A slurry device for sinter machine head dust water washing

Abstract

A kind of slurring device for sintering machine head ash water washing, the device includes slurry tank (1), slurry pump (2), solid-liquid separation device (3);The slurry outlet of slurry tank (1) is connected to the import of solid-liquid separation device (3) via slurry conveying pipeline (L1);Slurry conveying pipeline (L1) is equipped with slurry pump (2);Slurry tank (1) is equipped with slurry agitator (101);The device further includes cyclone (4) being arranged at the top of slurry tank (1);Cyclone (4) is equipped with sintering machine head ash import (a), process water import (b), discharge port (c), and the discharge port (c) is connected with the inside of slurry tank (1).The utility model adds cyclone as ash water premixing device, realizes high-speed shearing and sufficient premixing of ash water two-phase material by the strong turbulent field generated by cyclone, to solve the problem that small component in sintering machine head ash is strong hydrophobic and not easy to mix.

Description

Technical Field

[0001] This utility model relates to a sintering machine head ash treatment device, specifically a pulping device for washing sintering machine head ash, belonging to the field of solid waste resource utilization and disposal technology. Background Technology

[0002] During the dust removal process of sintering flue gas in steel enterprises, sintering machine head ash is generated. Sintering machine head ash mainly contains insoluble components such as iron, as well as soluble components such as potassium, sodium, and chlorine. The soluble components in sintering machine head ash typically account for 20%-60%, and the composition of the raw materials fluctuates greatly, requiring high control over the resource utilization process.

[0003] The sintering machine head ash has a wide and uneven particle size distribution, and its particle size is mainly related to the electric field distribution of the electrostatic precipitator. Generally speaking, from the first to the fourth electric field of the electrostatic precipitator in the sintering machine head, the particle size of the sintering machine head ash decreases from large to small, the Fe content gradually decreases, and the K and Na contents gradually increase. Different sintering machine head ashes have significantly different particle size distributions; the larger the particle size, the greater the risk of equipment wear and clogging.

[0004] Sintering machine head ash is rich in alkali metals and halogens, mainly existing in the form of low-melting-point soluble salts. These salts are easily volatilized during the high-temperature sintering process, causing serious impacts on equipment and processes. The main effects are as follows: (1) Deterioration of the metallurgical properties of sintered ore. (2) Threat to the smooth operation of the blast furnace. (3) Corrosion of the grate bars. (4) Causing caking of electrostatic precipitators. (5) Reduction in the efficiency of flue gas purification, desulfurization, and denitrification. (6) Causing the formation of colored plumes from activated carbon. Therefore, the proper treatment and resource utilization of high-salt solid wastes from steelmaking processes, such as sintering machine head ash, is of great significance for ensuring the stable and smooth operation of the steelmaking process.

[0005] Currently, the main method for resource utilization of sintering machine head ash is wet leaching technology. Soluble potassium, sodium, and chlorine are removed by washing with water, and the resulting iron-rich powder is returned to sintering. In the wet leaching process, a circular storage tank equipped with a stirrer is typically used for mixing the sintering machine head ash with water and dissolving soluble components. The existing wet leaching process flow for sintering machine head ash is as follows: Figure 1 As shown.

[0006] Figure 1In this process, sintering machine head ash is directly fed into the slurry tank and mixed with process makeup water. Because the particles of sintering machine head ash are mostly small and highly hydrophobic, they are not easily wetted by water. Therefore, directly feeding the ash into the slurry tank often results in the ash floating on the surface and failing to sink into the slurry. Furthermore, moisture and dust can impact the environment and easily cause caking and blockage of the conveying equipment. To address the problems of the fine size, high hydrophobicity, and difficulty in uniform mixing of sintering machine head ash, existing technologies employ methods such as humidification on a screw conveyor. However, this method is ineffective, the amount of water added is difficult to control, and it easily leads to blockage of the screw conveyor.

[0007] Figure 1 In this process, the slurry tank is a circular mixing tank, where coarse particles from the sintering mill head ash tend to settle to the bottom. During mixing, these coarse particles can cause wear on the tank body, severely affecting its operation. To address the wear and blockage of particles in the sintering mill head ash, existing technologies use magnetic separation and cyclone separation to screen for different particle sizes. However, this method increases the amount of equipment required and has poor operational stability.

[0008] Figure 1 In sintering, the slurry concentration in the pulping tank is controlled by adjusting the flow rate or mass of ash and water at the sintering machine head, i.e., the ash-to-water ratio. Typically, the ash-to-water ratio is 1:2 to 4. When the raw material composition fluctuates, the slurry concentration in the pulping tank will also fluctuate. These fluctuations in slurry concentration will affect pulping equipment such as agitators, pumps, and solid-liquid separation devices.

[0009] Furthermore, when controlling the salt concentration of high-salt washing ash water by maintaining a fixed ash-to-water ratio of 1:2~4, the salt concentration of the high-salt washing ash water will fluctuate when the raw material composition changes. Fluctuations in salt concentration will have a significant impact on the pulping process (selection of pulping stage) and subsequent high-salt water treatment processes. Figure 1 The high-salt washing water obtained in the process (whose salts are mainly potassium chloride and sodium chloride) can be purified by removing impurities and then separated into potassium chloride and sodium chloride products through evaporation and crystallization. The concentration of the high-salt washing water directly affects the amount of washing water and the energy consumption and efficiency of subsequent evaporation and crystallization.

[0010] Therefore, in view of the problems existing in the current wet leaching process of sintering machine head ash, it is urgent to develop a new type of pulping device and an optimized process method. Utility Model Content

[0011] To address the problems of difficult wetting and uneven mixing caused by the fine particle size and strong hydrophobicity of sintering machine head ash in existing wet leaching processes, this invention proposes a slurrying device and its supporting process for washing sintering machine head ash. In this invention, a hydrocyclone is added to the top of the slurrying tank as an ash-water premixing device. The hydrocyclone has a sintering machine head ash inlet, a process water inlet, and a discharge outlet, which is connected to the slurrying tank located below. Through the strong turbulent flow field generated by the hydrocyclone, the sintering machine head ash and process water enter the hydrocyclone and form a swirling scouring effect, achieving high-speed shearing and thorough premixing of the ash and water phases. This ensures that the sintering machine head ash is completely wetted and premixed with the process water before entering the slurrying tank, thus avoiding the problems of difficult mixing and uneven mixing caused by the fine particle size in existing technologies, and providing a uniform and stable slurry system for subsequent processes.

[0012] This invention also includes a slurry return pipe branched off from the slurry delivery pipe connected to the slurry outlet of the slurry tank and connected to the hydrocyclone. By optimizing the slurry return, the concentration of slurry in the slurry tank is controlled, ensuring the stable operation of the equipment.

[0013] Furthermore, this invention also includes a filtrate tank with a stirrer and a filtrate pump downstream of the solid-liquid separation device, and a filtrate return pipe is branched off from the filtrate delivery pipe connected to the outlet of the filtrate pump and connected to the hydrocyclone. The filtrate return optimizes the control of the salt concentration in the filtrate discharged from the filtrate tank, thereby ensuring the stability of the salt concentration in the final high-salt washing water.

[0014] In addition, this utility model also has a negative pressure device installed at the top of the slurry tank to avoid pollution and harm from water vapor and dust during slurrying, while ensuring smooth ash discharge.

[0015] This invention also includes a grid mesh installed at the bottom of the slurry tank to address the wear problem caused by coarse particles in the sintering machine head ash.

[0016] According to the first embodiment of this utility model, a pulping device for washing ash water at the sintering machine head is provided.

[0017] A slurry preparation device for washing sintering machine head ash includes a slurry preparation tank, a slurry pump, and a solid-liquid separation device. The slurry outlet of the slurry preparation tank is connected to the inlet of the solid-liquid separation device via a slurry delivery pipeline. A slurry pump is installed on the slurry delivery pipeline. A slurry agitator is installed inside the slurry preparation tank. The device also includes a hydrocyclone installed at the top of the slurry preparation tank. The hydrocyclone has a sintering machine head ash inlet, a process water inlet, and a discharge port, the discharge port being connected to the interior of the slurry preparation tank.

[0018] In this invention, the hydrocyclone is also provided with a slurry return port. A slurry return pipe is branched off from the slurry delivery pipe downstream of the slurry pump, and the slurry return pipe is connected to the slurry return port of the hydrocyclone.

