Numerical Investigation into Gas-Particle Inter-Phase Combustion and Reduction in the Flash Ironmaking Process

Abstract

Despite the dominance of the blast furnace ironmaking process, more attention is being paid to the new technologies with lower energy consumption and carbon dioxide emissions. A novel flash ironmaking technology using pulverized coals and iron concentrates as raw materials, which is different from flash ironmaking with the reductive gas as the reducing agent, is studied. In order to obtain the flow patterns, temperature, and gas composition distribution, as well as particle trajectories in the reaction shaft of the flash ironmaking furnace, the Euler–Lagrangian model with a custom user defined function (UDF) code is used to simulate the processes of the fluid flow, heat and mass transfer, and chemical reactions, including the combustion reaction of pulverized coals and reduction reaction of iron concentrates. The results indicate that the flow patterns, temperature, and gas composition distributions present symmetrical distribution characteristics. The central oxygen expands rapidly after entering the reaction shaft and its distribution is approximately bell-shaped. The temperature distribution in the reaction shaft is wing-shaped. The maximum temperature, 2615 K, is reached at 5 m below the roof of the reaction shaft. The O₂ is quickly consumed after entering the reaction shaft. At 6 m below the roof of the reaction shaft, the oxygen concentration becomes almost zero, with the CO concentration reaching the highest. The Fe₂O₃ and FeO in the iron concentrates are mostly reduced to Fe at 9 m below the roof of the reaction shaft, and more than 95 wt% iron particles could be obtained within 1.2–7.7 s.

1. Introduction

Steel and iron products are currently the most important structural materials, and are the functional materials with the largest output and the widest coverage [1]. With the rapid growth of the Chinese economy, there has been unprecedented growth in the iron and steel industry. In 2018, China’s steel production was more than 1.1 billion tons, most of which came from the blast furnace process. However, long processes, high-energy consumption, poor adaptability to poor resources, and especially environmental pollution problems are becoming increasingly prominent in the blast furnace process. To tackle the environmental and resource issues, a series of alternative ironmaking processes have been rapidly developed in recent decades, such as COREX, Midrex, FINEX, HIsarna and flash ironmaking [2,3]. The flash ironmaking technology, known as suspension reduction technology, is an advanced technology that aims at producing iron directly from iron concentrates without requiring palletization or sintering and also avoids the need for coke. The characteristic of the large specific surface area of iron concentrates is utilized to complete the reduction reaction at a very fast speed in the furnace with high temperature and a carbon monoxide atmosphere [4,5]. The chemical kinetics are incomparable because of the short process, less equipment required, and small energy consumption [6,7]. In order to increase steel production, and to effectively get rid of the shortage of coke resources and to save energy, it is important to conduct in-depth theoretical research on the flash ironmaking process.

Flash ironmaking technology has been developed since 2007, generally using natural gas, CH₄, CO, H₂, and pulverized coal as reducing agents. The technology was first conceived by Sohn [8] at the University of Utah, with reductive gas as the reducing agent. In recent years, Sohn and co-workers have conducted many interesting studies about the flash ironmaking process. Wang et al. [9,10] performed a set of experiments where H₂ was used to reduce the magnetite concentrate within different temperature ranges, obtaining nucleation and growth kinetics expression, which could be used to formulate the reduction rate of fine concentrate particles. A series of experiments were performed by Elzohiery et al. [11] where CH₄ was partially oxidized by oxygen to form reducing H₂ + CO gas mixtures. The experiment proved that the concentrate particles can be reduced directly in a flash reactor, and more than 80% reduction was achieved in the reactor. A computational fluid dynamics (CFD) model of a large-scale bench reactor for flash ironmaking was developed by Abdelghany et al. [5] to simulate the novel flash ironmaking process, which is based on the partial combustion of natural gas in the reactor. The reduction degrees and composition of the off-gas were obtained and compared with the experimental results, which is of great significance in the design and optimization of larger reactors. These works have given us certain insights into the flash ironmaking technology, but the reductive gases, such as natural gas, CH₄, CO, and H₂, are expensive, flammable, explosive, and not easy to store. As is well known, China is rich in coal resource. Gong and Wang et al. [12,13] used pulverized coals and iron concentrates as raw materials to carry out a lot of experiments in the flash ironmaking furnace, which is quite different from the studies by Sohn and co-workers. The prototype design of the key equipment and software package for the flash ironmaking furnace has almost been finished, which is a milestone of the development of the Chinese flash ironmaking furnace. However, the chemical reaction and physical field of the reaction shaft in the flash ironmaking furnace, with pulverized coals as the reducing agent, are obscure, whereas these are the core of the design of the reaction shaft. So, it is necessary to visualize the smelting process in the shaft through numerical simulation.

