CN217041335U - Nickel sulfate continuous crystallization integrated equipment - Google Patents
Nickel sulfate continuous crystallization integrated equipment Download PDFInfo
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- CN217041335U CN217041335U CN202220741341.4U CN202220741341U CN217041335U CN 217041335 U CN217041335 U CN 217041335U CN 202220741341 U CN202220741341 U CN 202220741341U CN 217041335 U CN217041335 U CN 217041335U
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Abstract
本实用新型涉及工业结晶技术领域，具体涉及一种硫酸镍连续结晶成套装置,它包括依次通过管道连接的上料泵、加热器、MVR循环泵、MVR分离器、MVR出料泵、真空闪蒸结晶器、闪蒸出料泵、稠厚器、离心机、母液罐，MVR分离器具有分离器气相出口和分离器液相出口，分离器液相出口与MVR出料泵的输入端通过管道连接，真空闪蒸结晶器具有闪蒸气相出口、闪蒸液相出口和闪蒸晶体物料出口，真空闪蒸结晶器的闪蒸晶体物料出口与闪蒸出料泵的输入端通过管道连接，闪蒸出料泵的输出端与稠厚器的输入端通过管道连接。本实用新型有益效果为：本系统采用MVR分离器加真空闪结晶器双重浓缩结晶技术，节能降耗晶体粒度稳定，生产效率高。
The utility model relates to the technical field of industrial crystallization, in particular to a complete set of nickel sulfate continuous crystallization device, which comprises a feeding pump, a heater, an MVR circulating pump, an MVR separator, an MVR discharging pump, and a vacuum flash evaporation which are sequentially connected by pipelines. Crystallizer, flash discharge pump, thickener, centrifuge, mother liquor tank, MVR separator has separator gas phase outlet and separator liquid phase outlet, separator liquid phase outlet is connected with the input end of MVR discharge pump through pipeline , the vacuum flash crystallizer has a flash vapor phase outlet, a flash liquid phase outlet and a flash crystal material outlet. The flash crystal material outlet of the vacuum flash crystallizer is connected to the input end of the flash discharge pump through a pipeline, and the flash The output end of the discharge pump is connected with the input end of the thickener through a pipeline. The beneficial effects of the utility model are as follows: the system adopts the double concentration and crystallization technology of the MVR separator and the vacuum flash crystallizer, which saves energy and reduces consumption, and has stable crystal particle size and high production efficiency.
Description
Technical Field
The utility model relates to an industrial crystallization technical field, in particular to a nickel sulfate continuous crystallization integrated equipment.
Background
Nickel sulfate is an important inorganic salt chemical raw material, and is widely used in the fields of electroplating, battery materials, semiconductor materials, catalysts, metal coloring and the like. The nickel sulfate product mainly exists in the form of hydrate, and mainly comprises nickel sulfate hexahydrate and nickel sulfate heptahydrate.
At present, nickel sulfate manufacturers generally adopt an intermittent operation mode. Firstly, the discharged material concentration of the concentration section is controlled to meet certain requirements and then discharged to a cooling crystallization tank. And (3) slowly introducing circulating cooling water, controlling the solution to slowly cool, adding seed crystals when the temperature of the solution is reduced to about 50-60 ℃, stopping circulating cooling water, and maintaining the temperature for a period of time, sometimes even needing to control the temperature to rise to some extent. Then continuously slowly cooling to about 35-40 ℃, and growing the crystal for a period of time at the end point temperature. The batch crystallization process is described in detail in Chinese patents CN200710027861.5, CN201811063611.2, etc. The intermittent crystallization has low production efficiency, complex operation and high labor intensity of workers. Meanwhile, the intermittent operation mode has the defects of wide particle size distribution range, large product difference among batches, unstable product performance index and the like.
SUMMERY OF THE UTILITY MODEL
The utility model aims to provide a nickel sulfate continuous crystallization complete device aiming at the defects and shortcomings of the prior art, the system adopts the double concentration crystallization technology of the MVR separator and the vacuum flash crystallizer, the MVR separator mechanically compresses secondary steam for repeated recycling, the consumption of fresh steam is reduced, and the energy is saved and the consumption is reduced; in the continuous operation process of the vacuum flash evaporation crystallizer, the grain size distribution of a product is controlled by adjusting the density of crystal mush in the crystallizer, and in the material circulation process, clear mother liquor circulation is mostly adopted, so that the crystal grain size is stable, and the production efficiency is high.