[0019] Preferably, a slurry return valve is provided on the slurry return pipeline. A slurry outlet valve is provided on the slurry delivery pipeline downstream of the location where the slurry return pipeline is located. Preferably, a slurry concentration monitoring device is provided on the slurry delivery pipeline, and the slurry concentration monitoring device is located upstream of the location where the slurry return pipeline is located (wherein, it can be located upstream or downstream of the slurry pump).

[0020] In this invention, the device further includes a filtrate tank and a filtrate pump located downstream of the solid-liquid separation device. The liquid outlet of the solid-liquid separation device is connected to the filtrate tank via a pipeline. The filtrate outlet of the filtrate tank is connected to the inlet of the filtrate pump via a filtrate discharge pipeline. The outlet of the filtrate pump is connected to a filtrate delivery pipeline. A filtrate stirrer is installed inside the filtrate tank.

[0021] Preferably, the hydrocyclone is also provided with a filtrate return port. A filtrate return pipe branches off from the filtrate delivery pipe and is connected to the filtrate return port of the hydrocyclone.

[0022] Further preferably, a filtrate reflux valve is provided on the filtrate reflux pipeline. A filtrate outlet valve is provided on the filtrate delivery pipeline downstream of the location where the filtrate reflux pipeline is located. Preferably, a filtrate density monitoring device is provided on the filtrate delivery pipeline, and the filtrate density monitoring device is located upstream of the location where the filtrate reflux pipeline is located.

[0023] In this invention, the hydrocyclone includes a straight section and an inverted conical section connected to the lower part of the straight section. The slurry return port is located on the side of the straight section. Preferably, the slurry return pipe is tangentially connected to the slurry return port.

[0024] Preferably, a bar screen is provided within the straight section of the hydrocyclone. Preferably, the bar screen is inclined. The higher end of the bar screen is positioned above the slurry return interface, and a discharge port is located at the corresponding position of the straight section at the lower end of the bar screen. Preferably, an automatic discharge valve is provided at the discharge port.

[0025] In this invention, the inclination angle θ of the inverted cone section of the hydrocyclone is 45°~70°, preferably 55°~65°.

[0026] In this invention, the inclination angle β of the bar screen inside the hydrocyclone is 5°~30°, preferably 10°~15°. Preferably, the relationship between the screen aperture size d1 and the ash particle size at the sintering mill head satisfies: d min ≤d1≤d max Among them, d min The smallest particle size of the sintering machine head ash is represented by d.max This indicates the maximum particle size of the sintering machine head ash.

[0027] In this invention, the device further includes a negative pressure device disposed at the top of the slurry tank. Preferably, the negative pressure device and the cyclone separator are disposed on opposite sides of the top of the slurry tank.

[0028] The negative pressure device includes an expansion section and a blower. The expansion section is located at the top of the slurry tank and communicates with the interior of the slurry tank. A tail gas discharge pipe is led out from the top outlet of the expansion section and is connected to the blower. Preferably, an exhaust valve is provided on the tail gas discharge pipe.

[0029] Preferably, the upper part of the side wall of the enlarged section is also provided with a flushing water interface. The flushing water interface is connected to a flushing water pipe. Preferably, the flushing water pipe is tangentially connected to the flushing water interface. More preferably, the flushing water pipe is provided with a periodic flushing valve.

[0030] More preferably, a vacuum pressure relief valve is also provided at the top of the expansion section. Preferably, the fan outlet is connected to the exhaust gas treatment system via a pipeline.

[0031] In this invention, a grid is also provided at the bottom of the slurry tank. Preferably, the relationship between the height h of the grid and the gap H between the slurry agitator and the bottom of the slurry tank satisfies: h ≤ (0.1~0.5)H.

[0032] Preferably, the individual grid size d2 within the grid is equal to the maximum particle size d of the sintering machine head ash. max The relation satisfies: d max ≤d2≤10d max .

[0033] More preferably, the grid is an assembly structure of multiple grid units. The relationship between the size L of a single grid unit and the inspection hole size D of the slurry tank satisfies: 0.5D≤L≤0.8D.

[0034] Further preferably, the materials of the hydrocyclone, the bar screen, and the bar mesh are selected from fiberglass, rubber-lined steel, stainless steel, and plastic, respectively. Preferably, the materials of the hydrocyclone, the bar screen, and the bar mesh are all fiberglass.

[0035] In this invention, the device also includes a first mass metering device installed at the ash inlet of the sintering machine head.

[0036] In this invention, the process water inlet of the hydrocyclone is connected to a process water pipe. The process water pipe is equipped with a second mass metering device and a water supply valve.

[0037] According to a second embodiment of the present invention, a pulping method for washing ash in sintering machine heads is provided.

[0038] A pulping method for washing ash from a sintering machine head, or a pulping method using the apparatus described in the first embodiment, comprising the following steps:

[0039] S1. Sintering machine head ash and process water enter the hydrocyclone through the sintering machine head ash inlet and process water inlet respectively for hydrocyclone premixing. The slurry obtained after premixing enters the slurry tank for stirring and slurrying.

[0040] S2. The slurry obtained after pulping is pumped to the solid-liquid separation unit via the slurry pump and the slurry conveying pipeline. The slurry is separated into high-salt washing water and iron-rich powder.

[0041] Preferably, the method further includes:

[0042] S3. The high-salt washing water enters the filtrate tank. The filtrate agitator installed in the filtrate tank agitates the high-salt washing water. The filtrate obtained after agitation is sent to the next process through the filtrate pump and the filtrate delivery pipeline.

[0043] S4. A filtrate density monitoring device installed on the filtrate delivery pipeline detects the real-time filtrate density and records it as ρ, g / mL. The target filtrate density is set as ρ. 目标 , g / mL. When ρ < ρ 目标 At this time, open the filtrate reflux valve and close the filtrate outlet valve. The filtrate is then returned to the hydrocyclone through the filtrate reflux pipe to increase the filtrate salt concentration until ρ = ρ 目标 When ρ≥ρ 目标 When the filtrate is in use, close the filtrate reflux valve and open the filtrate outlet valve. The filtrate is then sent to the next process via the filtrate delivery pipeline.

[0044] In this utility model, the method further includes:

[0045] S5. A first mass metering device installed at the sintering machine head ash inlet measures the mass flow rate of the sintering machine head ash, denoted as Q1, kg / h. A second mass metering device installed at the process water inlet measures the mass flow rate of the process water, denoted as Q2, kg / h. Calculate the slurry concentration X, %, discharged from the slurry tank. Specifically:

[0046]

[0047] In the formula: ρ 水 The density of the process water is expressed in g / mL.

[0048] Set the target slurry concentration for discharge from the slurry tank as X. 目标 ,%. Let X = X 目标Combined with the real-time filtrate density ρ detected by the filtrate density monitoring device, the ratio of the mass flow rate of sintering machine head ash to the mass flow rate of process water Q1:Q2 is calculated by formula (Ⅰ). This is used to control the mass flow rate ratio of sintering machine head ash to process water entering the hydrocyclone, so that the slurry concentration discharged from the slurry tank is within the target slurry concentration range.

[0049] Preferably, a slurry concentration monitoring device installed on the slurry delivery pipeline detects the real-time slurry concentration, denoted as X0,%. When X0 < X 目标 At this time, the slurry return valve is opened and the slurry outlet valve is closed. The slurry is then returned to the hydrocyclone through the slurry return pipe to increase the slurry concentration until X0 = X 目标 When X0 ≥ X 目标 At that time, the slurry return valve is closed and the slurry outlet valve is opened. The slurry is then transported to the solid-liquid separation device through the slurry conveying pipeline to obtain high-salt washing water.

[0050] Preferably, the target slurry concentration X 目标 The value range is 10% to 30%, preferably 15% to 20%.

[0051] During the dust removal process of sintering flue gas in steel enterprises, sintering machine head ash is generated. Generally speaking, sintering machine head ash mainly contains insoluble components such as iron, as well as soluble components such as potassium, sodium, and chlorine. Its main components are shown in Table 1 below. The particle size distribution of sintering machine head ash is wide and uneven, and its particle size distribution is shown in Table 2 below.

[0052] Table 1. Main components of a typical sintering machine head ash

[0053]

[0054] Table 2. Particle size distribution of ash from a typical sintering machine head.

