声场流化床流化特性研究
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摘要
声场流态化是将声波从流化床顶部或底部传入流化床中,达到改善颗粒流化质量的效果。声场流化床主要有两大优点:(1)声波能有效降低流化床中颗粒聚团的尺寸,使之在很低的操作速度下实现稳定流态化;(2)声能不受颗粒物性限制,可以采用辐射方式引入流化床而不需要内部构件等优点。本论文针对FCC颗粒、石英砂颗粒和生物质颗粒的声场流化特性以及声场射流流化床的流化特性进行了系统研究。
在内径140 mm,高1600 mm的鼓泡流化床中,以FCC颗粒和石英砂颗粒为流化介质,采用光导纤维探针和差压变送器分别测定不同轴/径向位置的颗粒浓度信号和压力波动信号,考察外加声场对密相区颗粒浓度和压力脉动的影响。结果表明:声场的引入可以降低颗粒最小流化速度,声压级越大,最小流化速度越小;固定声压频率存在一个最佳频率范围颗粒最小流化速度最小。鼓泡床密相区FCC颗粒浓度沿轴向逐渐减小,沿径向呈抛物线分布。操作气速越大,FCC颗粒浓度越小。随着声压强度的增大,床层中心区和上部密相区FCC颗粒浓度增大。固定声压级,频率在100～400 Hz范围内FCC颗粒浓度较大,频率低于100 Hz或高于400 Hz时,声波的作用效果减弱。
通过统计分析、功率谱分析和小波分析揭示外加声场对颗粒浓度信号的影响。结果表明:颗粒浓度功率谱呈现宽频且有明显主频的低频信号,声压越大主频的峰值越小,颗粒浓度信号的主频峰值随频率先下降后上升。对颗粒浓度信号进行5尺度离散小波变换,声场流化床中颗粒浓度信号高频部分增加,低频部分减小。气泡尺寸和鼓泡频率随声压的增大而减小,随声波频率的增大先减小后增大。
在内径53 mm,高800 mm的声场鼓泡流化床中,采用压力探针研究生物质颗粒的流化特性,考察添加惰性组分和引入声场对生物质流化质量的影响。结果表明:添加惰性组分可以显著改善生物质流化质量,惰性组分质量分数越大流化质量越好。声场的引入可以使生物质在较高质量分数下实现流化,降低生物质颗粒的最小流化速度。声波强度越大,生物质颗粒的最小流化速度越小;固定声压级,在最佳频率范围内生物质颗粒最小流化速度最小。
以FCC和石英砂颗粒为流化介质,采用光导纤维探针考察声场和射流耦合对颗粒流化的影响。结果表明:射流深度随射流气速、流化数和射流管径的增大而增大,随床料平均粒径和密度的增加而减小,声场的引入可以增大射流深度。对实验数据进行多元线性回归分析,得到了声场射流流化床水平射流的射流深度关联式,关联式的预测值与实验值吻合得较好。颗粒浓度径向呈抛物线分布,沿轴向高度颗粒浓度逐渐增大,其中射流区颗粒浓度最小,射流气速和流化数越大颗粒浓度越小。声场的引入可以减小气泡尺寸,增大颗粒浓度,扩大射流区域范围。
Many approaches were developed to improve the fluidization behavior of particles, such as adding another kind of particles to the bed and introducing a magnetic field, acoustic field, or vibrating field. Among these methods, sound-assisted fluidization is particularly attractive because no internals are needed. The application of an acoustic field can improve the fluidization quality of fine powders.
The radial and axial profiles of the FCC particle concentrations were measured using an optical fiber probe under different superficial gas velocities, sound pressure levels and frequencies in an acoustic fluidized bed (Φ140 mm×1600 mm). Meanwhile, the effects of sound wave frequency and sound pressure level on the particle concentrations were examined in this work. Experimental results showed that the particle concentrations were distributed non-uniformly in radial and axial directions, with particle concentration lower in fluidized bed center region and higher near the wall region. With increasing the bed height, the particle concentration tended to be lower. As superficial gas velocity is increased, the particle concentration decreased. The minimum fluidization velocity has a minimum value when the frequency of sound waves approached 150 Hz, whereas it decreased as the sound pressure level was increased at the same sound frequency. It was found that the particle concentration was increased at the sound pressure level greater than 100 dB and the sound frequency ranging from 100 Hz to 400 Hz. In the above sound wave frequency range, the particle concentration increased when the SPL was increased. However, acoustic field have slight effect on the particle concentration, and even disappeared when the sound frequency was below 100 Hz or greater than 400 Hz.
