# Numerical Simulation of the Tar Mist and Dust Movement Process in a Low-Temperature Dry Distillation Furnace

Authors: Qiuli Zhang; Xiangrong Hui; Long Yan; Min Luo; Wenru Feng; Jun Zhou; Xinzhe Lan
Journal: Journal of Chemistry
 (2020)

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## Abstract

In the low-temperature dry distillation of low-rank coal, the important liquid product of coal tar is produced, but its quality and utilization rate are degraded by entrained dust. The movement of coal tar and dust in the furnace is a key factor in causing particles such as dust to mix with coal tar. Therefore, the Euler–Lagrangian method is used to simulate the two-phase motion process of gas, tar, and dust in a furnace. By considering the effects of tar particle size, dust particle size, gas velocity, tar density, and dust density, the motion process mechanism is revealed, enabling the dust content in coal tar to be reduced and the quality improved. The results indicate that tar particles with sizes less than 0.20 mm can be removed from the furnace by gas, and the smaller the particle size is, the shorter the time required for removal. Dust particles greater than 0.18 mm in size cannot be completely removed from the furnace. As the gas velocity increases, the time required for complete removal of the tar mist and dust gradually decreases. When the speed is 0.70 m/s, all tar mist is removed, although some particles remain. Tar mist with a density of more than 900 kg/m3 can be extensively removed, but dust with a density of more than 1400 kg/m3 is difficult to remove and remains in the furnace. Finally, particle size distribution experiments in the product were conducted to verify the accuracy of the numerical simulation.


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## Body

## 1. Introduction

China’s coal resources are relatively abundant, and its reserves account for approximately 90% of the country’s mineral resource reserves and 95% of its fossil energy, with significant resource potential [1]. Moreover, the country’s coal resources include coal types from lignite to anthracite in various coalification stages, especially low-rank reserves that account for more than 40% of coal reserves and occupy a vital position in China’s coal resources [2, 3]. Coal accounts for approximately 72% of the country’s total energy consumption, and China’s coal-based energy structure is expected to remain stable for a long time [4].China’s northern Shaanxi region is rich in coal resources, with proven reserves of 146 billion tons. These resources are dominated by low-rank long-flame coal, which has a high oil content (average 6% to 7%) and has the characteristics of “three lows and one high” (low ash, low sulfur, low phosphorus, and high calorific value). This coal is an ideal raw material for low-temperature retorting [5]. Coal dry distillation is a necessary process for coal conversion processes such as coal liquefaction [6], gasification [7], combustion, and coking [8]. In addition, coal dry distillation is an efficient, low-pollution coal classification and conversion technology [9–11]; the gas produced during the dry distillation process can be used as a fuel and industrial raw material [12], and semicoke can be used in the metallurgical industry, syngas production, and other fields [13]. The phenols and hydrocarbons rich in coal tar become important raw chemical materials after separation and purification [14]; moreover, this material can partially replace oil and optimize the energy allocation of the petrochemical industry. China’s crude oil storage is small, and China has long relied on imports. Therefore, improving the production and quality of coal tar during low-temperature dry distillation can partially alleviate China’s petroleum energy crisis and substantially augment China’s reserve oil.In the low-temperature dry distillation process, the furnace type adopted in the northern part of Shaanxi is mainly an SJ-type internal heat low-temperature dry distillation furnace. This furnace type is a new process developed by a company based on the Lurgi-Spilgas three-stage furnace. It utilizes the advantages of related furnace types at home and abroad, combines local actual production experience, and designs according to the characteristics of low-rank coal. A moving bed reactor is used, and the burned gas is used as a gas heat carrier to heat coal in the bed to facilitate the pyrolysis reactions of the coal. The process is simple, and a high yield of tar can be obtained, making this process one of the preferred techniques for low-rank coal cryogenic dry distillation in China. However, the furnace gas produced by the process is cooled during the temperature rise, and part of the tar forms liquid tar mist. Moreover, dust such as pulverized coal and semicoke entrained in the furnace gas flow are also incorporated, which makes the separation and recovery of coal tar difficult, resulting in poor quality and greatly reducing the potential value of the tar. Therefore, the separation of coal tar and impurities has become a key problem. Based on actual observations of phase flow and the complexity of measuring industrial data, it is very difficult to solve this problem by experimental methods. However, with the rapid development of computers, the computational fluid dynamics (CFD) method has gradually become effective for studying complex multiphase flow processes in reactors. Many researchers have implemented the coupling of complex reaction kinetic models into CFD models for flow-phase simulation [15–18]. This work provides a technical basis for the simulation calculation of tar mist and dust movement processes by the CFD method.Currently, the calculation methods of fluid-solid coupling are divided into three categories: the Euler-Eulerian method, the Euler–Lagrangian method, and the Lagrangian-Lagrangian method. Because the Euler–Lagrangian method can accurately reflect the airflow-dust coupling characteristics [19–22], this method is increasingly widely used in the simulation of fluid-solid two-phase flow. Torañod et al. [23] studied the migration behavior of airflow and air-dust flow through a 14.7-m2 cross section on a fully mechanized excavation surface under strong exhaust ventilation conditions by the Euler–Lagrangian method. Kurnia et al. [24] used the Euler–Lagrangian method to study the diffusion and management of dust on the excavation surface. Patankar and Joseph [25] used the Lagrangian method to describe the movement of dust particles.In previous studies, numerical simulations have been widely used to study the dust diffusion pollution behavior in coal, and some useful results have been achieved. For example, Lu et al. [26] used CFD to evaluate various possible scenarios for underground mine configurations. Zhou et al. [27] combined CFD simulation and onsite measurement to study the diffusion behavior of inhalable dust. Cai et al. [28] studied the effect of airflow on the diffusion mode of coal dust particles in a fully mechanized mining face and found the optimal airflow.In the past 5 years, the model of pulverized coal-fired boilers has improved significantly. Modeling furnaces for coal-fired boilers is a complex task. Any model developed to predict critical performance parameters, such as furnace exit gas temperature and pollutant emission levels, will need to capture the multifarious nature of combustion in the boiler furnace. Despite the large amount of computationally expensive CFD codes, researchers have also developed simpler but effective reactor network models. Sankar et al. [29] reviewed the research status of calculation models for pulverized coal boilers from three perspectives: the development of coal combustion models, radiation models, and overall furnace models.Nevertheless, there are very few simulation studies on the movement process of focusing tar oil mist and dust in a low-temperature dry distillation furnace. Through numerical simulation of the gas-solid two-phase flow state, the two-phase motion mechanism of the coal retorting process is revealed. The physical parameters (e.g., particle size of tar and dust, gas velocity, and density of tar and dust) can be optimized so that the tar can be quickly removed by the gas, while the dust, such as pulverized coal and semicoke, remains in the furnace to continue pyrolysis. This condition can reduce the waste slag in the coal tar, improve the quality of the coal tar, partially alleviate China’s petroleum energy crisis, and substantially augment China’s reserve oil. In addition, the raw materials can be brought closer to the theoretically superior value before production, thereby improving the efficiency of pyrolysis production and reducing energy consumption and costs.


