Evaporative crystallization process convenient for producing large manganese sulfate particles

Abstract

The invention discloses an evaporative crystallization process convenient for producing large manganese sulfate particles, which specifically comprises the following steps: conveying an unsaturated manganese sulfate solution into a mother liquor tank through a stock solution pump, reducing the temperature of the mother liquor and increasing the solubility, and dissolving fine grains in the mother liquor tank through the unsaturated manganese sulfate solution; the manganese sulfate solution without fine grains is conveyed to a preheater to be preheated by distilled water, and is conveyed to a tube pass of a forced circulation heat exchanger through a forced circulation pump to exchange heat with secondary steam of a shell pass to be heated and pressurized; the heated and pressurized manganese sulfate solution enters a crystallizer to be subjected to flash evaporation, and materials obtained after flash evaporation are subjected to crystallization flotation in a crystallization chamber; conveying the crystallized material into a thickener through a discharge pump to thicken the crystallized material, feeding the thickened crystallized material into a centrifugal machine to carry out solid-liquid separation, overflowing clear liquid back to a mother liquid tank, and storing the separated crystallized salt for later use; good manganese sulfate crystal morphology and size distribution are obtained by controlling the saturation degree of the system, the content of fine grains in the crystallizer and the design of the crystallizer.

Description

Technical Field

[0001] The invention relates to the technical field of manganese sulfate production, in particular to an evaporation crystallization process for producing large manganese sulfate particles. Background Art

[0002] Manganese sulfate is easily soluble in water but insoluble in ethanol. It exists in the form of various hydrates. Manganese sulfate is a trace element required by crops that synthesize fatty acids. It can be applied to the soil as a fertilizer to increase production. Manganese sulfate can be added to animal feed to have a fattening effect. Manganese sulfate is also a raw material and analytical reagent for the preparation of other manganese salts. Manganese sulfate is also used in industrial production such as electrolytic manganese, dyes, papermaking, and ceramics.

[0003] The traditional manganese sulfate multiple-effect evaporator adopts a multiple-effect evaporation crystallization process to separate the manganese sulfate solution and recover it through a salt collector, but there are problems such as small crystal particle size and poor quality. Based on this, the present invention proposes an evaporation crystallization process that can solve the above problems and is convenient for producing large manganese sulfate particles. Summary of the invention

[0004] The object of the present invention is to provide an evaporation crystallization process for producing large manganese sulfate particles, so as to solve the problems raised in the above background technology.

[0005] To achieve the above object, the present invention provides the following technical solution: an evaporation crystallization process for producing large manganese sulfate particles, specifically comprising the following steps:

[0006] S1. The unsaturated manganese sulfate solution is transported to the mother liquid tank through the stock liquid pump to reduce the temperature of the mother liquid and increase the solubility, and the fine crystals in the mother liquid tank are dissolved by the unsaturated manganese sulfate solution;

[0007] S2, the manganese sulfate solution with fine crystals eliminated is transported to a preheater to be preheated with distilled water, and then transported to the secondary steam heat exchange between the tube side and the shell side of the forced circulation heat exchanger through a forced circulation pump to increase the temperature and pressure;

[0008] S3, the manganese sulfate solution with increased temperature and pressure enters the crystallizer for flash evaporation, and the material after flash evaporation is crystallized and floated in the crystallization chamber;

[0009] S4. The crystallized material is thickened in a thickener through a discharge pump conveyor. The thickened crystallized material enters a centrifuge for solid-liquid separation. The clear liquid overflows back to the mother liquid tank, and the separated crystallized salt is stored for standby use.

[0010] As a preferred technical solution, in step s3, the fine crystals and impurities floating on the top of the crystallization chamber of the crystallizer are pumped to the sedimentation tank through the impurity discharge pump, the settled fine crystals are discharged back to the mother liquid tank from the bottom, and the impurities overflow from the top of the sedimentation tank and are discharged.

