A baffle reverse type high-temperature smoke dust separator

Abstract

This invention relates to the field of converter steelmaking flue gas purification and waste heat recovery technology, specifically to a baffle-reversing high-temperature flue gas separator, comprising: a shell, an air inlet, an air outlet, a guide plate, an ash hopper, and a multi-stage telescopic turbulence structure; the top of the shell is provided with an air inlet and an air outlet, the interior of the shell is provided with a settling chamber, and a guide plate is provided on the settling chamber; the multi-stage telescopic turbulence structure is located in the settling chamber, and the multi-stage telescopic turbulence structure includes multiple layers of baffle assemblies, each layer of baffle assembly having its surface inclined towards the flue gas movement direction; the ash hopper is located at the bottom of the shell. By setting a multi-stage telescopic turbulence structure driven and adjusted by a servo motor inside the baffle-reversing high-temperature flue gas separator, flexible control of the baffle angle, length, and spacing can be achieved, effectively reducing the oxygen retention area and enhancing the flue gas deflection and particle collision separation effect, thereby improving particle separation efficiency and oxygen replacement efficiency.

Description

Technical Field

[0001] This invention relates to the field of converter steelmaking flue gas purification and waste heat recovery technology, specifically to a baffle-reversing high-temperature flue gas separator. Background Technology

[0002] In the converter steelmaking process, the primary flue gas has a high sensible calorific value, high dust concentration, and is rich in combustible gas components, mainly carbon monoxide. With the increasing demands for energy conservation, carbon reduction, and resource recovery in the steel industry, the primary dry flue gas purification and waste heat recovery technology for converters has gradually become an important development direction for converter flue gas treatment due to its advantages such as sensible heat recovery capability and no water resource requirements.

[0003] In existing dry or fully dry converter primary flue gas systems, high-temperature dust separators typically perform functions such as coarse dust removal and flow field regulation. However, existing equipment mainly uses coarse dust removal structures such as inertial classifiers, banana bends built into evaporative coolers, or traditional baffle components. These systems generally suffer from low separation efficiency (usually difficult to reach 40%), high system resistance (usually exceeding 500 Pa), severe local wear, and insufficient attention to the rapid gas replacement capability within the system. This can easily lead to excessive load on subsequent fine dust removal equipment, shortening its service life. For dry converter primary flue gas processes, the system is not always in a stable gas recovery state, but rather undergoes a dynamic process of switching from an air environment to a converter gas environment. If a high concentration of oxygen remains inside the separator during the switching process, it is highly likely to react with carbon monoxide and cause an explosion. Furthermore, since the flue gas temperature at the outlet of the vaporization cooling flue in dry systems is typically 600-800℃, this further amplifies the explosion risk. Therefore, rapidly reducing the oxygen concentration in the system at the initial stage of gas introduction is a crucial prerequisite for achieving safe gas recovery.

[0004] In existing technologies, high-temperature dust separators in primary dry or fully dry converter flue gas systems suffer from problems such as low initial particle separation efficiency, high system resistance, and insufficient gas replacement efficiency. In particular, there are safety hazards caused by the large oxygen retention area inside the separator and the slow rate of decrease in outlet oxygen concentration during the initial stage of gas recovery. Summary of the Invention

[0005] Therefore, the technical problem to be solved by the present invention is to overcome the problems of low initial particle separation efficiency, large system resistance and insufficient gas replacement efficiency of high temperature dust separators in the dry or fully dry converter flue gas systems of the prior art. In particular, it solves the safety hazards caused by the large oxygen retention area inside the separator and the slow rate of decrease of outlet oxygen concentration in the early stage of gas recovery, thereby providing a baffle-reversing high temperature dust separator.

[0006] To address the aforementioned technical problems, this invention provides a baffle-reversing high-temperature flue gas separator, comprising: a shell, an air inlet, an air outlet, a guide plate, an ash hopper, and a multi-stage telescopic turbulence structure; the top of the shell is provided with an air inlet and an air outlet, the interior of the shell is provided with a settling chamber, and a guide plate is provided on the settling chamber; the multi-stage telescopic turbulence structure is located in the settling chamber, and the multi-stage telescopic turbulence structure includes multiple layers of baffle assemblies, the surface of each layer of baffle assembly being inclined towards the direction of flue gas movement; the ash hopper is located at the bottom of the shell.