In this study, novel flash ironmaking technology using pulverized coals and iron concentrates as raw materials is studied. In order to obtain the flow patterns, temperature, and gas composition distribution, as well as the particle trajectories in the reaction shaft of the flash ironmaking furnace, a numerical model of the flash ironmaking process is established and calculated. The Euler method is used to solve the gas-phase governing equations and the Lagrangian method is used to solve the particle-phase governing equations. The ANSYS FLUENT software and custom user defined routine are employed to numerically simulate the smelting process of the flash ironmaking furnace, including the heat and mass transfer between the gas and particles phase, coal combustion, and reduction of iron concentrates. It can provide theoretical guidance for the structural design, optimizing operations, and feeding ratio of the flash ironmaking furnace.

2. Model Description

2.1. Physical Model

Flash ironmaking is an advanced technology that aims to reduce iron concentrates directly at a very fast speed in the furnace under high temperature and carbon monoxide atmosphere. Figure 1 shows the schematic of the flash ironmaking furnace, consisting of the reaction shaft, settler, and uptake. At the beginning of the smelting process, fine pulverized coal and 99% pure oxygen are injected from the nozzle and dispersed in the shaft to carry out a series of complex combustion reactions, releasing a lot of heat and creating a reducing atmosphere of carbon monoxide. Then, fine iron concentrates drop freely from the inlet, being reduced rapidly by high-temperature reducing gas during the falling process. Eventually, reduced metallic iron and off gas are separated through the settler and uptake. Due to the high temperature and violent redox process in the furnace, it is difficult to obtain the relative parameters through experiments. However, the flow patterns, temperature, and gas composition distribution, as well as particle trajectories, are very important for the safe operation of the flash ironmaking furnace. Therefore, in the present work, the numerical simulation method was used to visualize the distribution of the physical field in the furnace.

The smelting process of the flash ironmaking belongs to the gas-particle two-phase mixing flow. The processes of flow, mixing, pulverized coal combustion, and reduction of iron concentrates occur in the reaction shaft. The simulation study of the reaction shaft is very significant for the operation of the flash ironmaking furnace. The reaction shaft, with a height of 10 m, was taken as the research object. In order to effectively reduce the number of meshes and calculation time, only half of the reaction shaft was taken as the computational domain, because the reaction shaft is cylindrical and has good symmetry in structure. The physical model of the reaction shaft is shown in Figure 2.

The unstructured grid was adopted, and the total number of grids was 2,348,938. As the inlet of the central oxygen and pulverized coals is small and the thickness of the reaction shaft wall is thin, in order to improve the calculation accuracy, these computational domains were locally refined when the reaction shaft was meshed. Compared to the calculation results of the dense mesh size, the test of mesh independence showed that the relative error of temperature and concentration in the reaction shaft is less than 5%.

At boundaries, the inlet velocity of central oxygen was 12 m/s. The flow of pulverized coal and iron concentrate were 2.95 t/h and 6.48 t/h, respectively. The outlet of the reaction shaft was set as the free outflow, the symmetry plane of the reaction shaft was set as symmetric boundary, and the rest were set as constant temperatures based on the measurement of the spot.

The proximate and ultimate analyses of the coal can be seen in

Table 1. The proximate and ultimate analyses of the coal.

