CN211836413U - Electrolyte crystallization magnesium removal system - Google Patents
Electrolyte crystallization magnesium removal system Download PDFInfo
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- CN211836413U CN211836413U CN202020418783.6U CN202020418783U CN211836413U CN 211836413 U CN211836413 U CN 211836413U CN 202020418783 U CN202020418783 U CN 202020418783U CN 211836413 U CN211836413 U CN 211836413U
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- crystallizer
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- 239000003792 electrolyte Substances 0.000 title claims abstract description 52
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 title claims abstract description 32
- 229910052749 magnesium Inorganic materials 0.000 title claims abstract description 32
- 239000011777 magnesium Substances 0.000 title claims abstract description 32
- 238000002425 crystallisation Methods 0.000 title claims abstract description 31
- 230000008025 crystallization Effects 0.000 title claims abstract description 31
- 239000013078 crystal Substances 0.000 claims abstract description 30
- 239000012452 mother liquor Substances 0.000 claims abstract description 28
- 239000002002 slurry Substances 0.000 claims abstract description 28
- 239000007788 liquid Substances 0.000 claims abstract description 21
- 239000006228 supernatant Substances 0.000 claims abstract description 14
- 239000003507 refrigerant Substances 0.000 claims abstract description 9
- 238000003860 storage Methods 0.000 claims abstract description 6
- 238000004062 sedimentation Methods 0.000 claims description 10
- 238000001816 cooling Methods 0.000 claims description 9
- 238000006243 chemical reaction Methods 0.000 claims description 4
- 239000004743 Polypropylene Substances 0.000 claims description 3
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 claims description 3
- -1 polypropylene Polymers 0.000 claims description 3
- 229920001155 polypropylene Polymers 0.000 claims description 3
- 239000010936 titanium Substances 0.000 claims description 3
- 229910052719 titanium Inorganic materials 0.000 claims description 3
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 abstract description 11
- 229910052943 magnesium sulfate Inorganic materials 0.000 abstract description 5
- 235000019341 magnesium sulphate Nutrition 0.000 abstract description 5
- 239000002826 coolant Substances 0.000 abstract description 3
- 238000003795 desorption Methods 0.000 abstract description 2
- 238000005057 refrigeration Methods 0.000 abstract 1
- 238000000034 method Methods 0.000 description 13
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 10
- 229910001425 magnesium ion Inorganic materials 0.000 description 10
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical compound [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 description 7
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 7
- 229910052748 manganese Inorganic materials 0.000 description 7
- 239000011572 manganese Substances 0.000 description 7
- 239000011701 zinc Substances 0.000 description 7
- 229910052725 zinc Inorganic materials 0.000 description 7
- 239000000047 product Substances 0.000 description 5
- 239000007787 solid Substances 0.000 description 5
- 238000005868 electrolysis reaction Methods 0.000 description 4
- 238000009854 hydrometallurgy Methods 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 3
- 229910052751 metal Inorganic materials 0.000 description 3
- 239000002184 metal Substances 0.000 description 3
- 238000004070 electrodeposition Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 1
- 238000003723 Smelting Methods 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- PTFCDOFLOPIGGS-UHFFFAOYSA-N Zinc dication Chemical compound [Zn+2] PTFCDOFLOPIGGS-UHFFFAOYSA-N 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 125000001153 fluoro group Chemical class F* 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 description 1
- ORUIBWPALBXDOA-UHFFFAOYSA-L magnesium fluoride Chemical compound [F-].[F-].[Mg+2] ORUIBWPALBXDOA-UHFFFAOYSA-L 0.000 description 1
- 229910001635 magnesium fluoride Inorganic materials 0.000 description 1
- 239000000347 magnesium hydroxide Substances 0.000 description 1
- 229910001862 magnesium hydroxide Inorganic materials 0.000 description 1
- 229940099596 manganese sulfate Drugs 0.000 description 1
- 239000011702 manganese sulphate Substances 0.000 description 1
- 235000007079 manganese sulphate Nutrition 0.000 description 1
- WPBNNNQJVZRUHP-UHFFFAOYSA-L manganese(2+);methyl n-[[2-(methoxycarbonylcarbamothioylamino)phenyl]carbamothioyl]carbamate;n-[2-(sulfidocarbothioylamino)ethyl]carbamodithioate Chemical compound [Mn+2].[S-]C(=S)NCCNC([S-])=S.COC(=O)NC(=S)NC1=CC=CC=C1NC(=S)NC(=O)OC WPBNNNQJVZRUHP-UHFFFAOYSA-L 0.000 description 1
- SQQMAOCOWKFBNP-UHFFFAOYSA-L manganese(II) sulfate Chemical compound [Mn+2].[O-]S([O-])(=O)=O SQQMAOCOWKFBNP-UHFFFAOYSA-L 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 238000013508 migration Methods 0.000 description 1