[0007] Furthermore, each layer of the baffle assembly has two rows of baffles, which are spaced apart and mirrored.

[0008] Furthermore, the angle between the baffle and the direction of flue gas movement is 45°, 60°, or 75°.

[0009] Furthermore, the guide vane is located between two rows of baffles.

[0010] Furthermore, it also includes a support mechanism, a servo motor, and a rotating mechanism. The support mechanism is located inside the housing. One end of the support mechanism is connected to the servo motor, and the other end is connected to the rotating mechanism. The baffle is disposed on the rotating mechanism.

[0011] Furthermore, a rotating shaft is provided in the middle of the baffle, and the rotating shaft is connected to a rotating mechanism.

[0012] Furthermore, each of the baffles is provided with a vertical guide rail adjustment mechanism and a horizontal guide rail adjustment mechanism.

[0013] Furthermore, the outer surface of the baffle is provided with a wear-resistant layer.

[0014] Furthermore, the baffle is a ceramic liner.

[0015] Furthermore, the housing is provided with an air inlet pipe and an air outlet, the air inlet being located on the air inlet pipe and the air outlet being located on the air outlet pipe.

[0016] The technical solution of this invention has the following advantages: The baffle-reversing high-temperature flue gas separator provided by this invention achieves flexible control of the baffle angle, length, and spacing by incorporating a multi-stage telescopic turbulence structure driven and adjusted by a servo motor. This effectively reduces the oxygen retention area and enhances the deflection and particle collision separation effects of the flue gas, thereby improving particle separation efficiency and oxygen replacement efficiency. It provides a primary inertial separator for converter primary dry systems that combines high efficiency, low resistance, and safety and stability.

[0017] The baffle-reversing high-temperature flue gas separator provided by this invention is suitable for flue gas purification and waste heat recovery systems in a primary dry converter system. When the system switches from an air environment to a converter gas environment, the separator outlet is used as the monitoring section, and the oxygen mass fraction is set as a safety threshold of no more than 2%. By optimizing the baffle structure parameters, the time for the oxygen mass fraction to reach the safety threshold is shortened as much as possible to meet the requirements of safe gas recovery.

[0018] The summary section is provided to present the chosen concepts in a simplified form, which will be further described in the detailed description below. The summary section is not intended to identify essential or necessary features of this disclosure, nor is it intended to limit the scope of this disclosure. Attached Figure Description

[0019] To more clearly illustrate the specific embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the specific embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are some embodiments of the present invention. For those skilled in the art, other drawings can be obtained from these drawings without creative effort.

[0020] Figure 1 A schematic diagram of the baffle-reversing high-temperature flue gas separator provided by the present invention; Figure 2 A plan view of a similar experimental platform built for the baffle-reversing high-temperature flue dust separator provided by the present invention; Figure 3 The separation efficiency results of the baffle-reversing high-temperature flue gas separator provided by the present invention; Figure 4 The oxygen replacement time results for operating conditions 1-3 of the baffle-reversing high-temperature flue gas separator provided by the present invention; Figure 5 The oxygen replacement time results for operating conditions 4-6 of the baffle-reversing high-temperature flue gas separator provided by the present invention; Figure 6 The oxygen replacement time results for operating conditions 7-9 of the baffle-reversing high-temperature flue dust separator provided by the present invention; Figure 7 The results of oxygen replacement time for operating conditions 10-12 of the baffle-reversing high-temperature flue gas separator provided by the present invention.

[0021] Explanation of reference numerals in the attached figures: 1. Air inlet; 2. Settling chamber; 3. Air outlet; 4. Baffle plate; 5. Ash hopper; 6. Multi-stage telescopic turbulence structure; 7. Centrifugal variable frequency fan; 8. Heater; 9. Powder sprayer; 10. Inspection window; 11. Shell; 12. S-shaped Pitot tube; 13. Air inlet pipe; 14. Air outlet pipe. Detailed Implementation

[0022] In the following description, only certain exemplary embodiments are briefly described. As those skilled in the art will recognize, the described embodiments can be modified in various ways without departing from the spirit or scope of this disclosure. Therefore, the drawings and description are to be considered exemplary in nature and not restrictive.