[0055]

[0056] As shown in Table 1, the composition of sintering machine head ash fluctuates significantly. When the raw material composition fluctuates, the slurry concentration in the pulping tank and the salt concentration in the high-salt washing water in the existing wet leaching process will also fluctuate. This will have a significant impact on the operational stability of the pulping equipment, the pulping process, and the treatment effect of subsequent processes. In other words, precisely because of the large fluctuation in the composition of sintering machine head ash, the control requirements for its resource utilization and disposal process are quite high.

[0057] Table 2 shows that the particle size distribution of sintering machine head ash varies considerably. The larger the particle size, the greater the risk of equipment wear and blockage. Table 2 also shows that small-sized particles account for a large proportion of the sintering machine head ash. Due to their small particle size and strong hydrophobicity, they are not easily wetted by water. Therefore, in the existing wet leaching process, the sintering machine head ash tends to float on the liquid surface and is difficult to sink into the slurry during ash feeding. At the same time, water vapor and dust will have an impact on the environment and are prone to causing caking and blockage of the conveying equipment.

[0058] Based on the problems existing in the current wet leaching process for sintering machine head ash, this invention proposes a slurry device for washing sintering machine head ash. In this invention, a hydrocyclone is added to the top of the slurry tank as an ash-water premixing device. The hydrocyclone has a sintering machine head ash inlet, a process water inlet, and a discharge outlet, which is connected to the slurry tank located below. Through the strong turbulent flow field generated by the hydrocyclone, the sintering machine head ash and process water enter the hydrocyclone to form a swirling scouring effect, achieving high-speed shearing and thorough premixing of the ash and water phases. This ensures that the sintering machine head ash is completely wetted and premixed with the process water before entering the slurry tank, thus avoiding the problems of difficult mixing and uneven mixing caused by the small particle size of the material in the prior art, and providing a uniform and stable slurry system for subsequent processes.

[0059] This invention also includes a slurry return pipe branched off from the slurry delivery pipe connected to the slurry outlet of the slurry tank and connected to the hydrocyclone. By optimizing the slurry return, the concentration of slurry in the slurry tank is controlled, ensuring the stable operation of the equipment.

[0060] Furthermore, this invention also includes a filtrate tank with a stirrer and a filtrate pump installed downstream of the solid-liquid separation device, and a filtrate return pipe is branched off from the filtrate delivery pipe connected to the outlet of the filtrate pump and connected to the hydrocyclone. By optimizing the filtrate return, the salt concentration in the filtrate discharged from the filtrate tank is controlled, ensuring the stability of the salt concentration in the final high-salt washing water.

[0061] Furthermore, this invention also incorporates a negative pressure device at the top of the slurry tank to prevent pollution and hazards from water vapor and dust during slurry preparation, while ensuring smooth ash discharge. Additionally, this invention includes a grid mesh at the bottom of the slurry tank to address the wear and tear on the equipment caused by coarse particles in the sintering machine head ash.

[0062] Specifically, this invention features a hydrocyclone installed at the top of the slurry tank. The hydrocyclone includes a sintering machine head ash inlet, a process water inlet, and a discharge outlet. The sintering machine head ash inlet provides a channel for sintering machine head ash to enter the hydrocyclone, the process water inlet provides a channel for process water to enter the hydrocyclone, and the discharge outlet provides a channel for the premixed slurry to enter the slurry tank. To ensure the fluidity of the premixed slurry in the hydrocyclone, the hydrocyclone is configured with a structure including a straight section and an inverted conical section. The inclination angle θ of the inverted conical section (i.e., the angle between the inverted conical section and the horizontal plane) is 45°~70°, preferably 55°~65°. For example, the inclination angle θ of the inverted conical section can be set to 45°, 50°, 55°, 60°, 65°, or 70°, etc.

[0063] Preferably, a grid screen is inclinedly arranged within the straight section of the hydrocyclone. The inclination angle β of the grid screen is related to the flow characteristics of the ash particles at the sintering mill head. For example, the inclination angle β of the grid screen is 5°~30°, preferably 10°~15°. The inclination angle β of the grid screen can be set to 5°, 10°, 12°, 15°, 20°, 25°, or 30°, etc. Preferably, the screen aperture size d1 (not shown in the figures) of the grid screen is related to the ash particle size distribution at the sintering mill head, specifically: d min ≤d1≤d max Among them, d min The smallest particle size of the sintering machine head ash is represented by d. max This indicates the maximum particle size of the sintering machine head ash. This design allows coarse particles and foreign objects in the sintering machine head ash to be intercepted by the bar screen, thereby reducing clogging and wear in subsequent processes. The hydrocyclone is equipped with a discharge port located at the lowest point of the bar screen (i.e., the lower end of the bar screen). The discharge port is equipped with an automatic discharge valve, preferably an electric / start gate valve, butterfly valve, or ball valve, and more preferably a gate valve. In addition, a vibrator can be installed on the bar screen, preferably an electric vibrator, whose vibration frequency is adjustable and related to the feeding rate of the sintering machine head ash.

[0064] Preferably, this invention includes a slurry return port on the hydrocyclone, with a slurry return pipe branching off from the slurry delivery pipe and connected to the slurry return port. When the slurry concentration in the slurry tank is less than the target slurry concentration, the slurry is returned to the hydrocyclone through the slurry return pipe to increase the slurry concentration; conversely, when the slurry concentration is greater than or equal to the target slurry concentration, the slurry is sent to the next process through the slurry delivery pipe. Preferably, the slurry delivery pipe is also equipped with a slurry concentration monitoring device to monitor the concentration of the slurry discharged from the slurry tank in real time. The target slurry concentration is set based on practical experience and specific operating conditions, for example, the target slurry concentration ranges from 10% to 30%, preferably from 15% to 20%. Correspondingly, a slurry return valve is installed on the slurry return pipe, and a slurry outlet valve is installed on the slurry delivery pipe. These two valves are used to regulate and control the direction of the slurry. It is worth noting that the slurry return interface, or the slurry return to the hydrocyclone, can further ensure the premixing effect of the sintering head ash and process water entering the hydrocyclone. Therefore, within the allowable range of slurry concentration in the slurry tank, a portion of the slurry can be returned to the hydrocyclone via the slurry return pipe. The slurry return and the sintering head ash form a swirling scouring effect in the hydrocyclone, ensuring the premixing effect within the hydrocyclone and providing a uniform and stable slurry system for subsequent processes.

[0065] Preferably, the slurry return interface is located on the side of the straight section of the hydrocyclone, and the slurry return pipe is tangentially connected to the slurry return interface. The return slurry enters the hydrocyclone tangentially, causing the slurry to quickly form a high-speed swirling motion, thereby further improving the premixing effect of the slurry in the hydrocyclone. In addition, the higher end of the bar screen inside the hydrocyclone is higher than the slurry return interface. The purpose of this is to ensure that the sintering machine head ash passes through the screen first, and then slurries and mixes with the return slurry, so as to ensure the screening effect of the bar screen.

[0066] In this invention, the slurry processing device further includes a filtrate tank and a filtrate pump located downstream of the solid-liquid separation device. The slurry pump transports the slurry discharged from the slurry processing tank to the solid-liquid separation device, where the slurry undergoes solid-liquid separation to obtain filtrate (i.e., high-salt washing water) and iron-rich powder. The filtrate enters the filtrate tank, is stirred, and then discharged. The discharged filtrate is then pumped to the next process via a filtrate conveying pipeline. The solid-liquid separation device can be a centrifuge, filter press, vacuum belt filter, etc. Preferably, the hydrocyclone is equipped with a filtrate return port, and a filtrate return pipeline is branched off from the filtrate conveying pipeline and connected to the filtrate return port. When the density of the filtrate in the filtrate tank is less than the target filtrate density, the filtrate is returned to the hydrocyclone for slurry preparation via the filtrate return pipeline to increase the filtrate salt concentration; conversely, when the filtrate density is greater than or equal to the target filtrate density, the filtrate is conveyed to the next process via the filtrate conveying pipeline. Preferably, the filtrate delivery pipeline is also equipped with a filtrate density monitoring device to monitor the density of the filtrate discharged from the filtrate tank in real time. The target filtrate density is determined based on the filtrate's high potassium and low sodium content (as shown in Table 1, the main components of the sintering machine head ash). Using potassium chloride solubility as the standard, the solubility of potassium chloride in water at the current temperature is obtained from a table, and then the corresponding potassium chloride aqueous solution concentration is calculated. Finally, based on the potassium chloride aqueous solution concentration-density correspondence, the target filtrate concentration is obtained by referring to a table. Correspondingly, a filtrate reflux valve is installed on the filtrate reflux pipeline, and a filtrate outlet valve is installed on the filtrate delivery pipeline. These two valves are used to regulate and control the filtrate's destination.