Proximate Analysis	Wt (%)	Ultimate Analysis	Wt (%)
Fixed carbon	51.3%	C	78.6%
Volatile matter	43.2%	H	4.96%
Ash	3.2%	O	15.04%
Moisture	2.3%	N	0.9%
		S	0.9%

, and the composition of iron concentrates, in which just Fe₂O₃ and FeO are considered in the reduction reaction, is given in

Table 2. Concentrate compositions (mass fraction).

Fe2O3	FeO	CaO	MgO	Al2O3	SiO2	Others
73.1%	24.9%	0.5%	0.68%	0.21%	0.32%	0.3%

.

2.2. Mathematical Model

The smelting process in the reaction shaft involves the exchange of momentum, heat, and mass between the gas and particles. In this study, the gaseous model was based on the Euler method, and the particle phase was based on the Lagrangian method. The standard k-ε model was used to describe the turbulence.

2.2.1. Basic Assumptions

For the smelting process in the reaction shaft, the following simplifications were put forward:

(1) Particles including pulverized coal and iron concentrate were assumed to be spherical with specific equivalent diameters, and the shape factor of the particle was 1;

(2) The solid phase included pulverized coal, Fe₂O₃, FeO, Fe₃O₄, and Fe. The gas phase was assumed to be a mixture of volatile, O₂, CO, CO₂, H₂O, SO₂, and N₂;

(3) The influence of furnace slagging on the inner shape of the reaction shaft was ignored.

2.2.2. Gas-Phase Governing Equations

The governing equations include the continuity equation, momentum equation, energy equation, and species transport equation. These equations in steady state can be expressed in the following general form [14,15,16,17,18]:

$$\nabla \cdot \left(\rho v\phi \right)=\nabla \left({\Gamma }_{\phi }\nabla \phi \right)+S_{\phi }+S_{p\phi },$$

(1)

where ρ is the gaseous density, v is the velocity, φ is the general dependent variable, Γ_φ is effective diffusion coefficient, S_φ is the source term of the gaseous phase, and S_pφ is the source term generated from the interaction between gas and particles. When using Equation (1) to solve different equations, the specific forms of the variables are listed in

Table 3. General forms of turbulent transport equations.

Equation	φ	Γφ	Sφ
Continuity	1	0	0
Momentum	v	${\mu }_{eff}={\mu }_0+{\mu }_T$	$-\nabla p+\nabla \cdot \left({\mu }_{eff}\nabla \nu \right)$
Energy	h	$\frac{{\mu }_{eff}}{{\delta }_h}$	−qr
Species	Yi	$\frac{{\mu }_{eff}}{{\delta }_Y}$	−wi

.

In Table 3, μ₀ is molecular viscosity, μ_T is the turbulence viscosity, h is the enthalpy, Y_i is the mass fraction of species i, δ_h and δ_Y are dimensionless numbers of the corresponding equation. μ_eff is the effective viscosity (the sum of molecular viscosity and turbulent viscosity), p is the static pressure, q_r is the heat source due to the chemical reaction and radiation, and w_i is the source terms of the gas species.

2.2.3. Particle-Phase Governing Equations

The particle trajectories of pulverized coals and iron concentrates were solved by the Lagrangian discrete phase model (DPM). The uniform distribution function was used to represent the particle size distribution, and the governing equation was given by [16,17,18,19]:

$$m_p\frac{d{v}_p}{dt}=F_D+m_p\frac{g\left({\rho }_p-\rho \right)}{{\rho }_p}+F,$$

(2)

where m_p is the mass of the particle, v_p is the velocity vector of the particle, g is the gravity acceleration, ρ_p is the density of the particle, F_D is the drag force, and F is the additional force born by the particles. The additional force here represents forces related to the velocity gradient, pressure gradient, and the temperature gradient where they exist.