## 2. Physically Simplified Model of Airflow-Particle Motion

In an SJ-type internal heat type low-temperature dry distillation furnace, the tar that is dry distillated by coal exists in a gaseous form in the high-temperature region. The tar and gas move upward in the space between the coal particles, and when it reaches the low-temperature region (below the boiling temperature of the tar component), the tar condenses into a tar mist. The main components and boiling points of tar are shown in Table1.Table 1
Main components and boiling points of tar.
Main components
Boiling points (°C)
Alkanes
C11–C19
195.8–330.0
C≥20
≥343.0
Phenols
Phenol
181.9
Naphthol
285.3
Aromatic hydrocarbons
Benzene
80.1
Toluene
110.6
Dimethyl-benzene
139.1/138.4
Naphthalene
217.9
Anthracene
340.0
Nitrogen-containing compound
Pyridine
115.2
Quinoline
238.1The tar mist is brought out of the furnace by the rapidly rising gas. At the same time, the coal generates dust when it enters the furnace, and some of this dust is removed from the furnace by the gas. By simplifying the model, the process of tar mist and dust removal by gas is considered a pneumatic conveying process. Showing a characteristic length ofL (unit is m) and an equivalent diameter of d (unit is m) of the microelement tube as the research object, a schematic diagram of the tar mist and dust movement is shown in Figure 1, where u is the apparent velocity in m/s and n is the void fraction. Due to the presence of scattered solid particles in the tube, which increases the difficulty of establishing the geometric model, we arrange the scattered solid particles in Figure 1(a) in an orderly manner to obtain Figure 1(b). When the arrangement is tight enough, we can ignore its existence in the tube and then express it by a void fraction. The movement process of tar mist and dust in the tube is shown in Figure 1(c).Figure 1
Schematic diagram of the tar mist and dust movement.


## 3. Mathematical Model of Airflow-Particle Motion

In this study, gas is considered as the fluid phase, and tar mist and dust are considered as the particle phase. It is also assumed that the flow of gas in the model conforms to the continuous medium hypothesis, conservation of energy law, and Newton’s second law of motion [30]. On the basis of the standard k-ε model, we constructed the closed control equations to calculate the turbulence. This model only considered momentum transfer and ignored thermal conduction. Then, dust particles were treated as discrete media whose movements were calculated based on the Lagrangian method [27, 31, 32]. The associated mathematical models are as follows.


### 3.1. Mathematical Model of Air Movement

The continuity equation [33, 34]:(1)∂ρ∂t+∂∂xiρui=0.The Navier–Stokes equation:(2)∂∂tρui+∂∂xiρuiuj=−∂p∂xi+∂∂xjμ+μt∂ui∂xj+∂uj∂xi,where ρ is the fluid density; t is time; x is the coordinate; u is velocity; p is the turbulent pressure; and μt is the coefficient of turbulent viscosity.The energy equation [35]:(3)∂∂tρh+∂∂xiρuih=∂∂xjΓh∂h∂xj+∂p∂t+∂uip∂xi+Φ+Sh,where h is the specific enthalpy, Γh is the ratio of effective viscosity and the Prandtl number, Φ is the dissipation function, and Sh is the source of enthalpy generated on a volumetric source basis. Φ can further be calculated as(4)Φ=μ∂ui∂xj+∂uj∂xi−δij23∂uk∂xk∂ui∂xj.Standardk-ε equation:Thek-equation [36, 37]:(5)∂ρk∂t+∂ρkui∂xi=∂∂xiμ+μtσk∂k∂xi+Gk−ρε.Theε-equation:(6)∂ρε∂t+∂ρεui∂xi=∂∂xjμ+μtσε∂ε∂xj+C1εεkGk−C2ερε2k.In these equations,k is the fluid’s turbulent kinetic energy; ε is the viscous dissipation induced by a vortex; Gk is the turbulent kinetic energy; and C1ε, C2ε, and Cμ are the empirical constants with values of 1.44, 1.92, and 0.09, respectively.


### 3.2. Force Analysis of the Fluid Phase

As shown in Figure1, in the microelement length L, the intracavity void ratio is n, and it is assumed that the in-tube free cross section fraction is equal to n.The fluid phase is subjected to a frictional resistanceFf, g, the force of the pressure drop gradient on the fluid phase FΔp, g, the self-gravity, and the particle drag FD, g. All other forces are negligible:(7)Ff,g=Δpfnπd24,FΔp,g=−∂p∂znπd2ΔL4,FD,g=−18μρgd2CDRe24,where Δpf is the pressure difference generated by the fluid motion, and the unit is Pa.


### 3.3. Mathematical Model of Tar Mist and Dust Movement

In the Lagrangian coordinate system, the motion trajectory of discrete-phase particles was calculated by integrating the differential equation of the interaction among particles [30, 38–40].Time-averaged particle velocityu⟶p is calculated as the sum of particle convective velocity u⟶pc and diffusive velocity u⟶pd [41]. The convective velocity of particles is(8)mpdu⟶pcdt=CDρAp2u⟶−u⟶pcu⟶−u⟶pc+dp3π6ρp−ρg⟶.The diffusive velocity:(9)u⟶pd=−1NpΓp∇Np.The additional forces in the particle force balance, mainly including the pressure gradient force, virtual mass force, Saffman lift force, and Magnus lift force, are important under special circumstances [42].The pressure gradient force:(10)F⟶p=ρρpu⟶p∇u⟶.The virtual mass force:(11)F⟶vm=Cvmρρpu⟶p∇u⟶−du⟶pdt,where Cvm is the virtual mass factor with a fixed value of 0.5.The Saffman lift force [43, 44]:(12)F⟶Saf=2Kv1/2ρdijρpdpdlkdkl1/4u⟶−u⟶p,where K = 2.594; dij, dlk, and dkl refer to the deformation tensor; and v is the kinematic viscosity.The Magnus lift force:(13)F⟶Mag=πdp3ρω⟶u⟶−u⟶p2,where ω⟶ is the rotational angular velocity.


