CN217613030U - Battery-grade manganese sulfate production system - Google Patents
Battery-grade manganese sulfate production system Download PDFInfo
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- CN217613030U CN217613030U CN202221551665.8U CN202221551665U CN217613030U CN 217613030 U CN217613030 U CN 217613030U CN 202221551665 U CN202221551665 U CN 202221551665U CN 217613030 U CN217613030 U CN 217613030U
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Abstract
The utility model provides a battery level manganese sulfate production system, include: the system comprises a crude product crystallization area, a crude product dissolution area and a fine product crystallization area, wherein a crude product crystallizer is connected with a raw liquid pipeline, the top end of the crude product crystallizer is connected with a gas-liquid separator, one side of the gas-liquid separator is connected with a compressor, and one end of the compressor is connected with a crude product crystallization heat exchanger; one side of the crude product dissolver is connected with a dissolving heat exchanger, a vertical dissolving pump is arranged on the crude product dissolver, the vertical dissolving pump is connected with the dissolving heat exchanger, and the dissolving heat exchanger is provided with a cooling water inlet and a cooling water outlet; the fine product crystallizer is connected with the fine product thickener, a flash gas exhaust pipeline is connected to the fine product thickener, a fine product discharge pump is installed on a connecting pipeline of the fine product crystallizer and the fine product thickener, the bottom end of the fine product thickener is connected with a fine product centrifugal machine, and one end of the fine product centrifugal machine is connected with a product discharge pipe.
Description
Technical Field
The utility model belongs to the technical field of the evaporation, concretely relates to battery level manganese sulfate production system.
Background
Manganese sulfate plays an important role in manganese series products, is an important industrial intermediate product for producing other manganese oxides and manganese salt, is mainly used for preparing a ternary material precursor of a lithium battery anode, is also a basic raw material for preparing battery-grade high-purity trimanganese tetroxide and high-purity manganese dioxide, and is used for producing manganese sulfate monohydrate by adopting a reaction kettle for intermittent crystallization, but the yield is low, and the quality of each part cannot be controlled in time.
SUMMERY OF THE UTILITY MODEL
The utility model aims at solving the problems existing in the prior art, the utility model provides a battery level manganese sulfate production system.
The utility model provides a following technical scheme:
a battery-grade manganese sulfate production system, comprising:
the crude product crystallization area comprises a crude product crystallization heat exchanger and a crude product crystallizer, wherein a crude liquid pipeline is connected to the crude product crystallizer, a gas-liquid separator is connected to the top end of the crude product crystallizer, a compressor is connected to one side of the gas-liquid separator, and one end of the compressor is connected with the crude product crystallization heat exchanger;
the crude product dissolving area comprises a crude product dissolver and a dissolving heat exchanger, wherein one side of the crude product dissolver is connected with the dissolving heat exchanger, a vertical dissolving pump is arranged on the crude product dissolver and is connected with the dissolving heat exchanger, and the dissolving heat exchanger is provided with a cooling water inlet and a cooling water outlet;
and the fine product crystallization area comprises a fine product crystallizer and a fine product thickener, the fine product crystallizer is connected with the fine product thickener, the fine product thickener is connected with a flash gas discharge pipeline, a fine product discharge pump is installed on a connecting pipeline of the fine product crystallizer and the fine product thickener, the bottom end of the fine product thickener is connected with a fine product centrifugal machine, and one end of the fine product centrifugal machine is connected with a product discharge pipe.
Furthermore, another termination of crude product crystallization heat exchanger has the distilled water pitcher, distilled water pitcher bottom termination has the distilled water pump, takes out the distilled water in the distilled water pitcher through the distilled water pump, and distilled water pitcher top has connect noncondensable gas cooler, noncondensable gas outlet duct, cooling water inlet tube and cooling water outlet pipe have been connect on the noncondensable gas cooler, install the vacuum pump on the noncondensable gas outlet duct.
Furthermore, a crude product thickener is connected to the bottom end of the crude product crystallizer, a crude product discharge pump is installed between the crude product crystallizer and the crude product thickener, a crude product centrifuge is connected to the bottom end of the crude product thickener, and a crude product mother liquor tank is connected to the bottom end of the crude product centrifuge.
Furthermore, one end of the crude product crystallizer is connected with a crude product crystallization forced circulation pump, one end of the crude product crystallization forced circulation pump is connected with the crude product crystallization heat exchanger, one end of the crude product mother liquor tank is connected with the crude product crystallization forced circulation pump, and a crude product mother liquor pump is arranged between the crude product mother liquor tank and the crude product crystallization forced circulation pump.
Further, an outward concentrated liquid discharge port is arranged between the crude product mother liquid pump and the crude product crystallization forced circulation pump.