- 230000005012 migration Effects 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 238000006722 reduction reaction Methods 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Images
Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
Landscapes
- Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
Abstract
The utility model discloses an electrolyte crystallization magnesium removal system, including heat exchanger, 3 grades of series connection crystallizers, subsider, centrifuge, mother liquor groove and refrigeration unit. The liquid inlet end of the heat exchanger is connected with an electrolyte feeding pump, the liquid outlet end of the heat exchanger is connected with the inlet of the first-stage crystallizer, the first, second and third-stage crystallizers are sequentially connected in series, each crystallizer is provided with a built-in heat exchange coil and a crystal slurry mixed liquid outlet, and the crystal slurry mixed liquid outlet of the third-stage crystallizer is connected with the settling tank. The centrifuge is connected to the discharge gate of settling tank lower part, and centrifuge mother liquor export and settling tank supernatant export all are connected to the mother liquor groove, and mother liquor groove export is connected with heat exchanger coolant liquid entry, heat exchanger coolant liquid exit linkage electrolyte storage tank. The secondary refrigerant outlet of the refrigerating unit is connected with the inlet of the coil pipe in each crystallizer, and the outlet of the coil pipe is connected with the secondary refrigerant return port of the refrigerating unit. The utility model discloses magnesium sulfate in can effectual desorption electrolyte.
Description
Technical Field
The utility model relates to a non ferrous metal metallurgy field especially relates to an electrolyte crystallization magnesium removal system.
Background
In the processes of producing metal zinc by zinc hydrometallurgy and producing metal manganese by an electrolytic manganese process, the electrolyte contains impurity magnesium ions with higher concentration, and the electrolyte has a plurality of hazards to zinc electrodeposition and manganese electrodeposition.
The increase of the concentration of magnesium ions in the zinc hydrometallurgy electrolyte can increase the viscosity and density of the electrolyte, hinder the migration of zinc ions in the electrolytic process, increase the resistance, increase the electrolytic energy consumption and increase the production cost. In addition, magnesium ions in the electrolyte are easy to form crystals to separate out, so that pipelines are blocked, and the stable operation of the wet zinc smelting process is influenced.
In the process of electrolytic manganese, the concentration of magnesium ions in the electrolyte is increased, and the magnesium ions are crystallized and separated out in a diaphragm and a pipeline, so that the flowing and conveying of the solution are influenced, and the loss of effective components such as manganese sulfate, ammonium sulfate and the like is increased. In addition, magnesium ions in the electrolyte increase the solution density, reduce the current efficiency, influence the quality of manganese products and damage the normal production of the electrolytic manganese process.
Therefore, how to remove magnesium ions in the electrolyte is a common problem in the zinc hydrometallurgy and electrolytic manganese industries. The existing method for removing magnesium from electrolyte mainly comprises the steps of adding lime for neutralization, and removing magnesium in the form of magnesium hydroxide precipitate; or adding fluorine salt to form magnesium fluoride with low solubility to precipitate magnesium. The methods can reduce the concentration of magnesium ions in the electrolyte to a certain extent, and have certain advantages. However, a large amount of gypsum slag and wastewater containing heavy metals are inevitably produced in the magnesium removal process, and the defects limit the large-scale popularization and application of the existing magnesium removal method. Therefore, the further development of a cleaner and more environment-friendly new magnesium removal technology and a new process system has important significance.
Disclosure of Invention
An object of the utility model is to provide a remove efficient, the operation of magnesium is stable, energy-concerving and environment-protective useless electrolyte and remove magnesium system, through controlling the interior reaction temperature gradient of tertiary series connection crystallizer, with the form desorption that magnesium deposited with the sulfate crystallization. The system can be connected with the electrolyte of the zinc hydrometallurgy production process and can also be connected with the anolyte of the manganese electrolysis process, and the system has the characteristics of wide application range and high magnesium removal efficiency.