## 3.1. Mathematical Model of Air Movement

The continuity equation [33, 34]:(1)∂ρ∂t+∂∂xiρui=0.The Navier–Stokes equation:(2)∂∂tρui+∂∂xiρuiuj=−∂p∂xi+∂∂xjμ+μt∂ui∂xj+∂uj∂xi,where ρ is the fluid density; t is time; x is the coordinate; u is velocity; p is the turbulent pressure; and μt is the coefficient of turbulent viscosity.The energy equation [35]:(3)∂∂tρh+∂∂xiρuih=∂∂xjΓh∂h∂xj+∂p∂t+∂uip∂xi+Φ+Sh,where h is the specific enthalpy, Γh is the ratio of effective viscosity and the Prandtl number, Φ is the dissipation function, and Sh is the source of enthalpy generated on a volumetric source basis. Φ can further be calculated as(4)Φ=μ∂ui∂xj+∂uj∂xi−δij23∂uk∂xk∂ui∂xj.Standardk-ε equation:Thek-equation [36, 37]:(5)∂ρk∂t+∂ρkui∂xi=∂∂xiμ+μtσk∂k∂xi+Gk−ρε.Theε-equation:(6)∂ρε∂t+∂ρεui∂xi=∂∂xjμ+μtσε∂ε∂xj+C1εεkGk−C2ερε2k.In these equations,k is the fluid’s turbulent kinetic energy; ε is the viscous dissipation induced by a vortex; Gk is the turbulent kinetic energy; and C1ε, C2ε, and Cμ are the empirical constants with values of 1.44, 1.92, and 0.09, respectively.


## 3.2. Force Analysis of the Fluid Phase

As shown in Figure1, in the microelement length L, the intracavity void ratio is n, and it is assumed that the in-tube free cross section fraction is equal to n.The fluid phase is subjected to a frictional resistanceFf, g, the force of the pressure drop gradient on the fluid phase FΔp, g, the self-gravity, and the particle drag FD, g. All other forces are negligible:(7)Ff,g=Δpfnπd24,FΔp,g=−∂p∂znπd2ΔL4,FD,g=−18μρgd2CDRe24,where Δpf is the pressure difference generated by the fluid motion, and the unit is Pa.


## 3.3. Mathematical Model of Tar Mist and Dust Movement

In the Lagrangian coordinate system, the motion trajectory of discrete-phase particles was calculated by integrating the differential equation of the interaction among particles [30, 38–40].Time-averaged particle velocityu⟶p is calculated as the sum of particle convective velocity u⟶pc and diffusive velocity u⟶pd [41]. The convective velocity of particles is(8)mpdu⟶pcdt=CDρAp2u⟶−u⟶pcu⟶−u⟶pc+dp3π6ρp−ρg⟶.The diffusive velocity:(9)u⟶pd=−1NpΓp∇Np.The additional forces in the particle force balance, mainly including the pressure gradient force, virtual mass force, Saffman lift force, and Magnus lift force, are important under special circumstances [42].The pressure gradient force:(10)F⟶p=ρρpu⟶p∇u⟶.The virtual mass force:(11)F⟶vm=Cvmρρpu⟶p∇u⟶−du⟶pdt,where Cvm is the virtual mass factor with a fixed value of 0.5.The Saffman lift force [43, 44]:(12)F⟶Saf=2Kv1/2ρdijρpdpdlkdkl1/4u⟶−u⟶p,where K = 2.594; dij, dlk, and dkl refer to the deformation tensor; and v is the kinematic viscosity.The Magnus lift force:(13)F⟶Mag=πdp3ρω⟶u⟶−u⟶p2,where ω⟶ is the rotational angular velocity.


## 4. Geometry Model Establishment and Boundary Condition Setting

Figure2 is a schematic diagram of the structure of a 75,000-ton SJ-type internal heat low-temperature dry distillation furnace used by a coal chemical company in Shaanxi. The furnace adopts a cavity design. From top to bottom is a drying section, a dry distillation section, and a cooling section. Coal blocks gradually descend from the coal box through the cavity. The gas and air are mixed into the furnace from below, and the gas and oxygen burn to form a high-temperature heat carrier to heat the coal seam layer by layer. The tar produced by pyrolysis is removed from the riser by rising gas. According to this process, a geometrical model of the riser is constructed, which is divided into a square grid with a total of 15,320 cells, including 40 cells on the X-axis and 383 cells on the Y-axis. As shown in Figure 3, the mesh with quality higher than 0.3 accounts for more than 97% of all meshes, indicating that the mesh model is reasonable.Figure 2
Schematic diagram of the structure of SJ-type internal heat low-temperature dry distillation furnace.Figure 3
Geometric model of the riser.In practice, it is a continuous process for tar mist and dust to be removed from the furnace by the rising gas, but it is difficult to simulate this process. Therefore, in the numerical simulation, it is assumed that the lower part of the riser is filled with particles with a volume fraction of 30%, and the gas is then blown upward from the bottom of the tube at a certain speed to observe the rise of particles. Figure4 shows the state of the particles in the tube filling the bottom (red portion) before iteration after setting the particle volume fraction to 30% in ANSYS Fluent.Figure 4
Initial state particle volume fraction.Because the tar mist particles only exist in the riser, once they are removed from the furnace, they will agglomerate to form liquid tar. It is difficult to directly measure during the production process, so a large number of simulation experiments were performed in the early stage to determine the particle size scope. Finally, the research scope is determined as follows: the tar mist particle size is 0.1 mm–1.0 mm, and the dust particle size is 0.05 mm–0.20 mm. According to the density scope of tar and dust provided by the coal chemical company, numerous simulation experiments were carried out in the early stage. The final determination scope is as follows: tar mist density 900 kg/m3–1100 kg/m3 and dust density 1100 kg/m3–1500 kg/m3. The scope of gas velocity provided by the coal chemical company is 0.675–0.723 m/s. In this study, 0.68, 0.69, 0.70, 0.71, and 0.72 m/s were selected as the gas velocities. Table 2 lists the boundary conditions for the geometric model.Table 2
Boundary conditions of the geometric model.
Name
Parameter
Name
Parameter
Solver
Discrete solver
Inlet boundary type
Velocity_Inlet
Turbulence model
k-ε two-equation
Turbulence intensity
3.2%
Energy equation
Close
Outlet boundary type
Outflow
Discrete-phase model
Open
Convergence criterion
10–3
Drag law
Spherical
Particle size distribution
Rosin-Rammler
Drag coefficient
Syamlal–O’Brien
Shear condition
No slip
Pressure interpolation method
Standard format
Pressure-velocity coupling equation
SIMPLEC