Furthermore, the crude product dissolver is connected with the crude product centrifuge, a pure water inlet pipe is connected to the crude product dissolver, and a clear liquid tank is connected to one side of the crude product dissolver.
Further, the fine product crystallizer is connected with the clear liquid tank, a clear liquid conversion pump is installed between the fine product crystallizer and the clear liquid tank, a fine product mother liquid tank is further connected to the bottom end of the fine product centrifuge, one side of the fine product mother liquid tank is connected with the fine product crystallizer, and a fine product mother liquid pump is installed between the fine product mother liquid tank and the fine product crystallizer.
Furthermore, an outward concentrated liquid discharge port is arranged between the fine crystallizer and the fine mother liquid pump, and a condensed water outlet and a steam inlet are arranged on the fine crystallizer.
The utility model has the advantages that:
the continuous production process is adopted, and the crude product crystallization, the fine product dissolution and the fine product crystallization all adopt crystallizers, so that the processing conditions of all regions can be conveniently mastered, the adjustment can be carried out in time, and the continuous production process is suitable for large-scale production.
Drawings
The accompanying drawings are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention, and together with the description serve to explain the invention and not to limit the invention. In the drawings:
fig. 1 is a schematic view of the structure of the present invention.
Detailed Description
As shown in fig. 1, a battery-grade manganese sulfate production system comprises a crude product crystallization area 1, a crude product dissolution area 2 and a fine product crystallization area 3, and the production process is divided into three sections, wherein the first section is crude product crystallization, the second section is crude product dissolution, and the third section is fine product crystallization.
The crude product crystallization area 1 comprises a crude product crystallization heat exchanger 107 and a crude product crystallizer 108, wherein a crude liquid pipeline 106 is connected to the crude product crystallizer 108, a gas-liquid separator 110 is connected to the top end of the crude product crystallizer 108, a compressor 109 is connected to one side of the gas-liquid separator 110, and one end of the compressor 109 is connected with the crude product crystallization heat exchanger 107.
The other end of the crude product crystallization heat exchanger 107 is connected with a distilled water tank 102, the bottom end of the distilled water tank 102 is connected with a distilled water pump 101, distilled water in the distilled water tank 102 is pumped out through the distilled water pump 101, the top end of the distilled water tank 102 is connected with a noncondensable gas cooler 117, the noncondensable gas cooler 117 is connected with a noncondensable gas outlet pipe, a cooling water inlet pipe 104 and a cooling water outlet pipe 105, and the noncondensable gas outlet pipe is provided with a vacuum pump 103.
The bottom end of the crude crystallizer 108 is connected with a crude thickener 111, a crude discharging pump 116 is arranged between the crude crystallizer 108 and the crude thickener 111, the bottom end of the crude thickener 111 is connected with a crude centrifuge 112, and the bottom end of the crude centrifuge 112 is connected with a crude mother liquor tank 115.
One end of the crude product crystallizer 108 is connected with a crude product crystallization forced circulation pump 113, one end of the crude product crystallization forced circulation pump 113 is connected with the crude product crystallization heat exchanger 107, one end of the crude product mother liquor tank 115 is connected with the crude product crystallization forced circulation pump 113, a crude product mother liquor pump 114 is installed between the crude product mother liquor tank 115 and the crude product crystallization forced circulation pump 113, and an outward discharge concentrated liquor port is arranged between the crude product mother liquor pump 114 and the crude product crystallization forced circulation pump 113.
Raw material liquid enters a crude product crystallizer 108 through a raw material liquid pipeline 106, a crude product crystallization forced circulation pump 113 pumps material liquid in the crude product crystallizer 108 into a crude product crystallization heat exchanger 107 for circulation, secondary steam generated by flashing of a part of the material on the upper part of the crude product crystallizer 108 enters a gas-liquid separator 110, liquid drops are removed through the gas-liquid separator 110, the secondary steam enters a compressor 109 for temperature rise and pressure rise, the secondary steam enters the crude product crystallization heat exchanger 107 for heat exchange with the material inside, the steam is condensed after heat exchange, distilled water in a distilled water tank 102 is discharged through a distilled water pump 101 after being collected by the distilled water tank 102, a small amount of non-condensable gas passes through a non-condensable gas cooler 117 and a vacuum pump 103 to be discharged out of a system, the material is continuously circulated and evaporated in an evaporation system, and the concentration of the material is continuously increased to reach supersaturated crystallization; suspending larger particles of crystals at the lower part of a crude product crystallizer 108, sending the larger particles into a crude product thickener 111 through a crude product discharge pump 116, wherein clear liquid in the crude product thickener 111 overflows to a crude product mother liquid tank 115 from the upper part, discharging crystal slurry to a crude product centrifuge 112, separating manganese sulfate monohydrate crystals, returning the mother liquid to the crude product mother liquid tank 115 to an evaporation crystallization system through a crude product mother liquid pump 114, discharging part of the mother liquid to be treated after impurities in the system are accumulated to a certain amount, wherein the evaporation temperature in the crude product system is controlled to be 90-95 ℃, the content of the crystals entering the crude product centrifuge 112 is 35-40%, the particle size of the manganese sulfate monohydrate crystals is more than 400 and accounts for 80%, and the water content is about 10%.