The utility model relates to an electrolyte crystallization magnesium removal system, which comprises a heat exchanger, a 3-stage series crystallizer, a settling tank, a centrifuge, a mother liquor tank and a refrigerating unit; the liquid inlet end of the heat exchanger is connected with an electrolyte feeding pump, the liquid outlet end of the heat exchanger is connected with the inlet of the first-stage crystallizer, the second-stage crystallizer and the third-stage crystallizer are sequentially connected in series, each crystallizer is provided with a built-in heat exchange coil and a magma mixed liquid outlet, and the magma mixed liquid outlet of the third-stage crystallizer is connected with the settling tank; the settling tank is provided with a supernatant outlet and a lower underflow outlet, the lower underflow outlet of the settling tank is connected with the centrifuge, a mother liquor outlet of the centrifuge and a supernatant outlet of the settling tank are both connected to the mother liquor tank, an outlet of the mother liquor tank is connected with a cooling liquor inlet of the heat exchanger, and an outlet of the cooling liquor of the heat exchanger is connected with the electrolyte storage tank; the secondary refrigerant outlet of the refrigerating unit is connected with the inlet of the coil pipe in each crystallizer, and the outlet of the coil pipe is connected with the secondary refrigerant return port of the refrigerating unit.
The heat exchanger is a tube type heat exchanger.
The crystallizer is a polypropylene crystallization reaction kettle.
The coil is TA2 titanium coil.
The utility model relates to an electrolyte crystallization removes magnesium system, the mixed liquid export of third level crystallizer magma pass through the magma delivery pump and be connected with the subsider. The purpose of adding the magma transfer pump is to provide enough power to force the magma into the settling tank at a set rate.
The utility model relates to an electrolyte crystallization magnesium removal system, a settling tank is Y-shaped; wherein the supernatant outlet is arranged at the upper part of the settling tank; defining a horizontal plane where an inlet of a crystal slurry conveying pump for inputting the crystal slurry to a settling tank is located as A, and defining a horizontal plane where a supernatant outlet is located as B; B-A is greater than 0.
The utility model relates to an electrolyte crystallization magnesium removal system, a crystal slurry delivery pump inputs crystal slurry to the inlet of a settling tank, which is close to the wall of the settling tank; and is tangent to the inlet of the sedimentation tank from the crystal slurry conveying pump to the inlet of the sedimentation tank or the extension line of the inlet of the sedimentation tank. The utility model designs the settling tank into Y-shaped, and limits B-A to be larger than 0, and the magma conveying pump inputs magma to the inlet of the settling tank or the extension line of the inlet is tangent with the wall of the settling tank, so as to ensure that the magma enters the settling tank at a designed constant speed and forms a spiral vortex in the settling tank; under the condition that the parameter is set reasonably, the quick separation of the solid and the liquid (the liquid is cooled electrolyte) can be realized, and the liquid is ensured to be almost free of solid substances. This provides the necessary conditions for cooling the electrolyte for reuse in the heat exchanger. (conventionally, the heat exchanger is relatively small and curved, and once the solid matter content is slightly too high, the pipeline is likely to be blocked, and the electrolyte is directly used for electrolysis after passing through the heat exchanger, and once the solid matter content is too high, the quality of the later electrolysis product is affected).
The utility model relates to an electrolyte crystallization removes magnesium system, the equivalent diameter at subsider top be C, the equivalent diameter D of lower part underflow export, when C, D's unit is the same, C/D more than or equal to 20.
The utility model has the beneficial technical effects that:
(1) the system can effectively remove magnesium sulfate in the electrolyte, reduce the concentration of magnesium ions in the electrolyte, reduce the density and viscosity of the electrolyte, improve the current efficiency and reduce the energy consumption of electrolysis.
(2) The system adopts the mother liquor precooling and crystallizer built-in coil pipe combined heat exchange cooling device, can maintain the stable reaction temperature in the crystallizer, conveniently adjusts the temperature gradient in each stage of crystallizer, and has the advantages of convenient operation, high magnesium removal efficiency, stable operation, energy conservation, environmental protection and the like.
Drawings
Fig. 1 is a schematic view of the magnesium removal system for electrolyte crystallization of the present invention.
In the figure, 1 is a heat exchanger; 2-primary crystallizer; 3-secondary crystallizer; 4-three-stage crystallizer; 5-crystal slurry delivery pump; 6, a settling tank; 7-a centrifuge; 8-mother liquor tank; 9-mother liquor delivery pump; 10-a refrigerating unit; 11-coil pipe.