[0023] The preferred embodiments of this disclosure are described below with reference to the accompanying drawings. It should be understood that the preferred embodiments described herein are for illustration and explanation only and are not intended to limit this disclosure.

[0024] Please see Figures 1 to 7 As shown, this invention provides a baffle-reversing high-temperature dust separator, located at the outlet of the converter vaporization cooling flue. The core function of this baffle-reversing high-temperature dust separator is to achieve efficient separation of metal particles from the converter gas, while simultaneously achieving rapid oxygen replacement within the separator during the dynamic production process of switching from an air environment to a gas environment. This not only ensures efficient purification of the converter and guarantees the safe operation of subsequent fine dust removal equipment, but also ensures that the oxygen concentration inside the separator quickly reaches a safe threshold, guaranteeing the long-term safe operation of the converter steelmaking system.

[0025] The baffle-reversing high-temperature flue gas separator includes: a shell 11, an air inlet 1, an air outlet 3, a guide plate 4, an ash hopper 5, and a multi-stage telescopic turbulence structure 6; the top of the shell 11 is provided with an air inlet 1 and an air outlet 3, the interior of the shell 11 is provided with a settling chamber 2, and a guide plate 4 is provided on the settling chamber 2. The multi-stage telescopic turbulence structure 6 is located in the settling chamber 2 and includes a multi-layer baffle assembly, the surface of each baffle assembly is inclined towards the direction of flue gas movement, and the ash hopper 5 is located at the bottom of the shell 11.

[0026] The air inlet 1 is located on the left side of the separator shell 11 and is connected to the outlet of the converter vaporization cooling flue. It is used to introduce high-temperature dusty flue gas. The air outlet 3 is located on the right side of the separator shell 11 and introduces the flue gas after primary purification by the baffle reverse high-temperature dust separator into the next stage of converter operation equipment. The ash hopper 5 is located at the bottom of the separator and is used to collect particulate matter that settles under inertial and gravity.

[0027] The settling chamber 2 is preferably a truncated pyramidal structure with a tapering lower section, which reduces the adhesion of particles in the high-temperature dusty flue gas to the separator surface. The inclined wall design facilitates the smooth collection of settling particles to the bottom ash discharge area, and also reduces the problem of secondary dust generation caused by bottom backflow, thereby achieving stable recovery and cleaning of particulate dust.

[0028] The guide plate 4 is located between the two rows of baffles and is located in the upper middle part of the settling chamber 2. It is used to guide the flue gas to enter the flow channel area where the multi-stage telescopic turbulence structure 6 is located evenly, and to extend the effective flow distance of the flue gas in the separator, thereby reducing the possibility that the flue gas will escape directly without being fully separated due to local short-circuit flow.

[0029] The guide plate 4 is located in the upper middle part of the settling chamber 2, which separates the multi-stage turbulence baffle group. On the one hand, it extends the flow distance of the flue gas inside the separator, and on the other hand, it prevents the flue gas from escaping after being deflected by the first-stage turbulence baffle and failing to contact the second-stage turbulence baffle.

[0030] Each layer of the baffle assembly has two rows of baffles, which are spaced apart and mirrored.

[0031] The multi-stage telescopic turbulence structure 6 is arranged sequentially along the mainstream direction of the flue gas, with adjacent rows of baffles tilting in opposite directions, forming a baffle-reversing flue gas flow channel structure. The baffles effectively cause the high-temperature flue gas to collide and deflect multiple times as it flows through the separator, creating a velocity difference between the particles and the mainstream. This causes the particles to detach from the mainstream and fall into the ash hopper 5 based on inertia and gravity.

[0032] The adjacent two layers of baffles are tilted in opposite directions, forming a baffle-reversing flow channel structure. This causes the high-temperature flue gas to be deflected and recirculated multiple times as it flows through the separator, thereby enhancing the inertial separation of particles and accelerating the discharge of residual oxygen inside the separator.

[0033] The reverse-flow baffle arrangement maximizes the collision area between the flue gas and the baffle, while also reducing the potential large-scale backflow zone inside the separator and decreasing the residual time of oxygen in local areas of the separator, thereby improving gas replacement efficiency.

