Continuous production equipment and process for preparing ultrafine calcium carbonate from fly ash washing liquid

Abstract

The present invention discloses a continuous production device and process for preparing ultrafine calcium carbonate from fly ash washing liquid, which relates to the technical field of ultrafine calcium carbonate preparation, and aims to solve the technical problem of insufficient functionality of the existing equipment for preparing ultrafine calcium carbonate from fly ash washing liquid. It includes a preparation rack; a secondary liquid-phase pump feeding assembly is arranged on the preparation rack; a reaction assembly is also arranged on the preparation rack; the reaction assembly includes a number of reaction tanks; a stirring assembly is arranged inside the reaction tank; a planetary mechanism is arranged at the top of the reaction tank; the output end of the secondary liquid-phase pump feeding assembly is provided with a fly ash washing liquid shunt assembly; the output end of the fly ash washing liquid shunt assembly is respectively provided with a confluence pipe assembly and a sodium carbonate shunt pipe assembly through a number of three-way valves. The present invention realizes the diversification of functions through two different operation modes, and also realizes the production operation of calcium carbonate of different specifications.

Description

Technical Field

[0001] The present invention relates to the technical field of ultrafine calcium carbonate preparation, and more specifically, to a continuous production device and process for preparing ultrafine calcium carbonate from fly ash washing liquid. Background Art

[0002] Fly ash washing liquid is generated during the washing process of municipal solid waste incineration fly ash. Through a process, the calcium resources therein can be recovered and used to prepare ultrafine calcium carbonate. This not only reduces the environmental pollution problems caused by the direct discharge of fly ash washing liquid, but also converts waste into valuable products. For example, in industries such as building materials, plastics, and rubber, calcium carbonate is an important filler, and this process enables the originally wasted calcium resources to regain economic value. Improving resource utilization rate: effectively utilizes the calcium component in the fly ash washing liquid, and compared with traditional calcium source mining and processing methods, reduces the dependence on resources such as natural limestone. To a certain extent, it alleviates the damage to the ecological environment caused by ore mining, such as vegetation damage and soil erosion caused by mine exploitation.

[0003] Production equipment for preparing ultrafine calcium carbonate from fly ash washing liquid:

[0004] Settling tank: used to receive fly ash washing liquid and allow large particle impurities therein to undergo preliminary sedimentation. First plate-frame separator: installed on the pipeline between the settling tank and the reaction tank, which can further filter the fly ash washing liquid after preliminary sedimentation and intercept impurities such as larger particle suspended solids. Ceramic membrane: located on the pipeline between the first plate-frame separator and the reaction tank, which can finely filter the fly ash washing liquid to ensure that the content of suspended solids in the washing liquid entering the reaction tank is extremely low. Reaction tank: connected to the settling tank through a pipeline and includes three groups of reaction tanks arranged in parallel, and the number of operating reaction tanks can be adjusted according to the treatment volume of the fly ash washing liquid. A circulation pump is provided at the bottom of the reaction tank, and a stirrer is provided inside to facilitate full mixing and reaction of the materials. Sodium carbonate tank: used to store sodium carbonate solution and can add sodium carbonate into the reaction tank to provide carbonate ions for the reaction, reacting with calcium ions in the fly ash washing liquid to form calcium carbonate. Second plate-frame separator: used to separate solid and liquid from the materials discharged from the reaction tank, separating solid-phase substances such as the calcium carbonate generated by the reaction and the liquid. Washing tank: the separated solid phase is dispersed and then enters the washing tank, and the solid phase is washed by adding washing water to remove impurities such as chloride ions therein. Centrifuge: centrifugally separates the washed materials to further improve the purity and solid content rate of the solid phase. Dryer: adopts a pneumatic drying method to dry the solid phase obtained after centrifugal separation, and then obtains ultrafine calcium carbonate products after grinding and crushing.

[0005] Production process: Pretreatment of fly ash washing liquid: The fly ash washing liquid generated in the fly ash washing and dechlorination process first enters the sedimentation tank for pre-sedimentation to remove impurities with larger particles. Then it is filtered through the first plate and frame separator and further filtered through a ceramic membrane to control the suspended solids in the produced water below 30 mg / l and ensure that the pH is not lower than 10.5. Reaction operation: The fly ash washing liquid enters the reaction tank, samples are taken to detect the calcium ion concentrations of the fly ash washing liquid and the sodium carbonate solution, the dosage of the sodium carbonate solution is calculated, and they are mixed and reacted. Plate and frame separation: After the material is discharged from the reaction tank, it enters the second plate and frame separator for separation to obtain a solid phase and a liquid phase. Washing: The separated solid phase is dispersed and then enters the washing tank, and the ratio of washing water to the solid phase is controlled at 1:1.2 - 3 for sufficient washing to remove chloride ions in the ultrafine calcium carbonate product. Centrifugal separation: After washing, it enters a centrifuge for separation to further improve the purity and solid content of the solid phase.

[0006] During the reaction process, multiple reaction tank pipelines are connected in parallel. This setting enables flexible adaptability to production scale to meet different output requirements: In the actual production process, the supply of fly ash washing liquid may change due to various factors. For example, fluctuations in the treatment volume of the upstream fly ash washing process, adjustment of production plans at different time periods, etc. The three groups of reaction tanks connected in parallel can flexibly adjust the number of operating reaction tanks according to the treatment volume of the fly ash washing liquid. If the amount of fly ash washing liquid is small, only one group of reaction tanks needs to be opened to ensure that the reaction proceeds at an appropriate residence time and reactant concentration, avoiding problems such as incomplete reaction or low efficiency caused by insufficient raw materials; when the treatment volume is large, multiple groups of reaction tanks can be opened simultaneously to meet the needs of large-scale production and improve production efficiency. Adaptation to market changes: From the perspective of the market demand for products, the market demand for calcium carbonate products also fluctuates. When the market demand for ultrafine calcium carbonate is strong, the enterprise can open all the reaction tanks to increase production; while when the market demand is sluggish, the number of operating reaction tanks can be reduced to lower production costs and make the production process more flexible in adapting to market changes.

[0007] The parallel connection of multiple reactor pipelines can improve the reliability and fault tolerance of the system, providing emergency guarantee in case of equipment failure. During continuous production, if any reactor fails (such as agitator failure, circulation pump damage, tank leakage, etc.), other normal reactors can still continue to operate. This is like having multiple parallel roads in a traffic network. When one road (one reactor) has problems (such as maintenance, accident), materials can still pass through other roads (other reactors) normally (react), thus preventing the interruption of the entire production process. This design can provide sufficient time for equipment repair and maintenance, reducing production losses caused by sudden equipment failures. Ensure stable product quality: Even if the reaction conditions in a certain reactor are abnormal (such as temperature control error, abnormal reactant concentration, etc.), due to the simultaneous operation of multiple reactors, the normal reactions in other reactors can buffer the impact of this abnormal situation on the quality of the final product to a certain extent. For example, if the reaction temperature in one reactor is too high, resulting in a relatively large particle size of calcium carbonate crystals, but the qualified products produced by other reactors under normal temperature can be mixed with it. Through subsequent processing steps (such as grinding, classification, etc.), it is still possible to obtain ultrafine calcium carbonate products that meet the quality requirements.