The crude product dissolving area 2 comprises a crude product dissolver 203 and a dissolving heat exchanger 204, one side of the crude product dissolver 203 is connected with the dissolving heat exchanger 204, the crude product dissolver 203 is provided with a vertical dissolving pump 202, the vertical dissolving pump 202 is connected with the dissolving heat exchanger 204, and the dissolving heat exchanger 204 is provided with a cooling water inlet and a cooling water outlet; the crude product dissolver 203 is connected with the crude product centrifuge 112, a pure water inlet pipe 201 is connected with the crude product dissolver 203, and a clear liquid tank 205 is connected with one side of the crude product dissolver 203.
The crystallized salt from the crude product centrifuge 112 enters a crude product dissolver 203, pure water enters the crude product dissolver 203 through a pure water inlet pipe 201, the solubility of manganese sulfate is increased along with the reduction of the temperature, feed liquid is sent into a tube pass of a dissolving heat exchanger 204 through a vertical dissolving pump 202 to exchange heat with cooling water in the dissolving heat exchanger 204, then the feed liquid enters the bottom of the crude product dissolver 203 to be continuously cooled circularly, the dissolved clear liquid enters a clear liquid tank 205 through an overflow port at the top of the crude product dissolver 203, wherein the dissolving temperature of the system is controlled to be about 50 ℃, and the content of the dissolved manganese ions is 55g/l.
The fine product crystallization zone 3 comprises a fine product crystallizer 302 and a fine product thickener 307, the fine product crystallizer 302 is connected with the fine product thickener 307, a flash gas discharge pipeline is connected to the fine product thickener 307, a fine product discharge pump 303 is installed on a connecting pipeline of the fine product crystallizer 302 and the fine product thickener 307, the bottom end of the fine product thickener 307 is connected with a fine product centrifuge 306, and one end of the fine product centrifuge 306 is connected with a product discharge pipe 305.
The fine crystallizer 302 is connected with the clear liquid tank 205, a clear liquid conversion pump 301 is installed between the fine crystallizer 302 and the clear liquid tank 205, a fine mother liquid tank 308 is further connected to the bottom end of the fine centrifuge 306, one side of the fine mother liquid tank 308 is connected with the fine crystallizer 302, a fine mother liquid pump 304 is installed between the fine mother liquid tank 308 and the fine crystallizer 302, an outward discharge concentrated liquid port is arranged between the fine crystallizer 302 and the fine mother liquid pump 304, and a condensed water outlet and a steam inlet are formed in the fine crystallizer 302.
Manganese sulfate solution dissolved in a clear liquid tank 205 is fed into a fine crystallizer 302 through a clear liquid transfer pump 301, a central cylinder is arranged in the fine crystallizer 302, a steam heating coil is arranged on the central cylinder, a stirring device (not shown) is arranged in the central cylinder, the feed liquid enters the central cylinder, under the action of the stirring device, the feed liquid flows downwards along the axial direction and exchanges heat with the high-temperature wall of the central cylinder, a large amount of crystals are separated when the feed liquid runs to the bottom of the fine crystallizer 302 due to the reduction of the high-temperature solubility of manganese sulfate, a fine discharge pump 303 feeds the crystals into a fine thickener 307, after the high-pressure high-temperature material enters the fine thickener 307, part of steam is flashed, flashed steam is discharged from a flash steam discharge pipeline, after the clear liquid is separated, the crystal slurry enters a fine centrifuge 306 to separate battery-grade manganese sulfate monohydrate, the overflow clear liquid and the centrifugal mother liquid are fed back to the fine crystallizer 302 to be crystallized, the impurities are discharged and treated after being accumulated to a certain amount, wherein the temperature in the fine crystallizer 302 is controlled to be about 165 ℃, the content of the crystals of 35-40% of the manganese sulfate monohydrate in the fine centrifuge 306, the crystal monohydrate mother liquid is greater than 80%, and the water content of about 180% of the grain size of the crystal sulfate.