In order to achieve the above purpose, the utility model adopts the following technical scheme: a nickel sulfate continuous crystallization complete device comprises a feeding pump 1, a heater 2, an MVR circulating pump 3, an MVR separator 4, an MVR discharging pump 5, a vacuum flash evaporation crystallizer 6, a flash evaporation discharging pump 7, a thickener 8, a centrifuge 9 and a mother liquor tank 10 which are sequentially connected through pipelines, wherein the output end of the feeding pump 1 is connected with the input end of the heater 2 through a pipeline, the output end of the heater 2 is connected with the input end of the MVR circulating pump 3 through a pipeline, the output end of the MVR circulating pump 3 is connected with the input end of the MVR separator 4 through a pipeline, a raw material liquid enters the heater 2 for heating after passing through the feeding pump 1, the heated raw material liquid enters the MVR separator 4 after passing through the MVR circulating pump 3, the MVR separator 4 is provided with a separator gas phase outlet 41 and a separator liquid phase outlet 42, the separator gas phase outlet 41 is higher than the separator liquid phase outlet 42, the separator liquid phase outlet 42 is connected with the input end of the MVR discharging pump 5 through a pipeline, the output end of the MVR discharging pump 5 is connected with the input end of a vacuum flash evaporation crystallizer 6 through a pipeline, the concentrated material enters the vacuum flash evaporation crystallizer 6, the vacuum flash evaporation crystallizer 6 is provided with a flash vapor phase outlet 61, a flash liquid phase outlet 62 and a flash crystal material outlet 63, the flash vapor phase outlet 61 is arranged at the top of the vacuum flash evaporation crystallizer 6, the flash crystal material outlet 63 is arranged at the bottom of the vacuum flash evaporation crystallizer 6, the flash liquid phase outlet 62 is arranged between the flash vapor phase outlet 61 and the flash crystal material outlet 63, the flash crystal material outlet 63 of the vacuum flash evaporation crystallizer 6 is connected with the input end of a flash discharging pump 7 through a pipeline, the output end of the flash discharging pump 7 is connected with the input end of a thickener 8 through a pipeline, the output end of the thickener 8 is connected with the input end of a centrifuge 9 through a pipeline, the centrifuge 9 is provided with a centrifuge liquid phase outlet 91 and a centrifuge crystal material outlet 92, crystal slurry in the vacuum flash evaporation crystallizer 6 is extracted by a crystallization discharge pump 8 and is conveyed to a thickener 8 for thickening, supersaturation is eliminated, then the crystal slurry is filtered by a centrifuge 9 to obtain a nickel sulfate product from a centrifuge crystal material outlet 92, a centrifuge liquid phase outlet 91 is connected with the input end of a mother liquor tank 10 by a pipeline, and mother liquor in the centrifuge 9 enters the mother liquor tank 10 through a centrifuge liquid phase outlet 91.
Further, the nickel sulfate continuous crystallization system further comprises: and the input end of the compressor 11 is connected with the gas phase outlet 41 of the separator through a pipeline, and the output end of the compressor 11 is connected with the input end of the heater 2 through a pipeline.
Further, the continuous crystallization system of nickel sulfate also comprises: the indirect cooler 12 and the flash evaporation circulating pump 13, indirect cooler 12 passes through the pipeline and is connected with flash evaporation gaseous phase export 61, and the secondary steam after the flash evaporation passes through indirect cooler 12 full cooling, and flash evaporation circulating pump 13 passes through the pipeline and is connected with flash evaporation liquid phase export 62, and the output of flash evaporation circulating pump 13 passes through the pipe connection on the input of vacuum flash evaporation crystallizer 6.
Further, the nickel sulfate continuous crystallization system further comprises: the input end of the mother liquor pump 14 is connected with the output end of the mother liquor tank 10 through a pipeline, the output end of the mother liquor pump 14 is connected with the input end of the MVR separator 4 through a pipeline, and the mother liquor in the mother liquor tank 10 returns to the MVR separator 4 through the mother liquor pump 14 to be concentrated again.
After the technical scheme is adopted, the utility model discloses beneficial effect does: the system adopts a double concentration and crystallization technology of the MVR separator and the vacuum flash crystallizer, the MVR separator mechanically compresses secondary steam for repeated recycling, the consumption of fresh steam is reduced, and energy and consumption are saved; in the continuous operation process of the vacuum flash evaporation crystallizer, the granularity distribution of a product is controlled by adjusting the density of crystal mush in the crystallizer, and in the material circulation process, clear mother liquor circulation is mostly adopted, so that the granularity of crystals is stable, and the production efficiency is high.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings needed to be used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without inventive exercise.
Fig. 1 is a schematic structural diagram of the present invention.
Fig. 2 is a schematic structural view of the MVR separator of the present invention.
Fig. 3 is a schematic diagram of the structure of the vacuum flash evaporation crystallizer of the present invention.
Fig. 4 is a schematic structural view of the centrifuge of the present invention.