[0008] When the reactors are arranged in series, there are advantages of step-by-step reaction. The fly ash washing liquid and reactants (such as sodium carbonate) can undergo a step-by-step reaction process in different reactors. Each reactor can be designed to have specific reaction conditions and functions. For example, in the first reactor, the temperature can be controlled within a relatively low range to allow the preliminary reaction of calcium ions and carbonate ions to form smaller calcium carbonate crystal nuclei; in subsequent reactors, by gradually increasing the temperature or adjusting the stirring speed, etc., the crystal nuclei can slowly grow, which can more precisely control the crystallization process of calcium carbonate, facilitating the formation of ultrafine calcium carbonate with more uniform particle size and better crystallinity; and by precisely controlling the particle size growth through series-connected reactors, when the generated calcium carbonate particles are separated by centrifugation in a centrifuge, impurities and solids can be separated more efficiently. Under the action of centrifugal force, smaller and uniform particles can be better stratified, making it easier to remove impurities, thereby improving the purity of the product. During the drying and grinding processes, this calcium carbonate product with high purity and uniform particle size is also more conducive to obtaining high-quality ultrafine calcium carbonate. For example, during the pneumatic drying process, uniform particles are dried more evenly, avoiding situations such as local overheating, and during grinding, the degree of particle refinement can be better controlled, reducing over-grinding or uneven grinding.

[0009] Improve the utilization rate of reactants: Guarantee of sufficient reaction: The series-connected reaction tanks can provide a longer reaction path and residence time, allowing the calcium in the fly ash washing liquid and the added carbonate ions to have more sufficient time to react. Reactants that are not fully reacted in the first reaction tank can continue to react in subsequent reaction tanks. For example, since calcium in the fly ash washing liquid may exist in different chemical forms and have different reaction activities, some calcium components with lower activity may not have enough time to react in the first reaction tank. In subsequent reaction tanks, with the optimization of reaction conditions (such as increasing the concentration of reactants, extending the reaction time, etc.), these calcium components can participate in the reaction more fully, thereby improving the overall utilization rate of reactants and reducing production costs.

[0010] As disclosed in the invention application publication (announcement) number: CN118718945A: The present invention discloses a device and process method for preparing ultrafine calcium carbonate from fly ash washing liquid, which includes: a sedimentation tank capable of receiving fly ash washing liquid; a reaction tank connected to the sedimentation tank through a pipeline, and the fly ash washing liquid in the sedimentation tank can enter the reaction tank; a first plate and frame separator provided on the pipeline between the sedimentation tank and the reaction tank; a sodium carbonate tank capable of adding sodium carbonate into the reaction tank; the materials in the reaction tank pass through a second plate and frame separator, a washing tank, a centrifuge and a dryer in sequence through the pipeline to extract ultrafine calcium carbonate from fly ash, realizing the high-value utilization of fly ash and reducing the fly ash disposal cost.

[0011] Although the existing invention applications have many beneficial effects, they still have the following deficiencies:

[0012] During the reaction process of the existing device and process method for preparing ultrafine calcium carbonate from fly ash washing liquid, a parallel connection method is used to achieve flexible adaptability to production scale, meet different output requirements, and improve the reliability and fault tolerance of the system. However, its function is single, and it is difficult to maintain the refined control of reaction operation, guarantee of sufficient reaction, and preparation quality in the preparation process. Therefore, it is particularly important to propose a continuous production device and process for preparing ultrafine calcium carbonate from fly ash washing liquid that is convenient for batch single production, has relatively low preparation quality accuracy and specifications, and can ensure sufficient reaction and high preparation quality. In view of this, we propose a continuous production device and process for preparing ultrafine calcium carbonate from fly ash washing liquid. Summary of the Invention

[0013] The purpose of the present invention is to provide a continuous production device and process for preparing ultrafine calcium carbonate from fly ash washing liquid to solve the technical problem of insufficient functionality of the existing device for preparing ultrafine calcium carbonate from fly ash washing liquid.

[0014] To solve the above technical problems, the present invention provides the following technical solutions: A continuous production device and process for preparing ultrafine calcium carbonate from fly ash washing liquid, including a preparation frame; a secondary liquid-phase pump feeding assembly is arranged on the preparation frame; a reaction assembly is also arranged on the preparation frame; the reaction assembly includes a number of reaction tanks; a stirring assembly is arranged inside the reaction tank; a planetary mechanism is arranged on the top of the reaction tank; the output end of the secondary liquid-phase pump feeding assembly is provided with a fly ash washing liquid shunt assembly; the output end of the fly ash washing liquid shunt assembly is respectively provided with a confluence pipe assembly and a sodium carbonate shunt pipe assembly through a number of three-way valves; and, flow control valves are arranged on the shunt outputs of the fly ash washing liquid shunt assembly and the sodium carbonate shunt pipe assembly; a mixed liquid confluence pipe assembly is arranged at the bottom of the reaction tank; wherein, two adjacent reaction tanks are connected by an inclined series pipe; and, a sequential confluence pipeline is arranged on the surface of one reaction tank relatively far from the secondary liquid-phase pump feeding assembly; and, the input end of the sequential confluence pipeline is arranged in an equal-height arrangement with the input end of the series pipe; wherein, a number of the reaction tanks form a reaction tank group; a carrying frame is fixedly arranged on the reaction tank group; a driving mechanism for driving the planetary mechanism is arranged on the carrying frame; an adjusting mechanism for adjusting the power output of the planetary mechanism is arranged on the carrying frame; an auxiliary mechanism for driving the lifting adjustment of the stirring assembly is also arranged on the side of the carrying frame.

[0015] In the present invention, the stirring assembly is lifted by the stroke operation of the auxiliary mechanism; then, the multi - fly - ash washing liquid shunt assembly and the confluence pipe assembly are connected through the adjustment of the three - way valve, and the fly - ash washing liquid is transported to multiple reaction tanks by the secondary liquid - phase pump assembly. The sodium carbonate shunt pipe assembly and the confluence pipe assembly are connected through the adjustment of the three - way valve, and the required equivalent amount of sodium carbonate solution is transported to multiple reaction tanks. The locking of the adjustment mechanism is coordinated, and the planetary mechanism is driven by the driving mechanism to drive the stirring assembly to rotate and stir. Then, the inner cavity of the reaction tank and the mixed - liquid confluence pipe assembly are reflux - transported for the next treatment through the return stroke operation of the auxiliary mechanism. The parallel - type reaction processing operation is realized in this way; and the stirring assembly is lifted by the stroke operation of the auxiliary mechanism; then, one of the three - way valves relatively close to the secondary liquid - phase pump assembly is adjusted, so that the reaction tank is connected to the fly - ash washing liquid shunt assembly and the confluence pipe assembly. Then, the fly - ash washing liquid is transported to the reaction tank by the secondary liquid - phase pump assembly. Then, the flow control valve at the position of the reaction tank is opened, and the remaining reaction tanks can be appropriately opened according to the situation of the fly - ash washing liquid to add sodium carbonate; then, the driving of the adjustment mechanism and the driving mechanism drive the planetary mechanism to drive the stirring assembly to rotate and stir to form a sequentially decelerated rotation drive. After stirring, the stirring assembly is lifted to the high - end position of the series pipe by the stroke operation of the auxiliary mechanism, and the mixed liquid after the primary reaction is transported to the next reaction tank to form a continuous series - type reaction state. Then, through resetting and descending, the connecting part of the stirring assembly is opened due to the contact pressure of the mixed liquid, causing the mixed liquid to overflow above the stirring assembly. By repeating the above operations, a sequential and progressive sufficient reaction effect is formed. Through the above two different operation methods, the diversification of functions is realized, and the preparation operation of calcium carbonate under different production specification conditions is also realized.

[0016] Preferably, the secondary liquid - phase pump assembly includes a fly - ash washing liquid storage tank arranged on the preparation rack; a pump is arranged at the bottom of the fly - ash washing liquid storage tank through a pipeline; a lifting pipeline is arranged at the output end of the pump; the fly - ash washing liquid shunt assembly includes a fly - ash shunt primary pipe arranged obliquely at the output end of the lifting pipeline; several fly - ash shunt secondary pipes are arranged on the fly - ash shunt primary pipe; the confluence pipe assembly includes an adaptor connecting pipe arranged at one end of the three - way valve; and a movable connecting pipe part that is inserted and connected with the stirring assembly is arranged at the output end of the adaptor connecting pipe.