## 5. Results and Discussion

### 5.1. Effect of the Tar Mist Particle Size

When the gas velocity is 0.70 m/s and the density of the tar mist is 900 kg/m3, the particle size of the tar mist is changed to study the two-phase motion. Figure 5 shows the volume fraction of the tar mist at different times.Figure 5
Volume fraction of tar mist:u = 0.70 m/s and ρ = 900 kg/m3. (a) d = 0.10 mm. (b) d = 0.20 mm. (c) d = 0.30 mm. (d) d = 0.50 mm. (e) d = 1.00 mm.
(a)
(b)
(c)
(d)
(e)It can be seen from Figures5(a) and 5(b) that the distribution area of the particles in the furnace increases rapidly with time, and the entire area is filled within 1.8 s. Then, the distribution of the particles in the working area is continuously reduced until the particles are completely removed by the gas. When the particle size is 0.10 mm and the time is 6.1 s, only particles at a volume fraction of 0.03 are present in the furnace, and the remaining positions are filled with the gas phase, indicating that 97% of the tar particles are carried out by the gas. When the particle size is 0.20 mm and the time is 0.9 s, the particles are brought to a height of approximately 4/6 in the tube; when the time reaches 22.0 s, the particles are all carried out of the working area by the gas.It can be seen from Figures5(c) and 5(d) that within 1.8 s, the particle distribution area begins to decrease significantly; from 1.8 s to 120 s, 95% of the particles are below a height of 1/2, and the distribution area and state are similar. After 120 s, this state remains unchanged, indicating that the particles are difficult to remove. In Figure 5(e), the particle distribution area is always at a height of 1/6, and the area does not change very much with time, indicating that the particles are also hard to remove in this case.A comparison of Figures5(c)–5(e) indicates that the volume fraction of the particles at the bottom of the furnace is unevenly distributed, and the particles are fluidized. Moreover, as the particle size increases, the particle distribution area gradually decreases, as does the degree of fluidization of the particles. A comparison of the subfigures of Figure 5 reveals that as the particle size increases, the distribution area of the particles decreases at every time point, the volume at the bottom gradually increases, and the degree of fluidization gradually decreases. At the same gas velocity, the larger the particle size, the more difficult removal becomes.


### 5.2. Effect of the Dust Particle Size

When the gas velocity is 0.70 m/s and the dust density is 1100 kg/m3, the particle size of the dust is changed to study the two-phase motion. Figure 6 shows the volume fraction of dust at different times.Figure 6
Volume fraction of dust:u = 0.70 m/s and ρ = 1100 kg/m3. (a) d = 0.05 mm. (b) d = 0.10 mm. (c) d = 0.15 mm. (d) d = 0.18 mm. (e) d = 0.20 mm.
(a)
(b)
(c)
(d)
(e)Figures6(a)–6(d) show that the distribution area of the particles in the furnace increases rapidly with time, and the entire area is filled within 1.6 s. Then, the distribution of the particles in the working area is continuously reduced. Finally, only particles at a volume fraction of 0.015 remain, the rest having been removed by the gas. As the particle size of the dust increases, the time required for dust removal gradually increases. In Figure 6(e), when the particle size of the dust is 0.20 mm, the distribution area and the volume fraction at 23.0 and 120 s do not change much, and the particles are deemed difficult to remove.In Figure6, the particle distributions of 0.2 s and 0.4 s are the same, and only the proportions of the different volume fractions are different. Particles (with a volume fraction of 0.30) are gradually depleted, and the proportion of remaining particles gradually increases, producing a volume fraction between 0.27 and 0.03. At 0.8 s, the distribution of the upper part is unchanged, but the volume fraction is gradually reduced, the height of the particles is slightly lowered, and the volume fraction at the bottom is gradually increased. These effects are caused by the increase in particle size. At 1.6 s, the particles fill the entire working area; however, as the particle size increases, the upper distribution area decreases, and particles gradually gather at the bottom with a volume fraction of 0.30.


### 5.3. Experimental Verification

The above simulation results demonstrate that the influence of the particle size on the rise of oil mist and dust is important. Zhang et al. [42] used the AKFC-92A-type mine dust sampler to perform dust sampling 30 minutes after coal mining to verify the accuracy of the simulation results. To verify the accuracy of the simulation results, Cai et al. [28] set up multiple measurement points onsite and collected dust particle samples using a dust sampler to measure the dust concentration. However, due to the complicated structure of the coal low-temperature dry distillation furnace and the uninterrupted production process, it is difficult for the measuring instrument to be directly introduced into the rising pipe for measurement. The coal tar produced on-site by this type of a low-temperature dry distillation furnace in a factory is dissolved with an organic solvent such as toluene, acetone, or quinoline, followed by suction filtration and washing to obtain dust particles, and the particle size distribution of the dust is measured by the OMEC Topsizer Plus laser particle size analyzer. The obtained particle size distribution is shown in Table 3 and Figure 7.Table 3
Dust particle size frequency and cumulative distribution.
Dust particle size (mm)
Frequency distribution (%)
Cumulative distribution (%)
0.0020
0.00
0.00
0.0024
0.16
0.16
0.0028
0.05
0.22
0.0033
0.07
0.29
0.0039
0.09
0.38
0.0046
0.12
0.51
0.0055
0.16
0.67
0.0065
0.22
0.89
0.0077
0.29
1.17
0.0091
0.38
1.55
0.0108
0.50
2.05
0.0128
0.66
2.70
0.0151
0.86
3.57
0.0179
1.13
4.70
0.0212
1.48
6.18
0.0250
1.92
8.10
0.0296
2.49
10.58
0.0351
3.19
13.77
0.0415
4.05
17.82
0.0491
5.07
22.89
0.0688
7.50
36.63
0.0814
8.72
45.36
0.0964
9.74
55.09
0.1141
10.28
65.37
0.1350
10.09
75.46
0.1598
8.99
84.45
0.1811
7.05
91.05
0.2042
4.68
96.18
0.2255
2.50
98.68
0.2534
1.00
99.68
0.2911
0.27
99.95
0.3393
0.05
100.00
0.3904
0.00
100.00
0.4257
0.00
100.00Figure 7
Dust particle size frequency and cumulative distribution.As shown in Figure7, the dust particles less than 0.18 mm accounted for 90%, and the largest particle size was not more than 0.339 mm, indicating that the dust particles less than 0.18 mm were easily taken out by the gas and affected the quality of the tar. It can be seen from Figure 6(e) that the 0.20 mm dust cannot be completely taken out, but it is not solidified like tar mist deposited on the bottom, or a small part will be taken out, which accounts for about 4.68% (Table 3). In summary, it was found that the particle size distribution could achieve the expected simulation effect in practice. By comparing the particle size change in experiments and simulations, the effects on the dust rising process were investigated, and the accuracy of the mathematical models used in the simulation process and the reliability of the simulation results were verified. The rationality of particle size parameter selection was further proven.