[0067] It should be noted that, to ensure the swirling effect of the hydrocyclone, the inlets of the hydrocyclone (including the sintering machine head ash inlet, process water inlet, slurry return interface, and filtrate return interface) are preferably located on the edge of the hydrocyclone. For example... Figure 4 As shown, the sintering machine head ash inlet, process water inlet, and filtrate return interface are preferably located at the top of the hydrocyclone near the side, while the slurry return interface is directly located on the straight section side of the hydrocyclone, thereby achieving a better swirling effect and ensuring that the sintering machine head ash is completely soaked and premixed with the process water before entering the slurry tank.

[0068] In this invention, the slurry preparation device further includes a negative pressure device installed at the top of the slurry tank. The negative pressure device ensures that the slurry tank is under negative pressure during the slurry preparation process. This not only ensures smooth feeding of the premixed slurry from the hydrocyclone but also prevents secondary dust and moisture generated during slurry preparation from escaping and polluting the environment or clogging the hydrocyclone and feeding pipes. Specifically, as shown... Figure 5As shown, the negative pressure device is designed with an enlarged section. The size of the enlarged section (including its diameter and height) must meet the requirements for the settling of fine particles in the sintering machine head ash. A flushing water interface is provided on the upper side wall of the enlarged section, and the flushing water pipe is tangentially connected to the flushing water interface. A periodic flushing valve is also provided on the flushing water pipe. This utility model adds an enlarged section to the negative pressure device. By increasing the cross-sectional area, the exhaust gas velocity is reduced. On the one hand, this reduces the solid particles carried by the airflow, preventing them from entering the fan or exhaust gas discharge pipe and reducing the risk of blockage. On the other hand, it provides a pressure buffer space, stabilizes the negative pressure environment in the slurry tank, and prevents pressure fluctuations from affecting the slurry process. The larger space also allows particles entrained in the airflow to separate due to gravity settling, reducing the load on subsequent exhaust gas treatment. Moreover, the tangential connection between the flushing water pipe and the flushing water interface can form a swirling flush during the flushing process, further cleaning the inner wall of the enlarged section and preventing particle accumulation. Preferably, a vacuum pressure relief valve is also provided at the top of the enlarged section as a safety device. The vacuum pressure relief valve automatically releases pressure when the slurry tank is under abnormally high pressure, protecting the integrity of the system. For example, the system automatically activates when the pressure inside the slurry tank is ≥0.05MPa (based on the maximum pressure the slurry tank can withstand) to prevent excessive pressure in the slurry tank. The negative pressure device can also use a fan to extract the exhaust gas to the exhaust gas treatment system (not shown in the attached diagram). The exhaust gas treatment system uses water absorption, alkali absorption, and other treatment methods. The slurry after absorption by the exhaust gas treatment system can also be returned to the slurry tank for secondary use, thus achieving exhaust gas treatment without secondary pollution.

[0069] In this invention, a grid is also provided at the bottom of the slurry tank. The grid effectively reduces the flow velocity of particles in the sintering machine head ash within the slurry tank, and simultaneously traps some particles within the grid to prevent abrasion of the tank bottom. The height h of the grid is determined based on the gap height H between the bottom of the slurry agitator and the bottom of the slurry tank (the gap height H is generally 30~80 mm, not shown in the accompanying drawings), satisfying: h ≤ (0.1~0.5)H. The individual grid size d2 is determined based on the particle size of the sintering machine head ash, satisfying: d max ≤d2≤10d max d max This indicates the maximum particle size of the sintering machine head ash. This configuration allows coarse particles of the sintering machine head ash to be captured by the grid mesh. Preferably, the grid can be assembled from multiple grid units. The size L (i.e., side length L) of a single grid unit is determined based on the size of the inspection hole on the side wall of the slurry tank (i.e., diameter D, generally 300~800 mm; the grid unit and the inspection hole are not shown in the attached drawings), satisfying the condition: 0.5D≤L≤0.8D, which facilitates the inspection and cleaning of the grid.

[0070] In this invention, the hydrocyclone, bar screen, and bar mesh can be made of any one of the following materials: fiberglass, rubber-lined steel, stainless steel, or plastic. Considering the high strength, wear resistance, and corrosion resistance of fiberglass, fiberglass is more preferably used as the material for the hydrocyclone, bar screen, and bar mesh.

[0071] To measure and control the mass flow rate of sintering mill head ash and process water entering the hydrocyclone, this invention also includes a first mass metering device at the sintering mill head ash inlet, such as a mass metering device for sintering mill head ash conveying, preferably a belt conveyor or screw conveyor. Similarly, a process water metering device is designed, for example, the process water inlet can be connected to a process water pipeline, and a second mass metering device is installed on the process water pipeline. Preferably, a water supply valve is installed on the process water pipeline, which is used to adjust the flow rate of process water required for premixing in the hydrocyclone. The process water is directly supplied to the hydrocyclone, and the fine particles are premixed through the swirling mixing in the hydrocyclone.

[0072] Based on the aforementioned slurry preparation device for washing ash from the sintering mill head, this invention also proposes a corresponding slurry preparation method for washing ash from the sintering mill head. The core steps of this method mainly include cyclone premixing and slurry preparation, slurry conveying and solid-liquid separation, filtrate stirring and conveying, filtrate density feedback control, and slurry concentration feedback control. An online monitoring and feedback mechanism is employed to address concentration fluctuations during the ash washing process at the sintering mill head, ensuring process stability. The specific steps of the method are as follows:

[0073] S1. Cyclone premixing and slurry preparation: Sintering machine head ash (containing salt, iron powder, etc.) and process water enter the cyclone separator through the sintering machine head ash inlet and process water inlet, respectively, for cyclone premixing. The slurry obtained after premixing enters the slurry preparation tank for stirring and slurry preparation.

[0074] The hydrocyclone utilizes centrifugal force to enhance mixing, ensuring that ash is evenly dispersed in the process water and reducing the stirring load on the subsequent slurry tank. The premixed slurry enters the slurry tank for further stirring to ensure thorough slurrying (improving solid-liquid contact efficiency and promoting salt dissolution).

[0075] S2. Slurry conveying and solid-liquid separation: The slurry obtained after slurrying is conveyed to the solid-liquid separation device (such as centrifuge, filter press, etc.) through the slurry conveying pipeline by the slurry pump. The slurry is separated into filtrate (i.e., high salt washing water, containing dissolved salt, which needs to be further treated or the salt needs to be recovered) and filter residue (i.e. iron-rich powder, low salt, which can be returned to the sintering process).

[0076] S3. Filtrate Stirring and Transport: High-salt washing water enters the filtrate tank. A filtrate stirrer installed in the tank stirs the water to prevent salt precipitation and ensure uniform concentration. The tank also serves as a buffer for the filtrate. After stirring, the filtrate is pumped through a filtrate transport pipeline to the next process (such as evaporation and crystallization to recover salt).

[0077] S4. Filtrate density feedback control: The filtrate density monitoring device detects the filtrate density ρ in real time and compares the real-time filtrate density ρ with the target filtrate density ρ. 目标 Perform a comparison. When ρ < ρ 目标 If the filtrate salt concentration is insufficient, open the filtrate reflux valve and close the filtrate outlet valve. The filtrate is then returned to the hydrocyclone for reconcentration to increase the filtrate salt concentration. When ρ ≥ ρ 目标 When the salt concentration of the filtrate meets the standard, close the filtrate reflux valve and open the filtrate outlet valve, and the filtrate will be sent directly to the next process.