[0017] Preferably, the sodium carbonate shunt pipe assembly includes a sodium carbonate shunt secondary pipe arranged at the other end of the three-way valve; the input ends of a plurality of the sodium carbonate shunt secondary pipes are connected through a sodium carbonate shunt primary pipe; and the input end of the sodium carbonate shunt primary pipe is connected to a sodium carbonate tank; the mixed liquid confluence pipe assembly includes a mixed liquid confluence secondary pipe arranged at the bottom of the reaction tank body; the output ends of a plurality of the mixed liquid confluence secondary pipes are all connected through a mixed liquid confluence primary pipe, and a control valve for controlling the flow on-off of a plurality of the mixed liquid confluence secondary pipes is arranged on the mixed liquid confluence primary pipe; the output end of the sequential confluence pipeline is connected to the output end of the mixed liquid confluence primary pipe.

[0018] Preferably, the stirring assembly includes a hollow key shaft movably penetrating into the planetary mechanism; and a plurality of channels for liquid phase circulation are arranged on the surface of the hollow key shaft; a rotating floating disk is fixed at the bottom of the hollow key shaft; stirring blades are fixedly arranged on the top of the rotating floating disk; an overflow check ring is rotatably arranged on the outer edge side of the rotating floating disk; and the rotating floating disk is closely attached to the reaction tank body; a plurality of communication grooves are arranged inside the overflow check ring; an adjusting shaft is movably arranged inside the communication groove; and a limiting block for axially limiting the movement of the adjusting shaft is arranged in the middle of the adjusting shaft.

[0019] Preferably, the planetary mechanism includes a bearing seat arranged on the top of the reaction tank body through bolts; a central output gear shaft is rotatably arranged inside the bearing seat; and a key shaft cylinder is fixedly arranged at the bottom of the central output gear shaft through bolts; the key shaft cylinder is key-connected to the hollow key shaft; a planetary gear frame is movably sleeved on the side of the input end of the central output gear shaft; a planetary gear meshed with the central output gear shaft is hinged on the planetary gear frame; a sun gear shaft sleeve is movably sleeved outside the planetary gear frame; wherein, spiral teeth are arranged on the outer surface of the sun gear shaft sleeve.

[0020] Preferably, the driving mechanism includes a high-speed driving motor arranged on the carrying frame; a driving wheel is arranged at the output end of the high-speed driving motor; wherein, a plurality of the planetary gear frames are in transmission connection with the driving wheel through a transmission belt.

[0021] Preferably, the adjusting mechanism includes a multi-stage worm arranged on the carrying frame through a plurality of bearing shafts; and worm parts are arranged on the surface of the multi-stage worm relative to the spiral teeth; wherein, the axial diameters of a plurality of the worm parts decrease in sequence; and the number of spiral turns of a plurality of the worm parts within the same axial distance decreases in sequence; a servo driving motor is arranged at one end of the multi-stage worm.

[0022] Preferably, the auxiliary mechanism includes a cylinder arranged on the carrying frame; a synchronous seat is arranged at the pushing end of the cylinder; and the synchronous seat is rotatably connected with the hollow key shaft through a bearing.

[0023] Continuous production of ultrafine calcium carbonate from fly ash washing liquid, comprising the following steps:

[0024] S100, primary pretreatment: Determine the required specifications and quality for preparing ultrafine calcium carbonate;

[0025] S200, secondary pretreatment: The fly ash washing liquid generated from the fly ash washing and dechlorination process is subjected to pre-sedimentation, plate and frame filtration, and ceramic membrane filtration to intercept suspended solids in the fly ash washing liquid, and is filled and transported to the fly ash washing liquid storage tank;

[0026] S300, tertiary pretreatment: Prepare a sodium carbonate solution and fill it into the sodium carbonate tank;

[0027] S400, reaction adjustment treatment:

[0028] S401, reaction adjustment treatment for batch preparation: Drive the synchronous seat and the stirring assembly to be lifted as a whole through the cylinder stroke operation, and keep the top of the adjusting shaft in close contact and sealed with the communication groove; then adjust and connect multiple fly ash washing liquid shunt components with the confluence pipe assembly through a three-way valve, and then pump the treated fly ash washing liquid from the lifting pipeline into the fly ash water shunt primary pipe and transport it to several fly ash water shunt secondary pipes, and transport it to the adapter connecting pipe and the movable connecting pipeline part through the three-way valve, and cooperate with the hollow key shaft and the hole to transport it into multiple reaction tanks; then adjust the three-way valve to connect the sodium carbonate shunt pipe assembly with the confluence pipe assembly, pump the sodium carbonate solution to the sodium carbonate shunt primary pipe and the sodium carbonate shunt secondary pipe, control the pumping volume through the flow control valve, and then transport it to the adapter connecting pipe and the movable connecting pipeline part, and cooperate with the hollow key shaft and the hole to transport it into multiple reaction tanks;

[0029] S402, reaction adjustment treatment for high-quality preparation: Drive the synchronous seat and the stirring assembly to be lifted as a whole through the cylinder stroke operation, and keep the top of the adjusting shaft in close contact and sealed with the communication groove; then open one of the three-way valves close to the fly ash washing liquid storage tank; then pump the treated fly ash washing liquid from the lifting pipeline into the fly ash water shunt primary pipe and transport it to several fly ash water shunt secondary pipes, and transport it to the adapter connecting pipe and the movable connecting pipeline part through the three-way valve, and cooperate with the hollow key shaft and the hole to transport it into one of the reaction tanks; then adjust the three-way valve to connect the sodium carbonate shunt pipe assembly with the confluence pipe assembly, pump the sodium carbonate solution to the sodium carbonate shunt primary pipe and the sodium carbonate shunt secondary pipe, control the pumping volume through the flow control valve at the position of this reaction tank, and then transport it to the adapter connecting pipe and the movable connecting pipeline part, and cooperate with the hollow key shaft and the hole to transport it into this reaction tank;

[0030] S500, stirring treatment:

[0031] S501. If the stirring process for batch preparation is carried out: The adjusting mechanism remains locked, and the driving wheel and the transmission belt are driven by the high-speed driving motor to perform adaptive movement. The planetary gear carrier is synchronously driven by the transmission belt to perform a rotating action. The planetary gear is driven by the planetary gear carrier to perform revolution and rotation, so that the central output gear shaft drives the key shaft cylinder, the hollow key shaft, and the rotating floating disk to perform the stirring work;

[0032] S502. If the stirring process for high-quality preparation is carried out: The sun gear shaft sleeve is driven to rotate by the servo driving motor driving the multi-stage worm, and then the driving wheel and the transmission belt are driven by the high-speed driving motor to perform adaptive movement. The planetary gear carrier is synchronously driven by the transmission belt to perform a rotating action. The planetary gear is driven by the planetary gear carrier to perform revolution and rotation, so that multiple groups of central output gear shafts drive the key shaft cylinder, the hollow key shaft, and the rotating floating disk to perform the stirring work with sequential deceleration;

[0033] S600. Conveying work:

[0034] S601. If the conveying work for batch preparation is carried out: The whole stirring assembly is driven to descend by the cylinder return stroke, and the adjusting shaft contacts the inner wall of the reaction tank to open the adjusting shaft and the communication groove; All control valves are opened for conveying to the processing container of the plate-frame separator;

[0035] S602. If the conveying work for high-quality preparation is carried out: The whole stirring assembly is driven to rise by the cylinder stroke, so that the reacted mixed liquid flows into the lower part of the next reaction tank from the high end of the series pipe. Then the whole stirring assembly is driven to descend by the cylinder return stroke, and the reacted mixed liquid is lifted by continuously descending the adjusting shaft. The reacted mixed liquid is conveyed above the rotating floating disk, and then steps S402, S502, and S602 are repeated for continuous operation until the reacted mixed liquid is output from the sequential confluence pipeline to the processing container of the plate-frame separator;

[0036] S700. Primary separation treatment: The reacted mixed liquid is treated by the plate-frame separator to obtain a solid phase and a liquid phase;

[0037] S800. Washing treatment: The separated solid phase is dispersed and then enters the washing tank for sufficient washing to remove chloride ions in the ultrafine calcium carbonate product;

[0038] S900. Secondary separation treatment: After washing, it enters the centrifuge for separation to further improve the purity and solid content rate of the solid phase;

[0039] S1000. Crushing treatment: The separated solid phase enters the dryer, and is dried by air flow, ground and crushed to obtain ultrafine calcium carbonate.