### 5.4. Effect of the Gas Velocity on the Tar Mist and Dust Movement

Two-phase motion is studied by changing gas velocity. The volume fractions of tar mist and dust are shown in Figures8 and 9, respectively.Figure 8
Volume fraction of tar mist:d = 0.20 mm and ρ = 900 kg/m3. (a) u = 0.68 m/s. (b) u = 0.69 m/s. (c) u = 0.70 m/s. (d) u = 0.71 m/s. (e) u = 0.72 m/s.
(a)
(b)
(c)
(d)
(e)Figure 9
Volume fraction of dust:d = 0.18 mm and ρ = 1100 kg/m3. (a) u = 0.68 m/s. (b) u = 0.69 m/s. (c) u = 0.70 m/s. (d) u = 0.71 m/s. (e) u = 0.72 m/s.
(a)
(b)
(c)
(d)
(e)From Figures8 and 9, the distribution area of the particles in the furnace increases rapidly with time and fills almost the entire area within 2.0 s. At 4.0 s, the proportion of particles (with a volume fraction of 0.20 to 0.40) continuously decreases, the particles gradually move upward, and the bottom is gradually occupied by a volume fraction of less than 0.12. Finally, after approximately 20 s in the furnace, there is only a small amount of tar mist and dust particles with a volume fraction of 0.04. The simulation results reveal that as the gas velocity increases, the time over which the tar mist and dust are completely removed gradually decreases. The reason is that the gravity G of the mass per unit particle is constant in the case where the particle diameter and the density are the same. However, due to the difference in gas velocities, the resistance between the gas-solid phase and the additional force in the particle force balance may vary from equations (11)–(14). Following force balancing, an acceleration in the upward direction is finally obtained so that the time required for the belt to remove material decreases as the velocity increases.A comparison of Figures8 and 9 reveals that there is no change in the particle distribution shape, height, area, or volume fraction at 0.5 s and 1.0 s. The reason may be that the increase in the velocity is not very large; the particle phase is initially at the bottom of the furnace, and the acceleration in the upward direction needs to gradually increase with time. After 2.0 s, the acceleration starts to cause a visible change; the volume fraction at the bottom decreases, the particles spread upward, and increasingly more particles are removed, gradually reducing the total time required for complete removal. Taken together with the simulation results at the same velocity, these results reveal that the time required for the dust to be removed is more than that for the tar mist to be removed. Because the difference in particle size is not very large, the difference in density plays a large role. Density determines the gravity force, and the density of tar mist is less than that of dust, meaning that the gravity force on the tar mist is less than that of dust of the same mass. At the same velocity, the other additional forces are unchanged, so the time required for the tar mist to be carried out is less than that for the dust.Since the tar mist and dust are mixed into the furnace, the gas velocity is the same for both phases. The main purpose of this study was to separate the two phases, letting the tar mist be carried out and allowing as much dust as possible to flow back into the furnace for further dry distillation, so it is important to determine the appropriate corresponding velocity. Figure10 presents the time at which the particles are removed in Figures 8 and 9. The time difference between 0.68, 0.69, 0.71, and 0.72 m/s is small, and all values lie within a range of 0.7 s. At 0.70 m/s, the time difference is the largest, which is 1.7 s, which means that there is still more dust in the furnace when the tar mist is completely removed.Figure 10
Particle removal time as a function of the gas velocity.It can be seen from 5.1 and 5.2 that the above selected tar mist and dust particle size are the maximum values that can be removed by the gas. Select the two-phase particle with the smallest particle size when not removed and study the two-phase motion at the maximum velocity, as shown in Figures11 and 12.Figure 11
Volume fraction of tar mist:d = 0.30 mm and ρ = 900 kg/m3. (a) u = 0.70 m/s. (b) u = 0.72 m/s.
(a)
(b)Figure 12
Volume fraction of dust:d = 0.20 mm and ρ = 1100 kg/m3. (a) u = 0.70 m/s. (b) u = 0.72 m/s.
(a)
(b)Figure11 shows that the distribution area of particles in the furnace increases rapidly over time. At 1.8 s, the particle fills the area to 5/6, and the distribution area reaches its maximum. At 9.0 s, the particle distribution area is reduced to 4/6. At 120 s, it is reduced to 1/2, and the particles are always left in the furnace. A comparison of the simulation results at the same time reveals no change at 0.3 s. With increasing velocity at 0.6 s, the tar particles with a volume fraction of 0.35–0.45 aggregate in a higher location, and the particles with a bottom volume fraction of 0.20–0.30 are depleted. At 0.9 s, as the velocity increases, tar particles are concentrated with a volume fraction of 0.30 to 0.40 and 0.35 to 0.45 at the upper and bottom portions of the distribution area, respectively. At 9.0 s and 120 s, particles at a volume fraction of 0.35 to 0.50 disappear with increasing velocity, showing that although most of the particles remain in the furnace, some of them are still removed. It can be seen from Figure 12 that the distribution area of the particles in the furnace increases rapidly over time, and the entire area is filled in 1.6 s, with the distribution of particles at a volume fraction of 0.18–0.30 continuously decreasing in the working area. However, there are still some particles left in the furnace. A comparison of the simulation results at the same time reveals no change at 0.2 s and 0.4 s; at 0.8 s, particles (with a volume fraction of 0.21 to 0.27) are collected at a height of 4/6, and there is no significant difference in the remaining time except that the distribution area is expanded from 1/2 to 5/6.Figures8, 9, 11, and 12 verify that the gas velocity can change the length of time required for the two phases to be carried out, but the particle size of the particles is a key factor in determining whether removal is possible. The particle size of the tar mist should be less than 0.20 mm, and the particle size of the dust should be greater than 0.18 mm to achieve the aims of this study.


