Inﬂuence of the Application of a Sound Field on the Flow State Reduction of Newman Fine Iron Ore

: To improve the ﬂuidization of the ﬂuidized bed in ironmaking, the particle loss and bonding during the ﬂuidized bed are largely removed by changing the properties of the particle surface or by adding an external ﬁeld. Currently, the vibration, magnetic, sound, and electric ﬁelds have been commonly applied to provide external energy to the ﬂuidization bed systems. In this work, experiments are conducted for Newman ore particles under the application of an external sound ﬁeld at a reduction temperature of 1023 K, linear velocity of 0.6 m/s, duration of 60 min, pressure of 0.2 MPa, and typical mineral powder particle size of 80–100 mesh, with H 2 used as the reducing gas. The power and frequency of the ultrasonic ﬁeld are varied, and the effects of sound ﬁeld are evaluated by the comparative analysis of the effects of the sound ﬁeld with different powers of sound ﬁelds and application times on the metallization rate and binder ratio of the samples. The acoustic pressure and frequency were varied to determine the critical speed and inﬂuence on the bed and to study the interactions of the iron ore powder particles in the sound ﬁeld and the bonding mechanism of the particles. The results of this paper reproduce the actual particle ﬂuidization process and analysis of the interactions of the particles in the sound ﬁeld well. The inﬂuence of the external sound ﬁeld on the gas-solid ﬂow was studied from the perspective of macroscopic motion and force analysis.


Introduction
The promulgation and implementation of new environmental protection laws and the policy of reducing metallurgical production capacity poses a great challenge for the survival of smelting processes with high emissions, high energy consumption and high pollution. Additionally, the upsizing of blast furnaces and the strengthening of smelting lead to higher requirements for the quality of coke, giving rise to increasingly smaller room for decreasing the proportion of high-quality coking coal and other coking coal during coking and coal blending.
Due to the above considerations, fluidization technology has received increasing attention in the ironmaking industry. Fluidized bed ironmaking technology can directly use iron ore powder as the raw material to eliminate the process of coking and sintering. Thus, it is expected to realize the rational utilization of domestic composite cogeneration ore and reduce the dependence on imported iron ore [1][2][3]. At the same time, because the fluidization process does not require coke, it can reduce the dependence on coking coal and avoid the environmental pollution caused by coking. Fluidized bed ironmaking can also be used for the treatment of complex symbiotic iron ore. Fluidization enables good mixing of the gas and solid phases, which enhances the heat and mass transfer and improves kinetic conditions, leading to increased production efficiency and reduced environmental pollution [4][5][6]. However, the implementation of this process in the industry must still overcome the problem of the bonding of fine iron ore in the fluidized bed reduction process [7][8][9][10] that not only limits the improvement of the reduction rate of ore powder, but also affects the continuous operation of the process. The problem of bond loss not only deteriorates the dynamic condition of the fluidization process, but also affects its continuous operation and diminishes its advantages.
To improve the fluidization state and eliminate the above undesirable phenomena, researchers have mainly studied the following three aspects in recent years: optimization of the bed design (e.g., by adding various built-in accessories), modification of the material or addition of fluidized particles, and application of an external field to the fluidized bed (e.g., the vibrational, magnetic, sound, electric, and centrifugal fields). There exists some research on improving the fluidization quality of viscous particles by using a vibrational force field [11][12][13][14][15]. Mori et al. [15] first applied a new type of vibrated fluidized bed to study the vibration fluidization of single and multi-component fine particles. Zhu Qingshan, Li Hongzhong et al. [15] carried out experimental research on the fluidization mechanism of ultrafine particles in a magnetic field, and they found that the magnetic field could effectively eliminate the channel flow in the fluidized bed so that a stable fluidization operation could be realized. However, magnetic fluidization is only effective for ferromagnetic particles or mixed particles with ferromagnetic particles and not for nonferromagnetic particles. The introduction of a sound field can not only improve the mass transfer and heat transfer efficiency, but also significantly reduce the size of agglomerates and the initial fluidization velocity, thus significantly improving the fluidization quality. The present work focuses on the study of the reduction effect of Newman ore under the action of a sound field.

Experimental Materials
The reduced iron ore powder in this experiment was Newman ore and its chemical composition and scanning electron microscope diagram are shown in Table 1 and Figure 1, respectively. The size range of the selected Newman ore was 80-100 mesh. H 2 was used as the reducing gas, N 2 was used as the shielding gas, and the purity was 99.99%. T Fe is the total iron content.
Processes 2021, 9, x FOR PEER REVIEW 2 of 23 must still overcome the problem of the bonding of fine iron ore in the fluidized bed reduction process [7][8][9][10] that not only limits the improvement of the reduction rate of ore powder, but also affects the continuous operation of the process. The problem of bond loss not only deteriorates the dynamic condition of the fluidization process, but also affects its continuous operation and diminishes its advantages.
To improve the fluidization state and eliminate the above undesirable phenomena, researchers have mainly studied the following three aspects in recent years: optimization of the bed design (e.g., by adding various built-in accessories), modification of the material or addition of fluidized particles, and application of an external field to the fluidized bed (e.g., the vibrational, magnetic, sound, electric, and centrifugal fields). There exists some research on improving the fluidization quality of viscous particles by using a vibrational force field [11][12][13][14][15]. Mori et al. [15] first applied a new type of vibrated fluidized bed to study the vibration fluidization of single and multi-component fine particles. Zhu Qingshan, Li Hongzhong et al. [15] carried out experimental research on the fluidization mechanism of ultrafine particles in a magnetic field, and they found that the magnetic field could effectively eliminate the channel flow in the fluidized bed so that a stable fluidization operation could be realized. However, magnetic fluidization is only effective for ferromagnetic particles or mixed particles with ferromagnetic particles and not for nonferromagnetic particles. The introduction of a sound field can not only improve the mass transfer and heat transfer efficiency, but also significantly reduce the size of agglomerates and the initial fluidization velocity, thus significantly improving the fluidization quality. The present work focuses on the study of the reduction effect of Newman ore under the action of a sound field.

Experimental Materials
The reduced iron ore powder in this experiment was Newman ore and its chemical composition and scanning electron microscope diagram are shown in Table 1 and Figure  1, respectively. The size range of the selected Newman ore was 80-100 mesh. H2 was used as the reducing gas, N2 was used as the shielding gas, and the purity was 99.99%. TFe is the total iron content.

Experimental Equipment
The main device used in this study was a fluidized bed with an applied sound field (Shanghai in Chian Wuyi wy32003 signal generator) (Figures 2 and 3). It was mainly composed of a fluidized bed, acoustic duct, acoustic generation system, and test system. Double stainless steel tubes were used as the reactor in the fluidized bed, and the inner tube was a fluidized bed. The gas entered the fluidized bed after preheating through the interlayer space between the outer and the inner tubes. The outer tube contained a heating cabinet. The flow rates of CO, H 2 and N 2 were adjusted and controlled by multiple flow meters so that the gas entering the fluidized bed could meet the composition and linear velocity requirements of the experiment. The gas mass flow controller was used to control the flow at the inlet of the fluidized bed through the iron ore inner tube. The velocity of the fluidized bed inlet line was controlled by a gas mass flow controller, and the reduction temperature of the fluidized bed was measured by a thermocouple. Prior to the experiment, inert gas was introduced to check the air tightness of the device. The sound wave generating system consisted of a signal generator and a loudspeaker. The generator was used to obtain the positive dark wave of a specific frequency, which was amplified by a power amplifier and then sent to the loudspeaker to generate sound wave. The sound wave entered the fluidized bed through an acoustic waveguide. After each experiment, inert gas was added to protect the reduced ore powder from oxidation. To evaluate the fluidized reduction viscosity, a pressure sensor was used to measure the bed pressure difference ∆P, and the fluidized reduction viscosity was evaluated using an observation window.