[0040] Compared with the prior art, the beneficial effects of the present invention are:

[0041] 1. In the present invention, the stirring assembly is lifted to a certain position by the working stroke of the auxiliary mechanism; then, through the adjustment of the three-way valve, multiple fly ash washing liquid shunt assemblies are connected to the confluence pipe assembly, and the fly ash washing liquid is transported to multiple reaction tanks by means of the secondary liquid-phase pump assembly. Through the adjustment of the three-way valve, the sodium carbonate shunt pipe assembly is connected to the confluence pipe assembly, and the required equivalent amount of sodium carbonate solution is transported to multiple reaction tanks. The rotation and stirring of the stirring assembly are driven by the planetary mechanism driven by the driving mechanism in cooperation with the locking of the adjustment mechanism. Then, the inner cavity of the reaction tank and the mixed liquid confluence pipe assembly are subjected to reflux transportation for the next treatment by the return stroke work of the auxiliary mechanism. The parallel reaction processing operation is realized in this way; and the stirring assembly is lifted by the working stroke of the auxiliary mechanism; then, one of the three-way valves relatively close to the secondary liquid-phase pump assembly is adjusted, so that the reaction tank is connected to the fly ash washing liquid shunt assembly and the confluence pipe assembly. Then, the fly ash washing liquid is transported to the reaction tank by the secondary liquid-phase pump assembly. Then, the flow control valve at the position of the reaction tank is opened, and the remaining reaction tanks can be appropriately opened according to the situation of the fly ash washing liquid to add sodium carbonate; then, the rotation and stirring are formed by the driving of the adjustment mechanism and the driving mechanism driving the planetary mechanism to drive the stirring assembly to rotate in a sequentially decelerating manner. After the stirring is completed, the stirring assembly is lifted to the high-end position of the series pipe by the working stroke of the auxiliary mechanism, and the mixed liquid after the primary reaction is transported to the next reaction tank to form a continuous series reaction state. Then, through the reset and descent, the connecting part of the stirring assembly is opened under the contact pressure of the mixed liquid, causing the mixed liquid to overflow above the stirring assembly. By repeating the above operations, a sequential and progressive sufficient reaction effect is achieved. Through the above two different operation methods, the diversification of functions is realized, and the production operation of calcium carbonate with different specifications is also realized.

[0042] 2. In the present invention, the suspension height of the rotating floating disk near the bottom causes the adjustment shaft to block the communication groove of the overflow check ring due to gravity; through the cooperation of the setting of the limit block, the rising distance of the adjustment shaft is effectively controlled, and at the same time, the gap of the limit block facilitates the flow of the fly ash washing liquid.

[0043] 3. In the present invention, the hollow key shaft is key-connected to the key shaft cylinder, so that the hollow key shaft can perform lifting adjustment while maintaining the basic rotation action, meeting the requirements for the lifting adjustment and rotation drive of the rotating floating disk.

[0044] 4. In the present invention, by arranging the axial diameter of the worm part to decrease successively and the number of spiral turns within the same axial distance to decrease successively, a speed difference is generated in the transmission of the multi-stage worm to the sun gear shaft sleeve during the transmission operation. Due to this speed difference, in the state of continuous series-connected fly ash washing liquid reaction, the stirring speeds of multiple stirring components decrease successively. In this way, sufficient energy is provided during the primary relative height stirring process to rapidly and uniformly disperse the reactants, thereby promoting the formation of a large number of calcium carbonate crystal nuclei. In this case, the number of generated crystal nuclei is relatively large and the distribution is relatively uniform, laying a foundation for obtaining calcium carbonate with a small particle size subsequently; as the stirring speed decreases, the crystal nuclei grow in a relatively mild environment. During the crystal nucleus growth stage, a lower stirring speed can reduce the damage of the fluid shear force to the crystal nuclei, avoiding the fragmentation or agglomeration of newly generated crystal nuclei due to excessive stirring. At the same time, a lower stirring speed also makes the concentration distribution of the reactants around the crystal nuclei more stable, which is conducive to the growth of the crystal nuclei at a relatively slow and uniform speed, thereby helping to control the particle size of calcium carbonate and enabling it to grow into particles with a small and uniform size; by means of series connection, the utilization rate of the reactants is improved, resulting in continuous reaction between the fly ash washing liquid and the reactants; and under the locked state of the adjustment mechanism, by adapting to the parallel reaction, although the quality of the prepared ultrafine calcium carbonate is different during the processing operation, the processing efficiency is fast, simple, and high. BRIEF DESCRIPTION OF THE DRAWINGS

[0045] Figure 1 is a schematic three-dimensional structure diagram of the whole of the present invention;

[0046] Figure 2 is a schematic three-dimensional structure diagram of the whole from another perspective of the present invention;

[0047] Figure 3 is a schematic three-dimensional structure diagram of the fly ash washing liquid shunt component, sodium carbonate shunt pipe component, and mixed liquid confluence pipe component of the present invention;

[0048] Figure 4 is a schematic internal sectional structure diagram of the reaction tank of the present invention;

[0049] Figure 5 For the present invention Figure 4 is a schematic diagram of a partial enlarged structure at position A in;

[0050] Figure 6 is a schematic sectional structure diagram of the planetary mechanism of the present invention.

[0051] Explanation of the reference numerals in the drawings:

[0052] 1. Preparation rack; 2. Secondary liquid phase pump feeding assembly; 3. Reaction assembly; 4. Reaction tank body; 5. Stirring assembly; 6. Planetary mechanism; 7. Fly ash washing liquid shunt assembly; 8. Three-way valve; 9. Confluence pipe assembly; 10. Sodium carbonate shunt pipe assembly; 11. Mixed liquid confluence pipe assembly; 12. Series pipe; 13. Sequential confluence pipeline; 14. Mounting rack; 15. Driving mechanism; 16. Adjusting mechanism; 17. Auxiliary mechanism;

[0053] 201. Fly ash washing liquid storage tank; 202. Pump; 203. Lifting pipeline;

[0054] 501. Hollow key shaft; 5011. Conduit; 502. Rotating floating disc; 5021. Stirring blade; 503. Overflow check ring; 5031. Connecting groove; 5032. Adjusting shaft; 5033. Limiting block;

[0055] 601. Bearing seat; 602. Central output gear shaft; 603. Key shaft cylinder; 604. Planetary gear carrier; 605. Planetary gear; 606. Sun gear shaft sleeve; 6061. Scroll tooth;

[0056] 701. Fly ash water shunt primary pipe; 702. Fly ash water shunt secondary pipe;

[0057] 901. Adaptor connecting pipe; 9011. Movable connecting pipeline part;

[0058] 1001. Sodium carbonate shunt secondary pipe; 1002. Sodium carbonate shunt primary pipe;

[0059] 1101. Mixed liquid confluence secondary pipe; 1102. Mixed liquid confluence primary pipe; 1103. Control valve;

[0060] 1501. High-speed drive motor; 1502. Driving wheel;

[0061] 1601. Multi-stage worm; 1602. Worm part; 1603. Servo drive motor;