Detailed Description
The present invention will be further described with reference to the accompanying drawings and the following detailed description.
As shown in fig. 1, an electrolyte crystallization magnesium removal system comprises a heat exchanger 1, a primary crystallizer 2, a secondary crystallizer 3, a tertiary crystallizer 4, a crystal slurry delivery pump 5, a settling tank 6, a centrifuge 7, a mother liquor tank 8, a mother liquor delivery pump 9, a refrigerating unit 10 and a coil pipe 11. The liquid inlet end of the heat exchanger 1 is connected with an electrolyte feeding pump, the liquid outlet end of the heat exchanger is connected with the inlet of the first-stage crystallizer 2, the outlet of the second-stage crystallizer 3 is connected with the inlet of the third-stage crystallizer 4, the outlet of the third-stage crystallizer 4 is connected with the crystal slurry conveying pump 5, and the crystal slurry is conveyed to the settling tank 6 by the crystal slurry conveying pump 5. The settling tank 6 is divided into a supernatant outlet and a lower underflow outlet, and the supernatant outlet is connected with the mother liquor tank 8. The bottom flow outlet of the lower part is connected with a centrifuge 7, and the mother liquor outlet of the centrifuge 7 is connected with a mother liquor tank 8. The outlet of the mother liquor tank 8 is connected with a mother liquor delivery pump 9, the crystallized mother liquor is delivered to the inlet of the cooling liquor of the heat exchanger 1, and then is discharged from the cooling liquor outlet of the heat exchanger 1 to the electrolyte storage tank through self-flowing.
TA2 titanium coil pipes are arranged in the first-stage crystallizer 2, the second-stage crystallizer 3 and the third-stage crystallizer 4. The crystallizer is made of polypropylene.
The secondary refrigerant outlet of the refrigerating unit 10 is respectively connected with the inlet of the coil pipe 11 in the three-stage crystallizer, flows out from the outlet of the coil pipe 11 after flowing automatically, and is connected with the secondary refrigerant inlet of the refrigerating unit 10, and the secondary refrigerant forms a closed cycle.
In this embodiment, the settling tank is "Y" -shaped; wherein the supernatant outlet is arranged at the upper part of the settling tank; defining a horizontal plane where an inlet of a crystal slurry conveying pump for inputting the crystal slurry to a settling tank is located as A, and defining a horizontal plane where a supernatant outlet is located as B; B-A is greater than 0;
in this embodiment, the magma conveying pump inputs magma to the inlet of the settling tank close to the wall of the settling tank; and is tangent to the inlet of the sedimentation tank from the crystal slurry conveying pump to the crystal slurry inlet or the extension line of the inlet of the sedimentation tank and the wall of the sedimentation tank, and the phase tangent angle is 30 DEG
In this example, the equivalent diameter at the top of the settler is C, the equivalent diameter D at the bottom underflow outlet is D, and C/D equals 20 when C, D units are the same.
The utility model discloses a theory of operation does: the electrolyte is sent into the heat exchanger 1 by the feed pump to carry out heat exchange and cooling, and the cooled electrolyte enters the first-stage crystallizer 2 and is continuously cooled by adopting the coil pipe 11 to exchange heat for primary crystallization. And the crystal slurry produced by the first-stage crystallizer 2 enters the second-stage crystallizer 3, and is cooled continuously by adopting the heat exchange of the coil pipe 11 to perform secondary crystallization. And the crystal slurry produced by the second-stage crystallizer 3 enters a third-stage crystallizer 4, and is cooled by heat exchange of a coil 11 continuously to perform tertiary crystallization. And (3) obtaining magnesium sulfate crystal slurry after three times of crystallization, conveying the magnesium sulfate crystal slurry to a settling tank 6 by using a crystal slurry conveying pump 5 at a tangent angle of 30 degrees, settling a crystallization product into the lower part of the settling tank in the settling process, discharging the crystallization product from a bottom flow outlet, and allowing the crystallization product to enter a centrifugal machine 7 for centrifugal filtration to separate magnesium sulfate crystals. The mother liquor obtained by filtering and the solution flowing out of the supernatant outlet of the settling tank 6 are combined and enter a mother liquor tank 8 for storage, then the mother liquor is conveyed to the heat exchanger 1 by a mother liquor conveying pump 9 to be used as a cooling medium for heat exchange, and the mother liquor is discharged to an electrolyte storage tank after the heat exchange is finished. After the electrolyte is subjected to heat exchange and temperature reduction, three-stage temperature reduction and crystallization, and sedimentation and centrifugal separation, magnesium in the solution is separated from the solution in a magnesium sulfate salt solid form, so that the aim of removing magnesium ions in the electrolyte is fulfilled.