Experimental Equipment
The main device used in this study was a fluidized bed with an applied sound field (Shanghai in Chian Wuyi wy32003 signal generator) (Figures 2 and 3). It was mainly composed of a fluidized bed, acoustic duct, acoustic generation system, and test system. Double stainless steel tubes were used as the reactor in the fluidized bed, and the inner tube was a fluidized bed. The gas entered the fluidized bed after preheating through the interlayer space between the outer and the inner tubes. The outer tube contained a heating cabinet. The flow rates of CO, H2 and N2 were adjusted and controlled by multiple flow meters so that the gas entering the fluidized bed could meet the composition and linear velocity requirements of the experiment. The gas mass flow controller was used to control the flow at the inlet of the fluidized bed through the iron ore inner tube. The velocity of the fluidized bed inlet line was controlled by a gas mass flow controller, and the reduction temperature of the fluidized bed was measured by a thermocouple. Prior to the experiment, inert gas was introduced to check the air tightness of the device. The sound wave generating system consisted of a signal generator and a loudspeaker. The generator was used to obtain the positive dark wave of a specific frequency, which was amplified by a power amplifier and then sent to the loudspeaker to generate sound wave. The sound wave entered the fluidized bed through an acoustic waveguide. After each experiment, inert gas was added to protect the reduced ore powder from oxidation. To evaluate the fluidized reduction viscosity, a pressure sensor was used to measure the bed pressure difference ∆P, and the fluidized reduction viscosity was evaluated using an observation window.

Experimental Scheme and Procedure
Prior to the start of the experiment, N2 was introduced into the fluidized bed. After the air was discharged, the outlet valve was closed, the pressure of the fluidized bed was increased to 0.5-0.6 MPa, and the air tightness of the equipment was checked. Then, the fluidized bed started to heat up. When the reduction temperature reached the target experimental temperature, the N2 valve was closed, and the reduction gas used in the experiment was passed through the system. During this process, the pressure was controlled by the tightness of the valve, and the experiment started when the pressure stabilized at the set pressure. In the experiment, the reduction temperature, linear velocity, pressure, and other related factors were set to the specified values, and the reduction experiment was carried out using H2 as the reducing gas. The metallization rate and bonding ratio of Newman ore for the process durations of 10, 20, 40 and 60 min were obtained with sound field power levels of 150, 300, 500 and 1000 W, respectively. We illustrated the experimental procedure, using the conditions of a sound field with an input power of 150 W and a duration of 10 min as an example. First, the fluidized bed was heated to the set temperature, and then the mineral powder (20 g) was weighed and added into the conical flask. After the temperature of the fluidized bed was reached, the air was discharged into the N2, and the air tightness of the device was checked. Then, data measurement software was used to adjust the gas flow rate, and at the same time, the H2 reducing gas was introduced to maintain the fluidized bed temperature at approximately 1023 K during the reduction, which was carried out for 60 min. A sound field with a power of 150 W was applied for 10 min, starting at approximately 20 min after the beginning of reduction. After the end of reduction, N2 was passed for 5 min to protect the ore powder from oxidation. After cooling to room temperature, the bonded and unbonded mineral powder in the fluidized bed was removed, and the bonding ratio was calculated. The adhesion ratio is the ratio of the binding mass of the reducing powder to the total mass of the reducing powder. A smaller adhesion ratio indicates better fluidization. Then, the reduced samples were analyzed by the potassium dichromate volumetric method and the ferric chloride titration method. Finally, the metallic iron (MFe) and total iron (TFe) contents and the metallization rate η were calculated. The metallization rate is calculated as follows: where η represents the metallization rate; MFe stands for metal iron (g); and TFe stands for total iron (g).

Experimental Scheme and Procedure
Prior to the start of the experiment, N 2 was introduced into the fluidized bed. After the air was discharged, the outlet valve was closed, the pressure of the fluidized bed was increased to 0.5-0.6 MPa, and the air tightness of the equipment was checked. Then, the fluidized bed started to heat up. When the reduction temperature reached the target experimental temperature, the N 2 valve was closed, and the reduction gas used in the experiment was passed through the system. During this process, the pressure was controlled by the tightness of the valve, and the experiment started when the pressure stabilized at the set pressure. In the experiment, the reduction temperature, linear velocity, pressure, and other related factors were set to the specified values, and the reduction experiment was carried out using H 2 as the reducing gas. The metallization rate and bonding ratio of Newman ore for the process durations of 10, 20, 40 and 60 min were obtained with sound field power levels of 150, 300, 500 and 1000 W, respectively. We illustrated the experimental procedure, using the conditions of a sound field with an input power of 150 W and a duration of 10 min as an example. First, the fluidized bed was heated to the set temperature, and then the mineral powder (20 g) was weighed and added into the conical flask. After the temperature of the fluidized bed was reached, the air was discharged into the N 2 , and the air tightness of the device was checked. Then, data measurement software was used to adjust the gas flow rate, and at the same time, the H 2 reducing gas was introduced to maintain the fluidized bed temperature at approximately 1023 K during the reduction, which was carried out for 60 min. A sound field with a power of 150 W was applied for 10 min, starting at approximately 20 min after the beginning of reduction. After the end of reduction, N 2 was passed for 5 min to protect the ore powder from oxidation. After cooling to room temperature, the bonded and unbonded mineral powder in the fluidized bed was removed, and the bonding ratio was calculated. The adhesion ratio is the ratio of the binding mass of the reducing powder to the total mass of the reducing powder. A smaller adhesion ratio indicates better fluidization. Then, the reduced samples were analyzed by the potassium dichromate volumetric method and the ferric chloride titration method. Finally, the metallic iron (M Fe ) and total iron (T Fe ) contents and the metallization rate η were calculated. The metallization rate is calculated as follows: where η represents the metallization rate; M Fe stands for metal iron (g); and T Fe stands for total iron (g). The bonding ratio is calculated as follows: In the formula, M total is the total quantity of the reduced materials, which is used to evaluate the quality of the reduced total materials of fine iron ore (g); Ω is the binding ratio; and M sticking refers to the amount of reduced adhesive substance, which is used to evaluate the quality of the reduced adhesive substance of fine iron ore (g).
The total mass of the material after reduction can be calculated as follows: In order to reduce the experimental error, we repeated the measurement twice and finally took the average value as the final experimental result. The pressure in the experiment was not expressed as an absolute value, and the atmosphere was set to 0 MPa. Because of the five factors of fine iron ore powder caking flow loss-the reduction temperature, reduction time and reduction pressure, reduction of the gas linear velocity, and pressure reduction gas species-through the orthogonal experiment, we concluded that a reduction temperature of 1023 k, linear velocity of 0.6 m/s, reduction time of 60 min, reduction pressure of 0.2 MPa, and reducing gas of H 2 were the optimal operating parameters, which we used to analyze the bonding mechanism of fine iron ore and the influence of the sound field on the cohesive force of the Newman mine flow loss.
A higher metallization rate indicates better quality of the reduced ore powder. Therefore, the metallization rate and adhesion ratio were selected as the indices to determine the fluidized reduction effect.