[0062] 1701. Cylinder; 1702. Synchronous seat. Detailed implementation manners

[0063] Example 1: As Figures 1 to 6As shown in the figure, a continuous production device for preparing ultrafine calcium carbonate from fly ash washing liquid according to the present invention includes a preparation frame 1; a secondary liquid-phase pump feeding assembly 2 is arranged on the preparation frame 1; a reaction assembly 3 is also arranged on the preparation frame 1; the reaction assembly 3 includes a number of reaction tanks 4; a stirring assembly 5 is arranged inside the reaction tank 4; a planetary mechanism 6 is arranged on the top of the reaction tank 4; the output end of the secondary liquid-phase pump feeding assembly 2 is provided with a fly ash washing liquid shunt assembly 7; the output end of the fly ash washing liquid shunt assembly 7 is respectively provided with a confluence pipe assembly 9 and a sodium carbonate shunt pipe assembly 10 through a number of three-way valves 8; and, flow control valves are arranged on the shunt outputs of the fly ash washing liquid shunt assembly 7 and the sodium carbonate shunt pipe assembly 10; a mixed liquid confluence pipe assembly 11 is arranged at the bottom of the reaction tank 4; wherein, two adjacent reaction tanks 4 are connected by an inclined series pipe 12; and, a sequential confluence pipeline 13 is arranged on the surface of one reaction tank 4 relatively far from the secondary liquid-phase pump feeding assembly 2; and, the input ends of the sequential confluence pipeline 13 and the series pipe 12 are arranged in the same height; wherein, a number of reaction tanks 4 form a reaction tank group; a carrying frame 14 is fixedly arranged on the reaction tank group; a driving mechanism 15 for driving the planetary mechanism 6 is arranged on the carrying frame 14; an adjusting mechanism 16 for adjusting the power output of the planetary mechanism 6 is arranged on the carrying frame 14; an auxiliary mechanism 17 for driving the lifting adjustment of the stirring assembly 5 is also arranged on the side of the carrying frame 14. Through the stroke work of the auxiliary mechanism 17 of the present invention, the stirring assembly 5 is lifted to the state as shown in Figure 4 ; then, through the adjustment of the three-way valve 8, a number of fly ash washing liquid shunt assemblies 7 are communicated with the confluence pipe assembly 9, and the fly ash washing liquid is conveyed into a number of reaction tanks 4 in cooperation with the secondary liquid-phase pump feeding assembly 2. Through the adjustment of the three-way valve 8, the sodium carbonate shunt pipe assembly 10 is communicated with the confluence pipe assembly 9, and the required equivalent amount of sodium carbonate solution is conveyed into a number of reaction tanks 4. With the locking of the adjusting mechanism 16 and the driving of the planetary mechanism 6 by the driving mechanism 15 to drive the stirring assembly 5 to rotate and stir, then through the return stroke work of the auxiliary mechanism 17, the inner cavity of the reaction tank 4 and the mixed liquid confluence pipe assembly 11 are refluxed for the next treatment. Through this method, a parallel reaction processing operation is realized; and through the stroke work of the auxiliary mechanism 17, the stirring assembly 5 is lifted to the state as shown in Figure 4The state shown; then adjust one of the three-way valves 8 relatively close to the position of the secondary liquid-phase pump feeding assembly 2, so that the reaction tank body 4 is communicated with the fly ash washing liquid shunt assembly 7 and the confluence pipe assembly 9. Then, the fly ash washing liquid is transported into the reaction tank body 4 through the secondary liquid-phase pump feeding assembly 2. Next, open the flow control valve at the position of the reaction tank body 4, and the remaining reaction tank bodies 4 can be appropriately opened according to the situation of the fly ash washing liquid to add sodium carbonate; then, with the drive of the adjustment mechanism 16 and the drive of the drive mechanism 15, the planetary mechanism 6 drives the stirring assembly 5 to rotate and stir to form a sequentially decelerating rotation drive. After the stirring is completed, the auxiliary mechanism 17 works in a stroke to lift the stirring assembly 5 to the high-end position of the series pipe 12, and the mixed liquid after the primary reaction is transported to the next reaction tank body 4 to form a continuous series reaction state. Then, through resetting and descending, the connecting part of the stirring assembly 5 is opened due to the contact pressure of the mixed liquid, causing the mixed liquid to overflow above the stirring assembly 5. By repeating the above operations, a sequential and progressive full reaction effect is formed. Through the above two different operation methods, the diversification of functions is realized, and the production operation of calcium carbonate with different specifications is also realized.

[0064] In an embodiment of the present invention, the secondary liquid-phase pump feeding assembly 2 includes a fly ash washing liquid storage tank 201 arranged on the preparation rack 1; a pump 202 is arranged at the bottom of the fly ash washing liquid storage tank 201 through a pipeline; a lifting pipeline 203 is arranged at the output end of the pump 202; the fly ash washing liquid shunt assembly 7 includes a fly ash water shunt primary pipe 701 arranged in an inclined shape at the output end of the lifting pipeline 203; a number of fly ash water shunt secondary pipes 702 are arranged on the fly ash water shunt primary pipe 701; the confluence pipe assembly 9 includes an adapter connecting pipe 901 arranged at one end of the three-way valve 8; an active connecting pipe part 9011 that is inserted and connected with the stirring assembly 5 is arranged at the output end of the adapter connecting pipe 901. In the present invention, the fly ash water shunt primary pipe 701 arranged in an inclined shape can effectively gather the fly ash washing liquid remaining in the pipeline at one end, facilitating the collection work by opening the valve at the end.

[0065] In an embodiment of the present invention, the sodium carbonate shunt pipe assembly 10 includes a sodium carbonate shunt secondary pipe 1001 arranged at the other end of the three-way valve 8; the input ends of a number of sodium carbonate shunt secondary pipes 1001 are connected through a sodium carbonate shunt primary pipe 1002; and, the input end of the sodium carbonate shunt primary pipe 1002 is connected to the sodium carbonate tank; the mixed liquid confluence pipe assembly 11 includes a mixed liquid confluence secondary pipe 1101 arranged at the bottom of the reaction tank body 4; the output ends of a number of mixed liquid confluence secondary pipes 1101 are all connected through a mixed liquid confluence primary pipe 1102, and, a control valve 1103 for controlling the flow on-off of a number of mixed liquid confluence secondary pipes 1101 is arranged on the mixed liquid confluence primary pipe 1102; the output end of the sequential confluence pipeline 13 is connected to the output end of the mixed liquid confluence primary pipe 1102.

[0066] In an embodiment of the present invention, the stirring assembly 5 includes a hollow key shaft 501 that movably penetrates into the planetary mechanism 6; moreover, a plurality of channels 5011 for liquid phase flow are provided on the surface of the hollow key shaft 501; a rotating floating disk 502 is fixed to the bottom of the hollow key shaft 501; a stirring blade 5021 is fixedly arranged on the top of the rotating floating disk 502; an overflow check ring 503 is rotatably arranged on the outer edge side of the rotating floating disk 502; moreover, the rotating floating disk 502 is in close fit with the reaction tank body 4; a plurality of communication grooves 5031 are arranged inside the overflow check ring 503; an adjusting shaft 5032 is movably arranged inside the communication groove 5031; a limiting block 5033 for axially limiting the movement of the adjusting shaft 5032 is arranged in the middle of the adjusting shaft 5032. In the present invention, due to the suspended height of the rotating floating disk 502 close to the bottom, the adjusting shaft 5032 blocks the communication groove 5031 of the overflow check ring 503 based on gravity; by cooperating with the setting of the limiting block 5033, the rising distance of the adjusting shaft 5032 is effectively controlled, and at the same time, the notch of the limiting block 5033 facilitates the flow of fly ash washing liquid.