While the invention has been particularly shown and described with reference to a preferred embodiment, it will be understood by those skilled in the art that various changes in form and detail may be made therein without departing from the spirit and scope of the invention as defined by the appended claims.
Claims (8)
1. The utility model provides an electrolyte crystallization magnesium removal system which characterized in that: the electrolyte crystallization magnesium removal system comprises a heat exchanger, a 3-stage series crystallizer, a settling tank, a centrifugal machine, a mother liquor tank and a refrigerating unit; the liquid inlet end of the heat exchanger is connected with an electrolyte feeding pump, the liquid outlet end of the heat exchanger is connected with the inlet of the first-stage crystallizer, the second-stage crystallizer and the third-stage crystallizer are sequentially connected in series, each crystallizer is provided with a built-in heat exchange coil and a magma mixed liquid outlet, and the magma mixed liquid outlet of the third-stage crystallizer is connected with the settling tank; the settling tank is provided with a supernatant outlet and a lower underflow outlet, the lower underflow outlet of the settling tank is connected with the centrifuge, a mother liquor outlet of the centrifuge and a supernatant outlet of the settling tank are both connected to the mother liquor tank, an outlet of the mother liquor tank is connected with a cooling liquor inlet of the heat exchanger, and an outlet of the cooling liquor of the heat exchanger is connected with the electrolyte storage tank; the secondary refrigerant outlet of the refrigerating unit is connected with the inlet of the coil pipe in each crystallizer, and the outlet of the coil pipe is connected with the secondary refrigerant return port of the refrigerating unit.
2. The electrolyte crystallization magnesium removal system of claim 1, wherein: the heat exchanger is a tube type heat exchanger.
3. The electrolyte crystallization magnesium removal system of claim 1, wherein: the crystallizer is a polypropylene crystallization reaction kettle.
4. The electrolyte crystallization magnesium removal system of claim 1, wherein: the coil is TA2 titanium coil.
5. The electrolyte crystallization magnesium removal system of claim 1, wherein: the crystal slurry mixed liquid outlet of the third-stage crystallizer is connected with the settling tank through a crystal slurry conveying pump.
6. The electrolyte crystallization magnesium removal system of claim 5, wherein: the settling tank is Y-shaped; wherein the supernatant outlet is arranged at the upper part of the settling tank; defining a horizontal plane where an inlet of a crystal slurry conveying pump for inputting the crystal slurry to a settling tank is located as A, and defining a horizontal plane where a supernatant outlet is located as B; B-A is greater than 0.
7. The electrolyte crystallization magnesium removal system of claim 5, wherein: the crystal slurry conveying pump inputs the crystal slurry to the inlet of the settling tank, and the inlet is close to the wall of the settling tank; and is tangent to the inlet of the sedimentation tank from the crystal slurry conveying pump to the inlet of the sedimentation tank or the extension line of the inlet of the sedimentation tank.
8. The electrolyte crystallization magnesium removal system of claim 5, wherein: the equivalent diameter of the top of the settling tank is C, the equivalent diameter D of the bottom underflow outlet is D, and when the unit of C, D is the same, the ratio of C/D is greater than or equal to 20.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020418783.6U CN211836413U (en) | 2020-03-27 | 2020-03-27 | Electrolyte crystallization magnesium removal system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020418783.6U CN211836413U (en) | 2020-03-27 | 2020-03-27 | Electrolyte crystallization magnesium removal system |
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| Publication Number | Publication Date |
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| CN211836413U true CN211836413U (en) | 2020-11-03 |
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| CN202020418783.6U Active CN211836413U (en) | 2020-03-27 | 2020-03-27 | Electrolyte crystallization magnesium removal system |
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| Country | Link |
|---|---|
| CN (1) | CN211836413U (en) |
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- 2020-03-27 CN CN202020418783.6U patent/CN211836413U/en active Active
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Assignee: Kunming University of Technology Design and Research Institute Co.,Ltd. Assignor: Kunming University of Science and Technology Contract record no.: X2023980052068 Denomination of utility model: An electrolyte crystallization magnesium removal system Granted publication date: 20201103 License type: Common License Record date: 20231212 |