[0034] The structure of this baffle-reversing high-temperature flue gas separator is mainly reflected in the arrangement of the baffles and their working mechanism. The baffle reversal is mainly reflected in the arrangement of adjacent baffles with alternating inclined directions and continuous reversal of flow direction, which causes the flue gas to be deflected multiple times inside the separator, thereby enhancing the effect of particles leaving the mainstream and colliding and settling.

[0035] The main structural parameters of the multi-stage telescopic turbulence structure 6 include baffle angle, baffle length, baffle vertical spacing, and baffle horizontal spacing.

[0036] To adapt to changes in flue gas flow rate, flue gas dust concentration, and gas replacement requirements during different blowing processes in the converter, this baffle-reversing high-temperature flue gas dust separator also includes a support mechanism, a servo motor, and a rotating mechanism (not shown in the figure). The support mechanism is located inside the housing 11, with one end connected to the servo motor and the other end connected to the rotating mechanism. The baffle is mounted on the rotating mechanism; a rotating shaft is provided in the middle of the baffle and is connected to the rotating mechanism.

[0037] Each level of baffle is installed on the support mechanism, and the baffle angle, baffle length, and relative spacing between baffles are adjusted via servo motors. The baffle angle is adjusted via a rotating mechanism located at the central shaft end of the baffle. Since the baffles are telescopic, their length can also be adjusted. The vertical and horizontal spacing between the baffles can be adjusted using vertical and horizontal guide rail adjustment mechanisms (not shown in the figure), respectively, allowing for rapid adjustment of different parameter combinations.

[0038] By using a servo motor to drive and adjust, the parameters of the baffle are optimized and matched to adapt to different blowing stages and different flue gas flow rates. This allows for adaptive control of the internal flow field of the separator, creating a stable airflow field that is conducive to particle separation from the mainstream while avoiding excessive compression of the mainstream channel. This balances separation efficiency, system pressure drop, and oxygen replacement efficiency.

[0039] The baffle angle affects the particle trajectory by adjusting the intensity of the baffle wake vortex; the baffle length increases the particle collision probability by adjusting the collision area between the flue gas and the baffle; the vertical spacing of the baffles optimizes the particle inertial separation effect by affecting the number of vertically arranged baffles and the particle settling space; the horizontal spacing of the baffles determines the degree of interference of the upper baffle wake on the lower baffle by affecting the length of the flow channel between multiple baffles.

[0040] After passing through the first-stage baffle, the high-temperature flue gas undergoes a directional deflection and is further deflected by the subsequent baffles. This results in an inertial velocity difference between the particles and the airflow, causing the particles, especially large-diameter particles, to preferentially detach from the mainstream and settle into the ash hopper 5.

[0041] To ensure long-term stable operation in high-temperature and high-dust environments, the multi-stage telescopic turbulence structure 6 has an additional wear-resistant layer on its surface, preferably made of high-temperature resistant ceramic lining. When a part of the baffle surface is damaged, only the wear-resistant layer of the corresponding baffle needs to be replaced, without replacing the entire baffle structure, reducing equipment maintenance costs and improving equipment maintenance convenience.

[0042] An air inlet pipe 13 and an air outlet 3 are provided on the housing 11. The air inlet 1 is provided on the air inlet pipe 13, and the air outlet 3 is provided on the air outlet pipe 14.

[0043] In this embodiment, the separator outlet serves as the oxygen concentration monitoring section. The safety threshold, referencing relevant manuals, is set to an oxygen mass fraction not exceeding 2%. When the control system detects that the outlet oxygen concentration is higher than the preset value or the oxygen drop rate is lower than the set value, it automatically adjusts the parameter combination of the multi-stage turbulence baffle group to adapt to different environmental conditions. When the oxygen mass fraction meets the threshold requirement, the servo motor can be adjusted to the parameter condition with optimal separation efficiency. Similarly, when the oxygen mass fraction does not meet the threshold requirement, it automatically adjusts to the parameter condition with optimal replacement efficiency.