[0067] In an embodiment of the present invention, the planetary mechanism 6 includes a bearing seat 601 arranged on the top of the reaction tank body 4 through bolts; a central output gear shaft 602 is rotatably arranged inside the bearing seat 601; moreover, a key shaft cylinder 603 is fixedly arranged at the bottom of the central output gear shaft 602 through bolts; the key shaft cylinder 603 is key-connected to the hollow key shaft 501; a planetary gear carrier 604 is movably sleeved on the side of the input end of the central output gear shaft 602; a planetary gear 605 meshed with the central output gear shaft 602 is hinged on the planetary gear carrier 604; a sun gear shaft sleeve 606 is movably sleeved outside the planetary gear carrier 604; wherein, a spiral tooth 6061 is arranged on the outer surface of the sun gear shaft sleeve 606. In the present invention, through the key connection setting of the key shaft cylinder 603 and the hollow key shaft 501, the hollow key shaft 501 can perform lifting adjustment while maintaining the basic rotation action, realizing the lifting adjustment and rotation drive requirements of the rotating floating disk 502.

[0068] In an embodiment of the present invention, the driving mechanism 15 includes a high-speed driving motor 1501 arranged on the carrying frame 14; a driving wheel 1502 is arranged at the output end of the high-speed driving motor 1501; wherein, a plurality of planetary gear carriers 604 are in transmission connection with the driving wheel 1502 through a transmission belt. In the present invention, the high-speed driving motor 1501 is used to drive the driving wheel 1502 and the transmission belt to perform adaptive movement, and the planetary gear carrier 604 is synchronously driven to rotate through the transmission belt, and the rotational movement forms the input of rotational power to the stirring assembly 5.

[0069] In an embodiment of the present invention, the adjusting mechanism 16 includes a multi-stage worm 1601 arranged on the carrying frame 14 through a plurality of bearing shafts; moreover, worm parts 1602 are provided on the surface of the multi-stage worm 1601 opposite to the spiral teeth 6061; wherein, the axial diameters of the plurality of worm parts 1602 decrease in sequence; moreover, the number of spiral turns of the plurality of worm parts 1602 within the same axial distance decreases in sequence; a servo drive motor 1603 is provided at one end of the multi-stage worm 1601. In the present invention, due to the fact that the axial diameters of the worm parts 1602 decrease in sequence and the number of spiral turns of the plurality of worm parts 1602 within the same axial distance decreases in sequence, a speed difference is generated in the transmission of the multi-stage worm 1601 to the sun gear shaft sleeve 606 during the transmission operation. Due to this speed difference, in the state of continuous series reaction of the fly ash washing liquid, the stirring speeds of the plurality of stirring components 5 decrease in sequence. In this way, sufficient energy is provided during the primary relative height stirring process to quickly and uniformly disperse the reactants, thereby promoting the formation of a large number of calcium carbonate crystal nuclei. In this case, the number of generated crystal nuclei is relatively large and the distribution is relatively uniform, laying a foundation for obtaining calcium carbonate with a small particle size subsequently; as the stirring speed decreases, the crystal nuclei grow in a relatively mild environment. During the crystal nucleus growth stage, a lower stirring speed can reduce the damage of the fluid shear force to the crystal nuclei, avoiding the newly generated crystal nuclei from being broken or agglomerated due to excessive stirring. At the same time, a lower stirring speed also makes the concentration distribution of the reactants around the crystal nuclei more stable, which is conducive to the growth of the crystal nuclei at a relatively slow and uniform speed, thereby helping to control the particle size of calcium carbonate and making it grow into particles with a small and uniform particle size; by means of series connection, the utilization rate of the reactants is improved, resulting in continuous reaction in the fly ash washing liquid and the reactants; and in the locked state of the adjusting mechanism 16, by adapting to the parallel reaction, although the quality of the prepared ultrafine calcium carbonate is different during the processing operation, the processing efficiency is fast, simple and efficient.

[0070] In an embodiment of the present invention, the auxiliary mechanism 17 includes a cylinder 1701 arranged on the carrying frame 14; a synchronous seat 1702 is installed at the pushing end of the cylinder 1701; the synchronous seat 1702 is rotatably connected to the hollow key shaft 501 through a bearing.

[0071] Embodiment 2: This embodiment provides a continuous production process for preparing ultrafine calcium carbonate from fly ash washing liquid, and the use steps are as follows:

[0072] S100. Primary pretreatment: Determine the required specifications and quality for preparing ultrafine calcium carbonate.

[0073] S200. Secondary pretreatment: The fly ash washing liquid generated in the fly ash washing and dechlorination process is subjected to pre-sedimentation, plate-and-frame filtration, and ceramic membrane filtration to intercept the suspended solids in the fly ash washing liquid, and is filled and transported to the fly ash washing liquid storage tank 201.

[0074] S300. Tertiary pretreatment: Prepare a sodium carbonate solution and fill it into the sodium carbonate tank.

[0075] S400, Reaction adjustment process:

[0076] S401. If it is the reaction adjustment process for batch preparation: The synchronous seat 1702 and the stirring assembly 5 are driven to be lifted as a whole by the stroke of the cylinder 1701, and the top of the adjusting shaft 5032 is kept in close contact and sealed with the communication groove 5031. Then, the multiple fly ash washing liquid shunt components 7 and the confluence pipe assembly 9 are communicated by adjusting the three-way valve 8. Next, the treated fly ash washing liquid is transported through the lifting pipeline 203 to the fly ash water shunt primary pipe 701 by the pump 202 and then transported to several fly ash water shunt secondary pipes 702, and then transported to the adapter connecting pipe 901 and the movable connecting pipe part 9011 through the three-way valve 8, and is transported to the multiple reaction tanks 4 through the hollow key shaft 501 and the hole 5011. Then, the sodium carbonate shunt pipe assembly 10 and the confluence pipe assembly 9 are communicated by adjusting the three-way valve 8, and the sodium carbonate solution is pumped to the sodium carbonate shunt primary pipe 1002 and the sodium carbonate shunt secondary pipe 1001, and the pumping amount is controlled by the flow control valve. Then, it is transported to the adapter connecting pipe 901 and the movable connecting pipe part 9011, and is transported to the multiple reaction tanks 4 through the hollow key shaft 501 and the hole 5011.

[0077] S402. If it is the reaction adjustment process for high-quality preparation: The synchronous seat 1702 and the stirring assembly 5 are driven to be lifted as a whole by the stroke of the cylinder 1701, and the top of the adjusting shaft 5032 is kept in close contact and sealed with the communication groove 5031. Then, one of the three-way valves 8 close to the fly ash washing liquid storage tank 201 is opened. Next, the treated fly ash washing liquid is transported through the lifting pipeline 203 to the fly ash water shunt primary pipe 701 by the pump 202 and then transported to several fly ash water shunt secondary pipes 702, and then transported to the adapter connecting pipe 901 and the movable connecting pipe part 9011 through the three-way valve 8, and is transported to one of the reaction tanks 4 through the hollow key shaft 501 and the hole 5011. Then, the sodium carbonate shunt pipe assembly 10 and the confluence pipe assembly 9 are communicated by adjusting the three-way valve 8, and the sodium carbonate solution is pumped to the sodium carbonate shunt primary pipe 1002 and the sodium carbonate shunt secondary pipe 1001, and the pumping amount is controlled by the flow control valve at the position of the reaction tank 4. Then, it is transported to the adapter connecting pipe 901 and the movable connecting pipe part 9011, and is transported to the reaction tank 4 through the hollow key shaft 501 and the hole 5011.

[0078] S500, Stirring process:

[0079] S501. If performing the stirring process for batch preparation: The adjustment mechanism 16 remains locked. The high-speed drive motor 1501 is used to drive the drive wheel 1502 and the transmission belt for adaptive movement. The transmission belt synchronously drives the planet gear carrier 604 to rotate. The planet gear carrier 604 drives the planet gears 605 to revolve and rotate, causing the central output gear shaft 602 to drive the key shaft cylinder 603, the hollow key shaft 501, and the rotating floating disk 502 to perform the stirring work.