[0078] Generally, the higher the salt concentration of high-salt ash washing water, the smaller its volume, which can significantly reduce the processing scale of the next process (such as evaporation and crystallization), thereby reducing project investment costs and operating energy consumption. Conversely, if the salt concentration is low and the volume is large, it will lead to an increase in the processing load and a significant increase in operating and investment costs. Therefore, controlling the salt concentration of high-salt ash washing water is crucial in practical engineering. According to the data in Table 1 above, the mass ratio of K / Na in the raw material is 2~5:1, which is a typical high-potassium, low-sodium material. To simplify control, we can assume that the material component in the high-salt ash washing water is potassium chloride (KCl). The solubility of potassium chloride in water is shown in Table 3 below, and the correspondence between concentration and density is shown in Table 4 below. The solubility of potassium chloride is quite sensitive to temperature changes; its solubility increases with increasing temperature and decreases with decreasing temperature. In practical engineering, it is advisable to control the salt concentration of the high-salt ash washing water to be close to saturation, which satisfies both the optimal scale of evaporation and crystallization and prevents crystal precipitation and blockage due to temperature changes during actual operation.

[0079] Specifically, the method for determining the target filtrate density is as follows:

[0080] Considering the proportions of various components in the sintering machine head ash raw material, the filtrate discharged from the filtrate tank in this invention is a typical high-potassium, low-sodium material. Therefore, the solubility of potassium chloride in water at the current temperature is first determined based on the solubility of potassium chloride in water at different temperatures (see Table 3 below), and then the corresponding concentration of the potassium chloride aqueous solution (i.e., , where: C T At T℃, the corresponding saturated solubility (S) T The mass fraction of potassium chloride (i.e., the concentration of potassium chloride aqueous solution to be obtained) is then determined, and the density of the corresponding potassium chloride aqueous solution (i.e., the target filtrate density) is determined according to the potassium chloride aqueous solution concentration-density correspondence (see Table 4 below).

[0081] Table 3 Solubility of potassium chloride in water

[0082]

[0083] Table 4. Concentration-Density Correspondence of Potassium Chloride Aqueous Solution

[0084]

[0085] S5. Slurry concentration feedback control:

[0086] When the composition of the sintering mill head ash is constant, the change in slurry concentration corresponds to the change in salt concentration; that is, the higher the slurry concentration, the higher the salt concentration. However, when the composition of the sintering mill head ash fluctuates, the correlation between slurry concentration and salt concentration becomes uncertain. Therefore, to ensure stable system operation, it is necessary to independently control the slurry concentration. Furthermore, excessively high slurry concentration in the slurry tank will increase the risk of blockage in pipelines and equipment, and accelerate equipment wear. Thus, reasonable control of slurry concentration is crucial for the long-term stable operation of the sintering mill head ash washing process. The specific control process is as follows:

[0087] The first mass metering device detects the mass flow rate Q1 of the sintering machine head ash entering the hydrocyclone, and the second mass metering device detects the mass flow rate Q2 of the process water entering the hydrocyclone. The slurry concentration X discharged from the slurry tank is calculated using formula (Ⅰ):

[0088]

[0089] Set the target slurry concentration for discharge from the slurry tank as X. 目标 Let X = X 目标 By combining the real-time filtrate density ρ detected by the filtrate density monitoring device, the ratio of the mass flow rate of sintering machine head ash to the mass flow rate of process water Q1:Q2 can be calculated using the above formula (Ⅰ). This ratio is used to control the mass flow rate of sintering machine head ash to process water entering the hydrocyclone (monitored and controlled in real time by the first and second mass metering devices), so that the slurry concentration discharged from the slurry tank is within the target slurry concentration range.

[0090] Building upon the above-mentioned method of controlling the mass flow ratio of sintering machine head ash to process water to regulate slurry concentration, this invention further introduces a feedback adjustment mechanism to ensure stable control of the slurry concentration. Specifically, a slurry concentration monitoring device is installed on the slurry delivery pipeline to monitor the concentration of the slurry discharged from the slurry tank in real time. When the monitored real-time slurry concentration X0 < X... 目标When the slurry is too thin, open the slurry return valve and close the slurry outlet valve. The slurry returns to the hydrocyclone for remixing, which increases the slurry concentration and enhances the premixing effect within the hydrocyclone. When the monitored real-time slurry concentration X0 ≥ X... 目标 When the slurry concentration meets the standard, close the slurry return valve and open the slurry outlet valve. The slurry is then normally transported to the solid-liquid separation device.

[0091] In this application, the height of the slurry tank is 0.2-50m, preferably 0.3-35m, more preferably 0.5-30m, more preferably 0.8-25m, and even more preferably 1-20m.

[0092] In this application, the diameter of the pulping tank is 0.2-20m, preferably 0.3-15m, more preferably 0.5-12m, more preferably 0.8-10m, and even more preferably 1-8m.

[0093] Compared with existing technologies, this invention has the following beneficial technical effects:

[0094] 1. This utility model adds a hydrocyclone to the top of the slurry tank as an ash-water premixing device. Through the strong turbulent flow field generated by the hydrocyclone, the sintering machine head ash and process water enter the hydrocyclone to form a swirling scouring, realizing high-speed shearing and full premixing of the ash-water two-phase materials, thereby solving the problem that the fine components in the sintering machine head ash are highly hydrophobic and difficult to mix evenly.

[0095] 2. In this utility model, a slurry return pipe is branched off from the slurry delivery pipe connected to the slurry outlet of the slurry tank and connected to the hydrocyclone. On the one hand, the slurry return optimizes the control of the slurry concentration in the slurry tank, ensuring the stable operation of the equipment. On the other hand, the slurry return and the sintering machine head ash form a swirling scouring effect in the hydrocyclone, further improving the premixing effect in the hydrocyclone.

[0096] 3. This utility model sets up a filtrate tank with a stirrer and a filtrate pump downstream of the solid-liquid separation device, and branches a filtrate return pipe on the filtrate delivery pipe connected to the outlet of the filtrate pump and connects it to a hydrocyclone. The filtrate return optimizes the control of the salt concentration in the filtrate discharged from the filtrate tank, so as to ensure the stability of the salt concentration of the final high-salt washing water.

[0097] 4. This utility model is equipped with a negative pressure device at the top of the slurry tank, which avoids the pollution and harm of water vapor and dust during slurrying, while ensuring smooth ash discharge.

[0098] 5. This utility model sets a grid at the bottom of the slurry tank to solve the problem of wear on the equipment caused by coarse particles in the sintering machine head ash.

[0099] 6. Based on the slurry-forming device for washing ash water at the sintering machine head proposed in this utility model, this utility model also designs a matching slurry-forming method for washing ash water at the sintering machine head. This method adopts an online monitoring and feedback mechanism to solve the problem of fluctuations in salt concentration of high-salt washing ash water and slurry concentration during the washing process of ash water at the sintering machine head, thus ensuring the stable operation of the process. Attached Figure Description

[0100] Figure 1 Flow chart of the existing wet leaching process for sintering machine head ash;

[0101] Figure 2 This is a schematic diagram of the structure of a pulping device for washing ash water at the head of a sintering machine according to the present invention;

[0102] Figure 3 This is a cross-sectional view of the hydrocyclone in this utility model;

[0103] Figure 4 This is a plan view of the hydrocyclone in this utility model;

[0104] Figure 5 This is a schematic diagram of the negative pressure device in this utility model;

[0105] Figure 6 This is a cross-sectional view of the grid mesh in this utility model;

[0106] Figure 7 This is a plan view of the grid mesh in this utility model.

[0107] Figure label:

[0108] 1: Slurry tank; 101: Slurry agitator; 2: Slurry pump; 3: Solid-liquid separation device; 4: Hydrocyclone; 401: Straight section; 402: Inverted cone section; 5: Slurry concentration monitoring device; 6: Filtrate tank; 601: Filtrate agitator; 7: Filtrate pump; 8: Filtrate density monitoring device; 9: Bar screen; 10: Negative pressure device; 1001: Expansion section; 1002: Blower; 11: Bar screen; 1201: First mass metering device; 1202: Second mass metering device;

[0109] a: Sintering machine head ash inlet; b: Process water inlet; c: Discharge port; d: Slurry return port; e: Filtrate return port; f: Discharge port; g: Rinse water port;

[0110] L1: Slurry conveying pipeline; L2: Slurry return pipeline; L3: Filtrate discharge pipeline; L4: Filtrate conveying pipeline; L5: Filtrate return pipeline; L6: Tail gas discharge pipeline; L7: Rinse water pipeline; L8: Process water pipeline;

[0111] F1: Slurry reflux valve; F2: Slurry discharge valve; F3: Filtrate reflux valve; F4: Filtrate discharge valve; F5: Automatic discharge valve; F6: Exhaust valve; F7: Periodic flushing valve; F8: Vacuum pressure relief valve; F9: Water supply valve. Detailed Implementation

[0112] The technical solution of this utility model is illustrated below. The scope of protection of this utility model includes, but is not limited to, the following embodiments.