[0044] The specific values ​​for the baffle angle, baffle length, vertical spacing between baffles, and horizontal spacing between baffles can be determined based on the converter's tonnage, flue gas flow rate, particle size distribution, and allowable system pressure drop. Preferably, corresponding parameter matching relationships are established through numerical simulation, experimental verification, and engineering experience to obtain a parameter combination that simultaneously considers rapid oxygen replacement and separation performance, achieving a balance between particle separation efficiency, system pressure drop, and oxygen replacement efficiency.

[0045] The working process of the baffle-reversing high-temperature dust separator is as follows: High-temperature flue gas from the converter enters through inlet 1 after passing through the vaporization cooling flue. After flowing through settling chamber 2, the flue gas first collides and deflects with the first-layer baffle assembly, causing multiple changes in direction and localized backflow. Larger particles gradually detach from the mainstream due to inertia and settle into the ash hopper 5 under gravity. After passing through the first-layer baffle assembly, the flue gas is further rectified and redistributed by the guide plate 4. This ensures that most of the flue gas continues to collide and separate with the second-layer baffle assembly, while guiding the flue gas towards the longest path inside the separator, separating as many dust particles as possible. Subsequently, the flue gas further collides and deflects with the second-layer baffle assembly, enhancing the ability of fine particles to separate from the mainstream during collisions and the continuous changes in velocity direction and size. Simultaneously, the continuous deflection channels formed by the reverse arrangement of adjacent baffles weaken the oxygen retention zone inside the separator, allowing for rapid replacement of residual oxygen and shortening the time it takes for the oxygen concentration at the separator outlet to reach the safe threshold. Finally, the flue gas, after primary separation and oxygen replacement, is discharged from outlet 3 and enters the next stage of equipment. The separated particles are collected in ash hopper 5 and discharged through intermittent ash removal device.

[0046] The preferred ranges for the main structural parameters of the multi-stage telescopic turbulence structure 6 are: baffle angle adjustment range of 45° to 75°; baffle length adjustment range of 300mm to 700mm; baffle vertical spacing adjustment range of 300mm to 600mm; and baffle horizontal spacing adjustment range of 1000mm to 2000mm. Parameter adjustment is achieved by adjusting the support mechanism of the corresponding baffle using a servo motor. A total of 12 single-factor operating conditions were set up for analysis of separation efficiency and oxygen replacement results. Figure 4Optimization of baffle angle factors for working conditions 1-3 (baffle angles are 45°, 60°, and 75° respectively). Figure 5 The baffle length factor is optimized for working conditions 4-6 (baffle lengths are 300mm, 500mm, and 700mm respectively). Figure 6 The vertical spacing of the baffles in working conditions 7-9 is optimized (the vertical spacing of the baffles is 300mm, 500mm, and 600mm respectively). Figure 7 The horizontal spacing factor of the baffles in working conditions 10-12 is optimized (the horizontal spacing of the baffles is 1000mm, 1500mm, and 2000mm respectively).

[0047] Based on a steel plant, a similar experimental platform with a corresponding scale of 1:10 was built, such as... Figure 2 As shown, the system comprises an air heating section, a high-temperature flue gas generation system, a differential pressure testing section, a high-temperature flue gas separator, ventilation and purification, and a central control system. It can be used to approximately replicate the process of high-temperature flue gas removal in a high-temperature flue gas separator. Experiments can be conducted by placing the invention between two differential pressure testing sections.