The heat transfer between the particle phase and the continuous phase can be solved by the following equations [18,19]:

$$m_p\frac{d\left(C_P{T}_P\right)}{dt}=Q_r+Q_c+Q_{rad},$$

(3)

$$Q_C=\pi d_p\lambda (2.0+0.6{\mathrm{Re}}^{\frac{1}{2}}{\left(\mu C_P/\lambda \right)}^{\frac{1}{3}}\left)\right(T_g-T_p),$$

(4)

$$Q_{rad}={{\epsilon }^{\prime }}_p\sigma ({\epsilon }_g{T}_g{}^4-a_g{T}_p{}^4),$$

(5)

where C_p is the specific heat of the particles, and T_p is the temperature of a particle. Q_r, Q_c, and Q_rad represent the heat caused by the reaction, convection, and radiation between the gas and particles, respectively. d_p is the average diameter of the particles, λ is the thermal conductivity of the particles, Re is the Reynolds number, μ is the dynamic viscosity, and T_g and T_p are the temperatures of the gas phase and particles, respectively. ε’_p is the emissivity of particle surface, ε_g is the emissivity of the gas phase, a_g is the absorption rate of the gas phase, and σ is the Stefan–Boltzmann constant.

2.2.4. Combustion Modeling

The combustion process of pulverized coals is comprised of heating and evaporation, devolatilization, char oxidation, and gas phase reactions. The combustion process starts when the temperature of the coal particles is 100 °C, at which point the moisture evaporates and moves into gas phase [20]. Additionally, the devolatilization process begins at a particle temperature of 280 °C [21]. In the present study, the single rate equation was used to simulate the devolatilization process [21]. The change in the volatile mass of the coal particles was calculated by:

$$\frac{d{m}_{vol}}{dt}=k_{vol}\left(m_{o,vol}-m_{vol}\right),$$

(6)

$$k_{vol}=A_{vol}\exp \left(-\frac{E_{a,vol}}{RT}\right),$$

(7)

where m_vol is the mass of the volatile released from the coal particles, and m_0,vol is the initial volatile mass of the coal particles before combustion. R is the gas constant and T is the particle temperature. A_vol is the pre-exponential factor and E_a,vol is the activation energy. The empirical constants [22] used in present work were:

$$A_{vol}=2\times {10}^5{\mathrm{s}}^{-1}\hspace{1em}{E}_{a,vol}=6.7\times {10}^7\mathrm{J}/\mathrm{kmol}.$$

(8)

After the volatiles are completely driven out from the coal particles, the char oxidations start. The diffusion kinetics limited char combustion is used in the CFD model [23]. The char oxidation is affected by the diffusion rate of O₂ to the particle surface and the chemical reaction rate of the char oxidation process. Additionally, the char oxidation product is CO or CO₂ in this model. The oxidation product was CO in the present work, so the reaction of the char oxidation and the rate of char oxidation are shown in Equations (9) and (10), respectively:

$${\mathrm{C}}_{\left(\mathrm{s}\right)}+0.5{\mathrm{O}}_2\to {\mathrm{CO}}_{\left(\mathrm{g}\right)},$$

(9)

$$\frac{d{m}_{char}}{dt}=-A_P\frac{R_C{R}_{diff}}{R_C+R_{diff}}{P}_{O_2},$$

(10)

where A_P is the particle surface area, R_diff is the rate coefficient for the oxygen diffusion, R_c is the chemical reaction rate coefficient, and P_O2 is the partial pressure of oxygen in the gas phase surrounding the fuel particle.

$$R_{diff}=\frac{5\times {10}^{-12}}{d_p}{\left(\frac{T_g+T_p}{2}\right)}^{0.75}$$

(11)

$$R_C=A_C\exp \left(-\frac{E_{a,c}}{R{T}_p}\right)$$

(12)

The kinetics rate parameters for char oxidation were taken from the work by Sheng et al. [22], and the empirical constants used in the present study were:

$$A_C=0.0053\mathrm{kg}/({\mathrm{m}}^2\cdot \mathrm{s}\cdot \mathrm{Pa})E_{a,c}=8.37\times {10}^7\mathrm{J}/\mathrm{kmol}.$$

(13)