[0080] S502. If performing the stirring process for high-quality preparation: The servo drive motor 1603 is used to drive the multi-stage worm 1601 to drive the sun gear shaft sleeve 606 to rotate. Then, the high-speed drive motor 1501 is used to drive the drive wheel 1502 and the transmission belt for adaptive movement. The transmission belt synchronously drives the planet gear carrier 604 to rotate. The planet gear carrier 604 drives the planet gears 605 to revolve and rotate, causing multiple groups of central output gear shafts 602 to drive the key shaft cylinder 603, the hollow key shaft 501, and the rotating floating disk 502 to perform the stirring work with sequential deceleration.

[0081] S600. Conveying work:

[0082] S601. If performing the conveying work for batch preparation: The cylinder 1701 drives the return stroke to cause the entire stirring assembly 5 to descend. The adjustment shaft 5032 contacts the inner wall of the reaction tank 4, causing the adjustment shaft 5032 and the communication groove 5031 to open. All control valves 1103 are opened for conveying to the processing container of the plate-frame separator.

[0083] S602. If performing the conveying work for high-quality preparation: The cylinder 1701 drives the stroke to cause the entire stirring assembly 5 to rise, causing the reaction mixture to flow into the lower part of the next reaction tank 4 from the high end of the series pipe 12. Then, the cylinder 1701 drives the return stroke to cause the entire stirring assembly 5 to descend. The reaction mixture is lifted by continuously lowering the adjustment shaft 5032, and the reaction mixture is conveyed above the rotating floating disk 502. Then, steps S402, S502, and S602 are repeated for continuous operation until the reaction mixture is output from the sequential confluence pipeline 13 to the processing container of the plate-frame separator.

[0084] S700. Primary separation treatment: The reaction mixture is processed by a plate-frame separator to obtain a solid phase and a liquid phase.

[0085] S800. Washing treatment: The separated solid phase is broken up and enters the washing tank for thorough washing to remove chloride ions from the ultrafine calcium carbonate product.

[0086] S900. Secondary separation treatment: After washing, it enters a centrifuge for separation to further improve the purity and solid content rate of the solid phase.

[0087] S1000, Crushing treatment: The solid phase obtained after separation enters a dryer, where it is dried by air flow and ground and crushed to obtain ultrafine calcium carbonate.

[0088] The embodiments disclosed in the present invention are preferred embodiments, but are not limited thereto. Those of ordinary skill in the art can easily understand the spirit of the present invention based on the above embodiments and make different extensions and changes. However, as long as they do not depart from the spirit of the present invention, they are within the protection scope of the present invention.

Claims

1. A continuous production equipment for preparing ultrafine calcium carbonate from fly ash water washing liquid, characterized in that: It comprises a preparation rack (1); a secondary liquid phase pump assembly (2) is arranged on the preparation rack (1); and a reaction assembly (3) is also arranged on the preparation rack (1); The reaction assembly (3) comprises a plurality of reaction tank bodies (4); a stirring assembly (5) is provided inside the reaction tank body (4); a planetary mechanism (6) is provided on the top of the reaction tank body (4); a fly ash water washing liquid diversion assembly (7) is provided at the output end of the secondary liquid phase pump assembly (2); a manifold assembly (9) and a sodium carbonate diversion pipe assembly (10) are provided at the output end of the fly ash water washing liquid diversion assembly (7) through a plurality of three-way valves (8); and flow control valves are provided on the diversion outputs of the fly ash water washing liquid diversion assembly (7) and the sodium carbonate diversion pipe assembly (10); A mixed liquid manifold assembly (11) is provided at the bottom of the reaction tank body (4); Wherein, two adjacent reaction tanks (4) are connected via an inclined series pipe (12); Furthermore, a sequential confluence pipe (13) is provided on the surface of one of the reaction tank bodies (4) which is relatively far from the secondary liquid phase pump supply component (2); and the input end of the sequential confluence pipe (13) is arranged at the same height as the input end of the series pipe (12); A plurality of the reaction tank bodies (4) constitute a reaction tank group; a carrying frame (14) is fixedly arranged on the reaction tank group; a driving mechanism (15) for driving the planetary mechanism (6) is arranged on the carrying frame (14); an adjusting mechanism (16) for adjusting the power output of the planetary mechanism (6) is arranged on the carrying frame (14); an auxiliary mechanism (17) for driving the stirring assembly (5) to rise and fall is also arranged on the side of the carrying frame (14); The secondary liquid phase pumping assembly (2) comprises a fly ash water washing liquid storage tank (201) arranged on the preparation rack (1); a pump (202) is arranged at the bottom of the fly ash water washing liquid storage tank (201) via a pipeline; and a lifting pipeline (203) is arranged at the output end of the pump (202); The fly ash water washing liquid flow dividing assembly (7) comprises a fly ash water primary distribution pipe (701) arranged in an inclined manner at the output end of the lifting pipeline (203); a plurality of fly ash water secondary distribution pipes (702) are arranged on the fly ash water primary distribution pipe (701); The manifold assembly (9) comprises an adaptor connecting pipe (901) arranged at one end of the three-way valve (8); the output end of the adaptor connecting pipe (901) is provided with a movable connecting pipe portion (9011) which is interlaced and connected with the stirring assembly (5); The sodium carbonate shunt pipe assembly (10) comprises a sodium carbonate shunt secondary pipe (1001) arranged at the other end of the three-way valve (8); the input ends of a plurality of the sodium carbonate shunt secondary pipes (1001) are connected via a sodium carbonate shunt primary pipe (1002); and the input end of the sodium carbonate shunt primary pipe (1002) is connected to a sodium carbonate tank; The mixed liquid confluence pipe assembly (11) comprises a mixed liquid confluence secondary pipe (1101) arranged at the bottom of the reaction tank body (4); the output ends of a plurality of the mixed liquid confluence secondary pipes (1101) are connected via a mixed liquid confluence primary pipe (1102), and a control valve (1103) for controlling the flow on and off of the plurality of the mixed liquid confluence secondary pipes (1101) is provided on the mixed liquid confluence primary pipe (1102); The output end of the sequential confluence pipeline (13) is connected to the output end of the mixed liquid confluence primary pipe (1102).

2. The continuous production equipment for preparing ultrafine calcium carbonate from fly ash water washing liquid according to claim 1 is characterized in that: The stirring assembly (5) comprises a hollow key shaft (501) that movably penetrates into the planetary mechanism (6); Furthermore, a plurality of channels (5011) for liquid flow are provided on the surface of the hollow key shaft (501); A rotating floating plate (502) is fixed at the bottom of the hollow key shaft (501); a stirring blade (5021) is fixedly arranged at the top of the rotating floating plate (502); The rotating floating plate (502) is provided with an overflow one-way ring (503) for rotation on the outer side thereof; and the rotating floating plate (502) is tightly fitted to the reaction tank body (4); A plurality of connecting grooves (5031) are arranged inside the overflow one-way ring (503); an adjusting shaft (5032) is movably arranged inside the connecting groove (5031); and a limiting block (5033) for limiting the axial movement of the adjusting shaft (5032) is arranged at the middle end of the adjusting shaft (5032).

3. The continuous production equipment for preparing ultrafine calcium carbonate from fly ash water washing liquid according to claim 2 is characterized in that: The planetary mechanism (6) comprises a bearing seat (601) arranged on the top of the reaction tank body (4) by bolts; a central output gear shaft (602) is rotatably arranged inside the bearing seat (601); and a key shaft cylinder (603) is fixedly arranged at the bottom of the central output gear shaft (602) by bolts; the key shaft cylinder (603) is key-connected to the hollow key shaft (501); A planetary gear carrier (604) is provided on the movable sleeve on the side of the input end of the central output gear shaft (602); a planetary gear (605) meshingly connected to the central output gear shaft (602) is hingedly provided on the planetary gear carrier (604); The outer movable sleeve of the planetary wheel carrier (604) is provided with a sun gear shaft sleeve (606); Wherein, a volute (6061) is provided on the outer surface of the sun gear sleeve (606).