The time-series of the FCC particle concentrations were measured by an optical fiber probe under different superficial gas velocities, sound pressure levels and frequencies in an acoustic fluidized bed. It was demonstrated that the minimum fluidization velocity has a minimum value when the frequency of sound waves was 150 Hz, and it decreased as the sound pressure level was increased at the same sound frequency. Local particle concentration fluctuations was analyzed using both traditional statistical analysis and power spectrum analysis. The standard variance of local particle concentration was lower in an acoustic fluidized bed than in a common fluidized bed. In an acoustic fluidized bed, the frequency of power spectra tends to be width. With increasing the sound pressure level, the dominant frequency of the power spectrum was decreased. The dominant frequency of the power spectrum decreased first and then increased with increasing the sound frequency at the same sound pressure level. On basis of discrete wavelet transform, an original signal was resolved into five detailed scale signals (from detailed scale 1 to detailed scale 5). The results showed that high frequency was increased and low frequency was decreased in an acoustic fluidized bed. The bubbling frequency and bubble size decreased with increasing sound pressure level at a given frequency, the bubbling frequency and bubble size decreased with increasing sound frequency ranging from 50～150 Hz, but further increased with increasing sound frequency ranging from 150～500 Hz.
The fluidization behavior of binary mixtures of biomass and quartz sand has been investigated using pressure sampling system in a bubbling fluidized bed (Φ53 mm×800 mm). The biomass component was difficult to fluidize, while the mixture of quartz sand and biomass can fluidize smoothly. As the biomass content of binary mixtures was increased, the minimum fluidization velocity of the binary mixtures also increased. The effects of sound frequency, and sound pressure level on the fluidization behavior of binary mixtures were investigated in this work. It was observed that sound waves improved the fluidization of the high weight percentage of biomass in an acoustic fluidized bed. The minimum fluidization velocity decreased with an increase in sound pressure level at the same sound frequency. Note that the minimum fluidization velocity has a minimum value when the frequency of sound waves increased from 50～400 Hz at a fixed sound pressure level.
A cold model of an acoustic jetting fluidized bed was employed to study the jet penetration depth and the radial and axial profiles of particle concentrations. An optical fiber probe was developed to investigate the jet penetration depth. Experimental results indicated that the jet penetration depth increased with increasing fluidizing numbers, jet nozzle diameter and jet velocity. With increasing the particle diameter and particle density, the jet penetration depth decreased. Based on experimental data, two new empirical correlations for prediction of the jet penetration depth were presented, which were in good agreement with the experimental results from this study. The particle concentration was characterized by non-uniformly in radial and axial directions, with particle concentration low in fluidized bed center region and high near the wall region. With increasing fluidizing numbers and jet velocities, the particle concentration tends to be low.
在内径140 mm,高1600 mm的鼓泡流化床中,以FCC颗粒和石英砂颗粒为流化介质,采用光导纤维探针和差压变送器分别测定不同轴/径向位置的颗粒浓度信号和压力波动信号,考察外加声场对密相区颗粒浓度和压力脉动的影响。结果表明:声场的引入可以降低颗粒最小流化速度,声压级越大,最小流化速度越小;固定声压频率存在一个最佳频率范围颗粒最小流化速度最小。鼓泡床密相区FCC颗粒浓度沿轴向逐渐减小,沿径向呈抛物线分布。操作气速越大,FCC颗粒浓度越小。随着声压强度的增大,床层中心区和上部密相区FCC颗粒浓度增大。固定声压级,频率在100～400 Hz范围内FCC颗粒浓度较大,频率低于100 Hz或高于400 Hz时,声波的作用效果减弱。
通过统计分析、功率谱分析和小波分析揭示外加声场对颗粒浓度信号的影响。结果表明:颗粒浓度功率谱呈现宽频且有明显主频的低频信号,声压越大主频的峰值越小,颗粒浓度信号的主频峰值随频率先下降后上升。对颗粒浓度信号进行5尺度离散小波变换,声场流化床中颗粒浓度信号高频部分增加,低频部分减小。气泡尺寸和鼓泡频率随声压的增大而减小,随声波频率的增大先减小后增大。
在内径53 mm,高800 mm的声场鼓泡流化床中,采用压力探针研究生物质颗粒的流化特性,考察添加惰性组分和引入声场对生物质流化质量的影响。结果表明:添加惰性组分可以显著改善生物质流化质量,惰性组分质量分数越大流化质量越好。声场的引入可以使生物质在较高质量分数下实现流化,降低生物质颗粒的最小流化速度。声波强度越大,生物质颗粒的最小流化速度越小;固定声压级,在最佳频率范围内生物质颗粒最小流化速度最小。
以FCC和石英砂颗粒为流化介质,采用光导纤维探针考察声场和射流耦合对颗粒流化的影响。结果表明:射流深度随射流气速、流化数和射流管径的增大而增大,随床料平均粒径和密度的增加而减小,声场的引入可以增大射流深度。对实验数据进行多元线性回归分析,得到了声场射流流化床水平射流的射流深度关联式,关联式的预测值与实验值吻合得较好。颗粒浓度径向呈抛物线分布,沿轴向高度颗粒浓度逐渐增大,其中射流区颗粒浓度最小,射流气速和流化数越大颗粒浓度越小。声场的引入可以减小气泡尺寸,增大颗粒浓度,扩大射流区域范围。
Many approaches were developed to improve the fluidization behavior of particles, such as adding another kind of particles to the bed and introducing a magnetic field, acoustic field, or vibrating field. Among these methods, sound-assisted fluidization is particularly attractive because no internals are needed. The application of an acoustic field can improve the fluidization quality of fine powders.