Once the volatiles from the devolatilization and CO from the char oxidation are released into the gas phase, they would react with oxygen. The rate at which these species are oxidized is a function of the Arrhenius rates of the chemical reactions and the turbulence interaction with the chemical reactions [20]. The gas phase reactions solved in the shaft are:

$${\mathrm{C}}_{1.45}{\mathrm{H}}_{2.88}{\mathrm{O}}_{0.55}{\mathrm{N}}_{0.0376}{\mathrm{S}}_{0.0091}+1.18{\mathrm{O}}_2\to 1.45\mathrm{CO}+1.44{\mathrm{H}}_2\mathrm{O}+0.0188{\mathrm{N}}_2+0.0091{\mathrm{SO}}_2$$

(14)

$${2\mathrm{CO}+\mathrm{O}}_2\to {2\mathrm{CO}}_2.$$

(15)

C_1.45H_2.88O_0.55N_0.0376S_0.0091 is the pseudo volatile molecule. In our study, the eddy dissipation finite rate model was used [20,24]. The chemical Arrhenius rate of the reaction, the rate of the turbulent production eddies dissipation, and the rate of the dissipation of reaction eddies are shown in Equations (16)–(18). The gas combustion rate depends on the smallest of the three rates and the slowest step is the rate-controlling step.

$$R_r=A_r\exp \left(-\frac{E_{a,r}}{R{T}_g}\right)\left(v_{k,r}^{\prime }-v_{k,r}\right){{\displaystyle \prod _L\left[C_{l,r}\right]}}^{m,r},$$

(16)

$$R_{k,r}=v_{k,r}{M}_{w,k}A\rho \frac{\epsilon }{k}\min \left(\frac{Y_R}{v_{R,r}{M}_{w,R}}\right),$$

(17)

$$R_k{}_{,r}=v_{k,r}{M}_{w,k}AB\rho \frac{\epsilon }{k}\min \left(\frac{{\displaystyle \sum {}_P{Y}_R}}{{\displaystyle {\sum }_j^{}{v}_{j,r}{M}_{w,j}}}\right),$$

(18)

where Y_R is the mass fraction of a particular reactant R and Y_P is the mass fractions of any product species P. M_w,j is the molecular weight of species j. v_k,r is stoichiometric coefficient for reactant k in reaction r, [Cl,r]^m,r is the molar concentration of species l in reaction r with a rate exponent of m.

A_r is the pre-exponential factor of the chemical reaction r, and E_a,r is the activation energy of reaction r. The constants for the reaction in Equation (14) are shown in Equation (19), and the constants of CO oxidation in Equation (15) are shown in Equation (20).

$$\begin{array}{l}{A}_r=2.56\times {10}^{11}{\mathrm{s}}^{-1},E_{a,r}=1.081\times {10}^8\mathrm{J}/\mathrm{kmol}\\ A=4,B=0.5\end{array}$$

(19)

$$\begin{array}{l}{A}_r=8.83\times {10}^{11}{\mathrm{s}}^{-1},E_{a,r}=9.98\times {10}^7\mathrm{J}/\mathrm{kmol}\\ A=4,B=0.5\end{array}$$

(20)

The Arrhenius empirical constants used in Equation (19) were from the work of Guo et al. [25], and the constants used in Equation (20) were taken from the work of Kim et al. [26].

2.2.5. Reduction Reactions

The reduction reactions of the iron oxides considered in this model are listed in Equations (21)–(23) [27,28,29]. FeO is directly reduced to Fe at the appropriate temperature and carbon monoxide atmosphere. Fe₂O₃ is first reduced to Fe₃O₄, then to FeO, finally to Fe.

$${3\mathrm{Fe}}_2{\mathrm{O}}_3+\mathrm{CO}\to {2\mathrm{Fe}}_3{\mathrm{O}}_4{+\mathrm{CO}}_2$$

(21)

$${\mathrm{Fe}}_3{\mathrm{O}}_4+\mathrm{CO}\to {3\mathrm{FeO}+\mathrm{CO}}_2$$

(22)

$$\mathrm{FeO}+\mathrm{CO}\to {\mathrm{Fe}+\mathrm{CO}}_2$$

(23)