[0113] According to the first embodiment of this utility model, a pulping device for washing ash water at the sintering machine head is provided.

[0114] A slurry preparation device for washing sintering machine head ash includes a slurry preparation tank 1, a slurry pump 2, and a solid-liquid separation device 3. The slurry outlet of the slurry preparation tank 1 is connected to the inlet of the solid-liquid separation device 3 via a slurry delivery pipe L1. The slurry pump 2 is installed on the slurry delivery pipe L1. A slurry agitator 101 is installed inside the slurry preparation tank 1. The device also includes a hydrocyclone 4 installed at the top of the slurry preparation tank 1. The hydrocyclone 4 has a sintering machine head ash inlet a, a process water inlet b, and a discharge outlet c, which is connected to the interior of the slurry preparation tank 1.

[0115] In this invention, the hydrocyclone 4 is also provided with a slurry return port d. A slurry return pipe L2 is branched off from the slurry delivery pipe L1 located downstream of the slurry pump 2, and the slurry return pipe L2 is connected to the slurry return port d of the hydrocyclone 4.

[0116] Preferably, a slurry return valve F1 is provided on the slurry return pipe L2. A slurry outlet valve F2 is provided on the slurry delivery pipe L1 downstream of the location where the slurry return pipe L2 is located. Preferably, a slurry concentration monitoring device 5 is provided on the slurry delivery pipe L1, and the slurry concentration monitoring device 5 is located upstream of the location where the slurry return pipe L2 is located.

[0117] In this invention, the device further includes a filtrate tank 6 and a filtrate pump 7 disposed downstream of the solid-liquid separation device 3. The liquid outlet of the solid-liquid separation device 3 is connected to the filtrate tank 6 via a pipe. The filtrate outlet of the filtrate tank 6 is connected to the inlet of the filtrate pump 7 via a filtrate discharge pipe L3. The outlet of the filtrate pump 7 is connected to a filtrate delivery pipe L4. A filtrate stirrer 601 is installed inside the filtrate tank 6.

[0118] Preferably, the hydrocyclone 4 is also provided with a filtrate return port e. A filtrate return pipe L5 branches off from the filtrate delivery pipe L4 and is connected to the filtrate return port e of the hydrocyclone 4.

[0119] Further preferably, a filtrate reflux valve F3 is provided on the filtrate reflux pipeline L5. A filtrate outlet valve F4 is provided on the filtrate delivery pipeline L4 and downstream of the location of the filtrate reflux pipeline L5. Preferably, a filtrate density monitoring device 8 is provided on the filtrate delivery pipeline L4, and the filtrate density monitoring device 8 is located upstream of the location of the filtrate reflux pipeline L5.

[0120] In this invention, the hydrocyclone 4 includes a straight section 401 and an inverted conical section 402 connected to the lower part of the straight section 401. The slurry return port d is located on the side of the straight section 401. Preferably, the slurry return pipe L2 is tangentially connected to the slurry return port d.

[0121] Preferably, a bar screen 9 is provided within the straight section 401 of the hydrocyclone 4. Preferably, the bar screen 9 is inclined. The higher end of the bar screen 9 is positioned above the slurry return interface d, and a discharge port f is provided at the position of the straight section 401 corresponding to the lower end of the bar screen 9. Preferably, an automatic discharge valve F5 is provided at the discharge port f.

[0122] In this invention, the inclination angle θ of the inverted conical section 402 of the hydrocyclone 4 is 45°~70°, preferably 55°~65°.

[0123] In this invention, the inclination angle β of the inner grid screen 9 of the hydrocyclone 4 is 5°~30°, preferably 10°~15°. Preferably, the relationship between the screen aperture size d1 of the grid screen 9 and the ash particle size of the sintering machine head satisfies: d min ≤d1≤d max Among them, d min The smallest particle size of the sintering machine head ash is represented by d. max This indicates the maximum particle size of the sintering machine head ash.

[0124] In this invention, the device further includes a negative pressure device 10 disposed on the top of the slurry tank 1. Preferably, the negative pressure device 10 and the hydrocyclone 4 are disposed on opposite sides of the top of the slurry tank 1.

[0125] The negative pressure device 10 includes an expansion section 1001 and a blower 1002. The expansion section 1001 is located at the top of the slurry tank 1 and is connected to the interior of the slurry tank 1. A tail gas discharge pipe L6 is led out from the top outlet of the expansion section 1001, and the tail gas discharge pipe L6 is connected to the blower 1002. Preferably, an exhaust valve F6 is provided on the tail gas discharge pipe L6.

[0126] Preferably, the upper part of the side wall of the enlarged section 1001 is also provided with a flushing water interface g. The flushing water interface g is connected to a flushing water pipe L7. Preferably, the flushing water pipe L7 is tangentially connected to the flushing water interface g. More preferably, the flushing water pipe L7 is provided with a periodic flushing valve F7.

[0127] More preferably, a vacuum pressure relief valve F8 is also provided at the top of the enlarged section 1001. Preferably, the outlet of the blower 1002 is connected to the exhaust gas treatment system via a pipeline.

[0128] In this invention, a grid 11 is also provided at the bottom of the slurry tank 1. Preferably, the relationship between the height h of the grid 11 and the gap H between the slurry agitator 101 and the bottom of the slurry tank 1 satisfies: h ≤ (0.1~0.5)H.

[0129] Preferably, the individual grid size d2 within the grid 11 is the same as the maximum particle size d of the sintering machine head ash. max The relation satisfies: d max ≤d2≤10d max .

[0130] More preferably, the grid 11 is an assembly structure of multiple grid units. The relationship between the size L of a single grid unit and the inspection hole size D of the slurry tank 1 satisfies: 0.5D ≤ L ≤ 0.8D.

[0131] Further preferably, the materials of the hydrocyclone 4, the bar screen 9, and the bar mesh 11 can be selected from fiberglass, rubber-lined steel, stainless steel, and plastic, respectively. Preferably, the materials of the hydrocyclone 4, the bar screen 9, and the bar mesh 11 are all fiberglass.

[0132] In this utility model, the device also includes a first mass metering device 1201 installed at the ash inlet a of the sintering machine head.

[0133] In this invention, the process water inlet b of the hydrocyclone 4 is connected to a process water pipe L8. The process water pipe L8 is equipped with a second mass metering device 1202 and a water supply valve F9.

[0134] Example 1

[0135] like Figure 2-4 As shown, a slurry preparation device for washing sintering machine head ash includes a slurry preparation tank 1, a slurry pump 2, and a solid-liquid separation device 3. The slurry outlet of the slurry preparation tank 1 is connected to the inlet of the solid-liquid separation device 3 via a slurry delivery pipe L1. The slurry pump 2 is installed on the slurry delivery pipe L1. A slurry agitator 101 is installed inside the slurry preparation tank 1. The device also includes a hydrocyclone 4 installed at the top of the slurry preparation tank 1. The hydrocyclone 4 has a sintering machine head ash inlet a, a process water inlet b, and a discharge port c, which is connected to the interior of the slurry preparation tank 1.

[0136] Example 2

[0137] The same method as Embodiment 1 is used, except that the hydrocyclone 4 is also provided with a slurry return port d. A slurry return pipe L2 is branched off from the slurry delivery pipe L1 located downstream of the slurry pump 2, and the slurry return pipe L2 is connected to the slurry return port d of the hydrocyclone 4.

[0138] Example 3

[0139] Example 2 is repeated, except that a slurry return valve F1 is installed on the slurry return pipe L2. A slurry outlet valve F2 is installed on the slurry delivery pipe L1 downstream of the location where the slurry return pipe L2 is installed.

[0140] Example 4

[0141] The same method as Example 3 is used, except that a slurry concentration monitoring device 5 is installed on the slurry conveying pipeline L1, and the slurry concentration monitoring device 5 is located upstream of the location where the slurry return pipeline L2 is set.