Description of the reference numerals: the system comprises a feeding pump 1, a heater 2, an MVR circulating pump 3, an MVR separator 4, an MVR discharging pump 5, a vacuum flash evaporation crystallizer 6, a flash evaporation discharging pump 7, a thickener 8, a centrifuge 9, a mother liquor tank 10, a separator gas phase outlet 41, a separator liquid phase outlet 42, a flash evaporation gas phase outlet 61, a flash evaporation liquid phase outlet 62, a flash evaporation crystal material outlet 63, a centrifuge liquid phase outlet 91, a centrifuge crystal material outlet 92, a compressor 11, an intercooler 12, a flash evaporation circulating pump 13 and a mother liquor pump 14.
Detailed Description
Referring to fig. 1 to 4, the technical solution adopted by the present embodiment is: a nickel sulfate continuous crystallization complete device comprises a feeding pump 1, a heater 2, an MVR circulating pump 3, an MVR separator 4, an MVR discharging pump 5, a vacuum flash evaporation crystallizer 6, a flash evaporation discharging pump 7, a thickener 8, a centrifuge 9 and a mother liquor tank 10 which are sequentially connected through pipelines, wherein the output end of the feeding pump 1 is connected with the input end of the heater 2 through a pipeline, the output end of the heater 2 is connected with the input end of the MVR circulating pump 3 through a pipeline, the output end of the MVR circulating pump 3 is connected with the input end of the MVR separator 4 through a pipeline, a raw material liquid enters the heater 2 for heating after passing through the feeding pump 1, the heated raw material liquid enters the MVR separator 4 after passing through the MVR circulating pump 3, the MVR separator 4 is provided with a separator gas phase outlet 41 and a separator liquid phase outlet 42, the separator gas phase outlet 41 is higher than the separator liquid phase outlet 42, the separator liquid phase outlet 42 is connected with the input end of the MVR discharging pump 5 through a pipeline, the output end of the MVR discharging pump 5 is connected with the input end of a vacuum flash evaporation crystallizer 6 through a pipeline, the concentrated material enters the vacuum flash evaporation crystallizer 6, the vacuum flash evaporation crystallizer 6 is provided with a flash vapor phase outlet 61, a flash liquid phase outlet 62 and a flash crystal material outlet 63, the flash vapor phase outlet 61 is arranged at the top of the vacuum flash evaporation crystallizer 6, the flash crystal material outlet 63 is arranged at the bottom of the vacuum flash evaporation crystallizer 6, the flash liquid phase outlet 62 is arranged between the flash vapor phase outlet 61 and the flash crystal material outlet 63, the flash crystal material outlet 63 of the vacuum flash evaporation crystallizer 6 is connected with the input end of a flash discharging pump 7 through a pipeline, the output end of the flash discharging pump 7 is connected with the input end of a thickener 8 through a pipeline, the output end of the thickener 8 is connected with the input end of a centrifuge 9 through a pipeline, the centrifuge 9 is provided with a centrifuge liquid phase outlet 91 and a centrifuge crystal material outlet 92, the crystal slurry in the vacuum flash evaporation crystallizer 6 is extracted by a crystallization discharge pump 8 and is conveyed to a thickener 8 for thickening and eliminating supersaturation, and then is filtered by a centrifuge 9 to obtain a nickel sulfate product from a centrifuge crystal material outlet 92, a centrifuge liquid phase outlet 91 is connected with the input end of a mother liquor tank 10 by a pipeline, and the mother liquor in the centrifuge 9 enters the mother liquor tank 10 through the centrifuge liquid phase outlet 91.
Further, the nickel sulfate continuous crystallization system further comprises: and the input end of the compressor 11 is connected with the gas phase outlet 41 of the separator through a pipeline, and the output end of the compressor 11 is connected with the input end of the heater 2 through a pipeline.
Further, the nickel sulfate continuous crystallization system further comprises: the system comprises an intercooler 12 and a flash evaporation circulating pump 13, wherein the intercooler 12 is connected with a flash evaporation gas phase outlet 61 through a pipeline, secondary steam after flash evaporation is fully cooled through the intercooler 12, the flash evaporation circulating pump 13 is connected with a flash evaporation liquid phase outlet 62 through a pipeline, and the output end of the flash evaporation circulating pump 13 is connected to the input end of the vacuum flash evaporation crystallizer 6 through a pipeline.
Further, the continuous crystallization system of nickel sulfate also comprises: and an input end of the mother liquor pump 14 is connected with an output end of the mother liquor tank 10 through a pipeline, an output end of the mother liquor pump 14 is connected with an input end of the MVR separator 4 through a pipeline, and the mother liquor in the mother liquor tank 10 returns to the MVR separator 4 through the mother liquor pump 14 to be concentrated again.