According to previous works [29,30,31], the general reaction rate expression was used to describe the reduction reactions by:

$$R_n=\left(\frac{6{\mathsf{\alpha }}_s\cdot f_s}{{\mathsf{\phi }}_s\cdot d_s}\right)\frac{{\rho }_g}{W}{\displaystyle \sum _{m=1}^3\left[a_{n,m}\left(K_m\frac{w_{co,g}}{M_{co}}-\frac{w_{c{o}_2,g}}{M_{c{o}_2}}\right)\right]},$$

(24)

where R_n is the chemical reaction rate of reaction n (kmol·m⁻³·s⁻¹), n = 1,2,3, corresponding to Equations (21)–(23), α_s is the volume fraction of the solid phase in shaft furnace, f_s is the volume fraction of the species, φ_s is the shape factor of the solid particles. d_s is the diameter of solid particles; w_co,g and w_co2,g are the mass fractions of CO and CO₂, and M_CO and M_CO2 are the mole masses of CO and CO₂. W and a_n,m are grouped variables comprised of the parameters which characterize the reaction, including the equilibriums and rate constants, effective diffusivities, solid phase compositions, and radii of the unreacted cores from previous works [29,30,32]. In this study, the reduction reactions listed in Equations (21)–(23) were simulated with the shrink core model separately and the corresponding reduction reactions were assumed to be finished when their equivalent diameter was smaller than 0.74 μm.

2.3. Numerical Solution Technique

To solve the equations established and to obtain the flow field, temperature, species concentration distributions, and particle trajectories, the ANSYS FLUENT 18.0 software (Pittsburgh, PA, USA) with a custom UDF code was used. The PISO algorithm was used to couple the pressure and velocity. The first order upwind discretization scheme was chosen for the equations of species transport, and the second order upwind discretization scheme was chosen for other equations. During the solution, only the equations of flow and energy were initially solved to obtain a quasi-steady flow field in the reaction shaft of the ironmaking furnace. Then, the equation of species transport, radiation model, and discrete phase model was activated. The residuals for the conservation equations were set as 10⁻⁶.

2.4. Model Verification

Due to the exploration stage of the novel flash ironmaking furnace, as well as the high temperature in the shaft, it is difficult to measure the relative parameters in the shaft of the flash ironmaking furnace. In this paper, two thermocouples were used to measure the gas temperature in a test furnace.

Table 4. Comparison between calculated and measured gas temperatures.

Location (H, r)	Measuring Results/K	Simulation Results/K	Deviation/%
(1.6, 0.5)	1813	1896	4.37
(2, 0.9)	1937	2005	3.39

shows the simulated and measured results of the gas temperature, which proves a good accuracy of the mathematical model for the flash ironmaking process. The vertical distance below the roof of the reaction shaft is referred to as the shaft height H, and r is the distance from the measuring point to the center axis.

3. Results and Discussion

3.1. Velocity Distribution

Figure 3 and Figure 4 show the velocity contour and streamline diagram on the symmetry plane, respectively. It can be seen from Figure 3 that the flow in the reaction shaft presented a symmetrical distribution, and the high-velocity region where the velocity reached 12 m/s was mainly located at the inlet of the shaft. After the central oxygen was fed into the reaction shaft, a bell-shaped gas column was formed in the center of the shaft, surrounded by recirculating flows in the upper section near the shaft wall, as shown in Figure 4. At the same time, the gas flow continuously attenuated and homogenized during the movement so that the speed dropped along the flow direction. As a positive aspect, the existence of the recirculating flows can suppress the expansion of the main gas column and provides protection to the shaft wall. The hot gas in the lower part can be brought up to the upper part and becomes an important heat source for heating cold gas and particles. As a negative fact, the presence of recirculating flows rolls up the particles in the lower part and increases the dust in the furnace, which will exacerbate the scour of the refractory material and put forward higher requirements for scour resistance of the refractory material [33].