[0142] Example 5

[0143] The apparatus is repeated in Embodiment 4, except that it further includes a filtrate tank 6 and a filtrate pump 7 located downstream of the solid-liquid separation device 3. The liquid outlet of the solid-liquid separation device 3 is connected to the filtrate tank 6 via a pipe. The filtrate outlet of the filtrate tank 6 is connected to the inlet of the filtrate pump 7 via a filtrate discharge pipe L3. The outlet of the filtrate pump 7 is connected to a filtrate delivery pipe L4. A filtrate stirrer 601 is installed inside the filtrate tank 6.

[0144] Example 6

[0145] Example 5 is repeated, except that the hydrocyclone 4 is also provided with a filtrate return port e. A filtrate return pipe L5 is branched off from the filtrate delivery pipe L4, and the filtrate return pipe L5 is connected to the filtrate return port e of the hydrocyclone 4.

[0146] Example 7

[0147] Example 6 is repeated, except that a filtrate reflux valve F3 is provided on the filtrate reflux pipe L5. A filtrate outlet valve F4 is provided on the filtrate delivery pipe L4 downstream of the location where the filtrate reflux pipe L5 is located.

[0148] Example 8

[0149] The same method as Example 7 is used, except that a filtrate density monitoring device 8 is provided on the filtrate conveying pipeline L4, and the filtrate density monitoring device 8 is located upstream of the location where the filtrate return pipeline L5 is set.

[0150] Example 9

[0151] Example 8 is repeated, except that the hydrocyclone 4 includes a straight section 401 and an inverted conical section 402 connected to the lower part of the straight section 401. The slurry return port d is located on the side of the straight section 401.

[0152] Example 10

[0153] Repeat Example 9, except that the slurry return pipe L2 is tangentially connected to the slurry return interface d.

[0154] Example 11

[0155] Repeat Example 10, except that a grid screen 9 is provided in the straight section 401 of the hydrocyclone 4.

[0156] Example 12

[0157] Example 11 is repeated, except that the bar screen 9 is inclined. The higher end of the bar screen 9 is positioned higher than the slurry return interface d, and the lower end of the bar screen 9 has a discharge port f at the corresponding straight section 401.

[0158] Example 13

[0159] Repeat Example 12, except that an automatic discharge valve F5 is provided at the discharge port f.

[0160] Example 14

[0161] Example 13 is repeated, except that the inclination angle θ of the inverted cone section 402 of the hydrocyclone 4 is 60°.

[0162] Example 15

[0163] Example 13 is repeated, except that the inverted cone section 402 of the hydrocyclone 4 has an inclination angle θ of 55°.

[0164] Example 16

[0165] Example 13 is repeated, except that the inverted cone section 402 of the hydrocyclone 4 has an inclination angle θ of 65°.

[0166] Example 17

[0167] Example 14 is repeated, except that the inclination angle β of the inner grid screen 9 of the hydrocyclone 4 is 12°.

[0168] Example 18

[0169] Repeat Example 15, except that the inclination angle β of the inner grid screen 9 of the hydrocyclone 4 is 10°.

[0170] Example 19

[0171] Example 16 is repeated, except that the inclination angle β of the inner grid screen 9 of the hydrocyclone 4 is 15°.

[0172] Example 20

[0173] Repeat Example 17, except that the relationship between the screen aperture size d1 of the grid screen 9 and the ash particle size of the sintering machine head satisfies: d min≤d1≤d max Among them, d min =0.005mm, d max =5mm, d min The smallest particle size of the sintering machine head ash is represented by d. max This indicates the maximum particle size of the sintering machine head ash. In this embodiment, the sieve aperture size of the grid screen 9 is d1 = 3 mm.

[0174] Example 21

[0175] like Figure 5 As shown, Embodiment 20 is repeated, except that the device further includes a negative pressure device 10 disposed at the top of the slurry tank 1. The negative pressure device 10 and the cyclone separator 4 are respectively disposed on opposite sides of the top of the slurry tank 1. The negative pressure device 10 includes an expansion section 1001 and a blower 1002. The expansion section 1001 is disposed at the top of the slurry tank 1 and communicates with the interior of the slurry tank 1. A tail gas discharge pipe L6 is led out from the top outlet of the expansion section 1001, and the tail gas discharge pipe L6 is connected to the blower 1002.

[0176] Example 22

[0177] Repeat Example 21, except that an exhaust valve F6 is provided on the exhaust pipe L6.

[0178] Example 23

[0179] The embodiment 22 is repeated, except that a flushing water interface g is also provided on the upper part of the side wall of the enlarged section 1001. The flushing water interface g is connected to a flushing water pipe L7.

[0180] Example 24

[0181] Repeat Example 23, except that the flushing water pipe L7 is tangentially connected to the flushing water interface g.

[0182] Example 25

[0183] Repeat Example 24, except that a periodic flushing valve F7 is provided on the flushing water pipe L7.

[0184] Example 26

[0185] The embodiment 25 is repeated, except that a vacuum pressure relief valve F8 is also provided at the top of the enlarged section 1001.

[0186] Example 27

[0187] Repeat Example 26, except that the outlet of fan 1002 is connected to the exhaust gas treatment system via a pipe.

[0188] Example 28

[0189] Repeat Example 27, except that a grid 11 is also provided at the bottom of the pulping tank 1.

[0190] Example 29

[0191] Example 28 is repeated, except that the relationship between the height h of the grid 11 and the gap H between the agitator 101 and the bottom of the slurry tank 1 satisfies: h ≤ 0.3H; where H = 500 mm. In this example, the height h of the grid 11 is 60 mm.

[0192] Example 30

[0193] Example 29 is repeated, except that the size d2 of a single grid within the grid 11 is the same as the maximum particle size d of the sintering machine head ash. max The relation satisfies: d max ≤d2≤10d max ; where: d max =5mm. In this embodiment, the size of a single mesh within the grid 11 is d2=10mm.

[0194] Example 31

[0195] Example 30 is repeated, except that the grid 11 is an assembly structure of multiple grid units. The relationship between the size L of the grid unit and the inspection hole size D of the slurry tank 1 satisfies: 0.5D ≤ L ≤ 0.8D; where D = 500mm. In this example, the size of a single grid unit is L = 300mm.

[0196] Example 32

[0197] The same example 31 is repeated, except that the hydrocyclone 4, the bar screen 9, and the bar mesh 11 are all made of steel lined with rubber.

[0198] Example 33

[0199] The same embodiment 31 is repeated, except that the hydrocyclone 4, the grid screen 9, and the grid mesh 11 are all made of fiberglass.

[0200] Example 34

[0201] The embodiment 33 is repeated, except that the device further includes a first mass metering device 1201 located at the ash inlet a of the sintering machine head. The process water inlet b of the hydrocyclone 4 is connected to a process water pipe L8. The process water pipe L8 is equipped with a second mass metering device 1202 and a water supply valve F9.

[0202] The method of using the pulping device for washing ash water at the sintering machine head as described in this embodiment includes the following steps:

[0203] S1. Sintering machine head ash and process water enter hydrocyclone 4 through sintering machine head ash inlet a and process water inlet b, respectively, for hydrocyclone premixing. The slurry obtained after premixing enters slurry tank 1 for stirring and slurrying.

[0204] S2. The slurry obtained after pulping is pumped by slurry pump 2 and transported to solid-liquid separation device 3 via slurry conveying pipeline L1. The slurry is separated into high-salt washing water and iron-rich powder.

[0205] S3. The high-salt washing water enters the filtrate tank 6. The filtrate agitator 601 installed in the filtrate tank 6 agitates the high-salt washing water. The filtrate obtained after agitation is sent to the next process through the filtrate pump 7 and the filtrate delivery pipeline L4.

[0206] S4. The filtrate density monitoring device 8 installed on the filtrate conveying pipeline L4 detects the real-time filtrate density ρ, and sets the target filtrate density as ρ. 目标 When ρ < ρ 目标 At this time, open the filtrate reflux valve F3 and close the filtrate outlet valve F4. The filtrate is then returned to the hydrocyclone 4 through the filtrate reflux pipe L5, thereby increasing the filtrate salt concentration until ρ = ρ 目标 When ρ≥ρ 目标 When the filtrate is in the process of being discharged, close the filtrate return valve F3 and open the filtrate outlet valve F4. The filtrate is then sent to the next process via the filtrate delivery pipeline L4.