Influence of the Acoustic Power on the Reduction of Iron Ore Powder
Under the reduction temperature of 1023 K, linear velocity of 0.6 m/s, reduction time of 60 min, standard pressure, H 2 as the reducing gas, and the absence of a sound field, the metallization rate of the Newman ore and the bond ratio were obtained as 58.97% and 45.39%, respectively. The measured metallization rate and bond ratio obtained with the addition of sound fields of different powers and times are shown in Tables 2 and 3. An examination of the data presented in Tables 2 and 3 shows that upon the addition of the sound field, the metallization rate of the Newman ore increased slightly, while the As can be observed from Figure 4, after the addition of the sound field, the metallization rate of the Newman ore increased, but the increase was small, and a few samples even showed a decreased metallization rate. Moreover, the metallization rate of the Newman ore with different power sound fields showed fluctuations with respect to the ultrasonication time such that no meaningful systematic dependence on the ultrasonication time could be deduced from the data. Therefore, it can be concluded that the sound field had little effect on the metallization rate of the Newman ore.  As can be observed from Figure 4, after the addition of the sound field, the metallization rate of the Newman ore increased, but the increase was small, and a few samples even showed a decreased metallization rate. Moreover, the metallization rate of the Newman ore with different power sound fields showed fluctuations with respect to the ultrasonication time such that no meaningful systematic dependence on the ultrasonication time could be deduced from the data. Therefore, it can be concluded that the sound field had little effect on the metallization rate of the Newman ore. As can be observed from Figure 4, after the addition of the sound field, the metallization rate of the Newman ore increased, but the increase was small, and a few samples even showed a decreased metallization rate. Moreover, the metallization rate of the Newman ore with different power sound fields showed fluctuations with respect to the ultrasonication time such that no meaningful systematic dependence on the ultrasonication time could be deduced from the data. Therefore, it can be concluded that the sound field had little effect on the metallization rate of the Newman ore.  Based on the analysis of Figures 5 and 6, the following conclusions can be drawn: (1) The sound field significantly improved the fluidized state of the fluidized bed, and the bond ratio of the ore powder decreased strongly from 45.39% to less than 30%. (2) The optimal application time of the sound field was between 20 and 40 min. For the addition of the 150, 300, 500, and 1000 W sound fields, the optimal times were approximately 33, 25, 25, and 20 min, respectively. After the duration of the sound field application exceeded the optimal time, the bond ratio rose slightly. (3) Better results were obtained with the application of greater sound field power, with the bond ratio of the Newman mine ore decreasing monotonically with the increasing power of the sound field. However, the reduction of the bond ratio was small for powers greater than 500 W. In practical production, considering the economic cost, the sound field power should be set to approximately 500 W.

Influence of the Acoustic Frequency on the Fluidization Characteristics of Iron Ore Powder Particles
The acoustic frequency is also an important parameter affecting the particle fluidization quality in an acoustic fluidized bed. When an acoustic wave travels in a fluidized bed, the cross-sectional area of the bed is very small compared with that of a sphere centered around a loudspeaker, and the acoustic wave can be regarded as a plane wave. The effect of the acoustic frequency on the fluidized bed particle concentration is more complex. First, the attenuation of the acoustic wave in the medium is related not only to the frequency, but also to the temperature and pressure of the atmosphere. Acoustic attenuation can be calculated using Equations (4) and (5): where α is the attenuation caused by acoustic absorption in dB/100m; T is the absolute temperature in K; P* is the relative atmospheric pressure; μmaximum is the maximum Based on the analysis of Figures 5 and 6, the following conclusions can be drawn: (1) The sound field significantly improved the fluidized state of the fluidized bed, and the bond ratio of the ore powder decreased strongly from 45.39% to less than 30%. (2) The optimal application time of the sound field was between 20 and 40 min. For the addition of the 150, 300, 500, and 1000 W sound fields, the optimal times were approximately 33, 25, 25, and 20 min, respectively. After the duration of the sound field application exceeded the optimal time, the bond ratio rose slightly. (3) Better results were obtained with the application of greater sound field power, with the bond ratio of the Newman mine ore decreasing monotonically with the increasing power of the sound field. However, the reduction of the bond ratio was small for powers greater than 500 W. In practical production, considering the economic cost, the sound field power should be set to approximately 500 W.