4. The continuous production equipment for preparing ultrafine calcium carbonate from fly ash water washing liquid according to claim 3 is characterized in that: The driving mechanism (15) comprises a high-speed driving motor (1501) arranged on the mounting frame (14); a driving wheel (1502) is provided at the output end of the high-speed driving motor (1501); wherein a plurality of the planetary wheel carriers (604) are drivingly connected to the driving wheel (1502) via a transmission belt.

5. The continuous production equipment for preparing ultrafine calcium carbonate from fly ash water washing liquid according to claim 4 is characterized in that: The adjustment mechanism (16) comprises a multi-stage worm (1601) arranged on the mounting frame (14) via a plurality of bearing shafts; and a worm portion (1602) is provided on the surface of the multi-stage worm (1601) at a position opposite to the volute (6061); Wherein, the axial diameters of the plurality of worm parts (1602) decrease in sequence; Furthermore, the number of spiral turns of the worm parts (1602) decreases in sequence within the same axial distance; A servo drive motor (1603) is provided at one end of the multi-stage worm (1601).

6. The continuous production equipment for preparing ultrafine calcium carbonate from fly ash water washing liquid according to claim 5, characterized in that: The auxiliary mechanism (17) comprises a cylinder (1701) arranged on the mounting frame (14); a synchronous seat (1702) is installed on the pushing end of the cylinder (1701); and the synchronous seat (1702) is rotatably connected to the hollow key shaft (501) via a bearing.

7. A continuous production process for preparing ultrafine calcium carbonate from fly ash water washing liquid, which is applicable to the continuous production equipment for preparing ultrafine calcium carbonate from fly ash water washing liquid as claimed in claim 6, characterized in that: The following steps are involved: S100, primary pretreatment: determine the specifications and quality required for preparing ultrafine calcium carbonate; S200, secondary pretreatment: the fly ash washing liquid generated in the fly ash washing and dechlorination process is subjected to pre-sedimentation, plate and frame filtration, and ceramic membrane filtration to intercept suspended solids in the fly ash washing liquid, and is then filled and transported to a fly ash washing liquid storage tank (201); S300, tertiary pretreatment: preparing sodium carbonate solution and filling it into a sodium carbonate tank; S400, reaction adjustment processing: S401, if batch preparation reaction adjustment treatment is performed: the cylinder (1701) is driven to stroke and drive the synchronous seat (1702) and the stirring assembly (5) to be lifted as a whole, and the top of the adjustment shaft (5032) is kept in close contact and sealed with the connecting groove (5031); then the three-way valve (8) is adjusted to connect the multiple fly ash water washing liquid diversion assemblies (7) with the manifold assembly (9); then the pump (202) is used to transport the treated fly ash water washing liquid through the lifting pipeline (203) to the fly ash water diversion primary pipe (701) and to the multiple fly ash water diversion secondary pipes (702), and then transport it to the adapter connection through the three-way valve (8). The sodium carbonate solution is pumped to the sodium carbonate primary shunt pipe (1002) and the sodium carbonate secondary shunt pipe (1001) by adjusting the three-way valve (8) and the movably connected pipe part (9011), and the hollow key shaft (501) and the hole (5011) to be transported to the multiple reaction tank bodies (4); the sodium carbonate solution is pumped to the sodium carbonate primary shunt pipe (1002) and the sodium carbonate secondary shunt pipe (1001), and the pumping amount is controlled by the flow control valve; and the sodium carbonate solution is then transported to the sodium carbonate primary shunt pipe (1002) and the sodium carbonate secondary shunt pipe (1001) by adjusting the three-way valve (8) and the movably connected pipe part (9011), and the hollow key shaft (501) and the hole (5011) to be transported to the multiple reaction tank bodies (4); S402, if high-quality preparation is to be carried out, the reaction adjustment treatment is carried out: the synchronous seat (1702) and the stirring assembly (5) are driven to be lifted as a whole through the stroke operation of the cylinder (1701), and the top of the adjustment shaft (5032) is kept in close contact and sealed with the connecting groove (5031); then one of the three-way valves (8) close to the fly ash water washing liquid storage tank (201) is opened; then the treated fly ash water washing liquid is transported to the fly ash water distribution primary pipe (701) and to several fly ash water distribution secondary pipes (702) through the pump (202), and then transported to the adapter connecting pipe (901) and the movable pipe (901) through the three-way valve (8). The connecting pipe part (9011) cooperates with the hollow key shaft (501) and the hole (5011) to be transported to one of the reaction tank bodies (4); then the sodium carbonate diversion pipe assembly (10) is connected to the manifold assembly (9) by adjusting the three-way valve (8), and the sodium carbonate solution is pumped to the sodium carbonate diversion primary pipe (1002) and the sodium carbonate diversion secondary pipe (1001), and the pumping amount is controlled by the flow control valve at the position of the reaction tank body (4), and then the adaptor connecting pipe (901) and the movable connecting pipe part (9011) cooperate with the hollow key shaft (501) and the hole (5011) to be transported to the reaction tank body (4); S500, stirring treatment: S501, if a mixing process is performed for batch preparation: the adjustment mechanism (16) is locked, and the high-speed drive motor (1501) is used to drive the drive wheel (1502) and the transmission belt to perform adaptive movement, and the transmission belt is used to synchronously drive the planetary wheel carrier (604) to rotate, and the planetary wheel carrier (604) is used to drive the planetary gear (605) to revolve and rotate, so that the central output gear shaft (602) drives the key shaft cylinder (603), the hollow key shaft (501), and the rotating floating plate (502) to perform mixing; S502, if a high-quality preparation stirring process is to be performed: the servo drive motor (1603) drives the multi-stage worm (1601) to drive the sun gear sleeve (606) to rotate, and then the high-speed drive motor (1501) drives the drive wheel (1502) and the transmission belt to perform adaptive movement, and the transmission belt synchronously drives the planetary wheel carrier (604) to rotate, and the planetary wheel carrier (604) drives the planetary gear (605) to revolve and rotate, so that the multiple sets of central output gear shafts (602) drive the key shaft cylinder (603), the hollow key shaft (501), and the rotating floating plate (502) to perform a stirring process of decelerating in sequence; S600, conveying work: S601, if the transportation work of batch preparation is carried out: the cylinder (1701) is driven back to cause the stirring assembly (5) to descend as a whole, the adjustment shaft (5032) contacts the inner wall of the reaction tank body (4) so ​​that the adjustment shaft (5032) and the connecting groove (5031) are opened; all control valves (1103) are opened to transport to the processing container of the plate and frame separator; S602, if high-quality preparation and transportation work is to be carried out: the cylinder (1701) is driven by the stroke to cause the stirring assembly (5) to rise as a whole, so that the reaction mixture flows from the high end of the series pipe (12) to the bottom of the next reaction tank (4), and then the cylinder (1701) is driven by the return stroke to cause the stirring assembly (5) to descend as a whole, and the adjustment shaft (5032) and the reaction mixture are lifted by the continuous descending adjustment shaft (5032), and the reaction mixture is transported to the top of the rotating floating plate (502), and then the steps S402, S502, and S602 are repeated to work continuously until the reaction mixture is output from the sequential confluence pipe (13) to the processing container of the plate and frame separator; S700, primary separation treatment: treating the reaction mixture through a plate and frame separator to obtain a solid phase and a liquid phase; S800, washing treatment: the separated solid phase is broken up and enters the washing tank for thorough washing to remove chloride ions in the ultrafine calcium carbonate product; S900, secondary separation treatment: after washing, it enters the centrifuge for separation to further improve the purity and solid content of the solid phase; S1000, crushing treatment: the solid phase obtained after separation enters the dryer, is airflow dried, and is ground and crushed to obtain ultrafine calcium carbonate.

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