[0207] S5. A first mass metering device 1201 installed at the ash inlet a of the sintering machine head detects the mass flow rate of the sintering machine head ash, and a second mass metering device 1202 installed at the process water inlet b detects the mass flow rate of the process water. The target slurry concentration discharged from the slurry tank 1 is set to X. 目标 The mass flow rate ratio of sintering head ash to process water entering the hydrocyclone 4 is monitored and controlled in real time by the first mass metering device 1201 and the second mass metering device 1202, so that the slurry concentration discharged from the slurry tank 1 is within the target slurry concentration range.

[0208] A slurry concentration monitoring device 5, installed on the slurry delivery pipeline L1, detects the real-time slurry concentration X0. When X0 < X... 目标 At this time, open the slurry return valve F1 and close the slurry outlet valve F2. The slurry is then returned to the hydrocyclone 4 through the slurry return pipe L2 to increase the slurry concentration until X0 = X 目标 When X0 ≥ X 目标 At that time, close the slurry return valve F1 and open the slurry outlet valve F2, and transport the slurry to the solid-liquid separation device 3 through the slurry conveying pipeline L1 to obtain high-salt washing water.

Claims

1. A slurry preparation device for washing ash at the head of a sintering machine, the device comprising a slurry preparation tank (1), a slurry pump (2), and a solid-liquid separation device (3); the slurry outlet of the slurry preparation tank (1) is connected to the inlet of the solid-liquid separation device (3) via a slurry conveying pipe (L1); the slurry pump (2) is provided on the slurry conveying pipe (L1); a slurry agitator (101) is provided inside the slurry preparation tank (1); characterized in that: The device also includes a hydrocyclone (4) installed on the top of the slurry tank (1); the hydrocyclone (4) is provided with a sintering head ash inlet (a), a process water inlet (b), and a discharge port (c), the discharge port (c) being connected to the inside of the slurry tank (1).

2. The pulping apparatus according to claim 1, characterized in that: The hydrocyclone (4) is also provided with a slurry return port (d); a slurry return pipe (L2) is branched off from the slurry delivery pipe (L1) downstream of the slurry pump (2), and the slurry return pipe (L2) is connected to the slurry return port (d) of the hydrocyclone (4).

3. The pulping apparatus according to claim 2, characterized in that: A slurry return valve (F1) is installed on the slurry return pipe (L2); a slurry outlet valve (F2) is installed on the slurry delivery pipe (L1) downstream of the location where the slurry return pipe (L2) is installed.

4. The pulping apparatus according to claim 3, characterized in that: A slurry concentration monitoring device (5) is installed on the slurry conveying pipeline (L1), and the slurry concentration monitoring device (5) is located upstream of the location where the slurry return pipeline (L2) is set.

5. The pulping apparatus according to claim 1, characterized in that: The device also includes a filtrate tank (6) and a filtrate pump (7) located downstream of the solid-liquid separation device (3); wherein, the liquid outlet of the solid-liquid separation device (3) is connected to the filtrate tank (6) via a pipe; the filtrate outlet of the filtrate tank (6) is connected to the inlet of the filtrate pump (7) via a filtrate discharge pipe (L3); the outlet of the filtrate pump (7) is connected to a filtrate delivery pipe (L4); and a filtrate stirrer (601) is provided inside the filtrate tank (6).

6. The pulping apparatus according to claim 5, characterized in that: The hydrocyclone (4) is also provided with a filtrate return port (e); a filtrate return pipe (L5) is branched off from the filtrate delivery pipe (L4), and the filtrate return pipe (L5) is connected to the filtrate return port (e) of the hydrocyclone (4).

7. The pulping apparatus according to claim 6, characterized in that: A filtrate reflux valve (F3) is provided on the filtrate reflux pipeline (L5); a filtrate discharge valve (F4) is provided on the filtrate delivery pipeline (L4) downstream of the location where the filtrate reflux pipeline (L5) is located.

8. The pulping apparatus according to claim 7, characterized in that: A filtrate density monitoring device (8) is provided on the filtrate delivery pipeline (L4), and the filtrate density monitoring device (8) is located upstream of the location where the filtrate return pipeline (L5) is set.

9. The pulping apparatus according to claim 2, characterized in that: The hydrocyclone (4) includes a straight section (401) and an inverted conical section (402) connected to the lower part of the straight section (401); wherein the slurry return port (d) is located on the side of the straight section (401).

10. The pulping apparatus according to claim 9, characterized in that: The slurry return pipe (L2) is tangentially connected to the slurry return interface (d).

11. The pulping apparatus according to claim 9, characterized in that: A grid screen (9) is provided in the straight section (401) of the hydrocyclone (4).

12. The pulping apparatus according to claim 11, characterized in that: The screen (9) is inclined; wherein, the higher end of the screen (9) is positioned higher than the slurry return interface (d), and the lower end of the screen (9) is provided with a discharge port (f) on the straight section (401).

13. The pulping apparatus according to claim 12, characterized in that: An automatic discharge valve (F5) is provided at the discharge port (f).

14. The pulping apparatus according to claim 12, characterized in that: The inverted cone section (402) of the hydrocyclone (4) has an inclination angle θ of 45°~70°; and / or The inclination angle β of the inner grid screen (9) of the hydrocyclone (4) is 5°~30°.

15. The pulping apparatus according to claim 14, characterized in that: The inverted cone section (402) of the hydrocyclone (4) has an inclination angle θ of 55°~65°; and / or The inclination angle β of the inner grid screen (9) of the hydrocyclone (4) is 10°~15°.

16. The pulping apparatus according to claim 14, characterized in that: The relationship between the sieve aperture size d1 of the grid screen (9) and the particle size of the ash at the sintering machine head satisfies: d min ≤d1≤d max ; Where, d min The smallest particle size of the sintering machine head ash is represented by d. max This indicates the maximum particle size of the sintering machine head ash.

17. The pulping apparatus according to any one of claims 1-16, characterized in that: The device also includes a negative pressure device (10) installed at the top of the pulping tank (1); the negative pressure device (10) and the hydrocyclone (4) are respectively installed on opposite sides of the top of the pulping tank (1); The negative pressure device (10) includes an expansion section (1001) and a fan (1002); the expansion section (1001) is located at the top of the slurry tank (1) and is connected to the inside of the slurry tank (1); a tail gas discharge pipe (L6) is led out from the top outlet of the expansion section (1001) and the tail gas discharge pipe (L6) is connected to the fan (1002).

18. The pulping apparatus according to claim 17, characterized in that: An exhaust valve (F6) is installed on the exhaust pipe (L6).

19. The pulping apparatus according to claim 17, characterized in that: The upper side wall of the enlarged section (1001) is also provided with a flushing water interface (g); the flushing water interface (g) is connected to a flushing water pipe (L7).

20. The pulping apparatus according to claim 19, characterized in that: The flushing water pipe (L7) is tangentially connected to the flushing water inlet (g).

21. The pulping apparatus according to claim 19, characterized in that: A periodic flushing valve (F7) is installed on the flushing water pipe (L7).

22. The pulping apparatus according to claim 17, characterized in that: The top of the enlarged section (1001) is also equipped with a vacuum pressure relief valve (F8).

23. The pulping apparatus according to claim 17, characterized in that: The outlet of the blower (1002) is connected to the exhaust gas treatment system via a pipeline.

24. The pulping apparatus according to any one of claims 1-16, characterized in that: The bottom of the pulping tank (1) is also equipped with a grid (11).

25. The pulping apparatus according to claim 24, characterized in that: The relationship between the height h of the grid (11) and the gap H between the agitator (101) inside the slurry tank (1) and the bottom of the slurry tank (1) satisfies: h≤(0.1~0.5)H.

26. The pulping apparatus according to claim 24, characterized in that: The individual grid size d2 within the grid (11) is equal to the maximum particle size d of the sintering machine head ash. max The relation satisfies: d max ≤d2≤10d max .

27. The pulping apparatus according to claim 24, characterized in that: The grid (11) is a multi-grid unit assembly structure; wherein, the relationship between the size L of a single grid unit and the inspection hole size D of the slurry tank (1) satisfies: 0.5D≤L≤0.8D.

28. The pulping apparatus according to any one of claims 1-16, characterized in that: The device also includes a first mass metering device (1201) located at the ash inlet (a) of the sintering machine head; and / or The process water inlet (b) of the hydrocyclone (4) is connected to a process water pipe (L8); the process water pipe (L8) is equipped with a second mass metering device (1202) and a water supply valve (F9).

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