Influence of the Acoustic Frequency on the Fluidization Characteristics of Iron Ore Powder Particles
The acoustic frequency is also an important parameter affecting the particle fluidization quality in an acoustic fluidized bed. When an acoustic wave travels in a fluidized bed, the cross-sectional area of the bed is very small compared with that of a sphere centered around a loudspeaker, and the acoustic wave can be regarded as a plane wave. The effect of the acoustic frequency on the fluidized bed particle concentration is more complex. First, the attenuation of the acoustic wave in the medium is related not only to the frequency, but also to the temperature and pressure of the atmosphere. Acoustic attenuation can be calculated using Equations (4) and (5): where α is the attenuation caused by acoustic absorption in dB/100 m; T is the absolute temperature in K; P* is the relative atmospheric pressure; µ maximum is the maximum intensity loss per wavelength; f r is the relaxation frequency with great loss per unit wavelength (Hz); and f is the frequency of the sound wave in Hz.
According to Equations (4) and (5), the attenuation increases and the sound pressure decreases with a higher acoustic frequency, which is not conducive to enhanced fluidization due to the sound field. The increase in the frequency will increase the acceleration of medium particles and particle vibrations and will promote the overcoming of the attractive interparticle forces. Therefore, assuming that attenuation factors are taken into account and sound pressure levels of a sufficient intensity are maintained, an increased acoustic frequency is conducive to reducing the bubble size and obtaining more uniform particle dispersion.
For a sound pressure level of 100 dB and acoustic frequencies in the 50-500 Hz range, the relationship between the minimum fluidization velocity and acoustic frequency is shown in Table 4 and Figure 7. It was observed that the minimum fluidization velocity was the lowest for the frequency of approximately 150 Hz, and the minimum fluidization velocity increased for frequencies higher or lower than 150 Hz. This is mainly because when the frequency of a sound wave is too low, the vibration period is too long, which causes the particles to quickly restore the bond after the initial disturbance. When the frequency is too high, the vibration period is too short, which causes the particles to not follow, both of which weaken the effect of the sound wave and even have no effect when the frequency is too low or too high. When the frequency changes in the range of 150 Hz, the fluidization of ultrafine particles in the process of fluidization has been eliminated, while channeling, surge, and other fluidization phenomenon can achieve complete fluidization, and the fluidization quality is very good. However, when the frequency is lower than or higher than 150 Hz, the fluidization phenomena such as piston flow and flow channel appear in the process of fluidization, and the fluidization quality decreases. Therefore, there is an optimal range of the influence of the frequency on particle fluidization. If the frequency is too high or too low, the effect of the sound waves will be reduced or even eliminated entirely.
Processes 2021, 9, x FOR PEER REVIEW 8 of 21 intensity loss per wavelength; fr is the relaxation frequency with great loss per unit wavelength (Hz); and f is the frequency of the sound wave in Hz. According to Equations (4) and (5), the attenuation increases and the sound pressure decreases with a higher acoustic frequency, which is not conducive to enhanced fluidization due to the sound field. The increase in the frequency will increase the acceleration of medium particles and particle vibrations and will promote the overcoming of the attractive interparticle forces. Therefore, assuming that attenuation factors are taken into account and sound pressure levels of a sufficient intensity are maintained, an increased acoustic frequency is conducive to reducing the bubble size and obtaining more uniform particle dispersion.
For a sound pressure level of 100 dB and acoustic frequencies in the 50-500 Hz range, the relationship between the minimum fluidization velocity and acoustic frequency is shown in Table 4 and Figure 7. It was observed that the minimum fluidization velocity was the lowest for the frequency of approximately 150 Hz, and the minimum fluidization velocity increased for frequencies higher or lower than 150 Hz. This is mainly because when the frequency of a sound wave is too low, the vibration period is too long, which causes the particles to quickly restore the bond after the initial disturbance. When the frequency is too high, the vibration period is too short, which causes the particles to not follow, both of which weaken the effect of the sound wave and even have no effect when the frequency is too low or too high. When the frequency changes in the range of 150 Hz, the fluidization of ultrafine particles in the process of fluidization has been eliminated, while channeling, surge, and other fluidization phenomenon can achieve complete fluidization, and the fluidization quality is very good. However, when the frequency is lower than or higher than 150 Hz, the fluidization phenomena such as piston flow and flow channel appear in the process of fluidization, and the fluidization quality decreases. Therefore, there is an optimal range of the influence of the frequency on particle fluidization. If the frequency is too high or too low, the effect of the sound waves will be reduced or even eliminated entirely.    Figure 8 shows the distribution of the iron ore powder particles for a bed height of 130 mm, sound pressure of 100 dB, and frequency variation from 50 to 500 Hz. It is observed from the figure that the acoustic frequency had no obvious effect on the particle concentration in the bed wall area. There was an optimal frequency range for the effect on the particle concentration in the central region. When the frequency varied from 100 Hz to 400 Hz, the particle dispersion in the center area was more uniform, the bubble size was smaller, and the particle concentration was larger. When the frequency was higher than 400 Hz or lower than 100 Hz, the acoustic wave had no effect on the particle concentration distribution.  Figure 8 shows the distribution of the iron ore powder particles for a bed height of 130 mm, sound pressure of 100 dB, and frequency variation from 50 to 500 Hz. It is observed from the figure that the acoustic frequency had no obvious effect on the particle concentration in the bed wall area. There was an optimal frequency range for the effect on the particle concentration in the central region. When the frequency varied from 100 Hz to 400 Hz, the particle dispersion in the center area was more uniform, the bubble size was smaller, and the particle concentration was larger. When the frequency was higher than 400 Hz or lower than 100 Hz, the acoustic wave had no effect on the particle concentration distribution.  Figures 9 and 10 show the pressure drop and expansion curves of the fine iron ore powder particles in the fluidization in the absence of a sound field. As can be observed from Figure 9, after gas entered the bed, the bed pressure drop would initially rise rapidly due to the poor permeability of the ultrafine powder. After rising to a certain height, the piston was destroyed and fell onto the distribution plate in a block shape. Gas flowed through the gap between the blocks, forming the groove flow, and the bed pressure drop reached the minimum value. Then, the pressure drop increased slightly, indicating that the gully flow was stable during this period of time. At the same time, we also observed from Figure 10 that the bed height did not change much within this range of the gas velocity. Continuing to increase the gas velocity due to the action of the airflow, the powder would form small clusters in the trench flow, and the bed pressure drop rose. When the gas velocity exceeded approximately 80 mm·s −1 , all of the material was fluidized, and the pressure drop did not change, but the bed pressure was reduced to the theoretical pressure due to the removal of the powder. The results show that in the absence of the sound field, the fluidization process of the iron ore powder was similar to that of the other ultrafine powders and still proceeded through the three stages of piston flow, channel flow, and agglomeration fluidization.  Figure 9, after gas entered the bed, the bed pressure drop would initially rise rapidly due to the poor permeability of the ultrafine powder. After rising to a certain height, the piston was destroyed and fell onto the distribution plate in a block shape. Gas flowed through the gap between the blocks, forming the groove flow, and the bed pressure drop reached the minimum value. Then, the pressure drop increased slightly, indicating that the gully flow was stable during this period of time. At the same time, we also observed from Figure 10 that the bed height did not change much within this range of the gas velocity. Continuing to increase the gas velocity due to the action of the airflow, the powder would form small clusters in the trench flow, and the bed pressure drop rose. When the gas velocity exceeded approximately 80 mm·s −1 , all of the material was fluidized, and the pressure drop did not change, but the bed pressure was reduced to the theoretical pressure due to the removal of the powder. The results show that in the absence of the sound field, the fluidization process of the iron ore powder was similar to that of the other ultrafine powders and still proceeded through the three stages of piston flow, channel flow, and agglomeration fluidization.   Figure 11 shows the pressure fall-velocity and the expansion rate-velocity curves of the fine iron ore particles in fluidization for the acoustic frequency of 120 Hz and the sound pressures of 121, 131, and 135 dB. Under the above conditions, due to the addition of acoustic waves, there was no piston flow in the fluidization process, and the channel flow was well suppressed or even eliminated. As observed from the figure, except for the sound pressure of 121 dB, the gully flow was absent when the sound pressure was greater than 130 dB. A comparison of Figures 9 and 11 clearly shows that the introduction of an acoustic wave significantly reduced the minimum fluidization velocity of the particles,   Figure 11 shows the pressure fall-velocity and the expansion rate-velocity curves of the fine iron ore particles in fluidization for the acoustic frequency of 120 Hz and the sound pressures of 121, 131, and 135 dB. Under the above conditions, due to the addition of acoustic waves, there was no piston flow in the fluidization process, and the channel flow was well suppressed or even eliminated. As observed from the figure, except for the sound pressure of 121 dB, the gully flow was absent when the sound pressure was greater than 130 dB. A comparison of Figures 9 and 11 clearly shows that the introduction of an acoustic wave significantly reduced the minimum fluidization velocity of the particles,  Figure 11 shows the pressure fall-velocity and the expansion rate-velocity curves of the fine iron ore particles in fluidization for the acoustic frequency of 120 Hz and the sound pressures of 121, 131, and 135 dB. Under the above conditions, due to the addition of acoustic waves, there was no piston flow in the fluidization process, and the channel flow was well suppressed or even eliminated. As observed from the figure, except for the sound pressure of 121 dB, the gully flow was absent when the sound pressure was greater than 130 dB. A comparison of Figures 9 and 11 clearly shows that the introduction of an acoustic wave significantly reduced the minimum fluidization velocity of the particles, and the turning point of the pressure drop curve was sharper, indicating that the size of agglomeration was greatly reduced and uniform after the introduction of acoustic waves.