Although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that modifications may be made to the embodiments described in the foregoing embodiments, or equivalents may be substituted for elements thereof. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (8)
1. A battery-grade manganese sulfate production system is characterized by comprising:
the crude product crystallization area (1) comprises a crude product crystallization heat exchanger (107) and a crude product crystallizer (108), a crude liquid pipeline (106) is connected to the crude product crystallizer (108), a gas-liquid separator (110) is connected to the top end of the crude product crystallizer (108), a compressor (109) is connected to one side of the gas-liquid separator (110), and one end of the compressor (109) is connected with the crude product crystallization heat exchanger (107);
the crude product dissolving area (2) comprises a crude product dissolver (203) and a dissolving heat exchanger (204), one side of the crude product dissolver (203) is connected with the dissolving heat exchanger (204), a vertical dissolving pump (202) is installed on the crude product dissolver (203), the vertical dissolving pump (202) is connected with the dissolving heat exchanger (204), and the dissolving heat exchanger (204) is provided with a cooling water inlet and a cooling water outlet;
the fine product crystallization area (3) comprises a fine product crystallizer (302) and a fine product thickener (307), the fine product crystallizer (302) is connected with the fine product thickener (307), a flash steam exhaust pipeline is connected to the fine product thickener (307), a fine product discharge pump (303) is installed on a connecting pipeline of the fine product crystallizer (302) and the fine product thickener (307), a fine product centrifuge (306) is connected to the bottom end of the fine product thickener (307), and a product discharge pipe (305) is connected to one end of the fine product centrifuge (306).
2. The battery-grade manganese sulfate production system according to claim 1, wherein the other end of the crude crystallization heat exchanger (107) is connected with a distilled water tank (102), the bottom end of the distilled water tank (102) is connected with a distilled water pump (101), distilled water in the distilled water tank (102) is pumped out through the distilled water pump (101), the top end of the distilled water tank (102) is connected with a noncondensable gas cooler (117), the noncondensable gas cooler (117) is connected with a noncondensable gas outlet pipe, a cooling water inlet pipe (104) and a cooling water outlet pipe (105), and the noncondensable gas outlet pipe is provided with a vacuum pump (103).
3. The battery-grade manganese sulfate production system of claim 1, wherein a crude product thickener (111) is connected to the bottom end of the crude product crystallizer (108), a crude product discharge pump (116) is installed between the crude product crystallizer (108) and the crude product thickener (111), a crude product centrifuge (112) is connected to the bottom end of the crude product thickener (111), and a crude product mother liquor tank (115) is connected to the bottom end of the crude product centrifuge (112).
4. The battery-grade manganese sulfate production system as claimed in claim 3, wherein a crude crystallization forced circulation pump (113) is connected to one end of the crude crystallizer (108), one end of the crude crystallization forced circulation pump (113) is connected to the crude crystallization heat exchanger (107), one end of the crude mother liquor tank (115) is connected to the crude crystallization forced circulation pump (113), and a crude mother liquor pump (114) is installed between the crude mother liquor tank (115) and the crude crystallization forced circulation pump (113).
5. The battery-grade manganese sulfate production system according to claim 4, wherein an outward concentrate discharge port is provided between the crude mother liquor pump (114) and the crude crystallization forced circulation pump (113).
6. The battery-grade manganese sulfate production system as claimed in claim 1, wherein the crude dissolver (203) is connected with the crude centrifuge (112), a pure water inlet pipe (201) is connected with the crude dissolver (203), and a clear liquid tank (205) is connected with one side of the crude dissolver (203).
7. The battery-grade manganese sulfate production system of claim 1, wherein the fine crystallizer (302) is connected with the clear liquid tank (205), a clear liquid conversion pump (301) is installed between the fine crystallizer (302) and the clear liquid tank (205), a fine mother liquid tank (308) is further connected to the bottom end of the fine centrifuge (306), one side of the fine mother liquid tank (308) is connected with the fine crystallizer (302), and a fine mother liquid pump (304) is installed between the fine mother liquid tank (308) and the fine crystallizer (302).
8. The battery-grade manganese sulfate production system according to claim 7, wherein an outward concentrated liquid discharge port is provided between the fine crystallizer (302) and the fine mother liquid pump (304), and a condensed water outlet and a steam inlet are provided on the fine crystallizer (302).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202221551665.8U CN217613030U (en) | 2022-06-20 | 2022-06-20 | Battery-grade manganese sulfate production system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202221551665.8U CN217613030U (en) | 2022-06-20 | 2022-06-20 | Battery-grade manganese sulfate production system |
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| Publication Number | Publication Date |
|---|---|
| CN217613030U true CN217613030U (en) | 2022-10-21 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202221551665.8U Active CN217613030U (en) | 2022-06-20 | 2022-06-20 | Battery-grade manganese sulfate production system |
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| CN (1) | CN217613030U (en) |
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2022
- 2022-06-20 CN CN202221551665.8U patent/CN217613030U/en active Active
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