[0011] As a preferred technical solution, in step s3, the steam discharged from the crystallizer passes through a secondary separator for defoaming, enters a compressor for temperature and pressure increase, and after being compressed, enters a forced circulation heat exchanger for heat exchange with the manganese sulfate solution. The steam after heat exchange is condensed into water and flows to a distilled water tank, and is sent to a preheater by a distilled water pump to preheat the manganese sulfate solution before being discharged.

[0012] As a preferred technical solution, in s4, when the solid content of the material in the crystallization chamber reaches 10% to 20%, it is transported to the thickener, thickened to a solid content of 30% to 40% in the thickener, and then enters the centrifuge.

[0013] As a preferred technical solution, the crystallizer is of Oslo type.

[0014] As a preferred technical solution, the centrifuge comprises:

[0015] The casing has a cover body buckled on the top, the cover body is provided with an inlet pipe, and the bottom of the casing is provided with an outlet pipe;

[0016] A disc body is located in the housing, and a plurality of groups of centrifugal filter cartridges are circumferentially arranged on the disc body;

[0017] An adjusting component, a first motor body mounted on the bottom of the housing, an output end of the first motor body being connected to a telescopic rod, the telescopic rod extending into the housing and connected to the disc body;

[0018] The power assembly is used to drive a group of centrifugal filter cartridges to rotate the centrifugal crystallization material.

[0019] As a preferred technical solution, a pad is provided in each group of the centrifugal filter cartridges, and a lifting rod extending upward is provided on the pad.

[0020] As a preferred technical solution, the power assembly includes a second motor body installed in the casing and a liner column arranged on each group of the centrifugal filter cartridges, each group of the liner columns is rotatably penetrated on the disk body, and each group of the liner columns is connected to a slave gear, and the output end of the second motor body is connected to a main gear, and the main gear can mesh with a group of the slave gears.

[0021] As a preferred technical solution, the adjustment assembly also includes an electric cylinder body installed in the casing, the movable rod of the electric cylinder body is connected to a support rod, the support rod is provided with a ring sleeve and a top plate from top to bottom, the top plate is located on the lower side of the disk body, and the ring sleeve is mounted on the inlet pipe.

[0022] As a preferred technical solution, the movable rod of the electric cylinder body is extended, and the support rod drives the ring sleeve and the top plate to move up, driving the top plate to push the disc body to move upward, and the first motor body drives the disc body to rotate so that a group of centrifugal filter cartridges are vertically aligned with the feed pipe; the movable rod of the electric cylinder body is retracted and reset, and the support rod drives the ring sleeve and the top plate to move downward, driving the ring sleeve to cover the centrifugal filter cartridge vertically aligned with the feed pipe.

[0023] Compared with the prior art, the present invention has the following beneficial effects:

[0024] The unsettled fine crystals in the thickener, the fine crystals leaking from the centrifuge screen, and the fine crystals collected in the sedimentation tank are collected in the mother liquid tank. When the system is fed, the unsaturated raw material first enters the raw material tank, dissolves the fine crystals in the mother liquid tank, and then enters the evaporation crystallization system after preheating. By controlling the system saturation, the fine crystal content in the crystallizer, and the crystallizer design, the manganese sulfate solution undergoes controllable secondary nucleation in the crystallizer, thereby obtaining a good manganese sulfate crystal morphology and size distribution;

[0025] The first motor body drives the disc body to rotate, so that different centrifugal filter cartridges are vertically aligned with the feed pipe. In the process of producing large manganese sulfate particles, separated crystal salt can be stored in different centrifugal filter cartridges. The ring sleeve is downwardly covered on the centrifugal filter cartridge. During the centrifugation process, the ring sleeve blocks the clear liquid from splashing onto other centrifugal filter cartridges, that is, it is effectively prevented that the separated crystal salt stored in other centrifugal filter cartridges re-adheres to the supernatant, thereby ensuring the quality of the crystal salt. BRIEF DESCRIPTION OF THE DRAWINGS

[0026] Figure 1 It is a schematic diagram of the overall structure of the present invention;

[0027] Figure 2 This is a schematic diagram of the external structure of the centrifuge of the present invention;