Influence of the Sound Pressure on the Fluidization Characteristics of the Iron Ore Powder Particles
Processes 2021, 9, x FOR PEER REVIEW 11 of 21 and the turning point of the pressure drop curve was sharper, indicating that the size of agglomeration was greatly reduced and uniform after the introduction of acoustic waves.

Fluidization Characteristics
Levy et al. [16] concluded that acoustic waves can stimulate the vibration of bed materials, enhance the force between the particles to help destroy large clusters, and promote the stable fluidization of the bed. They analyzed the distribution law of the particle concentration in a fluidized bed under the application of a sound field and the effects of the operating gas velocity, as well as the effects of the intensity and frequency of the applied sound field on the particle concentration. It was found that with increasing sound pressure, the vibration velocity of the airflow and the shear action increase, the initial fluidization velocity of particles decreases significantly, and the bed is easy to fluidize. With the increasing acoustic frequency, the minimum fluidization velocity first decreases and then increases. For a low sound wave frequency, the vibration period is long, and the bed is affected by isolated rather than continuous sound waves. The increase in the frequency will increase the vibration acceleration of medium particles, weaken the interparticle forces, and help to reduce the bubble size. A larger sound pressure corresponds to a greater amplitude of acoustic wave vibration and airflow vibration velocity. This leads to larger particle displacement per unit of time, a smaller bubble size, higher bubble disintegration and regeneration frequencies, and a higher particle concentration. Increasing the sound pressure level can also reduce the uplift of fine particles [17].

Energy Transfer
Herrera and Levy [18] used a one-dimensional virtual fluid to simulate constant velocity acoustic waves and theoretically described the transmission of standing waves through the whole bed. Guo et al. [19] experimentally studied the influence of the acoustic frequency and acoustic pressure level on the fluidization state of nano and microparticles and predicted the influence of acoustic waves on the change of the agglomeration size through the energy conservation equation.
According to the Stokes-Kirchhoff formula [20], the absorption coefficient of a sound wave is proportional to the square of the sound wave frequency. As the frequency increases, the acoustic attenuation increases, and the acoustic energy acting on the particles decreases. Guo et al. [19] pointed out that the transmission of sound energy depends on a momentum exchange. The energy produced by sound waves increases with the increasing sound pressure, and therefore, a higher sound pressure is more conducive to the particle vibration acceleration. With the increase in the sound pressure level, the size of the particle clusters decreases. It was also found that the particle size decreases with the increasing acoustic frequency when the acoustic frequency is lower than the critical

Fluidization Characteristics
Levy et al. [16] concluded that acoustic waves can stimulate the vibration of bed materials, enhance the force between the particles to help destroy large clusters, and promote the stable fluidization of the bed. They analyzed the distribution law of the particle concentration in a fluidized bed under the application of a sound field and the effects of the operating gas velocity, as well as the effects of the intensity and frequency of the applied sound field on the particle concentration. It was found that with increasing sound pressure, the vibration velocity of the airflow and the shear action increase, the initial fluidization velocity of particles decreases significantly, and the bed is easy to fluidize. With the increasing acoustic frequency, the minimum fluidization velocity first decreases and then increases. For a low sound wave frequency, the vibration period is long, and the bed is affected by isolated rather than continuous sound waves. The increase in the frequency will increase the vibration acceleration of medium particles, weaken the interparticle forces, and help to reduce the bubble size. A larger sound pressure corresponds to a greater amplitude of acoustic wave vibration and airflow vibration velocity. This leads to larger particle displacement per unit of time, a smaller bubble size, higher bubble disintegration and regeneration frequencies, and a higher particle concentration. Increasing the sound pressure level can also reduce the uplift of fine particles [17].

Energy Transfer
Herrera and Levy [18] used a one-dimensional virtual fluid to simulate constant velocity acoustic waves and theoretically described the transmission of standing waves through the whole bed. Guo et al. [19] experimentally studied the influence of the acoustic frequency and acoustic pressure level on the fluidization state of nano and microparticles and predicted the influence of acoustic waves on the change of the agglomeration size through the energy conservation equation.
According to the Stokes-Kirchhoff formula [20], the absorption coefficient of a sound wave is proportional to the square of the sound wave frequency. As the frequency increases, the acoustic attenuation increases, and the acoustic energy acting on the particles decreases. Guo et al. [19] pointed out that the transmission of sound energy depends on a momentum exchange. The energy produced by sound waves increases with the increasing sound pressure, and therefore, a higher sound pressure is more conducive to the particle vibration acceleration. With the increase in the sound pressure level, the size of the particle clusters decreases. It was also found that the particle size decreases with the increasing acoustic frequency when the acoustic frequency is lower than the critical frequency and increases with the increasing acoustic frequency when the acoustic frequency is greater than the critical frequency. The acoustic energy in an acoustic field-assisted fluidized bed can be calculated by the following formula [18]: Roy et al. [21] studied the transmission of sound waves in a fluidized bed and obtained the natural frequency f n of the particle vibration: where L is the height of the static bed, R is the gas constant (286.7 J/(kg·K)), T is the absolute temperature of the fluidized bed (assumed to be 298 K), and ρ g and p p are the densities of the gas and particles, respectively, and are 1.185 kg/m 3 and 2500 kg/m 3 , respectively. The bed voidage ε b is 0.4. For 10 µm particles, the resonant frequency is approximately 100 Hz. When the sound wave frequency is greater than the resonant frequency, the attenuation coefficient of the sound wave in the fluidized bed increases significantly with the increasing frequency, and the sound pressure decreases rapidly.

External Force of Iron Ore Powder Particles in the Sound Field
The difference between the fluidized fine particles of the iron ore powder and the common granular materials is that the particles are small and there is a very strong attractive force between the particles. Therefore, to understand the fluidized characteristics of the fine particles and the bonding and agglomeration behavior in the fluidized bed, it is necessary to analyze the interaction between the particles in depth.