### 5.5. Effect of the Tar Mist and Dust Density

The density of tar mist and dust was changed, and the two-phase motion was studied. The motion simulation results are shown in Figures13 and 14.Figure 13
Volume fraction of tar mist:d = 0.20 mm and u = 0.70 m/s. (a) ρ = 900 kg/m3. (b) ρ = 950 kg/m3. (c) ρ = 1000 kg/m3. (d) ρ = 1050 kg/m3. (e) ρ = 1100 kg/m3.
(a)
(b)
(c)
(d)
(e)Figure 14
Volume fraction of dust:d = 0.18 mm and u = 0.70 m/s. (a) ρ = 1100 kg/m3. (b) ρ = 1200 kg/m3. (c) ρ = 1300 kg/m3. (d) ρ = 1400 kg/m3. (e) ρ = 1500 kg/m3.
(a)
(b)
(c)
(d)
(e)Figure13 shows that the distribution area of the particles in the furnace increases rapidly over time. At 2.7 s, the particles fill almost the entire area, and the distribution of particles gradually decreases. Finally, at 33.5 s, there is only a small amount of tar particles in the furnace, with a volume fraction of 0.03. As the density increases, the time required to remove the particles increases because of the influence of gravity. There is little difference between the results at 0.3 s and 0.9 s. The distribution area at 2.7 s is at a height of 5/6; however, the particles (with a volume fraction of 0.06–0.12) are enriched with increasing density, and the particles are slowly transported to the bottom, with a volume fraction of 0.30. At 8.1 s, only particles at a volume fraction of 0.12 or less remain in the furnace. As the density increases, the distribution area first increases and then decreases. Specifically, only a few particles (with a volume fraction of 0.03 to 0.09) are left at ρ = 900 kg/m3; at ρ = 950 kg/m3 and 1000 kg/m3, the density increases, and it is difficult to remove many particles at the same time, resulting in an increase in the distribution area. When ρ = 1050 kg/m3 and 1100 kg/m3, the volume fraction of the particles increases significantly, and the particles collectively move downward, resulting in a decrease in the distribution area. As shown in Figure 14, the distribution of particles in the furnace increases rapidly with time. The area is almost filled at 2.7 s, and the distribution of particles in the area is then gradually reduced. The final density is between 1100 kg/m3 and 1400 kg/m3, and removal is difficult when the density is 1500 kg/m3. A comparison of the simulation results indicates that since the density is less than that of the dust, the time required for tar mist removal is less than that of dust removal. The tar mist can be completely removed in the density range of 900–1100 kg/m3. When the dust density is 1500 kg/m3, the dust starts to gather at the bottom, and the degree of fluidization of the particles gradually decreases. At 120 s, the particle fluidization degree is the lowest, and the dust is difficult to remove.


## 5.1. Effect of the Tar Mist Particle Size

When the gas velocity is 0.70 m/s and the density of the tar mist is 900 kg/m3, the particle size of the tar mist is changed to study the two-phase motion. Figure 5 shows the volume fraction of the tar mist at different times.Figure 5
Volume fraction of tar mist:u = 0.70 m/s and ρ = 900 kg/m3. (a) d = 0.10 mm. (b) d = 0.20 mm. (c) d = 0.30 mm. (d) d = 0.50 mm. (e) d = 1.00 mm.
(a)
(b)
(c)
(d)
(e)It can be seen from Figures5(a) and 5(b) that the distribution area of the particles in the furnace increases rapidly with time, and the entire area is filled within 1.8 s. Then, the distribution of the particles in the working area is continuously reduced until the particles are completely removed by the gas. When the particle size is 0.10 mm and the time is 6.1 s, only particles at a volume fraction of 0.03 are present in the furnace, and the remaining positions are filled with the gas phase, indicating that 97% of the tar particles are carried out by the gas. When the particle size is 0.20 mm and the time is 0.9 s, the particles are brought to a height of approximately 4/6 in the tube; when the time reaches 22.0 s, the particles are all carried out of the working area by the gas.It can be seen from Figures5(c) and 5(d) that within 1.8 s, the particle distribution area begins to decrease significantly; from 1.8 s to 120 s, 95% of the particles are below a height of 1/2, and the distribution area and state are similar. After 120 s, this state remains unchanged, indicating that the particles are difficult to remove. In Figure 5(e), the particle distribution area is always at a height of 1/6, and the area does not change very much with time, indicating that the particles are also hard to remove in this case.A comparison of Figures5(c)–5(e) indicates that the volume fraction of the particles at the bottom of the furnace is unevenly distributed, and the particles are fluidized. Moreover, as the particle size increases, the particle distribution area gradually decreases, as does the degree of fluidization of the particles. A comparison of the subfigures of Figure 5 reveals that as the particle size increases, the distribution area of the particles decreases at every time point, the volume at the bottom gradually increases, and the degree of fluidization gradually decreases. At the same gas velocity, the larger the particle size, the more difficult removal becomes.


## 5.2. Effect of the Dust Particle Size

When the gas velocity is 0.70 m/s and the dust density is 1100 kg/m3, the particle size of the dust is changed to study the two-phase motion. Figure 6 shows the volume fraction of dust at different times.Figure 6
Volume fraction of dust:u = 0.70 m/s and ρ = 1100 kg/m3. (a) d = 0.05 mm. (b) d = 0.10 mm. (c) d = 0.15 mm. (d) d = 0.18 mm. (e) d = 0.20 mm.
(a)
(b)
(c)
(d)
(e)Figures6(a)–6(d) show that the distribution area of the particles in the furnace increases rapidly with time, and the entire area is filled within 1.6 s. Then, the distribution of the particles in the working area is continuously reduced. Finally, only particles at a volume fraction of 0.015 remain, the rest having been removed by the gas. As the particle size of the dust increases, the time required for dust removal gradually increases. In Figure 6(e), when the particle size of the dust is 0.20 mm, the distribution area and the volume fraction at 23.0 and 120 s do not change much, and the particles are deemed difficult to remove.In Figure6, the particle distributions of 0.2 s and 0.4 s are the same, and only the proportions of the different volume fractions are different. Particles (with a volume fraction of 0.30) are gradually depleted, and the proportion of remaining particles gradually increases, producing a volume fraction between 0.27 and 0.03. At 0.8 s, the distribution of the upper part is unchanged, but the volume fraction is gradually reduced, the height of the particles is slightly lowered, and the volume fraction at the bottom is gradually increased. These effects are caused by the increase in particle size. At 1.6 s, the particles fill the entire working area; however, as the particle size increases, the upper distribution area decreases, and particles gradually gather at the bottom with a volume fraction of 0.30.