[0048] The specific operating procedure is as follows: First, connect heater 8 to the existing test platform; set the air volume according to the preset wind speed, and then start running the centrifugal fan in the rightmost fan section. This fan is a variable frequency fan with an air volume of 1000~5000 m³ / h. 3 The speed is adjustable between / h. The fan draws air from the outside, and the air enters the system from the leftmost air inlet. At the same time, the heater 8 connected to the front end of the air inlet is turned on to start the heater 8. After running for a period of time, the temperature is monitored by the thermocouple at the inlet of the separator. When the temperature measured by the thermocouple reaches the predetermined temperature and stabilizes, the ferric oxide particles are sprayed into the dust generation section by the powder sprayer 9. The side opening of the dust generation section is designed to ensure that the outlet of the powder sprayer 9 can extend into the air duct for powder spraying. The powder sprayer 9 is mounted on the same height as the test bench using profiles. The particles are mixed evenly with the hot air flow after passing through the dust generation section and the mixing section. The device of this invention has differential pressure testing sections before and after it, allowing for simultaneous pressure measurement. An S-shaped Pitot tube 12 is installed within the differential pressure testing section, with the measuring point positioned facing the airflow direction. A multi-functional differential pressure gauge is connected below the Pitot tube, capable of reading static pressure, dynamic pressure, flow rate, airflow velocity, and temperature, and the data can be exported. After exiting the device, dust-laden particles pass through a purification section containing a filter plate, which acts as the final filter, capable of purifying particles smaller than 150 μm. The dust-laden flue gas, after being filtered in the purification section, flows to the fan section, and the upper section of the fan section leads directly to the outside for exhaust. The inspection window 10 allows observation of the flue gas movement inside the duct.

[0049] Utilize Figure 2 Experiments were conducted using the apparatus shown, and the corresponding results were obtained. Figure 3 The separation efficiency results corresponding to the 12 sets of operating conditions. Figure 3 The results show the overall separation efficiency under various operating conditions and the fractional separation efficiency for four typical particle sizes (10 μm, 30 μm, 50 μm and 70 μm).

[0050] Combination Figure 3 The separation efficiency results show that as the baffle angle increases from 45° to 75° (conditions 1-3), the overall separation efficiency exhibits a continuous upward trend. Taking 70 μm particles as an example, the separation efficiency increases from 31.43% to 56.37%. This is because large-diameter particles are significantly affected by inertia, and the increase in the baffle angle intensifies the deflection of the flue gas after passing through the baffle, making it easier for large-diameter particles to detach from the mainstream flow after collision. For small-diameter particles, taking 30 μm particles as an example, when the baffle angle increases from 60° to 75°, the separation efficiency increases from 18.80% to 20.10%, with a slow increase. At this point, due to the increase in the baffle angle, the turbulence intensity at the baffle tail increases, and fine particles are easily entrained by the turbulent vortex, thus affecting further improvement in separation efficiency.

[0051] Combination Figure 3 The separation efficiency results show that with the increase of baffle length (operating conditions 4-6), the separation efficiency for all particle size ranges is significantly improved, especially for large particles. Taking 70 μm as an example, as the baffle length increases from 300 mm to 700 mm, the separation efficiency increases from 32.33% to 71.51%. The baffle length significantly increases the effective collision area between the flue gas and the baffle, effectively preventing the flue gas from passing directly through the baffle gap.

[0052] Combination Figure 3 The separation efficiency results show that as the vertical spacing of the baffles increases (conditions 7-9), the separation efficiency exhibits a significant decreasing trend. Specifically, the vertical spacing d of the baffles... h When the vertical spacing of the baffles is 300 mm, the local flow velocity inside the channel is relatively high, increasing the probability of inertial collisions between particles and baffles. At this point, the overall separation efficiency is optimal, reaching 52.74%. When the vertical spacing of the baffles increases to d... h When the vertical spacing is 600 mm, the particle separation efficiency, especially the fine particle separation efficiency, is sensitive to changes in the vertical spacing, compared to d. h Under the condition of 300mm, the separation efficiency of 30 μm particles decreased from 20.40% to 14.67%, and the total separation efficiency decreased from 52.74% to 45.72%.

[0053] Combination Figure 3The separation efficiency results show that with the increase of the horizontal spacing of the baffles (operating conditions 10-12), the staged separation efficiency and system resistance of each particle size range show a certain downward trend. The highest separation efficiency is 43.32% when the horizontal spacing is 1000 mm. This structural parameter has a weak impact on the separation efficiency of particles below 30 μm, with an impact of less than 2%. The impact on the separation efficiency of particles 50 μm and above is relatively significant. With the increase of the horizontal spacing of the baffles, taking a 70 μm particle size as an example, its staged separation efficiency decreases from 45.15% to 38.07%. This indicates that the process of increasing the horizontal spacing of the baffles leads to a decrease in the distance between the two stages of baffles. As a result, the disturbance generated by the first stage baffle on the particles is weakened when the flue gas interacts with the second stage baffle, which weakens the effect of continuous inertial separation of particles and leads to a decrease in overall separation efficiency.