[0028] Figure 3 It is a schematic diagram of the internal structure of the casing of the centrifuge of the present invention;

[0029] Figure 4 It is a schematic diagram of the power assembly structure of the centrifuge of the present invention;

[0030] Figure 5 It is a schematic diagram of the positional relationship between the annular sleeve and the top plate of the centrifuge and the centrifugal filter cartridge of the present invention;

[0031] In the figure: 1, raw liquid tank; 2, raw liquid pump; 3, mother liquid tank; 4, mother liquid pump; 5, preheater; 6, forced circulation pump; 7, forced circulation heat exchanger; 8, crystallizer; 9, discharge pump; 10, thickener; 11, centrifuge; 111, casing; 1111, outlet pipe; 112, cover; 1121, inlet pipe; 113, adjustment component; 1131, first motor body; 1132, telescopic rod; 1133, electric cylinder body; 1134, support rod ; 1135, ring sleeve; 1136, top plate; 1137, ball body; 114, disc body; 1141, centrifugal filter cartridge; 1142, pad; 1143, lifting rod; 115, power assembly; 1151, second motor body; 1152, liner column; 1153, slave gear; 1154, main gear; 12, impurity discharge pump; 13, sedimentation tank; 14, secondary separator; 15, compressor; 16, distilled water tank; 17, distilled water pump. DETAILED DESCRIPTION

[0032] The following will be combined with the drawings in the embodiments of the present invention to clearly and completely describe the technical solutions in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0033] See also Figure 1-5 The present invention provides an evaporation crystallization process for producing large manganese sulfate particles, aiming to solve the problem of small crystal particle size and poor quality in traditional manganese sulfate evaporation crystallization;

[0034] The material crystallization process is divided into primary nucleation (homogeneous nucleation) and secondary nucleation (heterogeneous nucleation). Primary nucleation is driven by a higher supersaturation, and nucleation occurs rapidly at a certain moment, and the whole process is uncontrollable; secondary nucleation is the crystallization produced by destroying the homogeneous state of the liquid through dust and impurity particles in the material, shear stress of liquid flow, collision between liquid-liquid and liquid-equipment, etc. The advantage of secondary nucleation is mainly reflected in its ability to effectively control the crystallization process. By maintaining a stable supersaturation and other measures, effective control of secondary nucleation can be achieved, thereby obtaining the desired crystal morphology and size distribution.

[0035] In order to control the shape and size distribution of crystals during the production process, the control system needs to have a lower supersaturation to make the evaporation and crystallization process stable and gentle. In the continuous evaporation and crystallization process, the temperature rise (saturation) of the heat exchanger can be controlled by adjusting the forced circulation flow rate. Based on long-term design and operation experience, it is preferred that the temperature rise of manganese sulfate crystallization be controlled between 0.5 and 0.7°C. When the flow rate of the circulating pump is too large and it is difficult to select a type, multiple circulating pumps and heat exchangers can be connected in parallel to achieve the designed flow rate.

[0036] The surface of fine crystals is smooth, and it is difficult for supersaturated materials in the crystallizer to adhere to the surface of fine crystals and continue to grow into larger crystals. On the contrary, during the growth process, the fine crystals attached to the surface are easy to fall off, resulting in the production of more fine crystals, thus affecting the quality of the product salt. Therefore, the effective elimination of fine crystals in the evaporation crystallization process plays an important role in product quality control.

[0037] Embodiment 1

[0038] S1, transporting the unsaturated manganese sulfate solution to the mother liquid tank 3 through the stock solution pump 2, lowering the mother liquid temperature and increasing the solubility, and dissolving the fine crystals in the mother liquid tank 3 through the unsaturated manganese sulfate solution;

[0039] The manganese sulfate solution to be treated is stored in the stock liquid tank 1 and is sent to the mother liquid tank 3 through the stock liquid pump 2 to reduce the temperature of the mother liquid and increase the solubility. The unsaturated manganese sulfate solution dissolves the fine crystals in the mother liquid tank 3, thereby achieving the purpose of eliminating the fine crystals.