Viscous Force
In the gas-solid fluidized system, the small size and physical properties of particles make it necessary to consider the Van der Waals force between the particles in the analysis of particle interactions. For the two-dimensional numerical simulation study, the following assumptions were made: (1) The gas was a dry gas, and the particles were dry particles. Therefore, the liquid bridging force, electrophoresis force, and electrostatic force between particles were not considered. (2) In the calculation of the viscous force between the particle and the wall, only the Van der Waals interactions between the particle and the upper, lower, left, and right walls were considered, and the viscous force between the particle and the front and rear walls was ignored [22].
The Van der Waals force between particle I and particle J is calculated as The Van der Waals force between particle I and the wall is calculated as In the formula, Ha is the Hamaker constant, usually in the order of 10 −20 J, h ij is the distance between the surface of particle I and particle j, and h iw is the distance between the surface of particle I and the wall: (11) It is observed from the above formula that the Van der Waals force is related to the particle-particle or particle-wall distance. Since H ij or H iw is in the denominator, if its value is close to zero, the viscous force will be infinite, and the particle bonding is not in agreement with the experimental data. Therefore, the minimum distance h ij or h iw , when no bonding occurs between cohesive particles, is set as the shear distance or separation distance, usually 4.0 × 10 −10 m. When the particle-particle distance or particle-wall distance is less than the shear distance and particle collision deformation occurs, the viscous force is no longer calculated according to the Van der Waals formula; rather, the surface viscous force model is adopted: where γ is the surface energy constant per unit area: In the formula, h ct is the shear distance, which is 4.0 × 10 −10 m. Therefore, the viscous force between particles and between particles and the wall surface is, as shown in Figure 12, the following: Processes 2021, 9, x FOR PEER REVIEW 13 of 21 It is observed from the above formula that the Van der Waals force is related to the particle-particle or particle-wall distance. Since Hij or Hiw is in the denominator, if its value is close to zero, the viscous force will be infinite, and the particle bonding is not in agreement with the experimental data. Therefore, the minimum distance hij or hiw, when no bonding occurs between cohesive particles, is set as the shear distance or separation distance, usually 4.0 × 10 −10 m. When the particle-particle distance or particle-wall distance is less than the shear distance and particle collision deformation occurs, the viscous force is no longer calculated according to the Van der Waals formula; rather, the surface viscous force model is adopted: where γ is the surface energy constant per unit area: In the formula, hct is the shear distance, which is 4.0 × 10 −10 m. Therefore, the viscous force between particles and between particles and the wall surface is, as shown in Figure 12, the following:

Van der Waals forces
Van der Waals interactions give rise to mutual attraction between molecules. This force was first proposed by Van der Waals to explain the deviation of the behavior of gases from the ideal gas law under high pressure by assuming an attractive interaction between the gas molecules [23,24]. The following is a brief introduction to the calculation of the Van der Waals attraction:

Van der Waals forces
Van der Waals interactions give rise to mutual attraction between molecules. This force was first proposed by Van der Waals to explain the deviation of the behavior of gases from the ideal gas law under high pressure by assuming an attractive interaction between the gas molecules [23,24]. The following is a brief introduction to the calculation of the Van der Waals attraction: where A is the Hamaker constant, determined by material properties, hω is the Lifshitz constant, f s is the corresponding area, and Z 0 is the shortest distance between two solids. From the formula for the Van der Waals attraction, it can be seen that the particle spacing Z 0 is the most important parameter for determining the Van der Waals attraction between solids, and any effect that increases Z 0 will significantly reduce the viscous force, therefore affecting the fluidization behavior of the powder. Experiments have shown that Van der Waals forces are significant only when the particles are close enough together to be separated by molecular-scale distances (e.g., 0.2-1 nm) [25]. The factors affecting particle spacing can be divided into two categories: surface roughness and the use of isolators. a.
Effect of Surface Roughness A rough particle surface is a problem encountered in particle preparation, and its influence is only analyzed here. Figures 13 and 14  where A is the Hamaker constant, determined by material properties, hω is the Lifshitz constant, fs is the corresponding area, and Z0 is the shortest distance between two solids. From the formula for the Van der Waals attraction, it can be seen that the particle spacing Z0 is the most important parameter for determining the Van der Waals attraction between solids, and any effect that increases Z0 will significantly reduce the viscous force, therefore affecting the fluidization behavior of the powder. Experiments have shown that Van der Waals forces are significant only when the particles are close enough together to be separated by molecular-scale distances (e.g., 0.2-1 nm) [25]. The factors affecting particle spacing can be divided into two categories: surface roughness and the use of isolators. a.
Effect of Surface Roughness A rough particle surface is a problem encountered in particle preparation, and its influence is only analyzed here. Figures 13 and 14 represent different roughness conditions of the particles.  The surface of real particles is very complex, but for the effect of particle spacing, it can be divided into two categories. The first case is shown in Figure 13, where the surface roughness limits the proximity of two particles and makes the effective spacing larger. The second case is shown in Figure 14 and is completely opposite to the situation in Figure  13. By contrast, roughness makes particles come in closer contact, which may increase the overall Van der Waals force, such as at a high temperature. On the other hand, in the case of elastic deformation, although the contact surface is increased, the adhesive force will not increase because the particles will return to their original state once the adhesive is separated.

b. Use of Isolators
Isolators may be either small molecules attached to the interacting particles or small particles. The use of small molecule isolators enables the gas used to fluidize the powder to have an effect on convection, even when in the absence of capillary condensation. For the small particles used as isolators, the comparison between the size of the added fine particles and the fluidized particles plays the key role. When the size of the added particles is equal to the particle gap, the added particles can act as a bridge between adjacent particles, thus increasing their viscosity. When the addition of fine particles is properly selected to make the particles with larger particle spacing, the viscosity will also be where A is the Hamaker constant, determined by material properties, hω is the Lifshitz constant, fs is the corresponding area, and Z0 is the shortest distance between two solids. From the formula for the Van der Waals attraction, it can be seen that the particle spacing Z0 is the most important parameter for determining the Van der Waals attraction between solids, and any effect that increases Z0 will significantly reduce the viscous force, therefore affecting the fluidization behavior of the powder. Experiments have shown that Van der Waals forces are significant only when the particles are close enough together to be separated by molecular-scale distances (e.g., 0.2-1 nm) [25]. The factors affecting particle spacing can be divided into two categories: surface roughness and the use of isolators. a.
Effect of Surface Roughness A rough particle surface is a problem encountered in particle preparation, and its influence is only analyzed here. Figures 13 and 14 represent different roughness conditions of the particles.  The surface of real particles is very complex, but for the effect of particle spacing, it can be divided into two categories. The first case is shown in Figure 13, where the surface roughness limits the proximity of two particles and makes the effective spacing larger. The second case is shown in Figure 14 and is completely opposite to the situation in Figure  13. By contrast, roughness makes particles come in closer contact, which may increase the overall Van der Waals force, such as at a high temperature. On the other hand, in the case of elastic deformation, although the contact surface is increased, the adhesive force will not increase because the particles will return to their original state once the adhesive is separated.

b. Use of Isolators
Isolators may be either small molecules attached to the interacting particles or small particles. The use of small molecule isolators enables the gas used to fluidize the powder to have an effect on convection, even when in the absence of capillary condensation. For the small particles used as isolators, the comparison between the size of the added fine particles and the fluidized particles plays the key role. When the size of the added particles is equal to the particle gap, the added particles can act as a bridge between adjacent particles, thus increasing their viscosity. When the addition of fine particles is properly selected to make the particles with larger particle spacing, the viscosity will also be The surface of real particles is very complex, but for the effect of particle spacing, it can be divided into two categories. The first case is shown in Figure 13, where the surface roughness limits the proximity of two particles and makes the effective spacing larger. The second case is shown in Figure 14 and is completely opposite to the situation in Figure 13. By contrast, roughness makes particles come in closer contact, which may increase the overall Van der Waals force, such as at a high temperature. On the other hand, in the case of elastic deformation, although the contact surface is increased, the adhesive force will not increase because the particles will return to their original state once the adhesive is separated.

b. Use of Isolators
Isolators may be either small molecules attached to the interacting particles or small particles. The use of small molecule isolators enables the gas used to fluidize the powder to have an effect on convection, even when in the absence of capillary condensation. For the small particles used as isolators, the comparison between the size of the added fine particles and the fluidized particles plays the key role. When the size of the added particles is equal to the particle gap, the added particles can act as a bridge between adjacent particles, thus increasing their viscosity. When the addition of fine particles is properly selected to make the particles with larger particle spacing, the viscosity will also be reduced, and the otherwise difficult-to-fluidize particles will be fluidized. Therefore, the exact effect after the addition of fine particles depends on the specific system studied.

