤层反冲洗过程水的体积分数进行三维动态模拟,采用Gambit软件建立了石英砂过滤器的几何模型,并对几何模型进行了网格划分,以Mixture模型做为反冲洗过程水的体积分数的数值模拟模型。以当量粒径分别为1.06、1.2和1.5 mm的3种石英砂滤层为研究对象进行动态模型。为了验证模拟结果的准确性,开展了室内模型试验,并将模拟结果与试验结果进行对比,结果显示,水的体积分数的最大模拟误差为5.64%,说明数值模拟结果是可信的。在使用模拟数据进行流场分析时,为了得出更具普遍性的结论,引入了反冲洗流化倍数的概念,最小反冲洗流化速度的倍数称为反冲洗流化倍数。在此基础上,分别分析了反冲洗流化倍数为1.1、1.3、1.5、1.7和1.9时,滤层高度分别为15、25和35 cm共3个横截面上,反冲洗过程水的体积分数随时间的变化规律。计算了水的体积分数的均值和标准偏差,分析了水的体积分数的均值和标准偏差随随反冲洗流化倍数的变化规律。在3个截面上水的体积分数均值基本相同的情况下,根据标准偏差的大小,判定滤层反冲洗的稳定性。由此得出,使反冲洗水的体积分数波动保持稳定的反冲洗流化倍数的临界值为1.7。当反冲洗流化倍数范围为1~1.7时,标准偏差适中,反冲洗效果理想。结果表明,对于均质石英砂滤层,反冲洗效果是否理想,决定因素是反冲洗流化倍数。该文可为砂过滤器的反冲洗运行机理提供参考。 相似文献
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针对5HM-1型脉动流化干燥机存在的脉动效果不理想、物料输送不够流畅等问题，研制了脉动振动流化干燥机，重点解决了气流分配器的设计与布置、以及气流分配的均匀性问题，增设了振动输送装置和导料装置，解决了物料的输送与“反流”问题。利用该设备对玉米和啤酒糟这两种物料进行干燥时，加热温度分别以70～75℃和65～70℃为宜，最佳脉动频率分别为3.0 Hz和2.0 Hz左右，最佳床层倾角分别为2.5°～3.8°和3.5°～4.8°，最佳气流速度分别为0.8～1.0 m/s和0.9～1.1 m/s，在设定的床层倾角和气流速度条件下，最佳振动频率均为32 Hz左右。干燥上述两种物料时，其干燥强度分别为20.87 kg(H2O)/m2·h和21.76 kg(H2O)/m2·h，单位热耗分别为5.86 MJ/kg(H2O)和4.91 MJ/kg(H2O)，单位能耗分别为7.38 MJ/kg(H2O)和6.47 MJ/kg(H2O)。 相似文献
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沙层厚度和粒径组成对覆沙黄土坡面产流产沙的影响 总被引：6，自引：0，他引：6
片沙覆盖黄土区是水蚀风蚀交错带内土壤侵蚀最为强烈的区域,研究该区内土壤侵蚀特征可对水蚀风蚀交错带水土流失的预报及防治提供理论依据。采用室内模拟降雨,研究黄土坡面不同覆沙厚度(2 cm、5 cm和10 cm)和沙层粒径组成(100%0.25 mm、75%0.25 mm+25%0.25mm、50%0.25 mm+50%0.25 mm、未处理原沙和100%0.25 mm)对坡面产流产沙的影响。结果表明,覆沙黄土坡面较黄土坡面的初始产流时间明显延长,产流速率和产流量减小,产沙速率和产沙量增大,降雨过程中产流产沙波动性增大,且这些变化随覆沙厚度增加而明显加强;沙层粒径组成在不同覆沙厚度下对坡面产流产沙的影响不同,2 cm覆沙厚度坡面在降雨前期随粒径变粗产流产沙呈增大趋势,降雨后期无明显变化;5 cm覆沙厚度坡面随沙层粒径变粗产流速率呈增加趋势,降雨前期上覆粗粒径沙层坡面的侵蚀速率高于细粒径沙层坡面,降雨后期恰好相反;10 cm覆沙厚度的坡面产流产沙随沙层粒径组成变化不明显。典型覆沙黄土坡面的产流过程为雨水垂直入渗―沙土界面潜流―沙层边缘渗流―地表径流,产沙过程为沙层边缘渗流侵蚀―沙层坍塌重力侵蚀―地表径流输移,明显不同于无覆沙黄土坡面的超渗产流方式及溅蚀―片蚀―细沟侵蚀的侵蚀发展过程。 相似文献
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Diano N Grimaldi T Bianco M Rossi S Gabrovska K Yordanova G Godjevargova T Grano V Nicolucci C Mita L Bencivenga U Canciglia P Mita DG 《Journal of agricultural and food chemistry》2008,56(23):11471-11477
The catalytic behavior of a mixture of pectic enzymes, covalently immobilized on different supports (glass microspheres, nylon 6/6 pellets, and PAN beads), was analyzed with a pectin aqueous solution that simulates apple juice. The following parameters were investigated: the rate constant at which pectin hydrolysis is conducted, the time (tau(50)) in which the reduction of 50% of the initial viscosity is reached, and the time (tau(comp,dep)) required to obtain complete depectinization. The best catalytic system was proven to be PAN beads, and their pH and temperature behavior were determined. The yields of two bed reactors, packed or fluidized, using the catalytic PAN beads, were compared to the circulation flow rate of real apple juice. The experimental conditions were as follows: pH 4.0, T = 50 degrees C, and beads volume = 20 cm(3). The initial pectin concentration was the one that was present in our apple juice sample. No differences were observed at low circulation rates, while at higher recirculation rates, the time required to obtain complete pectin hydrolysis into the fluidized reactor was found to be 0.25 times smaller than in the packed bed reactor: 131 min for the packed reactors and 41 min for the fluidized reactors. 相似文献
14.