## 5.3. Experimental Verification

The above simulation results demonstrate that the influence of the particle size on the rise of oil mist and dust is important. Zhang et al. [42] used the AKFC-92A-type mine dust sampler to perform dust sampling 30 minutes after coal mining to verify the accuracy of the simulation results. To verify the accuracy of the simulation results, Cai et al. [28] set up multiple measurement points onsite and collected dust particle samples using a dust sampler to measure the dust concentration. However, due to the complicated structure of the coal low-temperature dry distillation furnace and the uninterrupted production process, it is difficult for the measuring instrument to be directly introduced into the rising pipe for measurement. The coal tar produced on-site by this type of a low-temperature dry distillation furnace in a factory is dissolved with an organic solvent such as toluene, acetone, or quinoline, followed by suction filtration and washing to obtain dust particles, and the particle size distribution of the dust is measured by the OMEC Topsizer Plus laser particle size analyzer. The obtained particle size distribution is shown in Table 3 and Figure 7.Table 3
Dust particle size frequency and cumulative distribution.
Dust particle size (mm)
Frequency distribution (%)
Cumulative distribution (%)
0.0020
0.00
0.00
0.0024
0.16
0.16
0.0028
0.05
0.22
0.0033
0.07
0.29
0.0039
0.09
0.38
0.0046
0.12
0.51
0.0055
0.16
0.67
0.0065
0.22
0.89
0.0077
0.29
1.17
0.0091
0.38
1.55
0.0108
0.50
2.05
0.0128
0.66
2.70
0.0151
0.86
3.57
0.0179
1.13
4.70
0.0212
1.48
6.18
0.0250
1.92
8.10
0.0296
2.49
10.58
0.0351
3.19
13.77
0.0415
4.05
17.82
0.0491
5.07
22.89
0.0688
7.50
36.63
0.0814
8.72
45.36
0.0964
9.74
55.09
0.1141
10.28
65.37
0.1350
10.09
75.46
0.1598
8.99
84.45
0.1811
7.05
91.05
0.2042
4.68
96.18
0.2255
2.50
98.68
0.2534
1.00
99.68
0.2911
0.27
99.95
0.3393
0.05
100.00
0.3904
0.00
100.00
0.4257
0.00
100.00Figure 7
Dust particle size frequency and cumulative distribution.As shown in Figure7, the dust particles less than 0.18 mm accounted for 90%, and the largest particle size was not more than 0.339 mm, indicating that the dust particles less than 0.18 mm were easily taken out by the gas and affected the quality of the tar. It can be seen from Figure 6(e) that the 0.20 mm dust cannot be completely taken out, but it is not solidified like tar mist deposited on the bottom, or a small part will be taken out, which accounts for about 4.68% (Table 3). In summary, it was found that the particle size distribution could achieve the expected simulation effect in practice. By comparing the particle size change in experiments and simulations, the effects on the dust rising process were investigated, and the accuracy of the mathematical models used in the simulation process and the reliability of the simulation results were verified. The rationality of particle size parameter selection was further proven.


## 5.4. Effect of the Gas Velocity on the Tar Mist and Dust Movement

Two-phase motion is studied by changing gas velocity. The volume fractions of tar mist and dust are shown in Figures8 and 9, respectively.Figure 8
Volume fraction of tar mist:d = 0.20 mm and ρ = 900 kg/m3. (a) u = 0.68 m/s. (b) u = 0.69 m/s. (c) u = 0.70 m/s. (d) u = 0.71 m/s. (e) u = 0.72 m/s.
(a)
(b)
(c)
(d)
(e)Figure 9
Volume fraction of dust:d = 0.18 mm and ρ = 1100 kg/m3. (a) u = 0.68 m/s. (b) u = 0.69 m/s. (c) u = 0.70 m/s. (d) u = 0.71 m/s. (e) u = 0.72 m/s.
(a)
(b)
(c)
(d)
(e)From Figures8 and 9, the distribution area of the particles in the furnace increases rapidly with time and fills almost the entire area within 2.0 s. At 4.0 s, the proportion of particles (with a volume fraction of 0.20 to 0.40) continuously decreases, the particles gradually move upward, and the bottom is gradually occupied by a volume fraction of less than 0.12. Finally, after approximately 20 s in the furnace, there is only a small amount of tar mist and dust particles with a volume fraction of 0.04. The simulation results reveal that as the gas velocity increases, the time over which the tar mist and dust are completely removed gradually decreases. The reason is that the gravity G of the mass per unit particle is constant in the case where the particle diameter and the density are the same. However, due to the difference in gas velocities, the resistance between the gas-solid phase and the additional force in the particle force balance may vary from equations (11)–(14). Following force balancing, an acceleration in the upward direction is finally obtained so that the time required for the belt to remove material decreases as the velocity increases.A comparison of Figures8 and 9 reveals that there is no change in the particle distribution shape, height, area, or volume fraction at 0.5 s and 1.0 s. The reason may be that the increase in the velocity is not very large; the particle phase is initially at the bottom of the furnace, and the acceleration in the upward direction needs to gradually increase with time. After 2.0 s, the acceleration starts to cause a visible change; the volume fraction at the bottom decreases, the particles spread upward, and increasingly more particles are removed, gradually reducing the total time required for complete removal. Taken together with the simulation results at the same velocity, these results reveal that the time required for the dust to be removed is more than that for the tar mist to be removed. Because the difference in particle size is not very large, the difference in density plays a large role. Density determines the gravity force, and the density of tar mist is less than that of dust, meaning that the gravity force on the tar mist is less than that of dust of the same mass. At the same velocity, the other additional forces are unchanged, so the time required for the tar mist to be carried out is less than that for the dust.Since the tar mist and dust are mixed into the furnace, the gas velocity is the same for both phases. The main purpose of this study was to separate the two phases, letting the tar mist be carried out and allowing as much dust as possible to flow back into the furnace for further dry distillation, so it is important to determine the appropriate corresponding velocity. Figure10 presents the time at which the particles are removed in Figures 8 and 9. The time difference between 0.68, 0.69, 0.71, and 0.72 m/s is small, and all values lie within a range of 0.7 s. At 0.70 m/s, the time difference is the largest, which is 1.7 s, which means that there is still more dust in the furnace when the tar mist is completely removed.Figure 10
Particle removal time as a function of the gas velocity.It can be seen from 5.1 and 5.2 that the above selected tar mist and dust particle size are the maximum values that can be removed by the gas. Select the two-phase particle with the smallest particle size when not removed and study the two-phase motion at the maximum velocity, as shown in Figures11 and 12.Figure 11
Volume fraction of tar mist:d = 0.30 mm and ρ = 900 kg/m3. (a) u = 0.70 m/s. (b) u = 0.72 m/s.
(a)
(b)Figure 12
Volume fraction of dust:d = 0.20 mm and ρ = 1100 kg/m3. (a) u = 0.70 m/s. (b) u = 0.72 m/s.
(a)
(b)Figure11 shows that the distribution area of particles in the furnace increases rapidly over time. At 1.8 s, the particle fills the area to 5/6, and the distribution area reaches its maximum. At 9.0 s, the particle distribution area is reduced to 4/6. At 120 s, it is reduced to 1/2, and the particles are always left in the furnace. A comparison of the simulation results at the same time reveals no change at 0.3 s. With increasing velocity at 0.6 s, the tar particles with a volume fraction of 0.35–0.45 aggregate in a higher location, and the particles with a bottom volume fraction of 0.20–0.30 are depleted. At 0.9 s, as the velocity increases, tar particles are concentrated with a volume fraction of 0.30 to 0.40 and 0.35 to 0.45 at the upper and bottom portions of the distribution area, respectively. At 9.0 s and 120 s, particles at a volume fraction of 0.35 to 0.50 disappear with increasing velocity, showing that although most of the particles remain in the furnace, some of them are still removed. It can be seen from Figure 12 that the distribution area of the particles in the furnace increases rapidly over time, and the entire area is filled in 1.6 s, with the distribution of particles at a volume fraction of 0.18–0.30 continuously decreasing in the working area. However, there are still some particles left in the furnace. A comparison of the simulation results at the same time reveals no change at 0.2 s and 0.4 s; at 0.8 s, particles (with a volume fraction of 0.21 to 0.27) are collected at a height of 4/6, and there is no significant difference in the remaining time except that the distribution area is expanded from 1/2 to 5/6.Figures8, 9, 11, and 12 verify that the gas velocity can change the length of time required for the two phases to be carried out, but the particle size of the particles is a key factor in determining whether removal is possible. The particle size of the tar mist should be less than 0.20 mm, and the particle size of the dust should be greater than 0.18 mm to achieve the aims of this study.