Electrostatic Force
Generally, when two solids come into contact, they can charge each other [26,27]. The contact potential difference between two solids is given by where ∅ 1 and ∅ 2 are two kinds of electron affinity for solid contact. The contact between solids will generate an electrostatic attraction between solids. In this case, due to the mutual attraction of induced charges, the attraction between charged particles and uncharged particles can be calculated by the classic Coulomb equation: where Q is the charge of the particle; R is the particle radius; Z is the adhesion distance; and ε 0 is the dielectric constant in the vacuum. For the latter contact charged case, such as between the particle and the bed wall, the calculation formula of the electrostatic attraction is [28] as follows: where ∆U is the contact potential difference.

Acoustic Force
We could first make the following assumptions: the sound pressure of the external sound field is far lower than the atmospheric pressure, the relationship between the parameters is linear, and the ultrasonic field is represented by plane wave propagation. Based on linear acoustics, the sound pressure level is expressed as [29] spl = 20lg µ ac √ 2µ ref (19) where spl is the sound pressure level in decibels, µ ref is the reference speed (4.83 × 10 −8 m/s), and µ ac is the acoustic velocity. The speed of sound increases exponentially with the sound pressure, as shown in Figure 15. Energy attenuation will occur when an acoustic wave propagates in a gas medium, and therefore, the one-dimensional damped wave propagation equation is adopted, as shown in Figure 16. In this equation, the classical attenuation coefficient is proportional to the square of the frequency, as shown in Equation (21). Taking the cosine propagation of the sound wave along the x-axis as an example, the particle velocity of the plane wave is given by µ ac (x, t) = u ac,max cos(ωt − kx + ϕ)e −αx (20) where µ ac,max is the peak velocity of the acoustic wave, α is the attenuation coefficient of the sound wave in the unit direction ω is the angular velocity, k is the wave number of the damped wave, ϕ is the phase angle, ρ is the density of the gas, and c 0 is the speed of sound at 15 degrees Celsius and one standard atmosphere. The order of magnitude of the general b value is usually 10 −5 kg/(m·s).  After the sound field is applied in the fluidized bed, the acoustic wave affects the state of convection in that the gas molecules propagate vibrationally from the position of the particles. Thus, the gas molecules can pick up the acoustic wave energy provided to the particle. Finally, the acoustic wave interacts with the particles. This force can be regarded as an aerodynamic force generated by the ultrasonic field, and the acoustic velocity is the additional pulsating velocity of the gas velocity. Therefore, the force can be calculated by the equation of the force between the gas and the particles [30].
If the particle is assumed to be in a state of stress equilibrium before the ultrasonic effect, the acoustic force can be expressed as follows: where vp is the volume of a single particle, μac is the acoustic velocity, vP is the particle velocity, and β is the gas-solid correlation coefficient. In the sound field, the relationship between the sound energy and sound pressure is shown as follows:  After the sound field is applied in the fluidized bed, the acoustic wave affects the state of convection in that the gas molecules propagate vibrationally from the position of the particles. Thus, the gas molecules can pick up the acoustic wave energy provided to the particle. Finally, the acoustic wave interacts with the particles. This force can be regarded as an aerodynamic force generated by the ultrasonic field, and the acoustic velocity is the additional pulsating velocity of the gas velocity. Therefore, the force can be calculated by the equation of the force between the gas and the particles [30].
If the particle is assumed to be in a state of stress equilibrium before the ultrasonic effect, the acoustic force can be expressed as follows: where vp is the volume of a single particle, μac is the acoustic velocity, vP is the particle velocity, and β is the gas-solid correlation coefficient. In the sound field, the relationship between the sound energy and sound pressure is shown as follows: After the sound field is applied in the fluidized bed, the acoustic wave affects the state of convection in that the gas molecules propagate vibrationally from the position of the particles. Thus, the gas molecules can pick up the acoustic wave energy provided to the particle. Finally, the acoustic wave interacts with the particles. This force can be regarded as an aerodynamic force generated by the ultrasonic field, and the acoustic velocity is the additional pulsating velocity of the gas velocity. Therefore, the force can be calculated by the equation of the force between the gas and the particles [30].
If the particle is assumed to be in a state of stress equilibrium before the ultrasonic effect, the acoustic force can be expressed as follows: where v p is the volume of a single particle, µ ac is the acoustic velocity, v P is the particle velocity, and β is the gas-solid correlation coefficient. In the sound field, the relationship between the sound energy and sound pressure is shown as follows: We can substitute Equation (19) into Equations (4)- (20) to obtain the relationship between the sound energy and sound velocity: It is observed from the above formula that the sound energy increases exponentially with the sound speed. This implies that when the sound energy is raised to a certain value, the growth range of the sound speed with the sound energy growth will be greatly reduced. It is found from Equation (24) that the acoustic force absorbed by the particle is directly proportional to the sound velocity. Therefore, it can be considered that when the sound field energy reaches a certain value, the influence of the sound field on the fluidization effect of the fluidized bed will be reduced, as shown in Figure 17.
We can substitute Equation (19) into Equations (4)- (20) to obtain the relationship between the sound energy and sound velocity: It is observed from the above formula that the sound energy increases exponentially with the sound speed. This implies that when the sound energy is raised to a certain value, the growth range of the sound speed with the sound energy growth will be greatly reduced. It is found from Equation (24) that the acoustic force absorbed by the particle is directly proportional to the sound velocity. Therefore, it can be considered that when the sound field energy reaches a certain value, the influence of the sound field on the fluidization effect of the fluidized bed will be reduced, as shown in Figure 17 The According to the experimental results and Equation (26), we could get the influence of different power on the fluidization effect, as shown in Figure 17. In the experiment, we measured the influence of four kinds of sound field power on the convection effect. It was found that when the power exceeded 500 W, the reduction of the bond ratio of the Newman ore was obviously decreased by increasing the sound field power. This is in agreement with the above theoretical analysis.