[0040] S2, the manganese sulfate solution with fine crystals eliminated is transported to the preheater 5 to be preheated with distilled water, and then transported to the forced circulation heat exchanger 7 through the forced circulation pump 6 for secondary steam heat exchange between the tube side and the shell side to increase the temperature and pressure;

[0041] After the fine crystals are eliminated, the liquid is sent to the preheater 5 through the mother liquor pump 4, and then preheated with distilled water and enters the evaporation crystallization system.

[0042] S3, the manganese sulfate solution with increased temperature and pressure enters the Oslo crystallizer 8 for flash evaporation, and the material after flash evaporation is crystallized and floated in the crystallization chamber;

[0043] The middle of the crystallization chamber of the Oslo crystallizer 8 is connected to the forced circulation pump 6, which circulates and pumps the clear liquid into the circulating heat exchanger to increase the temperature and pressure, and the circulation causes the material to evaporate and crystallize.

[0044] The fine crystals and impurities floating on the top of the crystallization chamber of the Oslo crystallizer 8 are sent to the sedimentation tank 13 through the impurity discharge pump 12. The settled fine crystals are discharged back to the mother liquid tank 3 from the bottom, and the impurities overflow from the top of the sedimentation tank 13 and are discharged externally;

[0045] The steam discharged from the Oslo crystallizer 8 passes through the secondary separator 14 for defoaming, enters the compressor 15 for temperature and pressure increase, and then enters the forced circulation heat exchanger 7 for heat exchange with the manganese sulfate solution after being compressed. The steam after heat exchange is condensed into water and flows to the distilled water tank 16, and is sent to the preheater 5 by the distilled water pump 17 to preheat the manganese sulfate solution before being discharged;

[0046] S4. When the solid content of the material in the crystallization chamber reaches 10%, it is transported to the thickener 10 for thickening through the discharge pump 9. After thickening to a solid content of 30% in the thickener 10, it enters the centrifuge 11 for solid-liquid separation. The clear liquid overflows back to the mother liquid tank 3, and the separated crystallized salt is stored for standby use.

[0047] Embodiment 2

[0048] S1, transporting the unsaturated manganese sulfate solution to the mother liquid tank 3 through the stock solution pump 2, lowering the mother liquid temperature and increasing the solubility, and dissolving the fine crystals in the mother liquid tank 3 through the unsaturated manganese sulfate solution;

[0049] The manganese sulfate solution to be treated is stored in the stock liquid tank 1 and is sent to the mother liquid tank 3 through the stock liquid pump 2 to reduce the temperature of the mother liquid and increase the solubility. The unsaturated manganese sulfate solution dissolves the fine crystals in the mother liquid tank 3, thereby achieving the purpose of eliminating the fine crystals.

[0050] S2, the manganese sulfate solution with fine crystals eliminated is transported to the preheater 5 to be preheated with distilled water, and then transported to the forced circulation heat exchanger 7 through the forced circulation pump 6 for secondary steam heat exchange between the tube side and the shell side to increase the temperature and pressure;

[0051] After the fine crystals are eliminated, the liquid is sent to the preheater 5 through the mother liquor pump 4, and then preheated with distilled water and enters the evaporation crystallization system.

[0052] S3, the manganese sulfate solution with increased temperature and pressure enters the Oslo crystallizer 8 for flash evaporation, and the material after flash evaporation is crystallized and floated in the crystallization chamber;

[0053] The middle of the crystallization chamber of the Oslo crystallizer 8 is connected to the forced circulation pump 6, which circulates and pumps the clear liquid into the circulating heat exchanger, and circulates to evaporate and crystallize the material.