The utility model discloses a theory of operation: the utility model discloses a MVR evaporation system adds the vacuum flash crystallizer and carries out dual concentrated crystallization, and former water salt share mainly is nickel sulfate, and the raw materials comes the liquid concentration low, adopts the MVR evaporation to reach near the saturated condition with the raw materials concentration, and the direct ration pump sending of high temperature saturated nickel sulfate supplied materials is to vacuum flash crystallization shrink ware, under the vacuum system effect, and the material flash distillation is cooled down. The crystal mush continuous pump in the vacuum flash crystallization condenser is extracted and sent to a thickener for thickening, the supersaturation is eliminated, then the nickel sulfate product is obtained by filtering through a centrifugal machine, and the separated mother liquor returns to the front-stage triple-effect evaporation for re-concentration. Material flow direction: raw material liquid gets into the heater heating behind the material loading pump, get into the MVR separator behind the circulating pump, the secondary steam returns the heater again after passing through the compressor pressurization and heats, the material after the concentration is sent to the vacuum flash evaporation crystallizer in through the MVR discharge pump, the secondary steam after the flash evaporation is through intercooler full cooling, the material circulates through the flash evaporation circulating pump in the vacuum flash evaporation crystallizer, upper portion is the vaporization zone, the lower part is the crystallization settlement zone, the large granule is discharged from the bottom, the feed ratio crystallization tank internal mixture temperature is high, utilize self heat to carry out the secondary evaporation, through circulation liquid and feeding mixed control supersaturation, tiny crystalline grain grows up in order to eliminate the supersaturation. The crystallizer pressure reaches a high vacuum state under the condition of auxiliary vacuum equipment, and the boiling temperature of the solution reaches the requirement of a cooling crystallization process point. In the continuous operation process, the product particle size distribution is controlled by adjusting the density of crystal slurry in the crystallizer, a material containing crystals is extracted by a flash evaporation material outlet pump and sent to a thickener for thickening, supersaturation is eliminated, and then a nickel sulfate product is obtained by filtering through a centrifugal machine, and a mother liquor of the centrifugal machine enters a mother liquor tank and returns to the MVR separator for re-concentration through a mother liquor pump.
After the technical scheme is adopted, the utility model discloses beneficial effect does: the system adopts a double concentration and crystallization technology of the MVR separator and the vacuum flash crystallizer, the MVR separator mechanically compresses secondary steam for repeated recycling, the consumption of fresh steam is reduced, and energy and consumption are saved; in the continuous operation process of the vacuum flash evaporation crystallizer, the grain size distribution of a product is controlled by adjusting the density of crystal mush in the crystallizer, and in the material circulation process, clear mother liquor circulation is mostly adopted, so that the crystal grain size is stable, and the production efficiency is high.
The above description is only for the purpose of illustrating the technical solutions of the present invention and not for the purpose of limiting the same, and other modifications or equivalent replacements made by those of ordinary skill in the art to the technical solutions of the present invention should be covered within the scope of the claims of the present invention as long as they do not depart from the spirit and scope of the technical solutions of the present invention.
Claims (4)
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202220741341.4U CN217041335U (en) | 2022-04-01 | 2022-04-01 | Nickel sulfate continuous crystallization integrated equipment |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202220741341.4U CN217041335U (en) | 2022-04-01 | 2022-04-01 | Nickel sulfate continuous crystallization integrated equipment |
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| CN217041335U true CN217041335U (en) | 2022-07-26 |
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| CN202220741341.4U Active CN217041335U (en) | 2022-04-01 | 2022-04-01 | Nickel sulfate continuous crystallization integrated equipment |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116328330A (en) * | 2023-05-30 | 2023-06-27 | 金川集团股份有限公司 | A kind of method utilizing nickel sulfate evaporation crystallization mother liquor to carry out nickel soap |
| CN116534919A (en) * | 2023-05-30 | 2023-08-04 | 金川集团股份有限公司 | Method for preparing nickel carbonate by utilizing nickel sulfate evaporation crystallization mother liquor |
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2022
- 2022-04-01 CN CN202220741341.4U patent/CN217041335U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116328330A (en) * | 2023-05-30 | 2023-06-27 | 金川集团股份有限公司 | A kind of method utilizing nickel sulfate evaporation crystallization mother liquor to carry out nickel soap |
| CN116534919A (en) * | 2023-05-30 | 2023-08-04 | 金川集团股份有限公司 | Method for preparing nickel carbonate by utilizing nickel sulfate evaporation crystallization mother liquor |
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Effective date of registration: 20260422 Granted publication date: 20220726 |