[0054] In this embodiment, the operating condition with the highest overall separation performance of the device of the present invention is operating condition 6, corresponding to an overall separation efficiency of 55.84%, which is an improvement of approximately 15.49% compared to the most unfavorable operating condition (i.e., operating condition 1 with the lowest separation efficiency), and the corresponding system resistance is 692.73 Pa. Furthermore, compared to the most unfavorable operating condition, the staged separation efficiency of the device at 10 μm, 30 μm, 50 μm, and 70 μm is improved by 1.31%, 12.96%, 22.53%, and 33.03%, respectively, demonstrating the device's highly efficient separation capability in the primary purification section of the converter primary flue gas dry system.

[0055] In the process of dry flue gas purification and waste heat recovery in a converter, the process is not always in a stable recovery state, but rather undergoes a dynamic production process, a dynamic change from the air environment to the converter gas environment. The converter gas contains components such as CO, CO2, and N2, with CO accounting for over 80%. Since CO is a combustible gas, when a large amount of high-concentration O2 remains inside the converter, the necessary conditions for combustion and explosion are met. Furthermore, this baffle-reversing high-temperature flue gas separator uses dry flue gas purification and recovery technology, and the separator inlet temperature exceeds 700℃, making it highly susceptible to explosion accidents. However, due to the high concentration of this gas and its tendency to undergo chemical reactions in the converter process, it is difficult to monitor. Therefore, monitoring of O2 inside the separator is usually performed. Based on this, in this embodiment, the monitoring surface is set at the separator outlet, with a safety threshold of oxygen volume concentration ≤2%, corresponding to an oxygen mass fraction of 0.0216.

[0056] Utilize Figure 2 Experiments were conducted using the apparatus shown, and the corresponding results were obtained. Figures 4 to 7 The results of oxygen replacement time for 12 sets of operating conditions. Combined with... Figures 4 to 7The oxygen replacement time results show that all three baffle angles (conditions 1-3) exhibit a trend of rapid initial decrease followed by a gradual and gradual decrease in oxygen mass fraction. The larger the baffle angle, the faster the oxygen concentration decays. When the angle changes from 45° to 60°, the oxygen replacement time is shortened by approximately 0.0181 s, while when the baffle angle increases from 60° to 75°, the oxygen replacement time is shortened by approximately 0.1489 s, a change of up to 8.21 times. Therefore, a higher baffle angle can significantly enhance airflow turbulence, thereby enabling the outlet oxygen concentration to quickly reach the set threshold, which is beneficial for rapid gas replacement.

[0057] Combination Figures 4 to 7 The oxygen replacement time results show that the change in baffle length has a significant impact on the gas replacement time (conditions 4-6). With increasing baffle length, the oxygen replacement time exhibits a trend of initially rapid growth followed by a slower increase. The smaller the baffle length (e.g., condition 4, corresponding to l=300mm), the shorter the time required for oxygen to reach the safe threshold. In this case, the direct contact area between the baffle and the flue gas is small, reducing flow resistance. Therefore, the flue gas can quickly pass through the baffle gap. Compared to the other two conditions, the time required for the flue gas to flow from the separator inlet to the outlet is the shortest. Therefore, condition 4 has the shortest oxygen replacement time, at 2.9487s. However, as the baffle length increases, the contact area between the flue gas and the baffle increases, obstructing the flue gas flow area. This leads to an increase in the distance and time the flue gas travels within the separator, thus increasing the oxygen replacement time. The longest oxygen replacement time, at 3.4138s, is when the baffle length is 700mm.

[0058] Combination Figures 4 to 7 The oxygen replacement time results show that as the vertical spacing of the baffles increases (conditions 7-9), the oxygen replacement time gradually shortens, but the decrease is relatively small. The main reason is that when the vertical spacing is 300mm, the short distance between the two baffles in the vertical direction restricts the airflow path inside the separator. Simultaneously, the decrease in vertical spacing increases the number of baffles in the same vertical direction, resulting in more recirculation zones inside the separator. This causes oxygen to accumulate and is difficult to replace immediately, thus resulting in a longer replacement time of 3.5883s. As the vertical spacing of the baffles increases, the flow distance between the two baffles increases, which facilitates airflow and improves the oxygen replacement efficiency to some extent. The shortest oxygen replacement time (3.4600s) is achieved when the vertical spacing is 600mm.