[0054] The fine crystals and impurities floating on the top of the crystallization chamber of the Oslo crystallizer 8 are sent to the sedimentation tank 13 through the impurity discharge pump 12. The settled fine crystals are discharged back to the mother liquid tank 3 from the bottom, and the impurities overflow from the top of the sedimentation tank 13 and are discharged externally;

[0055] The steam discharged from the Oslo crystallizer 8 passes through the secondary separator 14 for defoaming, enters the compressor 15 for temperature and pressure increase, and then enters the forced circulation heat exchanger 7 for heat exchange with the manganese sulfate solution after being compressed. The steam after heat exchange is condensed into water and flows to the distilled water tank 16, and is sent to the preheater 5 by the distilled water pump 17 to preheat the manganese sulfate solution before being discharged;

[0056] S4. When the solid content of the material in the crystallization chamber reaches 20%, it is transported to the thickener 10 through the discharge pump 9 for thickening. After thickening to a solid content of 40% in the thickener 10, it enters the centrifuge 11 for solid-liquid separation. The clear liquid overflows back to the mother liquid tank 3, and the separated crystallized salt is stored for standby use.

[0057] The Oslo crystallizer 8 in Example 1 and Example 2 is a supersaturation generation area and a crystal growth area respectively arranged at two places of the crystallizer 8. The crystals are fluidized and suspended in the circulating liquid, providing a good environment for crystal growth. Through the above process, the fine crystals that have not settled in the thickener 10, the fine crystals leaking from the screen of the centrifuge 11, and the fine crystals collected by the sedimentation tank 13 are collected in the mother liquid tank 3. When the system is fed, the unsaturated raw material first enters the raw material tank, dissolves the fine crystals in the mother liquid tank 3, and then enters the evaporation crystallization system after preheating, so that the manganese sulfate solution undergoes controllable secondary nucleation in the crystallizer 8 by controlling the system saturation, the fine crystal content in the crystallizer 8 and the design of the crystallizer 8, thereby obtaining a good manganese sulfate crystal morphology and size distribution.

[0058] Implementation Three

[0059] The thickened material enters the centrifuge 11 for solid-liquid separation, the clear liquid overflows back to the mother liquid tank 3, and the separated crystallized salt is stored for standby use. The centrifuge 11 includes a casing 111, a disc body 114, an adjustment component 113 and a power component 115.

[0060] A cover body 112 is buckled on the top of the casing 111, an inlet pipe 1121 is provided on the cover body 112, an outlet pipe 1111 is provided at the bottom of the casing 111, and the cover body 112 is buckled on the casing 111 to form a blockage and isolation to prevent external impurities from entering, and the casing 111 can be removed from the casing 111 to take out the stored crystallized salt.

[0061] The disk body 114 is located in the casing 111. A plurality of groups of centrifugal filter cartridges 1141 are circumferentially arranged on the disk body 114. A plurality of fine holes for discharging clear liquid are evenly distributed on the side walls of the centrifugal filter cartridges 1141. The thickened material can be transported to a group of centrifugal filter cartridges 1141 through the inlet pipe 1121. The power assembly 115 can drive the centrifugal filter cartridges 1141 to rotate the centrifugal crystallized material, so that the separated crystallized salt is stored in the centrifugal filter cartridges 1141 for standby use.

[0062] The adjustment assembly 113 is installed on the first motor body 1131 at the bottom of the casing 111. The output end of the first motor body 1131 is connected to a telescopic rod 1132. The telescopic rod 1132 extends into the casing 111 and is connected to the disk body 114. The first motor body 1131 drives the disk body 114 to rotate so that different centrifugal filter cartridges 1141 are vertically aligned with the feed pipe. That is, in the process of producing large manganese sulfate particles, the separated crystal salt can be stored in different centrifugal filter cartridges 1141.

[0063] A pad 1142 is provided in each set of centrifugal filter cartridges 1141. An upwardly extending lifting rod 1143 is provided on the pad 1142. By pulling the lifting rod 1143, the pad 1142 can be driven to move upward, and the stored and separated crystallized salt can be pushed upward out of the centrifugal filter cartridge 1141, so that the material can be easily taken out.