The radial and axial profiles of the FCC particle concentrations were measured using an optical fiber probe under different superficial gas velocities, sound pressure levels and frequencies in an acoustic fluidized bed (Φ140 mm×1600 mm). Meanwhile, the effects of sound wave frequency and sound pressure level on the particle concentrations were examined in this work. Experimental results showed that the particle concentrations were distributed non-uniformly in radial and axial directions, with particle concentration lower in fluidized bed center region and higher near the wall region. With increasing the bed height, the particle concentration tended to be lower. As superficial gas velocity is increased, the particle concentration decreased. The minimum fluidization velocity has a minimum value when the frequency of sound waves approached 150 Hz, whereas it decreased as the sound pressure level was increased at the same sound frequency. It was found that the particle concentration was increased at the sound pressure level greater than 100 dB and the sound frequency ranging from 100 Hz to 400 Hz. In the above sound wave frequency range, the particle concentration increased when the SPL was increased. However, acoustic field have slight effect on the particle concentration, and even disappeared when the sound frequency was below 100 Hz or greater than 400 Hz.
The time-series of the FCC particle concentrations were measured by an optical fiber probe under different superficial gas velocities, sound pressure levels and frequencies in an acoustic fluidized bed. It was demonstrated that the minimum fluidization velocity has a minimum value when the frequency of sound waves was 150 Hz, and it decreased as the sound pressure level was increased at the same sound frequency. Local particle concentration fluctuations was analyzed using both traditional statistical analysis and power spectrum analysis. The standard variance of local particle concentration was lower in an acoustic fluidized bed than in a common fluidized bed. In an acoustic fluidized bed, the frequency of power spectra tends to be width. With increasing the sound pressure level, the dominant frequency of the power spectrum was decreased. The dominant frequency of the power spectrum decreased first and then increased with increasing the sound frequency at the same sound pressure level. On basis of discrete wavelet transform, an original signal was resolved into five detailed scale signals (from detailed scale 1 to detailed scale 5). The results showed that high frequency was increased and low frequency was decreased in an acoustic fluidized bed. The bubbling frequency and bubble size decreased with increasing sound pressure level at a given frequency, the bubbling frequency and bubble size decreased with increasing sound frequency ranging from 50～150 Hz, but further increased with increasing sound frequency ranging from 150～500 Hz.
The fluidization behavior of binary mixtures of biomass and quartz sand has been investigated using pressure sampling system in a bubbling fluidized bed (Φ53 mm×800 mm). The biomass component was difficult to fluidize, while the mixture of quartz sand and biomass can fluidize smoothly. As the biomass content of binary mixtures was increased, the minimum fluidization velocity of the binary mixtures also increased. The effects of sound frequency, and sound pressure level on the fluidization behavior of binary mixtures were investigated in this work. It was observed that sound waves improved the fluidization of the high weight percentage of biomass in an acoustic fluidized bed. The minimum fluidization velocity decreased with an increase in sound pressure level at the same sound frequency. Note that the minimum fluidization velocity has a minimum value when the frequency of sound waves increased from 50～400 Hz at a fixed sound pressure level.
A cold model of an acoustic jetting fluidized bed was employed to study the jet penetration depth and the radial and axial profiles of particle concentrations. An optical fiber probe was developed to investigate the jet penetration depth. Experimental results indicated that the jet penetration depth increased with increasing fluidizing numbers, jet nozzle diameter and jet velocity. With increasing the particle diameter and particle density, the jet penetration depth decreased. Based on experimental data, two new empirical correlations for prediction of the jet penetration depth were presented, which were in good agreement with the experimental results from this study. The particle concentration was characterized by non-uniformly in radial and axial directions, with particle concentration low in fluidized bed center region and high near the wall region. With increasing fluidizing numbers and jet velocities, the particle concentration tends to be low.
引文
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