[0059] Combination Figures 4 to 7The oxygen replacement time results show that the replacement time initially increases and then decreases with the increase of the horizontal spacing of the baffles, with the shortest replacement time (3.1501s) occurring when the horizontal spacing is 1000mm. As the horizontal spacing increases from 1000mm to 1500mm, the replacement time slightly increases; when the horizontal spacing continues to increase to 2000mm, the replacement time decreases again, but the overall fluctuation range is only 0.1639s, indicating a relatively weak impact compared to other baffle structures. At this point, the horizontal spacing of the baffles mainly affects the length of the main channel and the size of the vortex shape, having a limited effect on the attenuation process of the outlet oxygen concentration.

[0060] In this embodiment, the shortest oxygen replacement time for the device of the present invention is under condition 4, which corresponds to a minimum oxygen replacement time of 2.9487s. Compared with the most unfavorable condition (condition 7), it can be shortened by 0.6396s, demonstrating the device's ability to rapidly replace the gas in the primary purification section of the converter's primary flue gas dry system, thus meeting the optimization goal of balancing separation performance and achieving rapid oxygen replacement.

[0061] Obviously, the above embodiments are merely illustrative examples for clear explanation and are not intended to limit the implementation. Those skilled in the art will recognize that other variations or modifications can be made based on the above description. It is neither necessary nor possible to exhaustively list all possible implementations here. However, obvious variations or modifications derived therefrom are still within the scope of protection of this invention.

Claims

1. A baffle-reversing high-temperature flue gas separator, characterized in that, include: Shell (11) and air inlet (1), air outlet (3), guide plate (4), ash hopper (5), multi-stage telescopic turbulence structure (6); The top of the shell (11) is provided with an air inlet (1) and an air outlet (3). The interior of the shell (11) is provided with a settling chamber (2) and a guide plate (4) is provided on the settling chamber (2). A multi-stage telescopic turbulence structure (6) is provided in the settling chamber (2). The multi-stage telescopic turbulence structure (6) includes a multi-layer baffle assembly. The surface of each baffle assembly is inclined towards the direction of flue gas movement. The ash hopper (5) is provided at the bottom of the shell (11).

2. The baffle-reversing high-temperature flue gas separator according to claim 1, characterized in that, Each layer of the baffle assembly has two rows of baffles, which are spaced apart and mirrored.

3. The baffle-reversing high-temperature flue gas separator according to claim 2, characterized in that, The angle between the baffle and the direction of flue gas movement is 45°, 60°, or 75°.

4. A baffle-reversing high-temperature flue gas separator according to claim 2, characterized in that, The guide plate (4) is located between the two rows of baffles.

5. A baffle-reversing high-temperature flue gas separator according to any one of claims 2-4, characterized in that, It also includes a support mechanism, a servo motor, and a rotating mechanism. The support mechanism is located inside the housing (11). One end of the support mechanism is connected to the servo motor, and the other end is connected to the rotating mechanism. The baffle is provided on the rotating mechanism.

6. A baffle-reversing high-temperature flue gas separator according to claim 5, characterized in that, The baffle has a rotating shaft in the middle, and the rotating shaft is connected to the rotating mechanism.

7. A baffle-reversing high-temperature flue gas separator according to claim 6, characterized in that, Each of the baffles is equipped with a vertical guide rail adjustment mechanism and a horizontal guide rail adjustment mechanism.

8. A baffle-reversing high-temperature flue gas separator according to claim 7, characterized in that, The outer surface of the baffle is provided with a wear-resistant layer.

9. A baffle-reversing high-temperature flue gas separator according to claim 8, characterized in that, The baffle is a ceramic liner.

10. A baffle-reversing high-temperature flue gas separator according to claim 9, characterized in that, The housing (11) is provided with an air inlet pipe (13) and an air outlet (3). The air inlet (1) is located on the air inlet pipe (13), and the air outlet (3) is located on the air outlet pipe (14).

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