## 5.5. Effect of the Tar Mist and Dust Density

The density of tar mist and dust was changed, and the two-phase motion was studied. The motion simulation results are shown in Figures13 and 14.Figure 13
Volume fraction of tar mist:d = 0.20 mm and u = 0.70 m/s. (a) ρ = 900 kg/m3. (b) ρ = 950 kg/m3. (c) ρ = 1000 kg/m3. (d) ρ = 1050 kg/m3. (e) ρ = 1100 kg/m3.
(a)
(b)
(c)
(d)
(e)Figure 14
Volume fraction of dust:d = 0.18 mm and u = 0.70 m/s. (a) ρ = 1100 kg/m3. (b) ρ = 1200 kg/m3. (c) ρ = 1300 kg/m3. (d) ρ = 1400 kg/m3. (e) ρ = 1500 kg/m3.
(a)
(b)
(c)
(d)
(e)Figure13 shows that the distribution area of the particles in the furnace increases rapidly over time. At 2.7 s, the particles fill almost the entire area, and the distribution of particles gradually decreases. Finally, at 33.5 s, there is only a small amount of tar particles in the furnace, with a volume fraction of 0.03. As the density increases, the time required to remove the particles increases because of the influence of gravity. There is little difference between the results at 0.3 s and 0.9 s. The distribution area at 2.7 s is at a height of 5/6; however, the particles (with a volume fraction of 0.06–0.12) are enriched with increasing density, and the particles are slowly transported to the bottom, with a volume fraction of 0.30. At 8.1 s, only particles at a volume fraction of 0.12 or less remain in the furnace. As the density increases, the distribution area first increases and then decreases. Specifically, only a few particles (with a volume fraction of 0.03 to 0.09) are left at ρ = 900 kg/m3; at ρ = 950 kg/m3 and 1000 kg/m3, the density increases, and it is difficult to remove many particles at the same time, resulting in an increase in the distribution area. When ρ = 1050 kg/m3 and 1100 kg/m3, the volume fraction of the particles increases significantly, and the particles collectively move downward, resulting in a decrease in the distribution area. As shown in Figure 14, the distribution of particles in the furnace increases rapidly with time. The area is almost filled at 2.7 s, and the distribution of particles in the area is then gradually reduced. The final density is between 1100 kg/m3 and 1400 kg/m3, and removal is difficult when the density is 1500 kg/m3. A comparison of the simulation results indicates that since the density is less than that of the dust, the time required for tar mist removal is less than that of dust removal. The tar mist can be completely removed in the density range of 900–1100 kg/m3. When the dust density is 1500 kg/m3, the dust starts to gather at the bottom, and the degree of fluidization of the particles gradually decreases. At 120 s, the particle fluidization degree is the lowest, and the dust is difficult to remove.


## 6. Conclusions

In this paper, a physical model of the two-phase motion of furnace gas, tar, and dust in the internal structure of the internal heat type low-temperature dry distillation furnace is established. The Euler–Lagrangian method is used to simulate the two-phase flow. The OMEC Topsizer Plus laser particle size analyzer is used to measure the particle size distribution of the dust to verify the accuracy of the mathematical model and the reliability of the simulation results. On this basis, the effects of gas velocity, tar particle size, and dust particle size on the movement of tar mist and dust are investigated. The following main conclusions are drawn:(1)
The tar particles with a particle diameter of less than 0.20 mm are removed from the furnace by the gas. The smaller the particle size, the shorter the time required for removal, the lower the probability of secondary pyrolysis of the tar, and the higher the tar recovery rate. In actual production, efforts should be made to reduce the particle size of the tar.(2)
Dust with a particle size greater than 0.18 mm cannot be removed from the furnace and remains in the furnace for pyrolysis, which not only increases the yield of the tar but also reduces the content of particulate impurities in the tar. In actual production, the coal powder generated by the breakage of coal in the furnace is reduced as much as possible.(3)
As the gas velocity increases, the time for the tar mist and dust to be completely removed gradually decreases. When the velocity is 0.70 m/s, the tar mist can be completely removed, but the dust with a particle diameter larger than 0.18 mm cannot be completely removed.(4)
Providing theoretical guidance for industrial production, the results indicate that the tar produced by low-temperature dry distillation can be quickly removed by the gas, while the dust such as pulverized coal and semicoke remains in the furnace. When the gas velocity is controlled to 0.70 m/s, the tar particle diameter at a density of 900 kg/m3 is 0.10 mm, and the particle size of the dust with a density of 1500 kg/m3 is 0.20 mm.



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*Source: 2356038-2020-03-02.xml*