Domestic wastewater with an influent COD of 160 to 327 mg L-1 was evaluated for treatment by the Biofilm Airlift Suspension-reactor (BAS-reactor). Ceramic materials withdiameters of 0.25–0.5 mm (for reactor (1)) and 0.5–0.71 mm(for reactor (2)) were used as carriers, respectively. Theresults show that reactor (1) with smaller carriers outperformedreactor (2) with larger carriers. At steady state, the BAS-reactors showed high COD removal efficiencies. When the HRT was kept at 0.5 hr, the mean effluent CODs were 33±4 and 58±5 mg L-1 for reactors (1) and (2), respectively, at a confidence interval of 95% (p = 95%). When HRT was extended to 1.0 hr, these values decreased to 24±2 and 30±3 mg L-1 for reactors (1) and (2), respectively (p = 95%). Biomass concentration increased whilebiofilm thickness decreased with an increase in carrierconcentration. Biomass concentrations as high as 6.16±0.12 and 5.50±0.10 g VSS L-1 (p = 0.95) were achieved at carrier concentrations of 100 g L-1 forreactors (1) and (2), respectively. Biofilm thickness had a significanteffect on reactor performance: with an increase in biofilm thickness, biomass concentration increased and the critical gas velocity to maintain carrier fluidization decreased. An oxygenation model for a BAS-reactor was proposed and the effectsof gas velocity and carrier concentration on the oxygen transfercoefficient were examined. It was found that oxygen transfer coefficient increased with gas velocity while the relationship between carrier concentration and oxygen transfer coefficient wascomplicated. During a period of more than three months of steadystate operation, carrier washout with the effluent was negligible.Comparison of the parameters of the conventional activated sludgeprocess to that of the BAS-reactor shows that the BAS-reactor isa promising wastewater treatment process with high efficiency andlow operation cost. 相似文献
15.
Sorghum [Sorghum bicolor (L.) Moench] cultivars were planted in 8 cm × 8 cm × 8 cm pots filled with ‘white quartz flintshot’ sand containing 0, 0.25, 0.50, 1.0, or 2.0 mg/kg metolachlor [2‐chloro‐N‐(2‐ethyl‐6‐methylphenyl)‐N‐(2 methoxy‐1‐methylethyl)acetamide] and the pots were watered on alternate days with 100 mL 0.1 M sodium acetate at pH 6.0, 5.5, 5.0, 4.5, or 4.0 to determine the influence of excess H+ and metolachlor concentrations on sorghum root growth. Cultivars utilized were Funk G522DR, SC574, SC283, GP‐10, 58M, and 38M. At pH 4.5 and 4.0 (0 metolachlor), root lengths of Funk G522DR and SC574 were significantly decreased compared to roots from plants grown at pH 6.0. The other four cultivars had decreased root growth at pH 4.0 (0 metolachlor). Metolachlor influence on sorghum cultivar root growth was dependent on pH, cultivar, and metolachlor concentration. None of the cultivars showed increased metolachlor activity which was influenced by pH. Metolachlor (0.25 mg/kg) reversed the influence of excess H+ concentration (pH 4.0) in SC574. Metolachlor (0.5, 1.0, and 2.0 ppmw) reversed the excess H+ concentration inhibition of root growth at pH 4.0 in Funk G522DR. 相似文献
16.
Covers of the nuclear waste repository are of great significance to the long-term safe storage and disposal of nuclear wastes. Capillary barriers have proven to be effective to resist the downward water seeping into the underlying nuclear wastes, especially in dry climate, and have been widely used worldwide. Infiltrating water is removed from the fine layer by evaporation or transpiration or through percolation into the coarse layer, which plays a critical role in preventing the water from further infiltration in the bulk wastes. In this paper, laboratory infiltration tests were conducted with an organic glass box, filled with fine-grained quartz sand in which a layer of coarse-grained quartz sand was emplaced horizontally or at various slopes (10° and 20°), and the capillary barrier effect under various conditions (different thickness, slop of coarse-grained quartz sand layer, and sprinkling intensity) was investigated in detail. The results show that the thickness of the underlying coarse layer plays a critical role in governing the performance of the capillary barrier. The efficiency of capillary barrier increases with increasing thickness and/or slope of the coarse layer, but decreases with increasing sprinkling intensity. For a sprinkling intensity of 20 mm/day, a 30-mm-thick coarse layer even emplaced horizontally can achieve 100% water diversion. In addition, a visible tracer test was performed with an inert red dyestuff to trace the streamlines; the results indicate that even with a 7-mm-thick coarse layer, the capillary barrier can offer marked ability to prevent water from percolating into the coarse layer. The findings could be useful for improving engineered uses of capillary barriers at waste repository sites. 相似文献