3.2. Temperature Distribution

The gaseous temperature within the reaction shaft was also simulated to indicate the smelting performance. The temperature contour in the reaction shaft is illustrated in Figure 5. Pulverized coals, oxygen, and iron concentrates, which were mixed in a certain ratio, were injected into the shaft. When the temperature and gas concentration reached the ignition condition, pulverized coals ignited and underwent intense combustion chemical reactions [34]. As can be seen from Figure 5, except for an obvious low temperature zone below the inlet, the temperature distribution was wing-shaped with high temperatures. Normal temperature oxygen, pulverized coals, and iron concentrates were heated by the high temperature gas during the injection process. During the heating process, the combustion chemical reaction between O₂ and pulverized coals took place violently, and produced CO and CO₂ gases, and also emitted a lot of heat, making the gas-phase temperature in the reaction shaft rise significantly along the direction of the gas flow. The maximum temperature, 2615 K, was reached at approximately 5 m below the roof of the reaction shaft. The temperature in the lower part of the shaft was more uniform, and large gradients existed in the upper part, especially near the central line of the reaction shaft. Affected by recirculating flows near the wall, high-temperature gas in the lower part was transferred to the upper side of the shaft, so the temperature in the upper zone of the reaction shaft was also high.

Plots were made of gaseous average temperature along the height of the shaft, as shown in Figure 6. Due to the violent combustion and the recirculating flows, the average gas temperature increased within 0–5 m below the roof of the reaction shaft. With the injected O₂ consumed, as shown in Figure 7a, the combustion reaction stopped gradually and the gas temperature decreased between 5–10 m below the roof of the reaction shaft. The average gas temperature along the height first increased and then reduced slowly, the maximum of which was located at 5 m below the roof of the reaction shaft, suggesting that the combustion between the pulverized coals and O₂ mainly happened in the upper section of the shaft.

3.3. Concentration Distribution

The concentration distribution of O₂, CO, and CO₂ on the symmetry plane is a good indicator of the smelting performance (as shown in Figure 7). It can be seen from Figure 7a that the highest mass fraction of oxygen was 99 wt% and the lowest is almost 0. The oxygen injected was quickly consumed and the oxygen concentration decreased rapidly with the combustion reactions. At 6 m below the roof of the reaction shaft, the O₂ concentration was almost 0, indicating that the combustion chemical reaction between O₂ and pulverized coals had basically been completed, which is almost consistent with the above results.

It can be seen from Figure 7b that the highest mass fraction of CO was 34 wt%, and the lowest was almost 0. Except for a low CO concentration zone below the inlet, CO was basically present. After the pulverized coals were fed into the reaction shaft, CO was immediately generated because the temperature of the particles increased rapidly under high-temperature radiation and heat convection, as well as the violent reaction of coal particles with O₂. From Figure 7b, the CO mass fraction in the down side of the reaction shaft was larger than that in the upper side, which may have been caused by the completion of the reduction reaction of most iron concentrates and the exhaustion of oxygen in the lower shaft.

It can be seen from Figure 7c that the highest mass fraction of CO₂ was up to 62 wt%, and was located in the upper section near the wall. The reason is that the pulverized coal was fully burned due to sufficient O₂ below the inlet, and there were many recirculating flows in the upper section near the wall. Comparing the CO₂ in the upper side of the reaction shaft and in the down side, lower CO₂ concentration was present in the down side, which was caused by the formation of massive CO because of the incomplete combustion of pulverized coal.

From the analysis above, at the inlet of pulverized coals and oxygen, the concentrations of CO and CO₂ were almost zero, because the combustion reaction had not yet happened. With the reaction of pulverized coals with O₂, the concentration of O₂ decreased rapidly, and the concentrations of CO and CO₂ increased quickly. At 6 m below the roof of the reaction shaft, the concentration of O₂ was almost zero and the concentration of CO almost reached its highest. Because the reduction process of iron concentrates was virtually completed, the concentration of CO₂ near the wall was about 50 wt%, which was much higher than that of CO. Except for the inlet of pulverized coals and oxygen, there was a reductive atmosphere in the other regions that guaranteed the basic conditions for the reduction of iron concentrates.