[0064] Embodiment 4

[0065] The power assembly 115 includes a second motor body 1151 installed in the casing 111 and a liner column 1152 arranged on each group of centrifugal filter cartridges 1141. Each group of liner columns 1152 is rotatably penetrated on the disk body 114, and each group of liner columns 1152 is connected to a slave gear 1153. The output end of the second motor body 1151 is connected to a main gear 1154, and the main gear 1154 can be meshed with a group of slave gears 1153. When a group of centrifugal filter cartridges 1141 is vertically aligned with the feed pipe, the corresponding slave gear 1153 can be meshed with the main gear 1154, thereby, centrifugal action can be performed under the drive of the second motor body 1151.

[0066] The adjustment assembly 113 also includes an electric cylinder body 1133 installed in the casing 111. The movable rod of the electric cylinder body 1133 is connected to a support rod 1134. The support rod 1134 is provided with a ring sleeve 1135 and a top plate 1136 from top to bottom. The top plate 1136 is located on the lower side of the disk body 114, and the ring sleeve 1135 is sleeved on the inlet pipe 1121.

[0067] The movable rod of the electric cylinder body 1133 extends out, and the support rod 1134 drives the ring sleeve 1135 and the top plate 1136 to move upward, driving the top plate 1136 to push the disc body 114 to move upward, and the first motor body 1131 drives the disc body 114 to rotate so that a group of centrifugal filter cartridges 1141 are vertically aligned with the feed pipe;

[0068] The top plate 1136 is preferably provided with a ball body 1137 that can contact the disc body 114. When the top plate 1136 pushes the disc body 114 to move upward, the slave gear 1153 that was originally engaged with the main gear 1154 is driven to disengage. At this time, the disc body 114 is driven to rotate by the first motor body 1131, and the friction resistance is reduced by the provided ball body 1137, so that a group of empty centrifugal filter cartridges 1141 can be moved and vertically aligned with the feed pipe.

[0069] The movable rod of the electric cylinder body 1133 is retracted and reset, and the support rod 1134 drives the ring sleeve 1135 and the top plate 1136 to move downward, driving the ring sleeve 1135 to cover the centrifugal filter cartridge 1141 vertically aligned with the feed pipe. After the top plate 1136 moves downward, the support plate is reset downward, so that the slave gear 1153 corresponding to the group of centrifugal filter cartridges 1141 moves downward and meshes with the main gear 1154. At the same time, the ring sleeve 1135 is driven to cover the centrifugal filter cartridge 1141 downward. During the centrifugation process, the ring sleeve 1135 is used to block the clear liquid from splashing onto other centrifugal filter cartridges 1141, that is, the crystallized salt separated and stored in other centrifugal filter cartridges 1141 is effectively prevented from re-adhering to the supernatant, thereby ensuring the quality of the crystallized salt. Although the embodiments of the present invention have been shown and described, it is understood by those skilled in the art that various changes, modifications, substitutions and variations can be made to these embodiments without departing from the principles and spirit of the present invention, and the scope of the present invention is defined by the appended claims and their equivalents.

Claims

1. An evaporation crystallization process for producing large manganese sulfate particles, characterized in that: The specific steps include: S1, transporting the unsaturated manganese sulfate solution to the mother liquid tank (3) through the stock solution pump (2), lowering the temperature of the mother liquid and increasing the solubility, and dissolving the fine crystals in the mother liquid tank (3) through the unsaturated manganese sulfate solution; S2, the manganese sulfate solution with fine crystals removed is transported to a preheater (5) to be preheated with distilled water, and then transported to a forced circulation heat exchanger (7) through a forced circulation pump (6) to increase the temperature and pressure by secondary steam heat exchange between the tube side and the shell side; S3, the manganese sulfate solution with increased temperature and pressure enters the crystallizer (8) for flash evaporation, and the material after flash evaporation is crystallized and floated in the crystallization chamber; S4, the crystallized material is thickened in a thickener (10) through a discharge pump (9), and the thickened crystallized material enters a centrifuge (11) for solid-liquid separation, and the clear liquid overflows back to the mother liquid tank (3), and the separated crystallized salt is stored for later use.