Breaking of the Cluster due to the Application of the Sound Field
Clusters are the main cause of bond flow loss. Clusters usually move as a whole under the action of acoustic waves [31]. Experiments show that at a certain apparent gas velocity, the viscous particles are fluidized in the form of clusters, and the clusters are broken after the introduction of acoustic fields. Therefore, cluster fragmentation can be used to illustrate fluidization characteristics, as shown in Figure 18. When the sound field is added, the particles will vibrate under the action of acoustic force, and the particles will collide with the air distribution plate, forming a high void area on the surface area of the air distribution plate. This helps the gas enter the bed and makes it easier for the air flow to blow up the bed. Deformation or even separation of the particles and aggregates will occur when the agglomerates collide or rub with the wall surface. Therefore, in this case, the bed can be regarded as an elastomer [32]. It is observed from Figure 18a that in the According to the experimental results and Equation (26), we could get the influence of different power on the fluidization effect, as shown in Figure 17. In the experiment, we measured the influence of four kinds of sound field power on the convection effect. It was found that when the power exceeded 500 W, the reduction of the bond ratio of the Newman ore was obviously decreased by increasing the sound field power. This is in agreement with the above theoretical analysis.

Breaking of the Cluster due to the Application of the Sound Field
Clusters are the main cause of bond flow loss. Clusters usually move as a whole under the action of acoustic waves [31]. Experiments show that at a certain apparent gas velocity, the viscous particles are fluidized in the form of clusters, and the clusters are broken after the introduction of acoustic fields. Therefore, cluster fragmentation can be used to illustrate fluidization characteristics, as shown in Figure 18. When the sound field is added, the particles will vibrate under the action of acoustic force, and the particles will collide with the air distribution plate, forming a high void area on the surface area of the air distribution plate. This helps the gas enter the bed and makes it easier for the air flow to blow up the bed. Deformation or even separation of the particles and aggregates will occur when the agglomerates collide or rub with the wall surface. Therefore, in this case, the bed can be regarded as an elastomer [32]. It is observed from Figure 18a that in the absence of a sound field, the particles are large and large agglomerates are formed while, as shown in Figure 18b, after the application of the sound field, the number of small particles clearly increases. This is because upon the application of the ultrasonic field, particles are acted on by an external force, breaking up the agglomerates into small particle clusters.
Processes 2021, 9, x FOR PEER REVIEW 18 of 21 absence of a sound field, the particles are large and large agglomerates are formed while, as shown in Figure 18b, after the application of the sound field, the number of small particles clearly increases. This is because upon the application of the ultrasonic field, particles are acted on by an external force, breaking up the agglomerates into small particle clusters. Whether or not a cluster is broken depends on the balance of forces acting on the cluster. For energy balance analysis, the following assumptions are made: (1) The agglomerates are spherical with a diameter da1, and (2) two clusters of the same size are formed after the cluster is broken.
In a viscous particle fluidized bed, the forces acting on the clusters are due to the laminar shear energy (Elam), the kinetic energy of the clusters (Ekin), and the acoustic field energy (Esou). All of these can break the cluster. When the sum of these three energies is equal to the cohesive energy of the cluster (Ecoh), the cluster is in equilibrium.
(1) Energy generated by laminar shear. In a low-speed fluidized bed, the agglomeration movement in the fluid is subjected to the shear action of the fluid on the agglomeration, and its energy expression [32] is where μ is the gas velocity and umf,a is the minimum fluidization velocity of the cluster.
(2) Kinetic energy of the cluster. Clusters have kinetic energy when moving in the fluid, and the expression is as follows: where, da1 is the aggregate diameter and ρa1 is the cluster density.
(3) Energy of the sound field. The propagation mode of the sound wave is simple harmonic, and the sound energy transfer in the sound field is carried out by momentum exchange. The medium of propagation is air. The acoustic field energy acting on the cluster [33] is where ω is the angular velocity; A is the amplitude; c is the speed of sound; and ρf is the fluid density.
(4) Energy required to break the cluster. When the particle cluster is broken from the middle, the cluster needs to overcome the work done on it by the viscous force. According to literature [34], it can be seen that Whether or not a cluster is broken depends on the balance of forces acting on the cluster. For energy balance analysis, the following assumptions are made: (1) The agglomerates are spherical with a diameter d a1 , and (2) two clusters of the same size are formed after the cluster is broken.
In a viscous particle fluidized bed, the forces acting on the clusters are due to the laminar shear energy (E lam ), the kinetic energy of the clusters (E kin ), and the acoustic field energy (E sou ). All of these can break the cluster. When the sum of these three energies is equal to the cohesive energy of the cluster (E coh ), the cluster is in equilibrium.
(1) Energy generated by laminar shear. In a low-speed fluidized bed, the agglomeration movement in the fluid is subjected to the shear action of the fluid on the agglomeration, and its energy expression [32] is E lam = 3πuu mf,a d a1 2 (27) where µ is the gas velocity and u mf,a is the minimum fluidization velocity of the cluster.
(2) Kinetic energy of the cluster. Clusters have kinetic energy when moving in the fluid, and the expression is as follows: where, d a1 is the aggregate diameter and ρ a1 is the cluster density.
(3) Energy of the sound field. The propagation mode of the sound wave is simple harmonic, and the sound energy transfer in the sound field is carried out by momentum exchange. The medium of propagation is air. The acoustic field energy acting on the cluster [33] is where ω is the angular velocity; A is the amplitude; c is the speed of sound; and ρ f is the fluid density. Figure 19. The relation between the intensity of the sound field and the diameter of the agglomeration.
The fluidization of iron ore powder is consistent with Equation (26). In a fluidized bed, the clusters reach dynamic equilibrium. It is observed from Equation (32) that in addition to the effect of the fluidized bed itself on particle agglomerations, the effect of the sound field on agglomerations is also obvious. When the sound field frequency is fixed, with the increase of the sound field power, the intensity of the sound field per unit area of agglomerated iron ore powder increases, the agglomerate diameter decreases, and the iron ore powder fluidizes, which is consistent with Equation (26). As can be seen from the Figure 19, as the diameter of the particle clusters decreases, the number of air molecules impacting on the surface of the clusters decreases, and the acoustic field energy obtained from the clusters decreases and is lower than the acoustic energy required to break up the particles. At a certain frequency, different SPL values correspond to different maximum cluster diameters. A larger SPL corresponds to smaller cluster diameters and promotes bed fluidization. Conversely, a smaller SPL leads to a larger agglomerate diameter and hinders bed fluidization. It can be seen that the application of a sound field in the reduction process of iron ore powder can effectively reduce the bond loss and improve the fluidization quality. The fluidization of iron ore powder is consistent with Equation (26). In a fluidized bed, the clusters reach dynamic equilibrium. It is observed from Equation (32) that in addition to the effect of the fluidized bed itself on particle agglomerations, the effect of the sound field on agglomerations is also obvious. When the sound field frequency is fixed, with the increase of the sound field power, the intensity of the sound field per unit area of agglomerated iron ore powder increases, the agglomerate diameter decreases, and the iron ore powder fluidizes, which is consistent with Equation (26). As can be seen from the Figure 19, as the diameter of the particle clusters decreases, the number of air molecules impacting on the surface of the clusters decreases, and the acoustic field energy obtained from the clusters decreases and is lower than the acoustic energy required to break up the particles. At a certain frequency, different SPL values correspond to different maximum cluster diameters. A larger SPL corresponds to smaller cluster diameters and promotes bed fluidization. Conversely, a smaller SPL leads to a larger agglomerate diameter and hinders bed fluidization. It can be seen that the application of a sound field in the reduction process of iron ore powder can effectively reduce the bond loss and improve the fluidization quality.