3.4. Particle Trajectory and Content Distribution

The particle trajectories could be obtained by the Lagrangian method. Figure 8 shows the particle trajectories and component contents of Fe₂O₃, FeO, Fe₃O₄, and Fe in the reaction shaft, and Figure 9 shows the mass fraction of Fe₂O₃, FeO, Fe₃O₄, and Fe at different heights of the reaction shaft. It can be seen from Figure 8a,b and Figure 9 that there were large amounts of Fe₂O₃ and FeO in iron concentrates under the inlet. With the reduction of Fe₂O₃ in Equation (21), the content of Fe₂O₃ decreased rapidly. The change in the FeO content was more complicated, which was caused by the existence of complex reactions, including the formation of FeO in Equation (22), and the reduction of FeO in Equation (23) at the same time. As shown in Figure 8c, the content of Fe₃O₄ first increased because of the reduction of Fe₂O₃ in Equation (21), then decreased because of the reduction of Fe₃O₄ in Equation (22). As shown in Figure 8 and Figure 9, the Fe₂O₃ and FeO were almost completely reduced at 9 m below the roof of the reaction shaft.

It can be seen from Figure 8d and Figure 9 that the mass fraction of Fe increased along the height when H was larger than 2 m. Between 3 and 7 m below the roof of the reaction shaft, the generation rate of Fe was significant, which may be related to the high temperature in this section, as shown in Figure 6. At 9 m below the roof of the reaction shaft, the Fe₂O₃ and FeO in iron concentrates were basically reduced to Fe, and the mass fraction of Fe reached more than 95%. According to statistical analysis of iron concentrate particles, the residence time of iron concentrates in the reaction shaft was within 1.2–7.7 s, which is consistent with Sohn’s results [10].

From the analysis above, the iron concentrates almost did not react with CO due to the low temperature and low CO content when they just entered the reaction shaft. The Fe₂O₃ and FeO in the iron concentrates were reduced to Fe between 2 and 9 m below the roof of the reaction shaft, and more than 95 wt% iron particles could be obtained, suggesting that the flash ironmaking process, using pulverized coals, oxygen, and iron concentrates as raw materials, is an alternative for ironmaking.

4. Conclusions

A novel flash ironmaking technology using pulverized coals and iron concentrates as raw materials was studied. This technology produces iron without requiring the palletization or sintering of iron and also avoids the need for coke. In the reaction shaft of the flash ironmaking furnace, the Euler–Lagrangian model with a custom UDF code was applied to conduct the simulation of the fluid flow, heat transfer, and chemical reactions, including the combustion of pulverized coals and the reduction of Fe₂O₃, Fe₃O₄, and FeO. The distribution characteristics of multi-physical fields such as velocity field, temperature field, concentration field, and particle trajectories, are studied. The main conclusions are as follows:

(1) The central oxygen expands rapidly after entering the reaction shaft and forms an approximately bell-shaped gas column. The temperature distribution in the reaction shaft is wing-shaped. The highest temperature, 2615 K, is reached at 5 m below the roof of the reaction shaft;

(2) The violent combustion of pulverized coals has basically been finished at 6 m below the roof of the reaction shaft. With the completion of the combustion chemical reaction and the generation of CO and CO₂, CO and CO₂ exist in most regions of the reaction shaft, except for the inlet of O₂ and pulverized coals;

(3) The Fe₂O₃ and FeO in iron concentrates have been completely reduced at 9 m below the roof of the reaction shaft, and more than 95 wt% iron particles could be obtained within 1.2–7.7 s, suggesting that the flash ironmaking process, using pulverized coals, oxygen, and iron concentrates as raw materials could be an alternative method for ironmaking.

The models and methods presented in this study can be extended to investigate the structure and operating parameters of the reaction shaft for the design of the flash ironmaking furnace.