2. The evaporation crystallization process for producing large manganese sulfate particles according to claim 1, characterized in that: In the step s3, the fine crystals and impurities floating on the top of the crystallization chamber of the crystallizer (8) are sent to the sedimentation tank (13) through the impurity discharge pump (12), and the settled fine crystals are discharged back to the mother liquid tank (3) from the bottom, and the impurities overflow from the top of the sedimentation tank (13) and are discharged externally.

3. The evaporation crystallization process for producing large manganese sulfate particles according to claim 2, characterized in that: In the step s3, the steam discharged from the crystallizer (8) passes through the secondary separator (14) to remove foam, enters the compressor (15) to increase temperature and pressure, and then enters the forced circulation heat exchanger (7) to exchange heat with the manganese sulfate solution after being compressed. The steam after heat exchange is condensed into water and flows to the distilled water tank (16), and is sent to the preheater (5) by the distilled water pump (17) to preheat the manganese sulfate solution before being discharged.

4. The evaporation crystallization process for producing large manganese sulfate particles according to claim 1, characterized in that: In the above s4, when the solid content of the material in the crystallization chamber reaches 10% to 20%, it is transported to the thickener (10), thickened to a solid content of 30% to 40% in the thickener (10), and then enters the centrifuge (11).

5. An evaporation crystallization process for producing large manganese sulfate particles according to any one of claims 1 to 4, wherein the crystallizer (8) is an Oslo type.

6. According to the evaporation crystallization process for producing large manganese sulfate particles as claimed in claim 1, the centrifuge (11) comprises: The housing (111) has a cover (112) buckled on the top, the cover (112) is provided with an inlet pipe (1121), and the housing (111) is provided with an outlet pipe (1111) at the bottom; A disk body (114) is located in the housing (111), and a plurality of groups of centrifugal filter cartridges (1141) are circumferentially arranged on the disk body (114); An adjusting component (113), a first motor body (1131) installed at the bottom of the housing (111), an output end of the first motor body (1131) being connected to a telescopic rod (1132), and the telescopic rod (1132) extending into the housing (111) and connected to the disk body (114); The power assembly (115) is used to drive a group of centrifugal filter cartridges (1141) to rotate and centrifuge the crystallized material.

7. According to the evaporation crystallization process for producing large manganese sulfate particles as described in claim 6, a pad (1142) is provided in each group of the centrifugal filter cartridges (1141), and a lifting rod (1143) extending upward is provided on the pad (1142).

8. According to claim 6, an evaporation crystallization process for producing large manganese sulfate particles, the power assembly (115) includes a second motor body (1151) installed in the casing (111) and a liner (1152) arranged on each group of the centrifugal filter cartridges (1141), each group of the liner (1152) is rotatably penetrated on the disk body (114), and each group of the liner (1152) is connected to a slave gear (1153), and the output end of the second motor body (1151) is connected to a main gear (1154), and the main gear (1154) can mesh with a group of the slave gears (1153).

9. According to the evaporation crystallization process for producing large manganese sulfate particles as described in claim 6, the adjustment component (113) also includes an electric cylinder body (1133) installed in the housing (111), the movable rod of the electric cylinder body (1133) is connected to a support rod (1134), and the support rod (1134) is provided with a ring sleeve (1135) and a top plate (1136) from top to bottom, the top plate (1136) is located at the lower side of the disk body (114), and the ring sleeve (1135) is sleeved on the inlet pipe (1121).

10. According to claim 9, an evaporation crystallization process for producing large particles of manganese sulfate, the movable rod of the electric cylinder body (1133) extends, the support rod (1134) drives the ring sleeve (1135) and the top plate (1136) to move upward, drives the top plate (1136) to push the disk body (114) to move upward, and the first motor body (1131) drives the disk body (114) to rotate so that a group of centrifugal filter cartridges (1141) are vertically aligned with the feed pipe; the movable rod of the electric cylinder body (1133) retracts and resets, the support rod (1134) drives the ring sleeve (1135) and the top plate (1136) to move downward, drives the ring sleeve (1135) to cover the centrifugal filter cartridge (1141) vertically aligned with the feed pipe.

Images